A review on lignin pyrolysis: pyrolytic behavior, mechanism, and relevant upgrading for improving process efficiency.

Lignin is a promising alternative to traditional fossil resources for producing biofuels due to its aromaticity and renewability. Pyrolysis is an efficient technology to convert lignin to valuable chemicals, which is beneficial for improving lignin valorization. In this review, pyrolytic behaviors of various lignin were included, as well as the pyrolytic mechanism consisting of initial, primary, and charring stages were also introduced. Several parallel reactions, such as demethoxylation, demethylation, decarboxylation, and decarbonylation of lignin side chains to form light gases, major lignin structure decomposition to generate phenolic compounds, and polymerization of active lignin intermediates to yield char, can be observed through the whole pyrolysis process. Several parameters, such as pyrolytic temperature, time, lignin type, and functional groups (hydroxyl, methoxy), were also investigated to figure out their effects on lignin pyrolysis. On the other hand, zeolite-driven lignin catalytic pyrolysis and lignin co-pyrolysis with other hydrogen-rich co-feedings were also introduced for improving process efficiency to produce more aromatic hydrocarbons (AHs). During the pyrolysis process, phenolic compounds and/or AHs can be produced, showing promising applications in biochemical intermediates and biofuel additives. Finally, some challenges and future perspectives for lignin pyrolysis have been discussed.

Introduction

Due to the natural aromatic polystructure, lignin (which can mainly be extracted from softwood, hardwood, and grass, and the model lignin structures is shown in Fig. 1 [1]) has been regarded as a sustainable alternative to fossil-derived resources to provide valuable biochemicals [2-7]. Interunits of lignin are connected by C–O and C–C bonds (such as β-O-4, β–β, and β-5, Fig. 1), wherein the later contains higher bond dissociation energies (BDE = 69–123 kcal/mol) than that of the former (BDE = 52–80 kcal/mol) [8]. Furthermore, C–C bonds in lignin mainly formed between bulky aromatic rings, making their cleavage more difficult. Besides, C–O bonds are the most abundant linkages in native lignin, accounting for two-thirds or more of total linkages [9-12]. Therefore, much attention has been paid to the efficient cleavage of C–O and C–C bonds in lignin, especially under mild conditions, such as catalytic [13-18], photocatalytic [19-21], ionic liquid promoted depolymerization [22-26], and reductive catalytic fractionation [27-31] to achieve efficient lignin transformation or selective conversion of lignin model compounds to target products. In these studies, some obvious defects can limit their wide applications in the industrial scale, such as the common utilization of noble metal (e.g., ruthenium and rhodium) supported catalysts and lignin model compounds (e.g., dimers containing C–O bonds or lignin-derived monophenols) with high price, non-noble metal supported catalysts with complex preparation processes (such as Ni/Al2O3 prepared from NiAl-LDH (layered double hydroxide), and Co/MoS2−x with defect sites), and low energy conversion efficiency (e.g., photocatalytic conversion).

Fig. 1

Model lignin structures containing 11 units for A a softwood, B hardwood, and C grass [1]

Commonly, strategies for lignin conversion to biofuels or biochemicals can be summarized into pyrolysis (thermal and catalytic pyrolysis), hydroprocessing (hydrogenolysis, hydrodeoxygenation, hydrogenation, and integrated hydrogen processing), oxidation (organometallic catalysis, metal-free organocatalytic system, base and acid catalysts, metal salt catalysis, photocatalytic oxidation, and electrocatalytic oxidation), gasification and liquid-phase or steam reforming [9, 32, 33]. Recently, catalytic self-transfer hydrogenolysis has been found as a sustainable method for lignin hydrogenolysis due to the renewable H2 source produced from lignin structure [34]. Among these conversion methods, pyrolysis technology has been confirmed as a more effective method in the absence of oxygen due to its easier operation and lower cost for lignin conversion to gases (containing H2O, CO, CO2, CH4, and H2), liquid biofuels (containing monophenols or polyphenols), and solid char with shorter reaction time, of which the performance mainly depends on the reaction temperature, time, heating rate and reactor configuration [35-37]. Massive studies have focused on lignin pyrolysis using different techniques such as TGA (thermogravimetric analysis), Py-GC/MS (pyrolysis-gas chromatograph/mass spectroscopy) and fixed-/fluidized-bed reactors, and the products evolution was investigated comprehensively [38-41]. For deeply understanding the pyrolysis mechanism, some studies also used lignin-derived model compounds as pyrolyzed subjects, revealing that several linkages cleavage (such as Cβ–O and Cα–Cβ) occurred simultaneously [42, 43].

Although lignin pyrolysis mechanism has been explored and lignin oils (rich in phenolic compounds) can be produced, due to the high oxygen content, acidity, and corrosiveness, further upgrading of liquid oils is necessary [44]. Recently, catalytic pyrolysis has been applied as an efficient method for improving oil quality and stability via deoxygenation reactions with assistance of suitable catalysts [45, 46]. The most used catalysts are zeolites, such as ZSM-5, MCM-41, beta, mordenite, ferrierite, and USY with low cost and vast availability, of which the catalytic effect would promote deoxygenation via dehydration, decarbonylation, and decarboxylation reactions [47-49]. Furthermore, functionalities of zeolites on acidity, mesoporosity, and large external surface area make positive effects on aromatics production and char inhibition [50-52]. Aromatic hydrocarbons (AHs), such as monocyclic aromatic hydrocarbons (MAHs) and polycyclic aromatic hydrocarbons (PAHs), are the major products from lignin catalytic pyrolysis using zeolites, wherein naphthalene and anthracene obtained from PAHs can be directly used as fuel additives [53, 54]. On the other hand, for improving oil quality, it is feasible to increase the effective hydrogen index (EHI) of pyrolyzed feedstock due to the uncompetitive content of effective hydrogen in lignin (only around 0.3) [55]. Therefore, lignin co-pyrolysis with other hydrogen-rich feedstock has been proposed as a useful method to improve oil quality [56]. For example, lignin co-pyrolysis with low-density polyethylene over ZSM-5 [57], with polyethylene terephthalate over calcium oxide and zeolites [58], or with plastics (such as polyethylene, polypropylene and polystyrene) over LOSA-1, spent FCC, and Gamma-Al2O3 [59] showed the enhanced production of AHs owing to the synergistic effect of deoxygenation (from catalysts) and hydrogen transferring (from hydrogen-rich co-feedstock) [60]. In addition, waste cooking oils have been used as hydrogen donors during lignin pyrolysis [61], showing the promising application of co-pyrolysis with some hydrogen-rich feedstock in lignin oil upgrading, which is also feasible for both lignin valorization and other wastes with high value-added recycling.

In this review, we comprehensively summarized the mechanism of lignin pyrolysis (detailedly divided into three stages, e.g., initial, primary and charring stages, and the characteristic products evolution, and mechanism during each stage was introduced, including gas, liquid, and solid). On the other hand, the pyrolytic behaviors of different kinds of lignin (e.g., Kraft lignin, alkali lignin, organosolv lignin, DES lignin, biological lignin, and ionic liquid lignin, also including their isolations, pretreatments, structures, and pyrolytic oil properties) were also introduced in this review. Furthermore, lignin catalytic pyrolysis using zeolites as the most used catalysts and co-pyrolysis with other hydrogen-rich feedstock were also included in this review for improving lignin oils quality via deoxygenation and increasing AHs content, and the corresponding products yield and selectivity were also obtained.

Lignocellulosic biomass pyrolysis

Background

Lignocellulosic biomass is a narrow concept of biomass materials, broadly including forestry/agricultural residues, industrial waste biomass, and grasses [62, 63], which is the most popular material for preparing biofuels [64, 65]. Pyrolysis is a kind of thermochemical reaction performed in the absence of oxygen with a certain of heating rate [66], which is an efficient method for converting biomass materials into biofuels [67-71]. Typically, lignocellulosic biomass conversion via pyrolysis technology involves the thermal decomposition of three main basic components in lignocellulosic biomass (i.e., cellulose, hemicellulose, and lignin) [72], which can be transformed into valuable products, such as sugars, cyclopentenes, furans, phenols, and aliphatics in biofuels [73].

Pyrolysis of cellulose, hemicellulose, and lignin

From Fig. 2A, cellulose is the most abundant polysaccharide in nature, which is a linear polymer of d-glucosyl surrounded by the heterogeneous polysaccharide, hemicellulose, and lignin, and connected by β-1,4-glycoside and intra/intermolecular hydrogen bonds [74]. Due to its relatively simple structure, cellulose has been widely applied in pyrolysis process, briefly including the starting depolymerization at around 350 °C, and further conversion into active cellulosic species, levoglucosan (LGA), levoglucone (LGO), and other monosaccharides via bonds cracking and dehydration. The primary pyrolytic products from cellulose are anhydrosugars, which can be further converted into some light oxygenates (e.g., furans, aldehydes, ketones, acids, etc.) at higher temperatures (Fig. 2B) [75, 76]. In comparison with cellulosic components, hemicellulose has a more complex structure with abundant branched chains and various substituents, which is mainly composed of xylan and glucomannans, where the later contains the similar pyrolytic properties to anhydrosugars (which leads to the similar pyrolytic characteristics to cellulose). Therefore, the pyrolysis process of xylan can be selected as a modifier to study the pyrolytic mechanism of hemicellulose, majorly including initial depolymerization, the generation of furan, and pyran derivatives via dehydration, and the breakage of furanose and pyranose-derived rings to form some light oxygenates (Fig. 2C) [77]. Lignin, a complex biopolymer with aromatic structure, mainly associates with cellulose and hemicellulose together to form plants skeleton. In the process of lignin pyrolysis, higher temperatures are required for linkages cleavage to generate large amounts of phenolic compounds together with small amounts of acid, alcohols, and light aromatic hydrocarbons (Fig. 2D) [78].

Fig. 2

A Composition and structure of lignocellulosic biomass, and possible pyrolysis mechanism of B cellulose, C hemicellulose, and D lignin

(Reproduced from Refs. [63, 75] with permission from Elsevier)

Influencing factors of lignocellulosic pyrolysis

Zhao et al. used commercial cellulose, hemicellulose, and lignin as raw materials without any pretreatments and found that the pyrolytic characteristics can be significantly influenced by the pyrolytic temperature [79]. Besides, different types of lignocellulosic biomass determine various compositions of cellulose, hemicellulose, and lignin, which also influence the pyrolytic characteristics. Typically, cellulosic components can produce the higher yield of biofuels (~ 60%) compared to those of hemicellulose (~ 40%) and lignin (~ 30%). Other influencing parameters, such as the contents of ash, metal, and moisture, also affect the production and properties of final generated biofuels. Higher contents of moisture in lignocellulosic biomass would reduce the calorific value and deteriorate the quality of biofuels.

During pyrolysis, the function of pyrolytic temperature is to provide heat to decompose the structure of substrates, and increasing the pyrolytic temperature can enhance the conversion efficiency. At lower pyrolytic temperatures, ash in raw materials would be retained in solid products to yield more semi-coke. In addition, metals existing in the ash, such as kalium and calcium, can enhance the pyrolytic heating rate while reduce the yield of biofuels due to their catalyzed effect to promote the secondary cracking reactions among products in biofuels [80]. For example, Tsai et al. used rice husk as raw material with further grinding and rose the pyrolytic temperature from 400 to 500 °C, leading to the higher production of biofuels from 11.26 to 35.92 wt% and reaching the maximum yield (i.e., 38.8 wt%) at 800 °C [81]. Lazzari et al. used mango fruit seeds as raw materials (which were separated into tegument and almond) and obtained the highest yield of biofuels at 38.8 wt% when the pyrolytic temperature increasing to 650 °C [82]. It is suggested that increasing the pyrolytic temperature makes a positive effect on the production of biofuels, while the opposite trend would be found at a very high temperature due to the occurrence of the secondary cracking reactions [83]. Jung et al. used rice straw and bamboo sawdust as raw materials with further sieving into small particle sizes and pointed out that as the pyrolytic temperature of bamboo sawdust increases over 500 °C, biofuel yield would gradually decrease, and the optimal pyrolytic temperature for rice straw is 445 °C to yield more biofuels [84]. In addition, the optimal pyrolytic temperature ranges for rice husks/sawdust and cotton stalk without ant pretreatments are confirmed at 420–540 and 480–530 °C, respectively [85-87], and the maximum yield of biofuels for rice husk (with further grinding) (70.0 wt%) [88], palm waste (with further grinding) (72.4 wt%) [89], neem de-oiled cake (without any pretreatments) (40.2 wt%) [90], Cynara cardunculus (without any pretreatments) (56.2 wt%) [91], olive bagasse (without any pretreatments) (46.3 wt%) [92], sugarcane bagasse (with further drying, grinding, and sieving) (61.4 wt%) [93], cassava rhizome (with further drying, grinding and sieving) (63.2 wt%) and cassava stalk (with further drying, grinding and sieving) (61.4 wt%) [94], Jatropha seed shell cake (without any pretreatments) (48.0 wt%) [95], pistachio shell (with further drying and grinding) (20.5 wt%) [96], and polar wood (without any pretreatments) (69.0 wt%) [97] can be obtained at 450, 500, 400, 400, 600, 475, 472, 469, 470, 550, and 455 °C, respectively. Biswas and Pattiya et al. also suggested that different kinds of biomass materials (e.g., corn cob, wheat straw, rice straw and rice husk, with further drying, crushing and sieving) contain their own ideal pyrolytic temperatures to generate the highest yield of biofuels [98, 99].

Except for the pyrolytic temperature, Qiu et al. pointed out that the type of biomass feedstock is also an important factor to influence the generation of biofuels due to the differences of their compositions and structures [72]. Oasmaa et al. found that wood biomass can produce more biofuels with lower yield of aqueous and gaseous products [100]. Among these formed biofuels, different compositions of raw materials lead to the different properties of biofuels. For example, cellulosic-derived biofuels are rich in acids, furans, and ketones, which are similar to those of hemicellulose-derived ones, while lignin-derived biofuels reveal a great capacity to produce phenolic compounds [101]. There is a positive correlation of ketones and cellulose, furans and holocellulose, and phenols and lignin, while there is a negative correlation of short-chain acids and ash, and hydrocarbons and cellulose. Furthermore, with increasing the pyrolytic temperature, various interactions occur to change the composition of biofuels. For example, Huang et al. found that alkenes, alkanes, long-chain fatty acids/esters, aliphatic nitriles, and amides can be obtained at lower pyrolytic temperatures, while higher pyrolytic temperatures favor the cracking reaction among aliphatic species and the formation of aromatic compounds [102]. Ly et al. found that a higher pyrolytic temperature produces biofuels with more short aliphatic carbons, low-molecular-weight alcohols, ketones, and their derivatives due to the further decomposition reaction occurring [103]. Alvarez et al. observed that increasing the pyrolytic temperature would reduce the yield of ketones and acids, while increase the yield of phenols [88]. In addition, the pyrolytic temperature is also an important factor for determining the quality of biofuels, such as H/C ratio, which is an essential indicator for HHV (high heating value, kJ/mol) [104]. Ates and Ly et al. also observed that increasing the pyrolytic temperature is beneficial for reducing oxygen content in biofuels, while increasing the content of hydrogen, showing the higher calorific value of biofuels [105, 106].

The meaning of further investigations on lignin pyrolysis

Even though massive studies have focused on lignocellulosic biomass pyrolysis, the biggest challenge is about the high-efficiency conversion of lignin. Lignin accounting for 40% of energy (higher than that of polysaccharides) has been considered as the most promising source for biochemical platform and bioenergy due to its aromatic structure [107, 108]. Nowadays, over 90% of lignin is burned with low efficiency, and only 2% of lignin is utilized efficiently due to its complex structure and low reactivity [109, 110]. As the stubbornest component in lignocellulosic biomass, the efficient conversion of lignin has attracted much attentions from both industry and research community and is still a researching hotspot up to now. Pyrolysis technology has been considered as an effective method for lignin conversion to well-fined chemicals due to its low cost, easy operation, high efficiency for energy extraction, and fuel production [111-114]. As the only renewable alternative of non-renewable fossil fuels for producing aromatic compounds, lignin can be thermally decomposed via pyrolysis technology to obtain low-molecular-weight phenolic compounds (important intermediates in biochemical platform) and to generate aromatic hydrocarbons (advanced fuel additives with sustainable energy density) [115]. On the other hand, biorefinery economic can benefit from high-quality recovery of lignin by lowering the manufacturing price of biochemicals and biofuels [116].

Lignin pyrolysis

Lignin is one of the three main components in lignocellulosic biomass, combined with cellulose and hemicellulose via hydrogen and ester bonds [117-119]. So far, large quantities of lignin have been produced from industrial and agricultural activities, and pyrolysis technology has been considered as an effective method for its high-efficiency conversion [120-122]. Unfortunately, the presence of cellulose and hemicellulose would affect the pyrolytic behavior of lignin owing to a series of coupling interactions occurring [123-125], hence leading to a more intangible pyrolysis process. After delignification, different kinds of lignin with high purity and homogeneity can be extracted from raw biomass and then pyrolyzed into low-molecular-weight compounds, which are the so-called pyrolytic oils (mainly composed of phenolic compounds, aldehydes, acids, and other aromatic hydrocarbons) [126, 127].

Lignin pyrolysis mechanism

Typically, the radical reaction of lignin pyrolysis has been established and divided into three stages: initial, primary, and charring stages (or namely the radical inducing, the main reacting and the quenching stages [126]). Prior to the detail description of their own pyrolytic characteristics and product distributions, we first introduce the general pyrolytic mechanisms of lignin pyrolysis.

General pyrolytic mechanism of lignin

Lignin pyrolytic mechanisms can be researched via several techniques, such as thermogravimetric analysis (TG), Fourier transform infrared spectroscopy (FTIR), and gas chromatography/mass spectrometry (GC/MS) to determine mass loss, volatiles evolution, and decomposed products distribution, respectively. For example, a coupling analysis of TG-FTIR-GC/MS was used by Yang et al. to investigate the pyrolytic mechanism of lignin-rich residue obtained from Arundo donax. Pyrolytic results including the composition, carbon number and atomic ratio (C/H, C/O) of bio-oils was obtained for proposing pyrolysis mechanism and possible reaction pathway [128]. Through TG analysis, three main stages of lignin pyrolysis can be obtained, including water evaporation (< 200 °C), primary decomposition (at 250–500 °C), and carbonization (> 500 °C) [129-132]. Through the coupling analysis of TG, FTIR, and GC/MS, lignin pyrolytic mechanism can be elucidated in Fig. 3, where chemical linkages, such as C–C and C–O–C bonds, can be cleaved to produce phenols and aromatic hydrocarbons, and functional groups, such as carboxyl, carbonyl, and methoxy, would be escaped from benzene ring to form some light gases. Finally, lignin biochar with abundant functional groups (such as –OH and –OCH3) would be generated via carbonization [133]. On one hand, functional groups in biochar would be further cracked with the temperature rising to form light gases. On the other hand, active aromatic species in bio-oils would be transformed into biochar via repolymerization.

Fig. 3

Proposed pyrolytic mechanism of lignin

(Reproduced from Ref. [128] with permission from Elsevier)

Influencing factors of lignin pyrolysis

Yu et al. investigated the importance of pyrolytic temperature on lignin pyrolysis, where monophenols are the main components at the temperature range of 450–525 °C, and higher temperatures prefer the generation of dimers [134]. Through the further cracking reactions of carboxylic acid, ketone, and aldehyde, and the inhibition of coupling reactions of free mono radicals, the production of phenols can be enhanced. Besides, some functional groups in lignin, such as methoxy and phenolic hydroxyls, significantly change the pyrolytic characteristics of lignin [135]. Methoxy is an important functional group in lignin, which can affect the repolymerization degree of lignin during pyrolysis [136], and also is defined as an important factor to promote the formation of char residues [137-139]. The positive effect of demethylation on repolymerization inhibition can be confirmed by the lower char yield of demethylated lignin compared to that of raw lignin. Besides, with the enhancement of demethylation degree, the main components of demethylated lignin pyrolytic products are adjusted from methoxyphenols to H-type phenols, such as phenols, methyl phenols, and catechol [140]. On the other hand, the charring mechanism of lignin pyrolysis suggests that (1) char cannot be generated when there is only one phenolic hydroxyl; (2) a bromine group as an electron withdrawing site can decrease electron cloud density in ortho position, reduce the bond dissociation energy of phenolic hydroxyl, and promote dehydrogenation, which is conductive for char formation; (3) methoxy, as an electron-donating group, does not promote the repolymerization reaction, while phenolic hydroxyl, as an electron donor group, can promote repolymerization by affecting electron could density; (4) the intramolecular reaction between methoxy and phenolic hydroxyl groups significantly promote the repolymerization, and the promotion of char formation is directly proportional to the amount of methoxy in the ortho position of phenolic hydroxyl [140].

Initial stage of lignin pyrolysis

Lignin pyrolysis process can be divided into three stages, including initial, primary, and charring stages, and each stage has its own characteristic pyrolytic behaviors (Fig. 4) and mechanisms (introduced in the following sections).

Fig. 4

Characteristic pyrolytic behaviors of initial, primary, and charring stages

Li et al. investigate the reaction pathway of initial stage comprehensively, revealing that a complex initial reaction of lignin pyrolysis mainly occurs at the temperature range of 160–330 °C (before 160 °C, external and internal water removing causes a light mass decrease) with mass loss of approximately 20% to form considerable amounts of volatile products [141]. During initial stage, some light gaseous products start to release (e.g., H2O releasing at the ranges of 160–330 and 330–400 °C due to dehydroxylation and hydroxyl cracking in lignin hydrogen bond network; CO2 releasing at the ranges of 160–270, 270–330, and 330–400 °C due to fatty ether bonds cleavage and oxidation, carboxylic acid group cleavage, and carbonyl group cleavage and oxidation; CO releasing at the ranges of 170–330 and 330–400 °C due to the cleavage of ether bonds and side chains C–O; CH4 releasing at the range of 330–400 °C due to the methoxy cleavage). The variations of activation energy of these light gases are mainly due to their formations from different sources with different bond energies [142]. When the temperature increases up to 150 °C, the polymerization reaction happens to form the condensed lignin phase with a larger molecular weight, and oil-based components (such as lignin monomers, dimers, and trimers) would be orderly generated after the temperature further rising to 330 °C [141]. On the other hand, lignin surface adhesion occurs to transform raw lignin into a bulk, and the evolution of functional groups illustrates that hydroxyl and hydrocarbon groups in bulk lignin are temperature induced (of which the content decreases as the temperature increases to form more light gases). In addition, non-conjugated carbonyl, conjugated carbonyl, aromatic, guaiacyl, and syringyl groups in lignin are all temperature induced, which can be converted into aromatic compounds, together with the escape of side chains to form light gases with increasing pyrolytic temperature. Finally, the structure polymerization of condensed lignin or the repolymerization among aromatic compounds happen to generate biochar with fused aromatic rings.

The structural changes of char produced from initial stage was investigated by Chua et al. [143]. With increasing temperature (over the softening temperature of lignin at ~ 140 °C [144]), the content of THF-insoluble fraction of obtained lignin char contains a larger molecular weight, indicating the occurrence of repolymerization reaction. For THF-soluble fraction, almost the half is transformed into volatile products and the remainder is repolymerized into THF-insoluble fraction (of which the structure is composed of mono, 2–3 fused, and 3–5 fused aromatic rings [145]) when the temperature increases up to 300 °C. From RT to 250 °C, the aromatic structure of char is reduced due to the generation of light gases and oil component compounds (e.g., phenolic monomers, dimers or trimers). The decrease of both H/C and O/C ratios in THF-soluble fraction with increasing temperature from 100 to 300 °C illustrates that some mono-aromatics would be repolymerized into condensed phases with fused-ring structures in THF-insoluble fraction. The change of char structure with the increase of temperature illustrates that (1) the aliphatic carbon structure decreases due to the escape of alkyl side chains, (2) the methoxy carbon structure decreases due to the decomposition of ether bonds (such as α-O-4 and β-O-4), (3) the aromatic carbon structure increases due to the enhanced aromaticity, and (4) the carbonyl carbon structure decreases due to the release of light gases (such as CO2).

Primary stage of lignin pyrolysis

Primary stage of lignin pyrolysis containing more intense structural decomposition happens at the temperature range of 400–600 °C after initial stage, where phenolic compounds (which is both temperature induced and time induced) are the major components during this stage [146-148]. The pyrolytic temperature and residence time have significant influences on products generation [149-151]. Lin et al. investigated the effect of temperature and time on the generation of phenolic products, illustrating that the maximum yield of phenolic products can be obtained at 450 °C [152]. With increasing temperature, the production of phenolic monomers is enhanced significantly due to the increasing conversion rate of lignin [153-155]. However, due to the secondary reaction occurring with the extension of reaction time, more phenolic monomers would be transformed into light gases (which leads to no further increase of the detecting response of phenolic monomers at 600 °C when the residence time increases from 1 to 5 s). On the other hand, the reaction equilibrium would also lead to no obvious enhancement of products generation at 600 °C with the extension of residence time [127, 155]. Expect for the temperature and reaction time, lignin structure also influences the pyrolytic behavior at primary stage [155, 156]. For example, Marathe et al. investigated the effect of molecular weight on lignin pyrolysis, and the results demonstrate that (1) the increasing molecular weight of lignin would decrease the oil yield due to higher yields of gases and solids obtained; (2) the molecular weight of liquid products is independent to that of lignin but is associated with the reaction pressure; and (3) the yield of liquid products is proportional to the reaction temperature [157]. Besides, Yuan et al. investigated the effect of lignin structure on the formation of phenolic compounds, and various lignin extracted from softwood (pine), hardwood (eucalyptus), and herbaceous feedstock (corn stalk and bamboo) were pyrolyzed, presenting different compositions of liquid products, wherein lignin samples from corn stalk and bamboo favor H-type phenols, and that from pine prefers G-type phenols, while that from eucalyptus majorly produces polyphenols [158].

At the temperature range of 400–600 °C, the structure decomposition of lignin is driven by the linkage cleavage (e.g., ether bonds with bond dissociation energy (BDE) of ~ 291 kJ/mol, and C–C bonds with BDE of ~ 323 kJ/mol), wherein the chemical linkage with lower BDE would be broken easier with the increase of temperature, while that with higher BDE would be more temperature resistance, which can be presented as functional groups in final products [159-161]. In the process of linkages cleavage, hydroxyl radicals are produced from scission of aliphatic side chains, and hydrogen radicals can be generated from β-scission reactions (from C–OH to C=O), which might migrate to either aliphatic side chains or aromatic rings with oxygen radicals [162, 163]. Furthermore, due to the high temperature resistance property of methoxy (i.e., BDE = 481 kJ/mol), large amounts of methoxylated phenols are generated [9, 164]. From Fig. 5, the obtained products can be mainly categorized as guaiacyl, cresol, and catechol types, where guaiacyl units are suggested to produce G-type phenols via depolymerization and dehydration (P1) [165]. Cresol and catechol are generated by the cleavage of interunit linkages and the cracking of aliphatic side chains (P2, P3, and P6). The higher temperature would lead to more demethylation and demethoxylation reactions of guaiacyl units (P2 and P6) to increase the yield of cresol and catechol-type compounds [160, 166]. In addition, cresol-type compounds can also be generated from p-hydroxyphenyl units via depolymerization (P3 and P4) [167]. Phenol-type compounds are created by demethoxylation (P5) of guaiacyl units [168], and acetaldehyde is suggested to be formed from carbohydrate fractions and side chains via dehydration (P8) and fragmentation (P7), respectively [77, 149, 169]. In addition, water can be produced via dehydration reaction between hydroxyl and hydrogen radicals, and methanol and methane can be generated from methyl radicals via demethoxylation promoted by hydrogen or hydroxyl radicals [163].

Fig. 5

Proposed reaction pathways for primary stage of lignin pyrolysis (P1: depolymerization and dehydration; P2: side-chain scission and demethylation; P3, P4: depolymerization; P5: demethoxylation; P6: side-chain scission and demethoxylation; P7: fragmentation of lignin side chains; P8: dehydration and fragmentation of carbohydrate) [39]

Yang et al. elucidated lignin pyrolysis at primary stage comprehensively (i.e., from 200 to 600 °C), especially for the structural evolution of char at this stage [170]. After 400 °C, H2 has been gradually generated and obtains its maximum content at 600 °C due to the polymerization of aromatic rings [127]. With the increase of temperature (from 350 to 600 °C), the condensation of aromatic rings happens to form char residues with polycondensed aromatic structure. The evolution of char structure includes the conversion of hydroxyl groups to carbonyls and aliphatic chain C–H to alkene C–C, mainly due to the primary structure decomposition, and aromatic condensation reactions occurring to cause the aromatic polycondensation over 400 °C. The pyrolysis mechanism can be summarized as (1) almost no lignin conversion happens before 200 °C due to its thermal stability, (2) aromatic side chains can be cleaved to form some light gases as the temperature increasing up to 250 °C [171], (3) from 250 to 350 °C, depolymerization and condensation exist as competing reactions to generate abundant liquid products (i.e., methoxyphenols) via linkages cleavage [172], (4) from 350 to 450 °C, the condensation reaction is enhanced, including repolymerization and condensation, to generate char with 1 × 2 and 2 × 2 fused-ring structures, (5) at 450–600 °C, demethylation, demethoxylation, and dehydrogenation reactions occur to form CH4 and H2, and further convert guaiacyl-type compounds into catechol-type ones and alkyl phenols [173], and (6) at 450–600 °C, the structure of lignin char can be generated consisting of 2 × 2, 3 × 3, 4 × 4, and other fusing rings.

Charring stage of lignin pyrolysis

Through the above studies on lignin pyrolysis, it is well known that the structure of lignin char changes obviously with increasing temperature. Zheng et al. studied the char structure evolution during lignin fast pyrolysis from 200 to 800 °C [40]. Raman spectra in Fig. 6A show that the graphitization degree of lignin char is relatively low due to the presence of low-strength G band of graphite crystals (~ 1585 cm−1) [174]. Figure 6A shows the fitting curves of Raman spectrum of char obtained at 800 °C, consisting of GL (at 1680 cm−1, carbonyl group C=O), G (at 1585 cm−1, graphite E22g; aromatic ring quadrant breathing; alkene C=C), GR (at 1540 cm−1, aromatics with 3–5 rings; amorphous carbon structures), VL (at 1465 cm−1, methylene or methyl; semi-circle breathing of aromatic rings; amorphous carbon structures), VR (at 1380 cm−1, methyl group; semicircle breathing of aromatic rings; amorphous carbon structures), D (at 1320 cm−1, D band on highly ordered carbonaceous materials; C–C between aromatic rings and aromatics with not less than 6 rings), SL (at 1230 cm−1, aryl–alkyl ether; para-aromatics), S (at 1185 cm−1, Caromatic–Calkyl; aromatic (aliphatic) ethers; C–C on hydro-aromatic rings; hexagonal diamond carbon sp3; C–H on aromatic rings), SR (at 1060 cm−1, C–H on aromatic rings; benzene (ortho-di-substituted) ring), and R (at 960–800 cm−1, C–C on alkanes and cyclic alkanes; C–H on aromatic rings) [174, 175]. Raman bands of inorganic matters are mostly below 1100 cm−1; therefore, organic components occupy the main proportion of lignin char. Figure 6B shows the relationship of ring condensation degree versus temperature, elucidating that the aromatization starts at 350 °C, followed by the evolution of char structure from 2 × 3 fused ring to 4 × 5 fused ring over 700 °C. The behavior of carbon deposit on fusing rings would be enhanced owing to the recombination and recondensation of volatile products at higher temperatures [176]. Besides, not only temperature but also heating rate can affect the formation and structure of char significantly. Li et al. investigated the effect of heating rate on the evolution of functional groups and structural properties of lignin char, indicating that the higher heating rate would increase the oxygen content and decrease the HHV value of char, and lead to the further structural decomposition [38].

Fig. 6

A Curve fitting for the first-order Raman spectrum of char obtained at 800 °C, and B relationships between ring condensation degree and pyrolytic temperature

(Reproduced from Ref. [40] with permission from Elsevier)

Recent progress of lignin pyrolysis

According to the pyrolysis mechanism presented above, in this section, we mainly introduce the pyrolytic behaviors of different types of lignin, including Kraft lignin (Table 1), alkali lignin (Table 1), organosolv lignin (Table 1), DES (deep eutectic solvents) lignin (Table 2), biological lignin (Table 3), and ionic liquid lignin (Table 4), and their own characteristic reaction pathways.

Table 1

Structures, isolations, and/or treatments of Kraft lignin, organosolv lignin, and alkali lignin, and their pyrolytic behaviors

Raw material	Isolation	Treatment	Lignin	Lignin properties	Pyrolysis temperature	Pyrolytic property		Refs.
						Yield	Major compositions in oils
Commercial Kraft lignin (KL)	N/A	N/A	KL	G/S-type lignin with C = 62.45%, H = 5.28%, N = 0.27%, O = 31.01%, S = 0.16%, ash = 0.83, H/Ceff = 0.63	RT-400–700 °Ca	400 °Ca—gas/oil/char (10/21/69%); 500 °Ca—gas/oil/char (19/33/48%); 600 °Ca—gas/oil/char (24/34/43%); 700 °Ca—gas/oil/char (33/29/38%)	400–700 °Cb (S-type phenols from 58 to 72%, G-type phenols from 18 to 22%)	[188]
Norway spruce (Picea abies)	LignoBoost process	N/A	KL (Lignoboost™ lignin)	G-type lignin with HHV (dry ash free) = 27.1 MJ/kg, HHV (moist) = 18.2 MJ/kg, C = 65.1%, H = 5.8%, N = 0.1%, O = 26.1%, S = 2.5%	RT-500 °Cc	500 °Cc—char (36%)	500 °Cc (guaiacols, catechols, alkylphenols)	[116]
Black liquor of eucalypt Kraft pulping	Acid precipitation	Thermal treatment (175, 200, 225 °C for 30, 90, 150 s)	Thermal-treated KL	KL-200 °C (90 s) (exp.): G/H/S-type lignin with C = 66.30%, H = 5.63%, N = 0.11%, O = 26.07%, S = 1.70%, HHV = 26.52 MJ/kg, soluble lignin = 5.97%, insoluble lignin = 91.41%, sugars = 0.80%, ash = 1.56%	RT-550 °Cc	550 °Cd—char (~ 10%)	225 °Cc (methoxycatechol syringol, 4-methylsyringol)	[189]
Black liquor of poplar Kraft pulping	Acid precipitation	Fractionation by ultrafiltration	KL and F1 (54.3%), F2 (25.9%), F3 (15.4%), F4 (4.4%) fractionated in series by membranes with 10, 5, 1 kDa	KL/F1/F2/F3/F4: G/H/S-type lignin with Mn = 584/1141/703/484 g/mol, Mw = 1507/2640/1119/700 g/mol, Ðe = 2.58/2.31/1.59/1.44, acid-insoluble lignin (AIL) = 76.68/78.41/77.62/75.35/76.56%, acid soluble lignin (ASL) = 5.19/5.31/7.09/7.13/6.97%, total carbohydrates = 4.99/8.11/3.69/0.07/0%, ash = 0.95/1.84/1.19/1.07/1.09%	RT-500, 650, 800 °Cc	750 °Cd—char: KL (35.1%), F1 (33.8%), F2 (25.3%), F3 (31.8%)	500 °Cc: KL, F1, F2, F3 (syringol, 4-methylguaiacol, guaiacol); 650 °Cc: KL (syringol, 4-methylguaiacol, guaiacol), F1 (4-methylguaiacol, guaiacol, 4-vinylguaiacol), F2 (syringol, guaiacol, phenol), F3 (syringol, guaiacol, 4-vinylguaiacol); 800 °Cc: KL (phenol, syringol, toluene), F1 (phenol, 4-methylphenol, 2,4-dimethylphenol), F2 (syringol, guaiacol, 4-vinylguaiacol), F3 (phenol, syringol, 4-vinylguaiacol)	[154]
Black liquor of eucalypt Kraft pulping	Acid precipitation	Fractionation by organic solvents	KL and F1 (59.65%), F2 (28.70%), F3 (10.93%) fractionated in series using ethyl acetate (F1), acetate/petroleum ether (F2), petroleum ether (F3)	KL/F1/F2/F3: G/S-type lignin with Mn = 2033/2872/1611/620 g/mol, Mw = 4664/6158/2397/814 g/mol, Ðe = 2.29/2.14/1.49/1.32, C = 61.30/61.01/62.26/62.49%, H = 5.56/5.59/5.80/5.92%; N = 0.19/0.28/0.01/0.00%, O = 30.81/30.86/29.92/29.91%, S = 2.14/2.26/2.01/1.68%, O/C (mol/mol) = 0.38/0.38/0.36/0.36, H/C (mol/mol) = 1.09/1.10/1.12/1.14, HHV = 24.86/24.80/25.55/25.73 kJ/kg, S/G (unit ratio) = 2.44/2.12/2.32/2.49, β-O-4 = 3.7/12.6/2.8/0%, β–β = 1.2/2.2/0.9/0.3%, β-5 = 5.4/5.5/4.8/4.2%, aliphatic OH = 1.06/1.47/0.84/0.29 mmol/g, total phenolic OH = 3.81/2.51/3.49/4.81 mmol/g, COOH = 0.54/0.49/0.52/0.73 mmol/g, condensed phenolic OH = 0.48/0.35/0.54/0.81 mmol/g, methoxy = 6.86/6.11/6.59/7.19 mmol/g	RT-400, 500, 600 °Cf	600 °Cd—char: KL (40.61%), F1 (38.88%), F2 (33.32%), F3 (18.37%)	400 °Cb, g: KL, F1, F2, F3 (G-/S-type phenols); 500 °Cb, g: KL, F1, F2, F3 (G-/S-type phenols); 600 °Cb, g: KL, F1, F2, F3 (G-/S-/H-type phenols)	[135]
Black liquor of poplar Kraft pulping	Acid precipitation	Fractionation by gradient acid precipitation	KL (extracted under pH = 2) and LpH6 (52.5%), LpH4 (29.7%), LpH2 (17.8%) fractionated in series under pH = 6, 4, 2	KL: G/S/H-type lignin with Mn = 821/1057/703/462 g/mol, Mw = 2118/2399/1057/712 g/mol, Ðe = 2.58/2.27/1.73/1.54, C = 52.89/60.31/60.27/48.42%, H = 4.85/5.28/5.28/3.86%, N = 0.15/0.16/0.30/0.22%, O = 29.51/32.57/32.13/23.61%, S = 12.60/1.76/2.02/23.89%	RT-500, 650, 800 °Cc	750 °Cd—char: KL (35.1%), LpH6 (38.4%), LpH4 (29.1%), LpH2 (26.8%)	500 °Cc: KL, LpH6, LpH4 (syringol, 4-methylguaiacol, guaiacol), LpH2: (syringol, 4-ethylguaiacol, guaiacol); 650 °Cc: KL (syringol, 4-methylguaiacol, guaiacol), LpH6, LpH2 (syringol, 4-ethylguaiacol, guaiacol), LpH4 (3-methoxycatechol, syringol, 4-methylguaiacol); 800 °Cc: KL (phenol, syringol, toluene), LpH6 (acetosyringone, 3-methoxycatechol, phenol), LpH4 (syringol, 4-ethylguaiacol, 4-methylguaiacol), LpH2 (syringol, phenol, guaiacol)	[190]
Commercial alkali lignin (AL)	N/A	N/A	AL	G/H/S-type lignin with C = 55.3%, H = 5.3%, N = 0.1%, O = 35.2%, S = 1.3%, HHV = 20.62 MJ/kg, volatiles = 62.3%, fixed carbon = 34.9%, ash = 2.8%	RT-400, 450, 500 550, 600, 650, 700, 750, 800 °Ca	600 °C–chard (39.0%); 800 °C—chard (40.8%); 400–800 °Ca—gas/oil/char (15/25/65%)	400–800 °Cb (phenol, 2-methylphenol, 4-methylphenol, 4-ethylphenol)	[221]
Commercial alkali lignin	N/A	N/A	AL	G/H/S-type lignin with C = 60.00%, H = 7.18%, N = 0.00%, O = 29.90%, S = 2.92%, HHV = 20.62 MJ/kg, moisture = 6.2%, volatiles = 88.0%, fixed carbon = 9.4%, ash = 2.6%	RT-300, 350, 400, 450 °Ca	300 °Ca—gas/oil/solid (11.8/26.2/62.0%); 350 °Ca—gas/oil/solid (12.7/32.3/55.0%); 400 °Ca—gas/oil/solid (16.5/33.5/50.0%); 450 °Ca—gas/oil/solid (20.9/34.1/45.0%)	300, 350, 400, 450 °Cb (guaiacols, alkyl phenols, catechols)	[204]
Commercial alkali lignin	N/A	N/A	AL	G/H/S-type lignin	40–900 °Cc, i	900 °Cd—char (~ 50%)	300, 500, 900 °Cc (2-methoxy-phenol)	[222]
Commercial alkali lignin	N/A	N/A	AL	G/H-type lignin with aliphatic OH/COOH/phenolic OH/total OH/H (unit)/G (unit) = 2.36/0.38/3.35/6.09/0.27/3.08 mmol/g	RT-400, 500, 600 °Cc	N/A	400 °Cb (no obvious response); 500, 600 °Cb (2-methoxyl-4-methylphenol, acetaldehyde, 2-methoxyl-4-vinylphenol, 2-methoxyl-phenol)	[39]
Black liquor (BL)	Acid precipitation	Fractionation by ultrafiltration	AL, AL-10/5/1 kDa	AL, AL-10/5/1 kDa: G/H-type lignin with Mn = 3284/6076/4045/2616 g/mol, Mw = 7423/12,060/6752/3864 g/mol, Ðe = 2.260/1.985/1.669/1.478, G-type OH = 0.90/1.07/0.86/0.77 mmol/g, H-type OH = 0.22/0.15/0.17/0.30 mmol/g, aliphatic OH = 1.23/1.47/1.06/1.05 mmol/g, condensed phenolic OH = 1.21/1.74/1.17/1.00 mmol/g, COOH = 1.02/1.19/0.74/0.76 mmol/g	RT-400, 600, 800 °Ch	1000 °Cd—char: AL (43.06%), AL-10 kDa (38.42%), AL-5 kDa (39.27%), AL-1 kDa (36.34%)	400 °Cb: AL, AL-10 kDa (guaiacol, 4-methylguaiacol, 4-ethylguaiacol), AL-5 kDa, AL-1 kDa (guaiacol, phenol, 4-methylguaiacol); 600 °Cb: AL, AL-10 kDa, AL-5 kDa (guaiacol, phenol, 4-methylguaiacol), AL-1 kDa (phenol, 4-methylphenol, 3-ethylphenol); 800 °Cb: AL, AL-10 kDa, AL-5 kDa (phenol, indene, naphthalene), AL-1 kDa (1-ethenyl-2-methyl-benzene, indene, naphthalene), (39.27%)	[205]
Corncob residue	Organosolv method (tetrahydrofuran)	N/A	Organosolv lignin (OL)	G/S/H-type lignin with Mn = 1238 g/mol, Mw = 3203 g/mol, Ðe = 2.59	RT-800 °Ca	350 °Ca—gas/oil/char (31.5/16.3/52.2%); 800 °C—chard (36.02%)	350 °Cb (4-vinylphenol, 4-vinylguaiacol, syringol)	[223]
Pine, poplar, bamboo	Organosolv method (dioxane)	N/A	PiL (29.3%), PoL (35.2%), BaL (48.9%)	PiL: G/H-type lignin with Mn = 2580 g/mol, Mw = 9940 g/mol, Ðe = 3.85, β-O-4 (A) = 46.02%, phenylcoumarans (B) = 8.63%, resinol (C) = 5.78%, cinnamyl alcohol end groups (I) = 6.72%, S/G/H (unit) = 0/99.35/0.65%; PoL/BaL: G/S/H-type lignin with Mn = 3540/3420 g/mol, Mw = 13,240/8840 g/mol, Ðe = 3.74/2.58, β-O-4 (A) = 56.31/59.52%, phenylcoumarans (B) = 7.13/5.68%, resinol (C) = 13.56/4.16%, cinnamyl alcohol end groups (I) = 0/0%, S/G/H (unit) = 69.00/30.62/0.38% (60.97/35.79/3.24%)	RT-800 °Ca	800 °Cd—char: PiL (39.33%), PoL (30.19%), BaL (20.71%)	400–600 °Cb: PiL (guaiacol), PoL (phenol), BaL (4-vinylphenol)	[110]
Sugarcane bagasse (BG)	Organosolv method (ethanol)	N/A	BG-Lignin	G/S/H-type lignin with G/S/H (unit ratio) = 0.82/0.02/0.16; moisture = 3.78%, volatiles = 67.34%, fixed carbon = 28.80%, ash = 0.09%, phenolic OH/aliphatic OH = 0.79	RT-400, 500, 600, 700 °Cc	800 °Cd—char (29%)	400 °Cc (2,6-dimethoxy-phenol); 500 °C–600 °Cc (2,6-dimethoxy-4-(2-propenyl)-phenol); 700 °Cc (4-ethyl-phenol)	[216]
Willow biomass	Organosolv method (ethyl acetate-EAC/tetrahydrofuran-THF/γ-butyrolactone-GBL)	N/A	L-EAC (83.8%), THF (92.3%), GBL (72.6%)	L-EAC/L-THF/L-GBL: G-type lignin with C = 65.00/66.25/66.88%, H = 6.26/6.03/6.32%, N = 0.22/0.30/0.21%, O = 28.09/27.00/26.61%, ash = 0.44/0.12/0%, moisture = 4.5/4.0/4.5%	RT-500 °Ca	500 °Ca—gas/oil/char: L-EAC (22.15/34.53/43.32%), L-THF (20.97/35.21/43.83%), L-GBL (21.70/33.55/44.75%)	500 °Cb: L-EAC, L-THF (guaiacol, 4-methylguaiacol), L-GBL (4-methylguaiacol)	[220]

aA fixed bed

bGC/MS and/or GC/FID (gas chromatograph/flame ionization detection)

cPy-GC/MS

dTG-DTG

eDispersity

fU-type tube pyrolysis device

gIn situ FTIR spectroscopy

hTube furnace

iTG–MS (thermogravimetry–mass spectrometry)

Table 2

Structures and isolations of DES lignin, and corresponding pyrolytic behaviors

Raw material	DES synthesis	Isolation	Lignin	Lignin properties	Pyrolysis temperature	Pyrolytic property		Refs.
						Yield	Major compositions in oils
Populus deltoides	DESs: ChCl coupled with urea and imidazole with molar ratio of 1:2 and 3:7, followed by heating at 60 °C until a homogeneous liquid formed	Lignin regenerated and purified from pretreated Populus by DESs (115/150 °C, 15 h) via ethanol/water (1:9, v:v)	Lyophilized lignin labeled as ChU-115 (26.4%), ChI-115 (27.0%), ChI-150 (12.1%)	ChU-115/ChI-115/ChI-150: G/S-type lignin with Mw = 2562–1544 g/mol, Ðe ≤ 1.60, ASL = 7.23/8.18/3.5%, AIL = 19.2/18.9/8.5%, total carbohydrates = 5.26/3.76/1.65%, aliphatic OH = 3.61/3.65/3.60 mmol/g, total phenolic OH = 1.18/0.94/1.28 mmol/g, COOH = 1.18/0.94/1.28 mmol/g, β-O-4 = 50.3/48.3/46.9%, β–β = 10.9/13.7/6.4%, β-5 = 5.5/2.5/2.8%, S/G = 1.38/1.42/2.27	RT-650 °Ca	600 °Cb—char (ChI-115 > ChI-150 > ChU-115)	650 °Ca: ChI-115, ChI-150, ChU-115 (phenol)	[240]
Oil palm empty fruit bunch (EFB)	DESs: choline chloride/lactic acid (CC-LA) with molar ratio of 1:1 and 1:15, and choline chloride/formic acid (CC-FA) with molar ratio of 1:2, heated at 80 °C until homogeneous phase	Lignin isolated and purified from pretreated EFB using DESs (120 °C, 8 h) via ethanol/water (1:2, v:v)	DES-extracted lignin (DEEL) by LA/CC-LA (1:1)/CC-LA (1:15)/CC-FA	LA/CC-LA (1:1)/CC-LA (1:15)/CC-FA-Lignin: G/S/H-type lignin with lignin content = 75.15/78.89/80.64.85.84%, glucan = 1.42/1.94/0.00/1.39%, xylan = 5.94/0.62/1.02/0.00%, C = 52.87/52.50/53.89/47.86%, H = 5.78/5.39/5.17/5.44%, N = 0.00/1.36/0.77/2.48%, O = 41.98/40.00/38.80/42.83%, S = 0.49/0.75/1.37/1.40%, G (unit) = 13.97/29.79/49.91/35.65%, S (unit) = 83.85/64.78/50.09/62.01%, H (unit) = 2.18/5.43/0/2.34%, methoxy = 14.16/10.32/29.04/25.95%	RT-650 °Ca	900 °Cb—char (CC-FA > CC-LA 1:15 > CC-LA 1:1 > LA)	650 °Ca: LA, CC-LA (1:1), CC-LA (1:15), CC-FA (phenol)	[241]
Commercial softwood lignin (SL)	DESs: ChCl/EG (CE), ZnCl2/EG (ZE), ChCl/Aa (CA) with the same molar ratio of 1:2 at 60 °C	Lignin treated by DESs at 120 °C for 2 h and collected by acid precipitation	CEL, ZEL, CAL	CAL/CEL/ZEL: G/H-type lignin with C = 63.05/63.11/62.95%, H = 5.85/6.15/6.02%, N = 0.13/0.13/0.13%, O = 30.04/29.48/29.93%, S = 0.49/0.75/1.37/1.40, HHV = 25.76/26.22/25.94 MJ/kg, H/Ceff = 0.38/0.45/0.42, Mw = 2650/2574/2529 g/mol, Mn = 1233/1238/1204 g/mol, Ðe = 2.15/2.08/2.10, β-O-4 = 2.9/1.7/0.3, β–β = 2.3/2.2/2.4, β-5 = 4.0/3.9/4.1, G-type OH = 2.23/2.16/2.05 mmol/g, C-type OH = 0.29/0.26/0.40 mmol/g, H-type OH = 0.06/0.11/0.05 mmol/g, condensed G-type OH = 2.15/2.12/2.14 mmol/g, aliphatic OH = 0.85/1.07/1.10 mmol/g, COOH = 0.65/0.54/0.46 mmol/g, methoxy = 4.02/3.76/3.45 mmol/g	RT-550 °Ca	900 °Ca-gas/oil/char: CEL, ZEL, CAL (15/35/50%)	550 °Ca: CEL (phenol, p-cresol, guaiacol, creosol), ZEL (creosol, catechol, guaiacol), CAL (guaiacol, creosol, catechol, toluene)	[229]
Eucalyptus tenuifolia	DESs: choline chloride/formic acid (FDES) and choline chloride/lactic acid (ADES) with the same molar ratio of 1:10, heated at 60–80 °C until homogeneous phase	Raw material extracted by toluene/ethanol (2:1, v:v) for 6–8 h, followed by DESs treatment at 110 °C for 2, 4, 6 h, and lignin isolated and purified by acetone/water (7:3, v:v)	A2, A4, A6, F2, F4, F6	A2/A4/A6/F2/F4/F6: G/S-type lignin with glucan = 5.69/3.34/12.17/0/1.12/0.23%, xylan = 9.25/8.86/13.29/8.11/4.96/4.98%, galactan = 1.34/1.33/1.86/3.64/1.64/1.50%, C = 58.85/58.24/58.79/60.24/59.86/60.84%, H = 5.72/5.75/5.60/5.70/5.94/5.75%, N = 0.28/0.35/0.21/0.95/1.66/1.02%, O = 34.28/35.33/35.18/29.86/29.50/30.59%, methoxy = 23.15/22.86/21.57/23.25/23.50/22.50%	RT-800 °Cc	800 °Cb—char: F4 > A4	200–600 °Cc: products rich in aromatic structures, of which the functional groups are temperature-induced to form light gases, H2O, CO2 CO, and CH4	[236]

aPy-GC/MS

bTG-DTG

cTG-FTIR

Table 3

Structures and isolations of biological lignin, and corresponding pyrolytic behaviors

Raw material	Enzyme	Isolation	Lignin	Lignin properties	Pyrolysis temperature	Pyrolytic property		Refs.
						Yield	Major compositions in oils
Softwood (Fir), hardwood (Eucalyptus), non-wood (moso-bamboo)	Industrial cellulase (CMCase)	Enzymatic treatment (hydrolysis) of biomass using CMCase at 40 °C for 48 h, followed by lignin collection via centrifugation and purification via mild acidolysis in dioxane/acidified water (0.01 mol/L HCl, 85:15, v:v) at 87 °C	Softwood/hardwood/non-wood EMAL lignin (> 50%)	Softwood EMAL lignin: G/H-type lignin with G (unit) = 91.2%, H (unit) = 2.8%, β-O-4 = 56.1%, α-O-4 and β-5 = 19.0%, β–β = 5.3%, β-1 = 2.9% Hardwood/non-wood EMAL lignin: G/S/H-type lignin with G (unit) = 24.7/36.1%, S (unit) = 54.6/42.9%, H (unit) 1.5/21.0%, β-O-4 = 36.3/38.7%, α-O-4 and β-5 = 4.4/5.2%, β–β = 9.6/6.0%, β-1 = 2.0/0%	RT-300, 400, 500, 600 °Ca	800 °Cb—char: ~ 30%	300 °Cb: softwood EMAL lignin (coniferyl alcohol, sinapyl alcohol); 400 °Cb: hardwood EMAL lignin (coniferyl alcohol, sinapyl alcohol); 400 °Cb: non-wood EMAL lignin (4-vinylphenol, 4-vinylguaiacol, 4-vinylsringol)	[126]
Ginkgo, poplar	White-rot fungus Physisporinus vitreus	Lignin isolated from biomass using Björkman method and modified by white-rot fungus at 30 °C and 150 rpm for 48 h	Ginkgo lignin-laccase, poplar lignin-laccase	Ginkgo lignin-laccase, poplar lignin-laccase: G/H-type lignin with acid soluble lignin (ASL) = 0.32/0.29%, Klason lignin = 97.26/97.05%, carbohydrates = 1.18/1.32%, ash = 0.38/0.41%, C = 59.98/58.89%, H = 6.01/5.57%, N = 0.43/0.15%, O = 33.32/35.21%, S = 0.26/0.18%, O/C (molar ratio) = 0.42/0.45, H/C (molar ratio) = 1.20/1.13, methoxy = 11.17/15.68%	RT-400, 600, 800 °Cc	600 °C (exp.)c—gas/oil/char: Ginkgo lignin-laccase (13.8/14.5/43.3%), poplar lignin-laccase (15.5/11.4/40.7%)	600 °C (exp.)c: Ginkgo lignin-laccase (2-methoxy-phenol, vanillin2-methoxy-4-methyl-phenol), poplar lignin-laccase (2,6-dimethoxy-phenol, 2-methoxy-phenol, isoeugenol)	[249]
Four technical lignin [sugarcane bagasse steam explosion (SE), sugarcane bagasse soda-anthraquinone (SAQ), sodium lignosulfonate from eucalyptus (NaE) and sodium lignosulfonate from a mixture of eucalyptus and pine wood (NaPE)]	Lignin peroxidase (LiP), quinone reductase (OR)	Lignin treated by LiP and OR in sodium tartrate buffer (pH 3.0) at 25 °C for 24 h	SE-Lignin, SAQ-Lignin, NaE-Lignin, NaPE-Lignin	SE-Lignin, SAQ-Lignin, NaE-Lignin, NaPE-Lignin: G/S/H-type lignin with Mw = 10,126/6087/10,833/9023 g/mol, Mn = 800/1112/3165/4351 g/mol, Ðe = 12.7/5.5/3.4/2.1	RT-550 °Cd	550 °Cd—gas/oil/char: SE-E-Lignin (8.8/47.4/43.8%), SAQ-E-Lignin (22.0/40.6/37.3%), NaE-E-Lignin (21.2/27.5/51.3%), NaPE-E-Lignin (36.4/19.8/43.8%)	550 °Ce: SE-Lignin, SAQ-Lignin, NaE-Lignin (phenol), NaPE-Lignin (guaiacol)	[255, 256]
Bamboo	White-rot fungus Echinodontium taxodii	Enzymatic hydrolysis performed in sodium acetate buffer (pH = 4.8) at 48 °C for 3 days, and lignin isolated by centrifugation	Lignin from enzymatic treated EHRL (86.4%)	G/S-type lignin with G/S (unit ratio) = 0.49, and with the decreasing content of β-O-4 structure	RT-600 °Ca	1100 Kf-char: 31.64, 32.18, 33.04% at 40, 20, 10 K/min	600 °Ca: 2,3-dihydrobenzofuran, syringol, vanillic acid	[257]

aPy-GC/MS

bGC-FID

cA fixed bed reactor

dA stainless steel tubular reactor

eGC/MS

fTG/DTG

Table 4

Structures and isolations/treatments of ionic liquid lignin, and corresponding pyrolytic behaviors

Raw material	Ionic liquid	Isolation/treatments	Lignin	Lignin properties	Pyrolysis temperature	Pyrolytic property		Refs.
						Yield	Major compositions in oils
Empty fruit bunches (EFB), palm mesocarp fiber (PMF) and palm kernel shells (PKS)	Pyridinium formate [PyFor]	Biomass pretreated by [PyFor], and lignin regenerated via dissolving in acetone/water followed by acetone evaporation	EFB lignin, PMF lignin, PKS lignin	EFB lignin, PMF lignin, PKS lignin: with C = 42.02/42.95/45.59%, H = 6.48/5.70/6.21%, N = 5.74/6.56/7.02%, O = 44.59/44.63/40.90%, S = 0.18/0.16/0.28%, acid insoluble lignin = 17.82/32.23/45.54%, HHV = 27.05/27.40/28.20 MJ/kg	50–550 °Ca	800 °C (10 °C/min)b—char (exp.): EFB lignin (3.87%), PMF lignin (5.79%), PKS lignin (9.25%)	550 °Ca: EFB lignin (cyclotetradecane, naphthalene, 4-t-butylcyclohexanone), PMF lignin (naphthalene, 4-t-butylcyclohexanone, phenol), PKS lignin (phenol, 2-methoxy-phenol, 2,4-dimethylphenol)	[271, 274]
Sugarcane straw (SCS)	1-Ethyl-3-methylimidazolium acetate [Emin][OAc]	SCS pretreated by [Emin][OAc] at 90 °C for 5 h, and lignin recovered via dissolving in acetone/water followed by acetone evaporation	Recovered lignin	N/A	50–700 °Cc	700 °C—chard: 44%	350 °Cc: phenols, methanol, formaldehyde	[125]
Industrial lignin	1-Butyl-3-methylimidazolium chloride (BMIC)	Lignin pretreated in a microwave apparatus using BMIC at 50, 100, 150 °C for 30 min and precipitated using water	BMIC-lignin50, BMIC-lignin100, BMIC-lignin150	N/A	RT-300, 400, 500, 600, 700, 800°Ce	300–400 °Ce-liquid (exp.): BMIC-lignin50 (~ 0.150 g/glignin), BMIC-lignin100 (~ 0.125 g/glignin), BMIC-lignin150 (~ 0.125 g/glignin)	300–500 °Cf: BMIC-lignin50, BMIC-lignin100, BMIC-lignin150 (phenolics, arenes, alkanes)	[280]
Industrial lignin	1-Sulfonic acid butyl-3-methylimidazolium trifluoromethanesulfonate [B(SO3H)min]-OTf	Lignin pretreated in a microwave apparatus using [B(SO3H)min]-OTf at 50, 100, 150, 200 °C for 1 h under N2, and regenerated by washing with water	Lignin-50, lignin-100, lignin-150, lignin-200	Industrial lignin: ash = 3.77%, volatiles = 56.73%, C = 66.22%, H = 6.30%, O = 25.58%, N = 1.09%, S = 0.81%	RT-300, 400, 500, 600, 800°Ce	300–400 °Ce—tar (exp.): Lignin-50 (0.1889 g/glignin) lignin-100 (0.1231 g/glignin) lignin-150 (0.1338 g/glignin) lignin-200 (0.0751 g/glignin)	300–500 °Cf: Lignin-50, lignin-100, lignin-150, lignin-200 (phenol, guaiacol, 2-ethylphenol, 4-methoxyguaiacol)	[279]
Industrial lignin	1-Butyl-3-methylimidazolium dihydrogen phosphate [Bmin]H2PO4	Lignin pretreated in a microwave reactor using [Bmin]H2PO4 at 50, 100, 150 °C for 30 min, and washed out by water	Lignin-50, lignin-100, lignin-150	Industrial lignin: moisture = 2.6%, ash = 2.5%, volatiles = 62.4%, C = 63.9%, H = 5.6%, O = 28.6%, N = 1.1%, S = 0.8%	RT-300, 400, 500, 800 °Ce	300–400 °Ce-liquid (exp.): Lignin-50 (~ 0.15 g/glignin) lignin-100 (~ 0.12 g/glignin) lignin-150 (~ 0.12 g/glignin)	300–500 °Cf: lignin-50, lignin-100, lignin-150 (phenolics, arenes, alkanes)	[270]

aPy-GC/MS

bTG-DTG

cTG-FTIR

dTG-DTG

eA vertical fixed-bed quartz reactor

fGC/MS

Kraft lignin

Kraft lignin (a kind of technical lignin) is generated from Kraft pulping process in the pulp and paper industries from black liquor, among which sulfide solutions (i.e., sulfuric acid) is commonly used [177]. In the delignification process, hydrogen sulfide would react with lignin. Although these sulfur-containing components would be decomposed at the later stage of cooking process, the formed elemental sulfur can combine with hydrogen sulfide to produce polysulfide, which still leads to 2–3% sulfur content in the Kraft lignin [178]. For example, organic sulfur-containing species in Kraft lignin are presented in forms of free sulfur, sulfides, sulfites, sulfones, sulfates, disulfides, polysulfides, thiols, etc. [179, 180]. Han et al. investigated the evolution of sulfur-containing compounds during Kraft lignin pyrolysis [181]. During pyrolysis process, the formed sulfur-containing compounds in pyrolytic products can be presented in forms of H2S, SO2, CH3SH, CH3SCH3, and CH3SSCH3. On the other hand, the role of inorganic sulfur compounds in the pyrolysis of Kraft lignin was reported by Dondi et al. that the presence of sulfates as oxidizers can increase the amount of CO2 formed at high pyrolytic temperatures (> 200 °C), higher than the theoretical value of CO2 production from carboxyl groups in lignin [182]. However, the remaining sulfur content in Kraft lignin is disadvantageous for its application on pyrolysis due to the acidity of generated oils and air pollution during pyrolysis due to the release of foul-smelling sulfur compounds [152, 183]. Furthermore, sulfur contaminations would also inhibit the depolymerization of Kraft lignin [184]. Therefore, before being used in pyrolysis, sulfur removing would be necessary to improve the oil production. For example, many methods, such as adsorption, sodium hydroxide treatment, the oxidation of thiols and sulfides to sulfoxides and sulfones followed by organosolv extraction, direct sulfur extraction by organic solvents, recovering organic sulfur compounds by P(III)-based systems as well as elemental sulfur recovery with heavy metals and sodium sulfite, and neutralization of acidic and basic sulfur-containing compounds to form salts, have been cited for reducing sulfur content [180].

The produced Kraft lignin mainly consists of guaiacyl- and syringyl-type units, and also contains considerable amounts of phenolic hydroxyl due to the extensive cleavage of β-O-4 linkage during pulping process [185, 186]. Therefore, massive studies have used Kraft lignin as pyrolytic subject to produce abundant phenolic products in recent years. Zhang et al. investigated the pyrolytic behaviors of synthetic Kraft lignin by TG–FTIR (thermogravimetric–Fourier transform infrared spectrometry) and Py-GC/MS techniques, and the resulted volatiles include H2O, CO2, CO, alkyls, carbonyls, alkenes, and aromatics (where guaiacol is the main component) [187]. Fan et al. studied the pyrolysis process of a commercial Kraft lignin, and the maximum oil yield can be obtained at 550–600 °C. The further increase of pyrolytic temperature would cause a significant increase in gas production, while have no obvious effect on char generation. Among phenolic products, S-type phenols occupy the main proportion (i.e., ~ 70%) from 400 to 700 °C. Besides, the proposed radical-mediated reaction processes during pyrolysis was proposed including lignin homolysis at 400–450/450–600 °C (to form active lignin radicals, such as phenolics), and radicals recombination at 600–700 °C (to generate some low-molecular-weight gases and char/coke) [188]. Thermal treatment was performed to treat Kraft lignin before pyrolysis via Demuner et al. to investigate the pyrolytic behaviors of thermally treated lignin. Results show that the thermal treatment promotes demethylation and demethoxylation [189]. On the other hand, various fractionations (e.g., fractionations via organosolv method [135], ultrafiltration [154], and gradient acid precipitation [190]) were used for the treatment of Kraft lignin. For example, Chen et al. fractionated Kraft lignin into different lignin fractions (F1, F2, and F3) and further investigated their pyrolysis characteristics [135]. Results show that lignin fractions with different molecular weight distributions, linkages type, functional groups content, and S/G ratio can be obtained, where lignin with more methoxy contains the stronger cracking of β aryl ether bonds [191]. Thermal stability of lignin shows that the smaller molecular weight, the faster maximum degradation rate, and the less char residue generated, which indicate that lower molecular weight leads to worse thermal stability with lower activation energy. Lower temperatures are disadvantageous for monomers production while good for oils generation, and the opposite trend can be obtained at higher temperatures. Ultrafiltration fractionation also influences the distribution of molecular weight of Kraft lignin, where the high-molecular-weight lignin fraction favors the generation of G-type compounds, and the low-molecular-weight one prefers S-type compounds. Temperature rising would cause the cleavage of methoxy of G- and S-type compounds to produce H-type ones [154]. Similarly, the lignin fractionation via gradient acid precipitation also affects molecular weight, which has an obvious effect on relative content of formed products from lignin pyrolysis [190].

Alkali lignin

Alkali lignin is a byproduct obtained from paper industry, which is produced by alkaline pulping procedure for separating lignin from the alkali lignin waste containing cellulose and lignin using NaOH and Na2S, which contains a large distribution of molecular weight [192, 193]. During cooking process, NaOH is commonly used as the chemical reagent to separate and degrade lignin fraction, wherein the cleavage of phenolic α-O-4, and non-phenolic/phenolic β-O-4 linkages, and the combination of Na+ and phenolic hydroxyl/carboxyl via chemical bonding to form phenolic-Na+ and carboxyl-Na+ groups happen simultaneously [194, 195], leading to obvious changes of lignin structure and significant influences on lignin pyrolysis via reducing activation energy [196].

For figuring out the influence of Na+ species on lignin pyrolysis, Dalluge et al. investigated the effect of Na treatment on lignin char and volatiles formations during fast pyrolysis, suggesting that the Na treated lignin exhibits the increasing yields of char (due to the catalytic effect derived from Na species [197]), the enhanced gasification of lignin [198] and the highest selectivity to aromatic volatiles from lignin pyrolysis compared to other alkali metals (e.g., Li, K, Cs) [199]. According to the above studies, Na species bonded with organic phase (e.g., –ONa+ and –COONa+) is a key factor for enhancing the conversion of alkali lignin. Guo et al. investigated the effect of Na groups on the production of lignin pyrolysis products [198]. The effect of different Na chemical forms (including organic/inorganic bonding Na groups, Or-/Inor-Na) on the condensable product composition is obtained that both two chemical forms of Na have the significant catalytic effect on phenolic hydroxyls removing to enhance the yield of benzenes (e.g., methoxybenzene, 1,2-dimethoxy-benzene, and 1,2,3-trimethoxy-benzene), and also have a positive effect on cracking alkyl substituents. The corresponding mechanism can be proposed that the β-O-4 linkage in lignin can be cleaved easily at low temperatures to generate alkyl guaiacols, of which the alkyl groups would be further eliminated by Or-Na, and Inor-Na is beneficial for removing phenolic hydroxyl to generate benzenes. Therefore, the quality of lignin oils obtained from pyrolysis process can be improved significantly via effective oxygen elimination [200, 201]. For the generation of light gases, both two Na chemical forms reduce the cracking of ether bond and methoxy to form CO and CH4, respectively. For condensed phase, char conversion with temperature indicates that both two Na chemical forms benefit gasification reaction due to their significant catalytic effects [202]. For Or-Na loaded char, char conversion rate is mainly influenced by the relative distribution of Na on char surface. At lower temperatures, the strong bonding strength of O–Na linkages inhibits the migration of Na element to the porous surface of char, leading to low catalytic activity. At higher temperatures, O–Na bonding strength becomes weaker, which is beneficial for Na adsorbing on char surface for enhancing catalytic activity [203]. For Inor-Na (i.e., NaCl) loaded char, the retention of Cl− greatly affects the catalytic activity of Na+ on char conversion. Besides, with increasing temperature, Na+ tends to combine with CO2 (which is formed from lignin pyrolysis) to generate Na2CO3, which significantly deteriorates the catalytic activity [203].

Expect for Na+ species, other parameters, like temperature, reaction time, and molecular weight, also have significant effects on alkali lignin pyrolysis. For example, the effect of temperature and residence time on thermal decomposition reactions during fast pyrolysis of a softwood alkali lignin was investigated by Supriyanto et al. and the results show that there is a general increase in the yield of organic volatiles (of which the majority is G-type phenols) with the increase of temperature from 400 to 600 °C, wherein the cleavage of the lignin polymeric structure to form linear carbonyl (acetaldehyde) and G-type aromatic compounds is enhanced by increasing temperature [39]. On the other hand, the promoted effect of residence time (from 0.5 to 5 s) on lignin pyrolysis is significant at a lower temperature (i.e., 500 °C), while the extension of residence time at a higher temperature (i.e., 600 °C) would lead to more secondary cracking reactions to inhibit the further increase of aromatic volatile compounds generation. Biswas et al. demonstrated that increasing temperature benefits oil production, and the higher temperature prefers to alkyl phenols and catechols via demethylation, demethoxylation, and deoxygenation [204]. Guo et al. investigated the effects of molecular weight on the pyrolysis products properties of alkali lignin, and the results show that the molecular weight of alkali lignin is not significantly influenced on the temperature and species of products evolution, while is positively affected on the yields of CH4, CO, phenols, aromatic products. The lower molecular weight benefits the cracking of methoxy of lignin to generate CH4, CO, CO2, phenol, and alkyl phenol, but the higher molecular weight favors the generation of guaiacol and alkyl guaiacol. Besides, the molecular weight of formed aromatic compounds is influenced by both lignin molecular weight and pyrolysis temperature [205].

Organosolv lignin

Due to the low requirement for strong acids or bases, sulfur absence, simple downstream separation, and solvent recycling, organosolv fractionation using ethanol (the most commonly used) [206-209], ethyl acetate [210], acetone [211], etc., can be used as an efficient and economical method to separate lignin from lignocellulosic biomass. In organosolv fractionation, cellulose fraction can be remained in solid phase, and removed via filtration. Lignin fraction can be separated via precipitation (e.g., by adding excessive water in the obtained previous liquid containing hemicellulose and lignin fractions) and collected by centrifugation/filtration, which contains better solubility (in many organic solvents) and higher purity with lower structural modification compared to those of lignin obtained Kraft and soda processes [212].

Yuan et al. obtained lignin from different lignocellulosic biomass materials, like pine (softwood), eucalyptus (hardwood), and corn stalk (herbaceous feedstock), and bamboo (herbaceous feedstock) via organosolv fractionation using 96% dioxane as organic solvent, and investigated the structural effect on phenolic production [158]. Herbaceous-derived lignin shows higher molecular weight and dispersity compared to other lignin obtained from softwood and hardwood, suggesting the generation of heterogeneous lignin structure [213]. Thermal stability is directly related to lignin structure (e.g., the content of methoxy [191]), which indicates that the higher dispersity, the lower yield of char residue, suggesting the worse thermal stability [214]. For deeply understanding the correlation between lignin structure and phenolic production, lignin pyrolysis was conducted at 500 °C, and the results show that lignin can be mainly decomposed into phenolic compounds, of which the distribution is significantly influenced by different lignin types. The majority of 4-vinylphenol (H-type phenol) can be obtained from the pyrolysis of herbaceous lignin (i.e., from corn stalk and bamboo) due to the dominant H-type structure and abundant β-O-4 linkage in herbaceous lignin after organosolv fractionation, and demethylation and demethoxylation reactions during pyrolysis (to convert G-/S-type phenolic hydroxyls into H-type one via reducing the content of methoxy) [110, 215]. Soongprasit et al. used sugarcane bagasse (BG) as raw material for lignin separation (i.e., BG-lignin) using organosolv method (95% ethanol) and investigated its phenolic production from fast pyrolysis using Py-GC/MS technique [216]. With the temperature rising, several interconversion reactions are all enhanced, such as (1) S-/G-type phenols converted to H-type ones via demethoxylation reaction of methoxy; (2) H-type phenols converted to aromatic hydrocarbons via dehydroxylation reaction [217, 218]; (3) monolignol compounds converted to hydrocarbons via dealkylation [127]. On the other hand, temperature rising also makes a significant influence on phenolic selectivity via enhancing the cleavage of methoxy and other functional aromatic substituent groups [219], leading to the generation of oxygenated-alkyl methoxy phenols (OR-Ph-OCH3), alkyl methoxy phenols (R-Ph-OCH3), methoxy phenols (Ph-OCH3), alkyl phenols (R-Ph), and phenols (Ph), where (1) the oxygen elimination from OR-Ph-OCH3 at C4 positon via deoxygenation would form R-Ph-OCH3 and Ph-OCH3; (2) the cleavage of methoxy from Ph-OCH3 via demethoxylation would generate Ph and/or R-Ph (especially at high temperatures due to the high BDE of methoxy); and (3) the gasification of Ph via secondary cracking would produce hydrocarbons or other oxygenated volatiles [163]. Wang et al. investigated the influence of solvent fractionation (including ethyl acetate-EAC, tetrahydrofuran-THF, and γ-butyrolactone-GBL fractionations) on lignin pyrolysis [220], finding that different structures of lignin separated using different organic solvents via organosolv fractionation (i.e., EAC lignin contains the most oxygen-containing functional groups, GBL-lignin has the highest content of large-molecule fragments, and THF-lignin possesses the highest Tmax at 398 °C) result in the different pyrolytic behaviors. For example, during pyrolysis, more intense cleavage of Cα–Cβ linkage can be obtained in GBL-lignin, while the C1–Cα linkage of in EAC- and THF-lignin is more fragile to be broken. After pyrolysis, (1) EAC-lignin mainly yields more guaiacol and 4-methylguaiacol via the cleavage of C1–Cα and Cα–Cβ linkages, (2) THF-lignin produces more guaiacol, 4-ethylguaiacol, and 4-methylguaiacol via cleaving C1–Cα, Cβ–Cγ, and Cα–Cβ linkages, and (3) GBL-lignin generated the dominant 4-methylguaiacol via breaking the Cα–Cβ linkage.

DES (deep eutectic solvents) lignin

Deep eutectic solvents (DES), composed of hydrogen bond donor and acceptor, is an eco-friendly, economical and non-toxic method used for lignin extraction [224-227]. DES can reduce lignin molecular weight via cleaving weak bonding linkages, like β-O-4, which is conductive to improve the subsequent lignin pyrolysis efficiency [135, 228]. Three different DESs [i.e., choline chloride/acetic acid (CA), choline chloride/ethylene glycol (CE), and zinc chloride/ethylene glycol (ZE)] were used by Li et al. to modify softwood Kraft lignin (SKL) for improving the pyrolytic products distribution [229]. TG-DTG analysis shows significant difference of lignin pyrolytic behaviors during the temperature of 250–600 °C, where the maximum degradation temperature (Tmax) of DES treated lignin increases, indicating the higher thermal stability caused by the removal of unstable chemical linkages, such as β-O-4. The decreasing content of lignin char after pyrolysis (especially for lignin treated by CE) indicates that DES treatment is beneficial for char inhibition. The volatile products distribution shows that G-type phenols are the major compounds due to the nature of Kraft lignin extracted from black liquor [230, 231]. Among all phenolic compounds, G- and H-type phenols are generated by lignin side-chain fragmentation and free radical polymerization, while C-type phenols are mainly derived from side-chain fracture and thermal demethylation of other types of monophenols [232, 233]. During pyrolysis, G-type phenols can be gradually transformed into H-type ones due to the enhanced cleavage of methyl aryl ether bond caused by DES treatment. On the other hand, a small amount of mono aromatic hydrocarbons (MAHs) can also be observed, formed via secondary reactions, such as dehydroxylation and demethoxylation at high temperatures [234]. In addition, compared to untreated lignin, DES-treated samples can produce more MAHs due to their improved hydrogen to carbon efficient ratio (i.e., H/Ceff) [235]. Furthermore, more phenolic products containing carbon number between C6 and C9 can be produced from DES-treated lignin pyrolysis, suggesting the positive effect of DES treatment on the generation of monophenols.

Li et al. extracted lignin with ChCl-formic acid/lactic acid systems (FDES/AEDS) for the comparative investigation of lignin structure, thermal stability, and pyrolytic products distribution [236]. The results show that lignin molecular weight can be reduced through DES treatment via initial lignin depolymerization [237], such as β-O-4 dissociation. On the other hand, DES treatment can also dissociate lignin–carbohydrate complex (LCC) and lignin substructures (e.g., aryl ether and carbon–carbon bonds) to purify lignin and make structural degradation. During pyrolysis, different stages can be observed, including drying stage (from 25 to 150 °C, including moisture removing) and pyrolysis stage (from 200 to 350 °C, mainly involving β-O-4 degradation; from 350 to 400 °C, mainly involving lignin side-chain oxidation; > 400 °C, mainly involving aromatic rings saturation and carbon–carbon bonds breaking; 400–600 °C, mainly involving the cleavage of methoxy group) [238], and lignin extracted from ADES contains more side chains and lower thermal stability compared to those of FDES extracting lignin. Volatiles releasing during pyrolysis shows that some low-molecular-weight gaseous products (e.g., CO, CO2, CH4, and H2O) are formed from the escape of functional groups outside the aromatic rings of lignin, where methoxy, methyl, and methylene are the main sources of CH4, CO2 is formed by decarboxylation and/or decarbonylation, CO is formed by the cleavage of ether bonds, and H2O mainly comes from dehydroxylation [239]. Furthermore, the yield of aromatic products of lignin increases with richer contents of non-condensable gaseous products after DES treatment, indicating that DES treatment is beneficial for thermal decomposition of lignin during pyrolysis.

Biological lignin

Biological treatment (an environmentally friendly method with low energy consumption) of lignin with assistance of fungus or bacterium has been recently reported as an effective pathway to facilitate lignin pyrolysis, including increasing thermal conversion rate and pyrolytic selectivity of lignin to specific products, decreasing pyrolytic temperature and activation energy [242-244]. For example, bio-treated bamboo lignin using white-rot fungi contained lower thermal stability, which can be decomposed into more G-type phenols through fast pyrolysis [245]. Lignin generated from bio-treatments (e.g., using cellular ligninolytic enzymes like laccase and peroxidases) can obtain certain structural modifications, of which the mechanism is based on the lignin structure oxidation and degradation (e.g., lignin side chains oxidation, demethoxylation, demethylation, and some linkages cleavage) [246-248]. For deeply understanding the effect of biological treatment on lignin pyrolysis, Wang et al. used a white-rot fungi in the bio-treatment of softwood ginkgo and hardwood poplar, where ligninolytic enzymes modified lignin structure and enhanced pyrolytic efficiency [249]. For example, oil production can be significantly improved after lignin enzymatic modification at all reaction temperatures, which is due to the decreasing content of C–C bonds in treated lignin samples [250], leading to the enhanced depolymerization of lignin structure, especially at higher temperatures. Besides, ether bonds (which can be cleaved at lower temperatures) are dominant in lignin interunit linkages, which are much easier to be decomposed compared to C–C bonds [251, 252], resulting in the significant increase of bio-oil from lignin (e.g., at 400 °C, Ginkgo lignin treated by Laccase yielding 52.2% oils, higher than 49.8% oils obtained from untreated Ginkgo lignin; at 400 °C, Poplar lignin treated by Laccase producing 51.9% oils, higher than 46.5% oils obtained from untreated Poplar lignin [249]). Besides, bio-treatment can also reduce the content of methoxy via enzymatic oxidation [253] and demethylation [254], thus decreasing char yield at high temperatures (e.g., at 800 °C, Poplar lignin treated by Laccase generating 21.2% char, lower than 23.2% char obtained from untreated Poplar lignin [249]). The selectivity of specific products of lignin can be improved significantly after bio-treatment, where G-/S-type phenols obtained from treated Poplar lignin can be effectively transformed into phenol at 800 °C due to the further temperature-induced cracking, including demethylation, demethoxylation, decarbonylation, and dealkylation in side chains [168].

Ionic liquid lignin

The strong electrostatic interactions between ions endow ionic liquid (ILs) with negligible vapor pressure and low flammability, which is beneficial for their applications under high-vacuum conditions without contamination problems. Also, their nature and properties can be adjusted by changing the chemical structures of both cations and anions according to specific applications [258, 259]. On the other hand, ILs can be recovered from the pretreated mixture by adding anti-solvents (e.g., ethanol or H2O, which would cause the generation of impurities in recovered ILs) [260], reverse micelle method (which can extract almost pure [Mmim] and [DMP] from pretreated mixture), or membrane distillation (separating ILs and water) [261].

Some ILs have been used as solvents for lignocellulosic biomass pretreatment, such as 1-butyl-3-methylimidazolium chloride ([Bmin][Cl]), 1-hexyl-3-methylimidazolium chloride [Hmin][Cl], 1-octyl-3-methylimidazolium chloride ([Omin][Cl]) [262], 1-ethyl-3-methylimidazolium acetate [Emin][OAc] [263, 264], and 1-butyl-3-methylimidazolium acetate [Bmin][OAc] [265]. Due to the high solubility of lignin (of which the mechanism is proposed to be realized by breaking H-bonds in lignin and combining the aromatic nucleus and aliphatic chain of lignin [266]), low energy consumption, environmentally friendly, solvent recycling, and low cost for synthesis [267, 268], many ILs have been used for lignin extraction from biomass, such as [Bmin][Cl], [Bmin][OAc], 1-ethyl-3-methylimidazolium lysinate [Emin][Lys], triethylammonium hydrogen sulfate [TEA][HSO4], and N,N-dimethylethanolammonium succinate ([DMEAS]) [269]. On the other hand, IL-treated lignin sample can exhibit the improved yields of pyrolytic oils and phenolic compounds during lignin pyrolysis due to the cleavage of hydrogen, ester, and ether bonds in lignin through IL treatment [270]. Rashid et al. used a protic ionic liquid pyridinium formate [PyFor] to extract lignin from various palm biomass, such as empty fruit bunches (EFB), palm mesocarp fiber (PMF), and palm kernel shell (PKS) [271], and three kinetic models (i.e., Flynn–Wall–Ozawa (FWO), Kissinger–Akahira–Sunose (KAS), and Starink) were used to investigate the activation energy of [PyFor] extracted lignin. Thermal stability of different lignin samples depends on their functional groups, intermolecular bonds, extraction methods, and condensation degree [272]. For example, due to the presence of increased branching/condensed structures and higher lignin content with higher molecular weight, higher thermal stability can be obtained [273-275]. Furthermore, heating rate is another important factor for lignin pyrolysis, indicating that the increasing heating rate would increase the reaction temperature and reduce the reaction period by accelerating pyrolysis [265, 276, 277]. Except for the nature of IL-extracted lignin, the secondary intra-particle reactions are also important factors in exothermic behaviors and thermal runway, thus having a significant effect on the kinetic mechanism and the magnitude of activation energy during pyrolysis [274, 278]. Halder et al. confirmed that the IL treatment would lead to the cleavage of β-O-4 bond in lignin and then cause the improved generation of phenolic compounds from lignin pyrolysis [125]. Lei et al. also found that the tar obtained from the pyrolysis of 1-sulfonic acid butyl-3-methylimidazolium trifluoromethanesulfonate [B(SO3H)min][OTf]-treated lignin (of which the content of aryl ether increases and that of fatty ether decreases) is mainly phenols and phenol derivatives, accounting for > 90% of all compounds, wherein the improved yields can be obtained for phenol, cresol, guaiacol, 2-ethylphenol, 4-ethyl-2-methoxy-phenol, and 4-methoxyguaiacol in light tar (of which the yield increases by 1.5 times compared to that of untreated lignin) [279].

Catalytic pyrolysis using zeolites

Zeolite-driven lignin catalytic pyrolysis with high MAHs selectivity

Table 5 shows the recent progress of some effective catalysts used in lignin catalytic pyrolysis for producing aromatic hydrocarbons (AHs), mainly including zeolites, carbon-based, and some metal-based catalysts. During catalytic pyrolysis, the main reaction pathway is divided into two parts, including in situ and ex situ catalytic pyrolysis. The feature of in situ catalytic pyrolysis is that the catalyst is mixed with lignin and then put into reactor together for pyrolysis, while ex situ one refers to the process of direct pyrolysis of lignin to form pyrolytic volatiles and then contact with the catalyst to obtain secondary catalytic pyrolysis [72].

Table 5

Recent progresses of catalysts used in lignin catalytic pyrolysis, and their selectivity

Lignin	Catalyst	Catalytic pyrolysis	Reaction conditions	Products yield	Important findings	Product selectivity	Ref.
Kraft lignin	Aluminosilicate	In situ	450, 550, and 650 °C, 12,500–40,625 °C/s, 6 s, He	N/A	HZSM5-30 showed the most promising anti-coking performance and the highest selectivity to desired products, HZSM5-500 showed good diffusion and high reaction rate, and the anti-coking performance of HY/MCM41 was weaker than HZSM5	Hydrocarbons selectivity: HZSM5-30 > HY > HZSM5-300/MCM41-40/MCM41-Si	[311]
Beech wood lignin	Micro/meso porous ZSM-5	In/Ex situ	400, 500, and 600 °C, 20 min, N2	Organic phase: 15–35 wt%; char: ~ 40 wt%; gas: < 20 wt%	Both two catalysts exhibited excellent dealkoxylation/aromatization reactivity to yield more aromatics. Meso-ZSM-5 induces higher dealkoxylation reactivity, leading to higher selectivity to BTX aromatics without the increase of PAHs	MAHs selectivity: meso-ZSM-5 > ZSM-5	[312]
Cellulolytic enzyme lignin	Micro-meso ZSM-5	In-situ	873 K, 30 s	Char: ~ 30 wt% > coke: ~ 15 wt% > aromatics: ~ 8 wt% > phenolics: ~ 3 wt% > catechols: ~ 2 wt%	Mesoporous structure was beneficial for the diffusion of heavy phenols and modulation of pyrolysis products	AHs selectivity: C6 > C8 > C10+ ≈ C7 > C9+ > C14+	[281]
Rice straw lignin	Modified ZSM-5	In situ	450, 500, 550, and 600 °C	N/A	These ZSM-5 catalysts showed shape selectivity and acidity, beneficial for pyrolytic products distribution, and demethoxylation and dehydroxylation of oxygenates	Hydrocarbons selectivity: (without catalyst) oxygenates > phenols > PAHs > MAHs; (with ZSM-5) PAHs > MAHs ≈ oxygenates ≈ phenols; (with alkali ZSM-5) PAHs > MAHs > phenols > oxygenates; (with Ni-ZSM-5) MAHs ≈ PAHs > oxygenates > phenols. MAHs: naphthalenes with 40–60%	[47]
Commercial lignin	Modified HZSM-5	Ex situ	500 °C (I) and 450–600 °C (II), 20 °C/min, N2	Organic liquid: 17.5–22.7 wt%; solid: 42.7–43.2 wt%; gas: 19.2–19.8 wt%	HZSM-5 treated by organic alkali exhibited a coordinated micro/meso-proportion with proper size and acidity, of which the acidity would be further enhanced after cobalt incorporation, exhibiting better MAHs selectivity	Alkali treated HZSM-5 preferred phenols, while Co-alkali-HZSM-5 exhibited much higher selectivity to MAHs (38%) than phenols (23%)	[313]
Commercial lignin	HZSM-5/biochar	Ex situ	500 °C, 10 min, N2	Oil: 35 wt%; total AHs: 50 mg/g (maximum)	LC (lignin carbon) incorporating lignin depolymerization produced more phenols, which can be further transformed into aromatic hydrocarbons through HZSM-5	The production of AHs from lignin/LC/HZSM-5 was almost two times higher than lignin/HZSM-5 (from 30 to 50 mg/g)	[297]
Alkali lignin	ZSM-5/biochar	In situ	500 °C, 10 min, N2	Oil: ~ 20 wt%; char: ~ 40 wt%; gas: < 20 wt%; aromatics: > 30 mg/g	The addition of biochar enhanced bond breaking of lignin to yield more oils, and ZSM-5 acted as a selective aromatization to obtain higher content of aromatics	Total aromatics (12.32%) > methoxyphenols (5.17%) > alkylphenols (4.4%) > phenols (2.42%) > acid (0.85%)	[314]
Corn cob lignin	HZSM-5@Al-SBA-15	In situ	550 °C, 10 °C/min, N2	Gas: ~ 35 wt%, water: < 10 wt%; organic liquid: < 15 wt%	Mixed zeolite with tailored properties of acidity and porosity regulated the composition of AHs by pre-cracking and enhanced diffusion	AHs selectivity: MAHs (~ 40%) > PAHs (~ 25%) > phenols (~ 13%) > aliphatics (~ 8%) > methoxyphenols (~ 0%)	[293]
Commercial lignin	Pine-Mo2C	In situ	300, 400, and 500 °C, WHSV = 1 h−1, H2(N2)	Total AHs: 12.36 wt%; light gases: 29.68 wt% (maximum)	Pine carbon supported Mo2C catalyst showed good selective deoxygenation targeting C-O cracking to produce more monocyclic aromatic hydrocarbons	Deoxygenation rate: pine-Mo2C (100%); MAHs selectivity: toluene (98%) > others (benzene and xylenes, < 2%)	[298]
Enzymatic hydrolysis lignin	Nb2O5	In situ	500–650 °C, 0.5 min	Phenols: ~ 4 wt%; MAHs: ~ 6 wt%	Nb2O5 exhibited excellent deoxygenation ability to convert lignin into AHs, especially for MAHs	AHs selectivity: C6+C7+C8+C9+C9+ (MAHs, up to 90%) > C10+C11+C12+C12+ (PAHs, up to 8%)	[303]
Kraft lignin	Biochar, activated carbon	In situ	550 °C, 5 min, N2	Oil: 13.15 wt%; char: 58.76 wt%; gas: 39.74 wt% (maximum)	The catalytic effect of biochar was derived from surface sodium and alkali metals. The addition of AC resulted in the high-phenol-concentration oils production	Products selectivity: phenols > PAHs > oxygenates	[296]
Bagasse lignin	Ca0.5Pr0.5FeO3	In situ	20 °C/min, 2 h, N2	Oil: ~ 25 wt%; char: > 50 wt%; gas: > 40 wt% (maximum)	Guaiacols, syringols, and phenols were the main component in pyrolytic oils, and the content of light aliphatic hydrocarbons increased after catalysts addition	Products selectivity: Guaiacols > syringols > phenyl ethers > phenolics > phenyl ketones	[306]
Bagasse lignin	La0.8M0.2FeO3 (M = La, Ca, Sr, Ba)	In situ	600 °C, 10 °C/min, 2 h, N2	Oil: ~ 25.73 wt%; char: > 40.65 wt%; gas: > 42.89 wt% (maximum)	Perovskites improved the generation of aliphatic hydrocarbons via inhibiting decarboxylation and decarbonylation, and increased aryl oxygen-containing compound yield	LaFeO3, La0.8Ca0.2FeO3, La0.8Sr0.2FeO3, and La0.8Ba0.2FeO3 produced the maximum selectivity of phenolics (24.59%), syringols (25.78%), guaiacols (23.79%), syringols (22.47%), respectively	[307]

Among all catalysts, zeolites have been widely used in lignin catalytic pyrolysis due to their availability, low cost, thermal stability, acidity, porosity, and excellent catalytic selectivity and charring inhibition capacity [44, 281–284]. Huang et al. [48] used five types of parent zeolites [HZSM-5 (25), HZSM-5 (85), Al-MCM-41, HY, and USY] in lignin pyrolysis, among which HZSM-5 (25) is the most effective one to produce AHs (BTX), showing the highest selectivity of 56.56%. Kumar et al. found that Y-zeolite is the most effective one for demethoxylation and dehydroxylation of both small and bulky oxygenates in lignin catalytic pyrolysis as compared to mordenite and ZSM-5 [285]. Some modifications further enhance the catalytic activity and selectivity to AHs, such as alkali treatment and metal incorporation. After alkali treatment (i.e., NaOH), the pore properties and acidic sites density of zeolites are all changed, with the enhanced performance on cracking bulky oxygenates (such as phenols) to produce AHs with sharper selectivity [47, 286, 287]. After metal incorporation (Fe, Co, Ni, Cu, Zn, Ga) to form bi-functional zeolite catalyst, deoxygenation and aromatization reactions are enhanced to sharply increase the selectivity to AHs (or MAHs), due to the increased mesoporous surface area, average size of parent zeolites, and enhanced lignin mass-transfer efficiency. The modification of zeolites conducted by Jin et al. obtained the highest MAHs content of 29.3% over Co-HZSM-5, which is also attributed to its better inhibition of carbon deposition [288]. In addition, Ni-ZSM-5 obtained the maximum selectivity of hydrocarbons at 72% [47] and Fe-ZSM-5 obtained the maximum selectivity to C2H4 at 80% and naphthalene at ~ 50% [289]. ZrO2/ZSM-5 realized the significant reduction of oxygen content from 30 to 10 wt% (with a higher share of aromatics and lower heavy components) [290], Zn-HZSM-5 improved total aromatics from 31.1 to 46.1 mg/g [291], and double-layer metal supported core–shell (ZSM-5@MCM-41, Z@M) catalysts (Me1Z@Me2M) showed synergistic effect on the promotion of MAHs selectivity via phenols, immoderate aromatization, and polymerization inhibitions [292]. Mixed zeolite, like HZSM-5@Al-SBA-15, was confirmed with both pre-cracking and enhanced diffusion (Al-SBA-15), and shape AHs selectivity (HZSM-5), which can improve MAHs production while inhibit PAHs generation [284, 293].

Carbon-based materials, such as activated carbon (AC), has also been confirmed as effective catalysts in upgrading pyrolysis of lignin, due to their well-developed pore structures and abundant acidic surface groups. Furthermore, AC has been investigated as an effective catalyst for the selective generation of phenols (the heavy components in bio-oils) [294, 295]. Yang et al. also confirmed that AC (produced from steam activation of lignin char) has the great potential to be used as upgrading catalyst for lignin catalytic pyrolysis. The catalytic effect of AC derived from surface sodium and alkali metals, and the enhanced diffusion efficiency for reactive intermediates attributed to its inside mesopores were believed to be the important determinant of high activity and selectivity of AC to produce guaiacol-rich oils. Another important factor is its efficient inhibition to tar production and char agglomeration [296]. Therefore, many studies focused on the combination of carbon-based materials and zeolites, on one hand, to increase intermediates yield via cleaving C–O bonds on carbon-based materials, on the other hand, to generate more AHs via sharp selectivity of zeolites. For example, HZSM-5/lignin char catalyst prepared by Zhang et al. both showed high depolyermization of lignin (to generate more small-molecular-weight intermediates) and created the increased yield of total aromatics (from 29.5 to 50.1 mg/g). Besides, the addition of char can also alleviate the deactivation of HZSM-5 caused by coke deposition [297].

Other catalysts-driven lignin catalytic pyrolysis

Other types of catalyst were also used in lignin pyrolysis (shown in Table 5), such as Mo2C, Nb2O5, and perovskites. Due to the similar properties to noble metal catalysts, transition metal carbides, which have good catalytic performance (such as C–O cleavage and deoxygenation abilities for Mo2C under H2 condition), were used in lignin catalytic pyrolysis. In situ pyrolysis products of biomass can be used as carbon source and supporter for carburizing Mo precursor to produce biomass-Mo2C, which would contain more activity to realize carbonization and metal reduction in one step [298]. On the other hand, lignin bonds breaking and deoxygenation can be achieved under normal pressure via biomass-Mo2C to obtain high yield of MAHs (13.26 wt%) with high selectivity to toluene (> 98%) and high deoxygenation ratio of > 95% [298]. Some metal oxides were also introduced in lignin catalytic pyrolysis, such as Fe2O3, CuO, ZnO, and CaO, which can also increase AHs yield and reduce heavy components in oils [299, 300]. Among these catalysts, niobium pentoxide (Nb2O5) has gained much attention in lignin catalytic pyrolysis both in batch- and fixed-bed reactions [301-303]. Lewis acid sites endow niobium pentoxide with high catalytic activity in hydrodeoxygenation of lignin or its derivatives [304], exhibiting high AHs yield at 11.2 wt% with extremely high selectivity of MAHs at 94% due to its efficient inhibition of PAHs and coke/char formation and effective deoxygenation ability [303]. Finally, perovskite-type oxides, due to their high activity, high stability, strong resistance to poisoning, low cost, and excellent properties of transporting oxygen ions and electrons, have played an important role in catalytic reactions [305]. They have also been selected as effective catalysts in lignin catalytic pyrolysis, such as Ca0.5Pr0.5FeO3 [306], La0.8M0.2FeO3 (M = La, Ca, Sr, Ba) [307], LaTixFe1−xO3 [308], and LaTi0.2Fe0.8O3 [309, 310]. The main component in bio-oils obtained after catalytic pyrolysis over perovskite-type oxides is aryl oxygen-containing compounds with high selectivity (from 60 to 80%, such as phenolics, guaiacols, syringols and phenylates) instead of MAHs, while the inhibition of decarboxylation and decarbonylation can reduce the generation of CO/CO2 and increase aliphatic hydrocarbons fracture on aromatic rings [307].

Co-pyrolysis with other hydrogen-rich feedstock

According to the description above (“Catalytic pyrolysis using zeolites” section), zeolite catalysts are applied widely for improving the quality of lignin-based oils via deoxygenation to increase the production of AHs, although their yields are relatively low owing to the low H/Ceffective ratio (or the low key hydrogen index) of mere lignin used [315]. On the other hand, the addition of catalysts would lead to the formation of coke which decreases the production of oils and affect the pyrolysis efficiency. The co-pyrolysis is a popular method to improve the oil quality via combination of lignin with other hydrogen-rich feedstock, such as the co-pyrolysis of lignin with plastics (a common hydrogen-rich substrate) [316, 317]. On the other hand, due to the massive agricultural, industrial and human activities, biomass and plastic wastes (e.g., polyethylene, polypropylene, polystyrene, polyvinylchloride, and polyethylene terephthalate [318-320]) have been remained with a huge production annually, which significantly requires us to take actions for their highly effective utilizations. Co-pyrolysis is a feasible and simple thermochemical technology for achieving the goal of high-efficiency utilization of these common wastes in our life due to the same heating system with pyrolysis technology without any significant adjustment [321]. Furthermore, blended substrates placed in the co-pyrolysis technique would produce more yields and wider distributions (i.e., MAHs, PAHs, and other long-chain hydrocarbons) of pyrolytic products as compared to those of single lignin used due to the synergistic effect (Table 6) [64, 322]. The quality of formed oils can be improved via co-feeding with plastics to increase the C/H content [323], and the heating value of condensable products obtained from co-pyrolysis would also be enhanced obviously [324]. Esso et al. summarized some important parameters, such as blending ratio, heating system (including heating rate and reaction temperature), and catalyst used on the synergy effect between biomass and co-feedings [316]. Lignin is hydrogen-deficient component in lignocellulosic biomass only with H/Ceffective range of 0–0.3; hence, the hydrogen donors (such as low-density polyethylene, high-density polyethylene, phenol–formaldehyde resins, polyolefins, and spent bleaching clay) can be used for promoting hydroprocessing (such as hydrogenolysis and/or hydrogenation) of lignin oxygenates species to increase the yield of AHs [55, 325–330]. Typically, hydrogen radicals produced from the thermal degradation of hydrogen donors were beneficial for lignin oils and char upgrading via hydrocracking, hydrogenolysis, dehydration, oligomerization, and polymerization [64]. On the other hand, some studies also focused on the enhancement of oil production and char evolution via co-pyrolysis, such as lignin–collagen [331], lignin–cellulose [123, 124], lignin–waste oil [61], lignin–oil shale [332], lignin/cellulose/sawdust-coke bottle [333], and lignin–coal [334, 335], of which the detailed information is listed in Table 6. Through co-pyrolysis, not only lignin but also other kinds of wastes with low-efficient utilization can achieve their valorizations.

Table 6

Detailed information of lignin co-pyrolysis

Blending mixture	Catalyst	Reactor	Synergistic effect	Yield	Selectivity	Ref.
Lignin/low-density polyethylene (LDPE)	HZSM-5	A thermogravimetric analyzer	1. The synergistic effect decreased the starting temperature of pyrolysis and accelerated the decomposition rate 2. The composition of pyrolysis products contained more alkane and aromatic hydrocarbons	800 °C—char: lignin > lignin + LDPE > lignin + LDPE + HZSM-5 > LDPE	Lignin + LDPE + HZSM-5: aromatics, alkanea	[325]
Lignin/plastics (PS)	Red clay (RC)	A micro reactor	The synergistic effect increased the yield of guaiacol	900 °Cb—char: lignin (14.9%), lignin/PS (6.04%), lignin/PS/RC (33.54%); 500 °Cc—lignin-/PS-/lignin + PS-/lignin + PS + RC-derived compounds: 0.81/6.03/4.67/14.67%	Lignin (guaiacol, 60.41%), lignin/RC (guaiacol, 67.37%), lignin/PS (styrene-C8, 70.22%), lignin/PS/RC (styrene-C8, 86.86%)	[317]
Lignin/phenol–formaldehyde resins (PF)	HZSM-5	A vertical pyrolysis reactor	The synergistic effect improved the yield of aromatic amines	650 °Cc—total compounds/aromatic amines: PF (24.5/14.2%), lignin (7.2/3.7%), lignin/PF = 1/5 (22.0/13.3%)	650 °Cc: lignin (simple phenols, 75.62%, catechols, 14.49%, aromatic hydrocarbon, 9.89%) lignin/PF (simple phenols, 84.16%, dimers, 6.30%, aromatic hydrocarbons, 4.23%), PF (simple phenols, 83.2%, aromatic hydrocarbons, 8.6%, dimers, 6.80%)	[326]
Lignin/spent bleaching clay (BC)	N/A	A fixed-bed reactor system	1. The synergistic effect promoted the production of P-type phenols and aromatic hydrocarbons, and the inhibition of oxygenates species 2. The addition of spent bleaching clay reduced the activation energy and improve the oil quality	550 °C—gas/oil/char: BC (~ 9/25/66%), lignin (~ 34/24/42%), lignin/BC = 1/1 (~ 19/25/57%)	550 °Cc: BC (aliphatic hydrocarbons), lignin (phenols), lignin/BC = 1/1 (H-type phenols)	[329]
Lignin/polyolefins	N/A	A fixed-bed reactor	1. Liquid yield was improved by adding polyolefins due to the formation of lower poly-hydrocarbons derived from polyolefins 2. The yield of gasoline and kerosene was climbed, revealing that lignin pyrolytic products enhanced the cracking of polyethylene (PE) intermediates 3. The rearrangement reactions of polypropylene (PP) intermediates enhanced liquid production via inhibiting the formation of solid	650 °C—gas/liquid/Wax/char: lignin/PE (~ 10/40/25/20%), lignin/PP (~ 10/50/15/20%)	Lignin + PE: hydrocarbons like > C26 and C19-C25, ad diesel (C14–C18)c; Lignin + PP: hydrocarbons like > C26 and C11–C13, and gasoline (C5–C10)c	[327]
Lignin/waste cooking oil (WCO)	HZSM-5	A Py-GCMS system	The addition of waste cooking oil in lignin with appropriate catalyst-to-feedstock ratio contributed to high selectivity to aromatics via enhancing alkylation and demethoxylation	823 Kc—feedstock conversion rate: lignin (~ 65%, phenolics, MAHs), WCO (~ 100%, MAHs, PAHs), lignin/WCO = 1/1 (~ 85%, MAHs, PAHs)	823 Kc: lignin (phenolics, MAHs, ~ 65%), lignin/WCO = 1/1 (MAHs, ~ 75%), WCO (MAHs, ~ 60%)	[61]
Lignin/collagen	N/A	An applied test system, Inc. series 3210 vertical tube furnace	1. Collagen addition benefited the formation and evolution of char with abundant oxygenated poly-aromatic structures 2. Collagen addition improved the hydrogen aromaticity index via reducing aromatic substitution and/or facilitating the removal of functional groups 3. Collagen acted as a binder for lignin to form stronger fused framework	600 °C—char: lignin (45.1%), lignin/collagen (45.4–48.4%), collagen (24.9%); 1000 °C—char: lignin (41.8%), lignin/collagen (42.2–43.6%), collagen (22.6%)	600 °Cd—C:O/C:H/C:N (aromatic ratio of char): lignin (3.21/0.90/0), lignin/collagen (3.17/0.84/32.26), collagen (2.32/0.54/3.18)	[331]
Cellulose/lignin/sawdust	N/A	A self-made fixed-bed reactor	1. Interactions between the volatiles generated from cellulose and sawdust promoted oil production 2. Repolymerization happened between light species from cellulose and heavy species from lignin to generate more condensable liquids 3. Interaction between heavy species from lignin and sawdust created more carbonaceous char	500 °C—gas/oil/char: cellulose (28.1/55.6/16.3%), sawdust/cellulose (11.5/71.0/17.5%), sawdust (25.2/50.0/24.8%), lignin (8.5/39.6/51.9%), sawdust/lignin (17.5/41.5/41%)	500 °Cc: lignin (phenols), cellulose (sugars, aldehydes, ketones), sawdust (sugars), sawdust/lignin (phenols, aldehydes, ketones), cellulose/sawdust (aldehydes, ketones), cellulose/lignin (sugars)	[123]

aTG-FTIR

bTG-DTG

cGC/MS, GC/FID

dElemental analysis

Condensing and separating processes of pyrolytic oils

The determination of oil compositions can be achieved by Py-GC/MS [222], and volatile evolutions can be detected by TG-FTIR [205] during the pyrolysis reaction. In addition, through dissolving oils in some specific solvents (e.g., isopropanol), GC/MS/FID, 2D-GC/FID, or NMR techniques can be used to obtain their chemical compositions/structures [116, 204]. Gooty et al. proposed a condensing system consisting of two cyclonic condensers (i.e., condensers 1 and 3), an electrostatic precipitator-cum-condenser (i.e., C-ESP), and a cotton wool filter for pyrolytic oils collection [336]. The generated vapor/gas flows through condenser 1, C-ESP, condenser 3, and the cotton wood filter in series, wherein the liquid yield can be obtained by measuring the weight of cyclonic condensers and C-ESP before and after each run, and oil deposit can be recovered with a specially designed scraper [337]. However, the complexity of oil composition makes the subsequent separation difficult. So far, solvent extraction is an efficient method for products separation. For example, Deng et al. performed the extraction of phenols from bio-oil aqueous fraction using hydrophobic ionic liquids (i.e., [Bmin][NTf2]), where the extraction efficiencies of acetic acid, phenol, guaiacol, and 2-methylguaiacol in aqueous fraction were 2.71, 95.41, 92.04, and 97.98% [338]. Yao et al. extracted and recovered phenolic compounds from aqueous solution by thermo-separating magnetic ionic liquid aqueous two-phase system (two polypropylene glycol, PPG600-based thermo-separating magnetic ionic liquid aqueous), where the extraction efficiencies of phenol, o-cresol, and m-cresol were higher than 95% [339]. A hydroxyl-functionalized ionic liquid (i.e., [C2OH-4-pic][NO3]) was used by Xu et al. to extract phenolic compounds from model coal tar, which obtained the extraction efficiency of 98.99, 98.39, 98.65, and 99.99% for m-cresol, o-cresol, p-cresol, and phenol, respectively [340]. A binary petroleum ether/dichloromethane solvent (PE/DCM) was used by Yang et al. to extract aromatic monomers from lignin oils, of which the extraction efficiency was 80% [341]. In addition, PAHs can be efficiently extracted by various techniques, such as supercritical and subcritical fluid extraction, microwave-assisted solvent extraction, plant oil-assisted extraction, and some microextraction techniques using less organic solvents [342].

Summary and future perspective

In this review, we introduced pyrolysis technology for lignin conversion and further lignin oils upgrading via catalytic pyrolysis using zeolites and co-pyrolysis with other hydrogen-rich feedstock. Different lignin samples, such as Kraft lignin, alkali lignin, organosolv lignin, DES lignin, biological lignin, and ionic liquid lignin, and their corresponding pyrolytic behaviors were presented, which indicated the effect of lignin type, reaction temperature, and time on lignin pyrolytic properties. Lignin pyrolysis can be mainly divided into three stages (initial, primary and charring stages), where light gases (H2O, CO2, CO, CH4), phenolic compounds (G-/S-/H-/C-type phenols), and char with aromatic fused-ring structures can be obtained. In addition, zeolites and other catalysts (activated carbon, Mo2C, metal oxides, and perovskites) were used for lignin oils upgrading to generate AHs via deoxygenation. Finally, hydrogen-rich co-feedings were applied to form more AHs (MAHs, PAHs) via increasing H/Ceff ratio of blending substrates and generating hydrogen radicals from hydrogen donors during co-pyrolysis.

In spite of huge effort put on lignin pyrolysis, there still some challenges. Some suggestions are made below for the future perspective.

Lignin is a natural source of phenolic compounds, of which the production of G-/S-/H-/C-type phenolic compounds are majorly determined by the composition and content of corresponding phenolic units in lignin. For example, G-type phenolic compounds (e.g., guaiacol) can be significantly produced from G-type lignin. However, the complexity of lignin structure always leads to the complexity of formed phenolic products (mainly including G-/S-/H-type phenolic compounds). The efficient removal of methoxy from lignin can adjust and regularize lignin structure to improve the selectivity of generated phenolic compounds (which is beneficial for the formation of H-type phenolic compounds). On the other hand, the removal of methoxy can reduce the formation of light gases, which is beneficial for lignin conversion to liquid products.

Holocellulose can also be converted into phenolic compounds via the promotion of specific catalysts. Furthermore, electronegative products and radicals generated from lignin pyrolysis can be involved in the secondary reaction of polyhydroxy volatiles from holocellulose. Therefore, further investigations should be made on concerning the interactions between volatiles of lignin and holocellulose, which can be solved by isotope-labeled model compounds with typical functional groups together with the control of pyrolysis conditions.

For lignin catalytic pyrolysis, other capacities (except for deoxygenation) of catalysts used should be obtained, such as hydrogenation, alkylation, decarbonylation, and demethylation, to avoid the generation of phenolic compounds with distinct substituents. The development of promising catalysts used for lignin upgrading will never be an outdated researching topic for a long time.

Co-pyrolysis is an efficient method, and will be a main direction of lignin pyrolysis in the future. Hydrogen donors provided from other co-feedings are significantly beneficial for oil hydroprocessing to generate high yield of AHs. On the other hand, these co-feedings used in co-pyrolysis can be produced from agricultural, industrial, and human activities in large quantities annually. Therefore, lignin co-pyrolysis with other new co-feedings and their pyrolysis mechanisms should be investigated in the near future.

Hydrogen provided by lignin itself (self-hydrogen transfer) used for lignin hydrogenolysis has been a popular researching topic in recent years, which can also be applied in lignin pyrolysis with certainly controlling pyrolysis conditions, reactor designed, and/or catalysts used.