Upgrading end-of-line residues of the red seaweed Gelidium sesquipedale to polyhydroxyalkanoates using Halomonas boliviensis.

Agar extraction from Gelidium and Gracilaria red seaweed species produces hundred thousand ton of carbohydrate-rich residues annually. Gelidium sesquipedale waste biomass obtained after agar extraction, still contained 44.2 % w/w total carbohydrates (dry-weight basis). These residues were biologically up-graded to poly-3-hydroxybutyrate (P3HB) after saccharification of their carbohydrate fraction to simple sugars. A combined hydrolysis treatment using sulfamic acid followed by enzymatic hydrolysis with cellulases produced a glucose-rich hydrolysate with a negligible content of inhibitors. With this treatment a sugar yield of circa 30 % (g glucose/g biomass) was attained. The algal hydrolysates were assessed as carbon source for the production of P3HB by the halotolerant bacteria Halomonas boliviensis. A cell concentration of 8.3 g L-1 containing 41 % (w/w) of polymer and a yield (YP/S ) of 0.16 gpolymer/gglucose were attained in shake flask assays. In this work, cellulose-rich seaweed waste was shown to be an upgradable, sustainable source of carbohydrates.

Introduction

n class="Chemical">Polyhydroxyalkanoatespan> (n class="Chemical">PHAs) are a family of biodegradable polyn class="Chemical">esters with recognized advantages over synthetic plastics. These polymers are composed of hydroxyalkanoic acid monomers forming chains with variable molecular weight (50–1000 kDa). Different types of monomers and arrangements are possible conveying thus different properties and applications to PHAs. Applications can range from daily uses in packaging to niche areas in the medicine field such as the fabrication of resorbable medical devices like sutures, meshes, implants, and tissue engineering scaffolds. Drug release applications have also been reported [1]. Despite the obvious advantages, their commercialization has limited success. A high production cost caused mainly by the price of the carbon-source and a difficult downstream step encompassing either the use of high volumes of organic solvents or multiple steps when using aqueous solutions for PHA separation, remain the main weaknesses to reach a competitive price in the plastic sector [2,3]. To reduce the cost of the raw materials, several waste streams have been tested [[4], [5], [6]] including cellulose-rich agricultural residues such as sugar cane bagasse [7] and wheat straw [8]. These renewable feedstocks have been tested as carbon platforms for PHA production with promising results [9,10]. To be used as carbon-source by most microbes, cellulose and hemicellulose need to undergo hydrolysis and release simple sugars. However, due to the high lignin content of lignocellulosic biomass (approx. 15–25 % of the dry-weight) [11], the pre-treatment step aiming at delignification of the biomass (and some hemicellulose degradation), generally involves harsh conditions like high temperatures (160–240 °C) and pressures (0.7 and 4.8 MPa) (High Pressure Saturated Steam) that can be followed by an explosive decompression (Steam Explosion). Alternatively, acid (e.g. H2SO4, HCl) or alkaline (NaOH, KOH, NH4OH) pre-treatments have also been applied either to hydrolyse hemicellulose or remove the lignin, respectively [12,13]. Depending on the conditions used in the pre-treatment, toxic compounds may be released that are harmful to the microbes in the subsequent biological process. Those compounds result from the further degradation of simple monosaccharides as glucose and xylose to furan aldehydes, namely hydroxymethyl furfural (HMF) and furfural, respectively, as well as from the monomers of lignin.

Because man class="Chemical">crpan>on class="Species">algae, also called sean class="Chemical">weed, lack lignin and have a high carbohydrate content (50–70 % dw) they are considered potential carbon platforms for many bioprocesses [14]. Seaweeds are classified in three groups: green (Chlorophyta), brown (Phaeophyta) and red (Rhodophyta). Particularly concerning the carbohydrate fraction, seaweed includes characteristic complex polysaccharides that are typical from marine biomass: green seaweed contain ulvan, while brown seaweed present alginate and fucoidan and red species contain agar or carrageenan [15,16]. Besides these characteristic polysaccharides, seaweed have glucose polysaccharides (glucans) like cellulose, starch and laminarin. Cellulose is present in all groups while starch exists in green and red algae and laminarin is typical of brown species (Table 1). Macroalgal polysaccharides are classified according to their biological function in two groups: storage and structural polysaccharides. While starch and laminarin are examples of reserve polysaccharides of green and brown algae, respectively, structural polysaccharides like cellulose and agar (red algae) belong to the cell wall of macroalgae. Cellulose reaches approximately 15 wt % of dry biomass in red macroalgae [17].

Table 1

Typical storage and structural polysaccharides of the three macroalgae groups and the monosugars resulting from their complete hydrolysis.

Seaweedgroup	Examples	Polysaccharides		Major monosaccharides upon hydrolysis
		Storage	Structural	Storage	Structural
Red	Gelidium sesquipedale,Gracilaria sp.	Floridean starch	CelluloseAgar	glucose	glucoseD-galactoseanhydro-D-galactose (L- AHG)
	Chondrus crispusGigartina papillata		CelluloseCarrageenan		glucoseD-galactoseanhydro-D-galactose (L-AHG)
Green	Ulva lactuca,Ulva pertusa	Starch	Ulvan	glucose	glucosexyloseL-rhamnoseglucuronic acididuronic acid
			Cellulose		glucose
Brown	Laminaria hyperborea,Fucus vesiculosus,Macrocystis pyrifera	Laminarin+ mannitol	Alginate	glucose + mannitol	mannuronic acidguluronic acid
			Fucoidan		fucoseD-xyloseD-galactoseD-mannoseglucuronic acid
			Cellulose		glucose

Typical storage and structural papan class="Chemical">n class="Chemical">polysaccharides of the three maclass="Chemical">pan> class="Chemical">croalgae groups and the monosugars resulting from their complete hydrolysis.

Sean class="Chemical">wpan>eed n class="Chemical">wastes from phycocolloid extraction industries are n class="Chemical">carbohydrate-rich materials which, in most cases, are underexploited. Some authors have already considered the use of waste seaweed biomass for the production of bioethanol [18,19]. These residues contain mainly cellulose and some phycocolloid leftovers that are potential sugar feedstocks for the production of value-added chemicals and materials. Their utilization using a biorefinery perspective enhances the sustainability of the seaweed industry through the complete valorisation of the carbohydrate fraction besides phycocolloid extraction.

In this papan class="Chemical">n class="Chemical">work, residues of the red class="Chemical">pan> class="Chemical">agarophyte Gelidium sesquipedale, also called Gelidium corneum, supplied by a local agar-extraction plant, were used. The residues still contained significant amounts of cellulose and agar which were tested as sugar platforms for the production of poly-3-hydroxybutyrate (P3HB). This red alga is abundant in the Western Europe and Morocco coasts [20] and is harvested mainly for the extraction of agar. Agar consists of two fractions: agarose and agaropectin. Agarose is the gelling component, while the agaropectin has only a low gelling ability. Industrial agar extraction is carried out in boiling water for 4 h, after which the solution is separated from the residue by filtration [20]. The extraction yield is generally not complete (60–85 %; personal communication) and thus residues of agar are present in the solid waste. To produce a sugar-rich hydrolysate, Gelidium residues must undergo hydrolysis. Unlike terrestrial biomass that contains lignin, the complete hydrolysis of the carbohydrates in seaweed residues potentially does not require a pre-treatment step, the enzymatic step alone being enough for the release of simple sugars. Yet, the presence of agar leftovers hampers the processing of high biomass loads and for that reason a dilute acid pre-treatment was carried out to break the agar to oligosaccharides. The enzymatic hydrolysis of the Gelidium solid wastes was carried out with a mixture of cellulases and β-glucosidase.

A halophilic bacterial species, able to consume the maipan class="Chemical">n n class="Chemical">sugars inpan> the class="Chemical">pan> class="Chemical">Gelidium hydrolysate and to accumulate high amounts of PHAs, was selected from literature. Halophiles have properties that make them desirable in industrial biotechnology processes due to their tolerance to high salt concentrations and the ability to work at high pH values. This allows to operate in non-strict sterile conditions, facilitating large-scale continuous cultivation and potentially decreases operational costs, rendering PHA production processes more competitive. Besides, the selection of a halophilic strain was a logic choice due to the high salt concentration in seaweed hydrolysates. In this work, Halomonas boliviensis [21,22] a halotolerant bacteria able to consume glucose and galactose released from Gelidium residues, was chosen.

Materials and methods

Raw biomass

n class="Species">Gelidium sesquipedalepan> residues obtained after pan> class="Chemical">agar-agar extraction n class="Chemical">were a courtesy of Iberagar SA- Sociedade Luso-Espanhola de Colóides Marinhos, Portugal. Upon reception, biomass was maintained at −18 °C. When needed, it was washed several times under tap water and residues such as shell fragments and sand were removed manually. The biomass was left to dry at room temperature for 24 h and was subsequently frozen at −80 °C before lyophilisation (Christ, model Alpha 1−2 LD plus). The lyophilised biomass was subsequently blended using a coffee grinder (1 min in pulses of 10 s) to attain even pieces of biomass and was left in a desiccator till use.

Enzymes

Cellulase complex (n class="Chemical">Npan>S 22086) and β-glucosidase (pan> class="Chemical">NS 22118) from Novozymes® (Bagsvaerd, Denmark), n class="Chemical">with an activity of 1000 Biomass Hydrolysis Unit (BHU (2))/g and 250 CelloBiase Unit (CBU)/g, respectively, were used. The cellulase complex activity was determined using the procedure described in the NREL/TP-510-42628 technical report [23], while the β-glucosidase activity determination followed the protocol described by [24]. NS 22086 had a filter paper activity of 111.2 Filter Paper Unit (FPU)/mL, while NS 22118 had a cellobiase activity of 20.1 CBU/mL. Filter paper Grade 1 from Whatman and cellobiose (≥99 %) from Sigma Aldrich, respectively, were used in the activity assays.

Amylolytic enzymes, pan class="Chemical">namely α-amylase from n class="Species">Bacillus amyloliquefaciens (>250 Kilo Novo alpha-amylase Unit (KNU/g) from Sigma and amyloglucosidase (NS22035) from Novozymes (750 AmyloGlucosidase Unit (AGU /g) were used in the enzymatic assays for starch determination.

Chemicals

The chemicals used n class="Chemical">wpan>ere n class="Chemical">sulphuric acid 96 % (An class="Chemical">cros Organics), sulfamic acid (VWR Chemicals), phosphoric acid 85 % (Pancreac Quimica), di-potassium hydrogen phosphate 99 % (Pancreac Quimica), potassium di-hydrogen phosphate 98 % (Pancreac Quimica), (D)+ glucose anhydrous 99.5 % (Fischer Chemical), D(+) galactose ≥98 % (Carl Roth Chemicals), 5-hydroxymethylfurfural ≥98 % (Sigma Aldrich), hydrochloric acid min. 37 % (Riedel-de Haën) and calcium carbonate min.99 % (Merck).

Microorganism and culture media

pecies">Halomonas boliviensis DSM 15516 [22] was selected from literature for its ability to synthesize polyhydroxyalkanoates from glucose and galactose, the monosugars released upon the hydrolysis of cellulose and agar, respectively.

Strain storage

n class="Species">Halomonas boliviensis DSM 15516pan> n class="Chemical">was purchased from the DSMZ collection and activated n class="Chemical">with HM medium described in Quillaguaman, 2004 [22]. This medium had the following composition (g/L): NaCl, 45.0; MgSO4.7H2O, 0.25; CaCl2.2H2O, 0.09; KCl, 0.5; NaBr, 0.06; peptone (Difco), 5.0; yeast extract (Difco), 10.0; glucose, 1.0, and 2.0 % granulated agar (for solid medium).The pH was adjusted to 7.5 by using 1 M KOH. The solid cultures were renewed monthly to reactivate the microorganisms.

n class="Chemical">Cupan>ltures of n class="Species">H. boliviensis n class="Chemical">were stored at −80 °C in 2 mL micro tubes containing 300 μL of glycerol and 1500 μL of a previously grown liquid culture in the late exponential phase prepared with seed culture medium [25,26] and supplemented with 20 g/L of glucose.

Seed medium and inoculum preparation

The inopapan class="Chemical">n class="Chemical">culationclass="Chemical">pan> medium (or n class="Chemical">seed medium) for n class="Species">H. boliviensis contained: 45 g/L of NaCl; 25 mL/L of a 100 g/L MgSO4 x 7 H2O solution; 0.55 g/L K2HPO4; 2.3 g/L NH4Cl; 15 g/L, Tris; 3 g/L monosodium glutamate (MSG) and 0.005 g/L FeSO4 x7 H2O. Solutions of NaCl (300 g/L) and MgSO4 x7 H2O (100 g/L) were prepared and sterilized separately to avoid precipitation during the sterilization in the autoclave. After all salts were dissolved the pH was adjusted to 7.5 with 37 % (w/w) HCl.

The n class="Species">H. boliviensispan> inopan> class="Chemical">culum was prepared by transn class="Chemical">ferring the contents of a microtube (2 mL) to 500 mL shake flasks containing 76.5 mL of seed medium; 15 mL of a 300 g/L NaCl solution; 2.5 mL of a 100 g/L MgSO4 x 7 H2O solution and 4 mL of a 500 g/L glucose solution to attain a total volume of 100 mL. Cultivations were carried out in an orbital shaker at 30 °C and 170 rpm. After circa 24 h, when the culture reached an O.D.600nm of 5 (exponential phase), a given volume was withdrawn and used as inoculum in the production assays.

Production medium

The medium for n class="Chemical">P3HBpan> production inpan> shake flasks assays (medium A) conpan>tainpan>ed: 45 g/L pan> class="Chemical">NaCl; 50 mL/L of 100 g/L MgSO4 .7 H2O; 2.2 g/L K2HPO4; 1.0 g/L NH4Cl; 0.005 g/L n class="Chemical">FeSO4 .7 H2O; 15 g/L Tris and 20 g/L of MSG. Solutions of NaCl (300 g/L) and MgSO4.7 H2O (100 g/L) were prepared and sterilized separately to avoid precipitation during the sterilization in the autoclave. In a particular study to determine the influence of the nitrogen content on P3HB production, different concentrations of NH4Cl (0 or 1 g/L) and MSG (0; 5; 10 g/L) were tested. After all salts were dissolved the pH was adjusted to 7.5 with 37 % (w/w) HCl.

For the gron class="Chemical">wpan>th on G. n class="Chemical">sesquipedale hydrolysates, a 20-fold concentrated production medium was prepared. The pH of this concentrated medium n class="Chemical">was not adjusted as previously. The concentrated NaCl and MgSO4 .7 H2O were also prepared and sterilized separately.

Algal biomass characterization

The compositional apan class="Chemical">nalysis of the n class="Chemical">waste seapan> class="Chemical">weed biomass was determined following several established procedures. To determine ash, moisture and total solids in the algal biomass the procedure described in the Technical Report NREL/TP-5100-60956 procedure was followed [27]. These determinations were done in triplicate. A pre-conditioned crucible (575 °C in a muffle furnace overnight) was weighed and 100 mg of lyophilized Gelidium biomass added. The sample was then placed in a convection drying oven at 60 °C for at least 18 h until constant weight, thus allowing the determination of total solids and moisture.

To determine the ash copan class="Chemical">ntent, the cooled n class="Chemical">crucible conpan>tainpan>inpan>g the dried sample n class="Chemical">was subsequently put in the muffle furnace at 575 °C using the temperature gradient according to the n class="Chemical">NREL protocol. The cooled sample was then weighed and the ash content determined.

The determinatiopan class="Chemical">n of total n class="Chemical">carbohydrates follopan> class="Chemical">wed the procedure in Van Wychen & Laurens, 2013a [28] and was initiated by the hydrolysis of 25 mg of biomass with 250 μL of 72 % (w/w) sulphuric acid in glass tubes, at 30 °C. After an hour the hydrolysate was diluted to a final concentration of 4% (w/w) sulphuric acid with 7 mL of demineralised water. Samples were then placed in an autoclave for one hour at 121 °C. Once the samples were cooled to room temperature, an aliquot was taken for neutralization to pH 6–8 using calcium carbonate. Centrifugation was then applied (9167 g, 5 min), to separate the solids after neutralization and the supernatant collected for sugar quantification. These determinations were done in triplicate.

Total fibre, protein apan class="Chemical">nd n class="Chemical">lipid conpan>tenpan>ts (% dry-n class="Chemical">weight) n class="Chemical">were evaluated using AOAC official methods of analysis: AOAC Method 991.43 for the determination of the total fibre, AOAC 960.52 for the determination of protein and the conventional Soxhlet extraction for lipid determination. The mineral composition was assessed by nitric-perchloric digestion and Inductively Coupled Plasma- Atomic Emission Spectrometry (ICP-AES) for P, Na, K, Ca, Fe, Cu, Zn determination, while nitric-perchloric extraction followed by ICP-AES analysis was used for Cr and Pb assessment. All these determinations were performed in duplicate.

Production of Gelidium sesquipedale hydrolysates

Mild acid hydrolysis took place at 121 °C and 1 bar. Difpapan class="Chemical">n class="Chemical">ferenpan>t catalysts, catalyst concenpan>trationpan>s, conpan>tact times anpan>d biomass conpan>cenpan>trationpan>s pan> class="Chemical">were tested. Sulfuric acid, phosphoric acid and sulfamic acid were evaluated as catalysts at various concentrations namely: 0.25, 0.5 and 1.0 % (w/v) for H2SO4; 0.5, 1.0 and 1.5 % (w/v) for H3PO4 and 1.0, 1.5 and 2.0 % (n class="Chemical">w/v) in the case of sulfamic acid.

The efn class="Chemical">fepan>ct of the biomass load on the hydrolysis degree was also examined. This was carried out n class="Chemical">with sulfuric acid as catalyst and a contact time of 30 min. This assay was performed with a constant working volume by changing the biomass load resulting in biomass concentrations of 2.1 %, 4.3 % and 8.6 % (w/v).

The biomass n class="Chemical">wpan>as n class="Chemical">weighed in 50 mL glass flasks and 10 mL of acid n class="Chemical">was added to each flask. These flasks were then sealed with a rubber stop and an aluminium cap and placed in the autoclave. After chemical hydrolysis, aliquots from the three samples were centrifuged (9167 g, 5 min) and supernatant samples prepared for sugar determination by HPLC.

Enzymatic hydrolysis papan class="Chemical">n class="Chemical">was carried out at 50 °C anclass="Chemical">pan>d pH 4.8 for 30 h under conpan>tinpan>uous magnpan>etic stirrinpan>g (660 rpm). This was accomplished in a thermostatically controlled incubator chamber (JP Selected). The assays were performed with different biomass concentrations in 50 mL glass flasks with a total volume of 10 mL. The enzyme cocktail consisted of 10 μl cellulase /mL plus 7.5 μL β-glucosidase/mL (V enzyme solution/ V biomass suspension) using 10 x diluted enzyme solutions. This corresponded to adding 1.1 FPU/mL of cellulase complex (n class="Chemical">NS 22086) and 0.15 CBU/mL of β-glucosidase (NS 22118) to 10 mL of seaweed slurry. The best enzyme ratio (cellulase: β-glucosidase) was previously defined (results not shown). Previous assays have indicated that the enzymatic hydrolysis is complete within 30 h. Aliquots from the supernatant were taken during the hydrolysis and the sugar concentration determined by HPLC. The assays were carried out in duplicate.

Prior to use, the commercial enzyme solutiopan class="Chemical">ns n class="Chemical">were diluted 10 times n class="Chemical">with milli Q water to ease the handling of the originally viscous solutions. The presence of glucose was detected in both commercial enzyme solutions. This reducing sugar is most probably used as preservative in the formulation. Glucose concentration was determined at the onset of each enzymatic assay and its concentration deduced from the final glucose concentration obtained after polysaccharide hydrolysis.

The combined hydrolysis of the papan class="Chemical">n class="Chemical">algal biomass class="Chemical">pan> class="Chemical">was performed by chemical pre-treatment followed by enzymatic hydrolysis. After pre-treatment, the pH of the algal slurry was adjusted to 4.8 with NaOH 8 M and enzyme addition took place so as to reach the concentrations given above. The enzymatic hydrolysis was carried out for 30 h at 50 °C and 660 rpm. After 30 h aliquots were taken, centrifuged at 9167 g for 5 min and prepared for sugar quantification.

Production of larger volumes of hydrolysate for growth and P3HB production assays

To produce larger volumes of n class="Chemical">Gelidium hydrolysatepan>, a 2 L shake flask n class="Chemical">with a n class="Chemical">working volume of 700 mL and a biomass load of 8.6 % (w/v) was used. Hydrolysis, combining dilute acid pre-treatment with 0.5 % (v/v) sulfamic acid (30 min, 121 °C) followed by enzymatic hydrolysis, took place. Before enzyme addition, the biomass slurry was brought to a pH of 4.8 with NaOH 2 M. Enzyme solutions were then added to a concentration of 1.1 FPU/mL biomass suspension + 0.15 CBU/mL biomass suspension of cellulase and β-glucosidase, respectively. Enzymatic hydrolysis was conducted at 50 °C for 30 h in an orbital shaker at 200 rpm (Agitorb). The hydrolysate slurry was centrifuged to remove the solids and the supernatant autoclaved. The supernatant was then cooled overnight at 4 °C and centrifuged again, to discard formed precipitates, before use.

Shake flasks assays

The shake flask assays n class="Chemical">wpan>ere carried out to follon class="Chemical">w gron class="Chemical">wth and P3HB production by H. boliviensis under different conditions. These assays were performed in 500 mL shake flasks containing production medium supplemented with 20 g/L glucose or G. sesquipedale hydrolysate to a 100 mL final working volume. A 5 % (v/v) previously grown inoculum volume was added to attain an initial OD600nm of 0.5. Samples from shake flasks were periodically taken for cell growth determination by optical density and cell dry weight (CDW), sugar consumption and P3HB production. The assays were performed in duplicate and the average of the results considered.

Analytical methods

Biomass quantification

Cellular gron class="Chemical">wpan>th n class="Chemical">was monitored off-line by measuring the optical density (O.D.) at a n class="Chemical">wavelength of 600 nm (O.D.600nm) in a double beam spectrophotometer Hitachi U-2000.

The cell dry n class="Chemical">wpan>eight (n class="Chemical">CDW) of the min class="Chemical">crobial culture was determined by transferring 1.2 mL of the broth to a previously weighed and dried 1.5 mL microtube. These samples were centrifuged in a Sigma 1−15 P microcentrifuge (9168 x g during 4 min) and the supernatant was separated after centrifugation. The pellet was then washed by resuspension in distilled water and centrifuged for the second time. After the second centrifugation step the supernatant was discarded. The cleaned pellet was then dried in an oven (Memmert model 200) at 60 °C for at least 48 h.

Sugar quantification

The quantificatiopan class="Chemical">n of n class="Chemical">monosaccharides anpan>d class="Chemical">pan> class="Chemical">HMF in the hydrolysates was performed by High-Performance Liquid Chromatography (HPLC) (Hitachi LaChrom Elite), using a Rezex ROA Organic acid H + 8% (30 mm x 7.8 mm) column, an autosampler (Hitachi LaChrom Elite l-2200), an HPLC pump (Hitachi LaChrom Elite L-2130) and a Hitachi L-2490 refraction index detector or a Hitachi L-2420 UV/VIS detector. The injection volume was 20 μL and elution was achieved using a 5 mM solution of H2SO4. The pump was operated at a flow rate of 0.5 mL/min. The column was kept at 65 °C in a column heater for large columns (Croco-CIL 100-040-220 P, 40cm × 8cm × 8 cm, 30–99 °C) and connected externally to the HPLC system.

Samples for n class="Chemical">sugarpan> quantificationpan> pan> class="Chemical">were firstly centrifuged (1−15 P microcentrifuge, Sigma) for 5 min at 9167 g. After the first centrifugation, a sample of supernatant (200 μL) was diluted n class="Chemical">with 200 μL of 50 mM H2SO4 and the mixture vortexed and centrifuged. HPLC vials were then prepared with 100 μL of the supernatant from the second centrifugation and 900 μL of 50 mM H2SO4. Prior to the analyses, calibration curves for glucose, galactose and HMF in the adequate concentration ranges were obtained. The detection of monosaccharides and HMF was done by the RI and UV/VIS detector, respectively

Vials n class="Chemical">wpan>ith the standards pan> class="Chemical">were prepared using the same procedure as with the samples.

P3HB quantification

The amount of papan class="Chemical">n class="Chemical">P3HB produced class="Chemical">pan> class="Chemical">was determined after centrifuging 1.2 mL of the culture broth and washing the cell pellet. To determine the concentration of P3HB produced, the polymer was converted into stable and volatile hydroxycarboxylic acid methyl esters, through acidic methanolysis and the esters were further analysed by gas chromatography (GC).

One millilitre of papan class="Chemical">n class="Chemical">chloroform class="Chemical">pan> class="Chemical">was added to the cell pellet, the cells were resuspended and then transferred to a glass tube. In order to initiate the acidic methanolysis, 1 mL of “solution A” containing 97 mL methanol, 3 mL of 96 % H2SO4 and 330 μL hexanoic acid, was added to each glass tube. After vortexing, the tubes were placed in an oven (Memmert model 200) at 100 °C. After 5 h the reaction was stopped by adding 1 mL of 60 g/L Na2CO3 solution to each tube. Each glass tube was vortexed and subsequently centrifuged. After centrifugation (5 min at 2 697 g in a Heraeus Labofuge 200 from Thermo Scientific), 200 μL from the bottom phase (organic phase) was transferred to a GC vial. The vials were stored at −18 °C until analysis.

The organic papan class="Chemical">n class="Chemical">phase class="Chemical">pan> class="Chemical">was analysed in a gas chromatograph (Hewlett Packard 5890 series II) equipped with a FID detector and a 7683B injector. The oven, injector and detector temperatures were set to 60, 120 and 150 °C, respectively. The GC column used in this study was a HP-5 from Agilent J&W Scientific, 30 m length and 0.32 mm internal diameter. The data acquisition and integration were performed by the Shimadzu CBM-102 communication Bus Module and Shimadzu GC solution software (Version 2.3).

Peak identificatiopan class="Chemical">n n class="Chemical">was achieved by usinpan>g anclass="Chemical">pan> internpan>al stanpan>dard of pan> class="Chemical">3-methyl hydroxybutyrate from Sigma-Aldrich. Calibration curves were obtained using samples of P(3HB) produced previously (purity 98.2 %), n class="Chemical">which were subjected to the same methylation process as the cells.

Results and discussion

Biomass characterization

The chemical composition of papan class="Chemical">n class="Species">Gelidium sesquipedale residues class="Chemical">pan> class="Chemical">was determined and is shown in Table 2. As these determinations were carried out with lyophilized biomass, the moisture content was very low (6.1 %). The largest component of the dry-weight was the carbohydrate fraction (44.80 %) that is composed of cellulose, residual agar and starch.

Table 2

Composition of Gelidium sesquipedale residues.

Parameter	Value	Unit	Method
Dry-weight (DW)	93.90 ± 0.83	(%)	NREL 60956
Moisture	6.10 ± 0.83	(%)	NREL 60956
Total fiber	76.26	(% dry-weight)	AOAC 991.43
Proteins	0.68	Idem	Kjeldahl method
Lipids	3.36	Idem	Soxhlet method
Ash	16.39 ± 1.15	Idem	NREL 60956
Carbohydrate	44.80 ± 1.90	Idem	NREL 60957
Agar	7.3	Idem	NREL60957 and Eq. (2)
Cellulose	37.05 ± 0.02	Idem	NREL60957 and Eq. (1)
Starch	0.80 ± 0.33	Idem	Megazyme total starch procedure
Minerals
Phosphorous	7.16	g/Kg dry-weight	Nitric-perchloric digestion + ICP-AES
Sodium	1.68	Idem	Idem
Potassium	1.86	Idem	Idem
Calcium	31.68	Idem	Idem
Iron	1248.2	mg/Kg dry-weight	Idem
Copper	25.4	Idem	Idem
Zinc	243.3	Idem	Idem
Chromium	23.3	Idem	Nitric-perchloric extraction + ICP-AES
Lead	5.8	Idem	Idem

Composition of papan class="Chemical">n class="Species">Gelidium sesquipedale residues.

The total n class="Chemical">carbohydratepan> contenpan>t was determined using the NREL 60957 protocol [28], considering that storage (starch) and structural (cellulose and n class="Chemical">agar) polysaccharides in the algal biomass were completely hydrolysed into monomeric subunits after a two-step hydrolysis reaction with sulfuric acid. The released monosaccharides D-glucose and D-galactose were analyzed by HPLC. The amount of starch in the residues was quantified based on the glucose released upon enzymatic hydrolysis using an amylolytic cocktail of α-amylase and amyloglucosidase and the Total Starch Megazyme (Megazyme, Bray, Ireland) procedure (including search for resistant starch). The amount of starch was calculated using Eq. (3) and it was found to be very low. The glucose released from the hydrolysis of starch was subtracted from the total amount of glucose determined using the Van Wychen and Laurens, 2013a protocol, and the value obtained used to determine the amount of cellulose (Eq. (1)). The amount of agar in the biomass was calculated from the D-galactose concentrations, using Eq. (2).where: 162 is the molecular weight (Mw) of glucose and galactose monomeric units in polymeric glucan and galactan, 180 is the Mw of glucose and galactose and 1.27 is the weight ratio between L-3,6- anhydro galactose (AHG) and D-galactose in agar, i.e. 1:1.27 (0.44 % D-galactose: 0.56 % L-AHG) [29].

The results shon class="Chemical">wpan>ed that n class="Species">G. sesquipedale residues still contain a non-negligible content of n class="Chemical">carbohydrates (44.8 % dw), the main being cellulose with circa 37. 5% of dw, followed by agar with 7.3 % dw. The later indicates that the extraction process was not complete, i.e., the waste biomass still contains a significant amount of agar. It is interesting that the cellulose content in seaweed waste is comparable to that of agricultural biomass residues of 33–47 % [30].

The protein copan class="Chemical">ntent n class="Chemical">was determinpan>ed from the total pan> class="Chemical">nitrogen by the Kjeldhal method multiplied by a factor of 5.0 [31]. As expected, the protein content of Gelidium residues was very low (0.68 % dry weight), because proteins are most probably removed during the agar extraction procedure. In reality, prior to agar extraction, the algae are washed with 0.5 % (w/v) sodium carbonate (90 °C, 30 min) for the removal of undesired components, namely red pigments (phycoestrine). Subsequently, the agar is extracted from the solid phase using a hot aqueous solution with pH adjusted between 4.8 and 8.0 (depending on the temperature of the extraction) [32]. Since proteins are easily extracted under alkaline conditions [33], they are being probably extracted during the hot alkaline washing step with sodium carbonate and discarded in the liquid phase.

Diluted acid pretreatment

Enzymatic saccharificatiopan class="Chemical">n aiming at the release of n class="Chemical">galactose anpan>d pan> class="Chemical">AHG from agar is costly because a complex cocktail of endoagarases (α -agarase and β-agarase), exoagarases (agarase II) and finally neoagarobiose hydrolase (NABH) is required. Moreover, saccharification is not efficient primarily because agarose has a low solubility in water. Yun et al., 2016 suggest the combination of enzymatic hydrolysis with acid hydrolysis for an efficient hydrolysis of agarose into monomeric sugars with high titres and yields [17].

In this papan class="Chemical">n class="Chemical">work because of the loclass="Chemical">pan> class="Chemical">w content of agar in the Gelidium residues (Table 2), enzymatic hydrolysis using solely cellulases was chosen. Nonetheless, a mild chemical pre-treatment was carried out to accomplish the hydrolysis of agar to galactose monomers.

Difn class="Chemical">fepan>rent acid catalysts such as pan> class="Chemical">sulphuric, phosphoric and sulfamic acids, catalyst concentrations and time of hydrolysis n class="Chemical">were evaluated aiming to improve agar hydrolysis while minimizing the formation of 5-hydroxymethyl furfural. HMF is formed by the dehydration of hexoses during the thermal acid treatment and it is proven to be an inhibitor of microbial cell growth [34,35]. In the particular case of agar, HMF is released from the degradation of 3,6-anhydro-L-galactose (AHG), as this monomer is acid-labile [17].

For each hydrolytic treatment the recovery yield of papan class="Chemical">n class="Chemical">galactose class="Chemical">pan> class="Chemical">was calculated based on the amount of agar in the biomass.

The results of the digestion of lyophilized papan class="Chemical">n class="Chemical">Gelidium residues (43 g/L) by class="Chemical">pan> class="Chemical">sulfuric acid are shown in Table 3. Different H2SO4 concentrations of 0.25, 0.5 and 1.0 % (w/v) and reaction times of 15, 30 and 60 min were tested. The best results were attained with 1% (w/v) sulfuric acid for 30 min, resulting in a recovery yield of galactose from agar of 54.7 %. This represents a complete hydrolysis of agar since the remaining fraction is AHG. The 5-HMF generated under these conditions reached a concentration of 0.7 g/L. A shorter treatment or a less concentrated acid treatment led to a significant decrease of the agar hydrolysis yield, with no D-galactose and negligible amounts of HMF (0.25 % w/v) being released. The hydrothermal treatment without acid addition generated neither D-galactose nor 5-HMF (results not shown). A longer treatment (60 min) with 0.5 or 1% (w/v) H2SO4 led to slightly lower sugar titres due to sugar degradation.

Table 3

Summary of the results of the pre-hydrolysis step of Gelidium residues with different acid catalysts: biomass load 4.3 % (w/v) at 121 °C; no mixing, total working volume 10 mL.

Summary of the results of the pre-hydrolysis step of n class="Chemical">Gelidiumpan> residues n class="Chemical">with difn class="Chemical">ferent acid catalysts: biomass load 4.3 % (w/v) at 121 °C; no mixing, total working volume 10 mL.

Like n class="Chemical">sulphuric acidpan>, n class="Chemical">phosphoric acid is a strong n class="Chemical">inorganic acid that has been used as a catalyst during the hydrothermal pretreatment of lignocellulosic biomass [36]. It has the additional advantage of the formation of a phosphate salt upon neutralization of the hydrolysate, which can be used as a phosphate source for the subsequent fermentation process. Phosphoric acid was also successfully used in the saccharification of the red macroalga Gracilaria verrucosa [37] at a concentration of 1.5 % (w/v), 140 °C and 60 min reaction time.

n class="Chemical">Phosphoric acidpan> n class="Chemical">was tested as catalyst in the hydrothermal treatment of n class="Chemical">Gelidium residues. Acid concentrations of 0.5, 1.0 and 1.5 % (w/v) were used at 121 °C, for 15, 30 and 60 min hydrolysis time and with a biomass concentration of 43 g/L. Increasing H3PO4 concentrations improved slightly the release of D-galactose. The optimal hydrolysis conditions were attained with 1.5 % (w/v) phosphoric acid and a 60 min treatment (Table 3). Under these conditions the concentrations of galactose and HMF attained were 1.3 and 0.6 g/L, respectively, resulting in a galactose recovery yield of 37.9 %. The produced HMF increased with higher acid concentrations.

n class="Chemical">Sulfamic acidpan> (n class="Chemical">H3NSO3), also knon class="Chemical">wn as amidosulfonic acid, is considered a green catalyst [38]. It is a moderately strong acid (pKa = 1.01), non-corrosive and has a dual active site. It was tested as catalyst in the hydrothermal hydrolysis of the red alga Gracilaria verrucosa at a concentration of approximately 1 % (w/v) (130 °C and 90 min reaction time), resulting in a total reducing sugar yield of 39.9 % [29]. In this work sulfamic acid (H3NSO3) was also tested as catalyst in the hydrothermal hydrolysis of Gelidium residues. Acid concentrations of 0.5, 1.0 and 1.5 (w/v) were used at 121 °C, for 30, 60 and 90 min contact time (except for 0.5 % H3NSO3 where only 30 and 60 min reaction time was tested). The results on Table 3 show that the release of D-galactose improves with increasing acid concentrations and reaction time. The same happens with the HMF formed. The best results were attained with 1.5 % (w/v) H3NSO3 and a contact time of 90 min, resulting in 1.7 g/L D- galactose and 0.8 g/L HMF and a galactose recovery yield of 50 %.

During the acid-catalysed hydrothermal hydrolysis upan class="Chemical">nder the tested conditions only n class="Chemical">D- galactose was released from agar, no glucose being freed from the saccharification of cellulose. The generation of HMF was observed in all cases with no further inhibitory compounds being identified in the hydrolysates. Although phosphoric and sulfamic acids proved to be promising catalysts the highest yield of sugars (over 54 %) was attained with 1 % sulfuric acid after 30 min.

Sequential acid hydrolysis and enzymatic treatment

To perform the saccharification of the cellulose fractiopan class="Chemical">n after acid pre-treatment, hydrolysis n class="Chemical">with anpan> enpan>zyme cocktail of cellulases anclass="Chemical">pan>d β-glucosidase n class="Chemical">was used. Enzymatic hydrolysis n class="Chemical">was carried out after pre-treatment with sulfuric acid (1% (w/v), 30 min, 121 °C) or after treatment with sulfamic acid (0.5 % (w/v), 30 min, 121 °C). These were the chosen conditions due to their promising results concerning the yield of sugar release or the low levels of produced HMF, respectively. Different biomass concentrations, namely 21.5, 43.2 and 86.4 g/L biomass were tested aiming at increasing the sugar concentration in the hydrolysates. The enzymatic hydrolysis was carried out for 30 h using 1.1 FPU /mL biomass slurry of cellulase and 0.15 CBU/mL of β-glucosidase. Results of the combined hydrolysis assays can be seen in Fig. 1. A significant increase of the total amount of sugars released is observed with the increase of the biomass load. However, the combined treatment with sulfuric acid yielded slightly higher amounts of sugars at similar biomass concentrations as compared to that obtained with sulfamic acid. The hydrolysis yield increased in both cases when the amount of biomass doubled from 21.5 g/L to 43 g/L, but slightly decreased when the biomass concentration was again doubled in the treatment with sulfamic acid. This suggests a lower accessibility of the acid and/or the enzymes to the algae at high biomass concentrations. It might be caused by inadequate agitation conditions during the hydrolysis i.e. no agitation during the hydrothermal treatment (assays carried out in the autoclave) plus insufficient agitation during the enzymatic hydrolysis.

Fig. 1

Effect of the biomass concentration on the amount of sugars and HMF released by the combined hydrolysis with A: sulphuric acid (1 % (w/v); 30 min) and B: sulfamic acid (0.5 % (w/v); 30 min) followed by enzymatic hydrolysis.

Efn class="Chemical">fepan>ct of the biomass concenpan>trationpan> onpan> the amounpan>t of pan> class="Chemical">sugars and HMF released by the combined hydrolysis with A: sulphuric acid (1 % (w/v); 30 min) and B: sulfamic acid (0.5 % (n class="Chemical">w/v); 30 min) followed by enzymatic hydrolysis.

n class="Chemical">Wpan>hen pan> class="Chemical">sulfamic acid was used, the hydrolysis of 86.4 g/L biomass yielded a n class="Chemical">hydrolysate with 24.1 g/L total sugars and a concentration of HMF below 0.01 g/L, corresponding to 29.7 % total sugar yield (g total sugars/ g algae dry weight * 100 %). In this case glucose was predominantly released. A small concentration of 0.3 g/L of galactose was released at 21.6 g/L biomass concentration and this could be explained by the higher accessibility of the acid to the biomass, causing a partial hydrolysis of agar.

Aiming at the productiopan class="Chemical">n of larger quantities of n class="Chemical">Gelidium hydrolysates, a scale-up of the combinpan>ed hydrolysis process was conducted. The extent of hydrolysis will most probably depend on the agitation that the reaction medium experiences. To keep the degree of mixing constant in orbitally shaken bioreactors, the Froude number (Fr) should be maintained constant during scaling-up [39,40]. In an attempt to obtain comparable hydrolytic yields at increasingly higher working volumes, experimental parameters leading to a constant Fr number were thus set in the scale-up assays. For the purpose, the rotation speed N (rpm) was decreased at increasing working volumes according to Eq. (4):where N is the rotational speed (rpm) and d is the characteristic length scale – flask diameter. If d increases during the scale-up, N should correspondingly decrease to maintain Fr constant.

The results of the scale-up experiments are givepan class="Chemical">n in Fig. 2. The release of n class="Chemical">glucose obtainpan>ed inpan> the ranclass="Chemical">pan>ge 10 mL–700 mL n class="Chemical">was in fact approximately constant.

Fig. 2

Scale-up of the combined hydrolysis process. Effect of the total working volume on the amount of glucose released during the combined hydrolysis with a pre-treatment with sulfamic acid (0.5 % (w/v); 30 min) followed by enzymatic hydrolysis. The biomass concentration was 86.4 g/L in all assays.

Scale-up of the combined hydrolysis process. Efpapan class="Chemical">n class="Chemical">fect of the total class="Chemical">pan> class="Chemical">working volume on the amount of glucose released during the combined hydrolysis with a pre-treatment with sulfamic acid (0.5 % (w/v); 30 min) followed by enzymatic hydrolysis. The biomass concentration was 86.4 g/L in all assays.

Shake flask cultivations

n class="Species">Halomonas boliviensis DSM15516pan>, a halotolerant bacterium able to acpan> class="Chemical">cumulate high P3HB amounts [21] using n class="Chemical">glucose and galactose, the monosaccharides released in the hydrolysis of Gelidium residues was selected to perform this work. The choice of a halophilic strain was based on a potentially high salt content in the algal hydrolysates caused by a high mineral content of the algal biomass itself (Table 2) and also by the salts formed upon neutralization of the biomass suspension after the acidic pre-treatment. Moreover, salt-rich media were chosen to perform the cultivations because they are less prone to contamination and thus non-strict sterile conditions can be used, leading to savings in equipment and operation costs at large scale.

The gron class="Chemical">wpan>th and pan> class="Chemical">P3HB production on 20 g/L glucose or 20 g/L n class="Chemical">galactose was carried out using the production medium with 1 g/L NH4Cl and 20 g/L MSG. This medium composition was based on the one reported by Quillaguaman [25]. Maximum CDW and P3HB concentrations on glucose were attained at 90 h cultivation (Fig. 3) reaching 10.8 ± 1.5 g/L and 5.0 ± 0.2 g/L, respectively, corresponding to a 46.7 ± 6.8 % PHB cell content. These results are in accordance with previous observations in shake flasks [21] where 55 % polymer accumulation was reached. The growth and polymer production on galactose attained slightly lower results with a maximum CDW and P3HB accumulation of 8.4 ± 0.4 g/L and 35.1 ± 0.7 % P3HB, respectively, at 90 h cultivation. Both sugars were confirmed to be good substrates for P3HB production by H. boliviensis and this strain is thus a promising choice for the valorization of Gelidium hydrolysates to PHAs.

Fig. 3

H. boliviensis growth and P3HB production on A. 20 g/L glucose; B. 20 g/L d- galactose.

n class="Species">H. boliviensispan> gron class="Chemical">wth and n class="Chemical">P3HB production on A. 20 g/L glucose; B. 20 g/L d- galactose.

Growth and production on Gelidium hydrolysates

The n class="Chemical">Gelidium hydrolysatespan> were examined as n class="Chemical">carbon source for the production of P3HB by Halomonas boliviensis in shake flask cultures. The first assays were carried out with the hydrolysate prepared with 43.2 g/L biomass using the combined treatment with sulfuric acid (1% w/v, 30 min, 121 °C) followed by enzymatic treatment. The assay was compared to a control featuring a mixture of glucose and galactose simulating the hydrolysate composition (Fig. 4). Similar biomass concentrations were attained in the control with a CDW of 10.1 g/L versus a CDW of 9.3 g/L with the hydrolysate. However the maximum concentration of polymer produced in the sugar mixture was much higher (P3HB = 4.7 g/L) compared to the hydrolysate (P3HB = 3.0 g/L), corresponding to approx. 47 % and 32 % of the P3HB cell content, respectively. Besides a lower production of polymer, a delay in cell growth and production was observed. This might be ascribed to the effect of possible inhibitors in the hydrolysate. Typical inhibitors present in seaweed hydrolysates are HMF, as well as acetic and levulinic acids [17]. The hydrolysate was tested for the presence of these inhibitors and only HMF was found. Its effect on cell growth was determined in H. boliviensis cultures containing 20 g/L initial glucose concentration and HMF in the range 0−1 g/L (Fig. 5). The results indicate that the inhibitory effect of HMF on H. boliviensis growth is significant for HMF concentrations above 0.1 g/L. At this concentration, the μ was 92.8 % of the attained in the control with no HMF (μ =0.25 h−1). For this reason the choice of a mild chemical pre-treatment releasing lower inhibitor titres is an asset.

Fig. 4

H. boliviensis growth and P3HB production on A. control simulating the sugar hydrolysate composition of the hydrolysate; B. hydrolysate produced using a pre-treatment with 1% (w/v) sulfuric acid followed by enzymatic hydrolysis.

Fig. 5

Effect of the HMF concentration on the maximum specific growth rate of H. boliviensis cultivated in production medium supplemented with 20 g/L glucose.

n class="Species">H. boliviensispan> gron class="Chemical">wth and n class="Chemical">P3HB production on A. control simulating the sugar hydrolysate composition of the hydrolysate; B. hydrolysate produced using a pre-treatment with 1% (w/v) sulfuric acid followed by enzymatic hydrolysis.

Efn class="Chemical">fepan>ct of the n class="Chemical">HMF concentration on the maximum specific gron class="Chemical">wth rate of H. boliviensis cultivated in production medium supplemented with 20 g/L glucose.

The hydrothermal hydrolysis n class="Chemical">wpan>ith 0.5 % (n class="Chemical">w/v) n class="Chemical">sulfamic acid at 121 °C for 30 min was the chosen pre-treatment method for subsequent production of hydrolysates from the G. sesquipedale residues as, under these conditions no more than 0.01 g/L of HMF were released, even though this treatment was unable to release galactose from agar. This is acceptable for processing waste Gelidium because the amount of agar and thus of released galactose is quite low and so it might be neglected for further valorisation to P3HB. The pre-treatment step is nevertheless very important, especially at higher biomass loads (>5 % (w/v)) in order to break the gel structure of agar and ease the processing of the biomass.

To assess the gron class="Chemical">wpan>th and pan> class="Chemical">P3HB production of H. boliviensis on the produced n class="Chemical">algal hydrolysate a 20-fold concentrated production medium along with magnesium and NaCl solutions (medium “A” in Table 4) was added to the algal hydrolysate to attain an initial glucose concentration of approx. 20 g/L. The results were compared to a control with the same glucose concentration. It was observed that a similar CDW of 9 g/L is attained in both conditions (Fig. 6). Concerning polymer production, the highest accumulated polymer content in H. boliviensis cells grown on algal hydrolysate was only 21 % (w/w), while this value attained 44.2 % (w/w) on the control with glucose.

Table 4

Effect of the nitrogen content, supplemented to the cultivation media in the form of monosodium glutamate (MSG) and ammonium chloride (NH4Cl), on the biomass and polymer production. A combined hydrolysate prepared with sulfamic acid and featuring an initial glucose concentration of 20 g/L was used in all assays.

Medium	NH4Cl(gL−1)	MSG(gL−1)	CDW(gL−1)	P3HB(g L−1)	P3HB(%)	Y P/S(gPHB/gglu.cons)	Prod vol max(gPHB L−1 h−1)
A	1	20	8.6	1.8	21.3	0.12	0.028
B	1	0	4.7	2.7	56.7	0.11	0.047
C	1	5	7.1	3.7	52.2	0.15	0.057
D	1	10	8.7	3.5	40.8	0.16	0.056
E	0	10	8.3	3.4	41.1	0.16	0.056

Fig. 6

Growth and P3HB production of H. boliviensis on A: Gelidium hydrolysate produced using a combined hydrolysis with 0.5 % w/v sulfamic acid for 30 min followed by enzymatic hydrolysis and B: control on glucose.

Efn class="Chemical">fepan>ct of the n class="Chemical">nitrogen content, supplemented to the n class="Chemical">cultivation media in the form of monosodium glutamate (MSG) and ammonium chloride (NH4Cl), on the biomass and polymer production. A combined hydrolysate prepared with sulfamic acid and featuring an initial glucose concentration of 20 g/L was used in all assays.

Gron class="Chemical">wpan>th and pan> class="Chemical">P3HB production of H. boliviensis on A: n class="Chemical">Gelidium hydrolysate produced using a combined hydrolysis with 0.5 % w/v sulfamic acid for 30 min followed by enzymatic hydrolysis and B: control on glucose.

Engineering the cultivation medium based on the hydrolysate composition

The acn class="Chemical">cupan>mulation of pan> class="Chemical">P3HB by H. boliviensis ocn class="Chemical">curs predominantly under nitrogen, phosphorous or oxygen limitation, like in many others bacterial species [41,42]. The low accumulation attained by supplementing the hydrolysate with medium “A” could be explained by an excess of nitrogen that can arise either from medium “A” or from the algal hydrolysates. To infer on the influence of the N content on the growth and P3HB cellular content, both the NH4Cl and the monosodium glutamate concentrations of the mineral medium supplemented to the hydrolysate were varied, while the other concentrations were maintained constant. The different medium compositions and the respective results attained are summarized in Table 4.

From these results it is evident the copan class="Chemical">ntribution of n class="Chemical">MSG to the genpan>erationpan> of biomass inpan> detriment of higher pan> class="Chemical">polymer concentrations. Medium A, the basal medium used in the shake flask assays, was clearly not the best medium to supplement the n class="Chemical">Gelidium hydrolysates when aiming at high polymer concentrations. This result might be due to the high N content of the cultivation medium resulting in a low carbon/nitrogen ratio. Some authors have described the need to have C/N ratios above 20 to obtain a significant polymer accumulation [7,43]. The composition of the hydrolysate alone was analysed (Table 5) and showed a C/N ratio of 15.1, i.e. below 20. This result indicates that the supplementation of high concentrations of an N-rich source like MSG to the cultivation medium is not beneficial to attain high polymer productions. The composition of medium C or E was considered more suitable because it generated both higher yields of product on sugar and higher polymer productivities when compared to medium A. Medium E was tested as supplement to the hydrolysate and the results compared to a control with glucose (Fig. 7). Although similar biomass concentrations were attained (approx. 8.5 g/L), higher polymer contents were observed in the control (circa 50 %) compared to the hydrolysate (circa 40 %) as already expected. Despite the lower concentration of polymer attained in the hydrolysate, the overall polymer productivities were similar (0.056 g/L.h) for both the hydrolysate and the control. The hydrolysate produced from the Gelidium residues was thus shown to be a good alternative C-source for the production of PHAs.

Table 5

Composition of the hydrolysate prepared after a combined pre-treatment using 0.5 % (w/v) sulfamic acid at 121 °C and 30 min of 8.6 % (w/v) biomass slurry followed by an enzymatic hydrolysis with cellulolytic enzymes (50 °C; 30 h).

Parameter	Value	Method
Carbon (g C /L)	13.6	HPLC (M&M)
Nitrogen Kjeldhal (g N/L)	0.9	M.M. 8.9 (2018-04-12)
Calcium (g/L)	1.9	ISO 11885:2007
Magnesium (g/L)	0.2	ISO 11885:2007
Phosphorous (mg P/L)	79.0	M.M. 4.8 (2016-05-06)
Sodium (mg/L)	39.0	ISO 11885:2007

Fig. 7

H. boliviensis growth and P3HB production on Gelidium hydrolysate supplemented with medium E (A) and control on glucose (B).

Composition of the papan class="Chemical">n class="Chemical">hydrolysate prepared after a combinpan>ed pre-treatment usinpan>g 0.5 % (pan> class="Chemical">w/v) sulfamic acid at 121 °C and 30 min of 8.6 % (w/v) biomass slurry follon class="Chemical">wed by an enzymatic hydrolysis with cellulolytic enzymes (50 °C; 30 h).

n class="Species">H. boliviensispan> gron class="Chemical">wth and n class="Chemical">P3HB production on Gelidium hydrolysate supplemented with medium E (A) and control on glucose (B).

Conclusions

The n class="Chemical">wpan>aste material resulting from the extractionpan> of pan> class="Chemical">agar from Gelidium sesquipedale is an underexploited and yet valuable material still containing non-negligible amounts of carbohydrates (44.80 ± 1.90 % dn class="Chemical">w basis), of which approx. 35 % w/w is cellulose.

The present papan class="Chemical">n class="Chemical">work shoclass="Chemical">pan> class="Chemical">ws that hydrolysates from Gelidium residues are suitable C-sources for P3HB production by Halomonas boliviensis. High polymer yields and productivities were attained after adjusting the composition of the cultivation media to adequate C/N ratios, pinpointing the importance of assessing the hydrolysates composition to design a suitable production medium.

The utilization of this by-product is apan class="Chemical">n inspiring example of a cirn class="Chemical">cular econpan>omy approach n class="Chemical">with the extra-advantage of minimizing its disposal in the environment.

CRediT authorship contribution statement

S. Tůma: Visualization, Ipan class="Chemical">nvestigation. J.K. Izaguirre: Visualization, Investigation. M. Bondar: Validation. M.M. Marques: Visualization, Investigation. P. n class="Chemical">Fernpan>anpan>des: Supervisionpan>, Conpan>ceptualizationpan>, n class="Chemical">Writing - review & editing. M.M.R. da Fonseca: Supervision, Writing - review & editing, Project administration. M.T. Cesário: Conceptualization, Supervision, Writing - original draft, Writing - review & editing, Project administration, Funding acquisition.

Declaration of Competing Interest

The authors declare no copan class="Chemical">nflict of interest.