Developing a CO2 bicarbonation absorber for promoting microalgal growth rates with an improved photosynthesis pathway.

In order to solve the problems of the short residence time and low utilization efficiency of carbon dioxide (CO2) gas added directly to a raceway pond, a CO2 bicarbonation absorber (CBA) was proposed to efficiently convert CO2 gas and sodium carbonate (Na2CO3) solution to sodium bicarbonate (NaHCO3), which was dissolved easily in the culture medium and left to promote the microalgal growth rate. The CO2 gas reacted with the Na2CO3 solution (initial concentration = 200 mM L-1 and volume ratio in CBA = 60%) for 90 min at 0.3 MPa to give the optimized molar proportion (92%) of NaHCO3 product in total inorganic carbon and increase the microalgal growth rate by 5.0 times. Quantitative label-free protein analysis showed that the expression levels of the photosystem II (PSII) reaction centre protein (PsbH) and PSII cytochrome (PsbV2) in the photosynthesis pathway increased by 4.8 and 3.4 times, respectively, while that of the RuBisCO enzyme (rbcL) in the carbon fixation pathway increased by 3.5 times in Arthrospira platensis cells cultivated with the NaHCO3 product in the CBA at 0.3 MPa. This journal is © The Royal Society of Chemistry.

Introduction

Cultivating microalgal for the carbon dioxide (CO2) fixation from coal-fired power plants has been extensively studied in the past few decades. Normally, 1 ton of microalgal can consume 1.83 tons of CO2 with a carbon content of 50% in the microalgal cells. It was reported that around one-third of global CO2 fixation was attributed to the microalgal.[1,2] The reason for this is because there is a CO2-concentrating mechanism (CCM) in the pyrenoid organelle of the algal cell that accelerates CO2 assimilation.[3,4] According to the CCM, the HCO3− passes successively through the plasma membrane, the chloroplast envelope and the thylakoid membrane and this is mediated by the enzyme, carbonic anhydrase (CA). Then when the HCO3− reaches the thylakoid lumen, it is catalysed to CO2. Finally, the CO2 is fixed by ribulose-1,5-biphosphate carboxylase/oxygenase (RuBisCO) and channelled into the Calvin cycle.[1,2] The HCO3− is therefore the dominant type of carbon to be absorbed for photosynthesis in microalgal cells.

Normally, the CO2 gas is added directly into the microalgal solution by using an aerator.[5-9] Researchers have proposed several aerators[10-12] and baffles[13-18] for use in the raceway pond (RWP) to increase the CO2 bubble residence time for improving the conversion efficiency of CO2 to HCO3− (CO2 + CO32− + H2O → 2HCO3−). However, the reaction of CO2 and CO32− requires relatively high pressure and sufficient reaction time.[19,20] Because the bubble residence time is relatively low (usually several seconds) when the CO2 gas is added directly by the aerator[21,22] at atmospheric pressure, and was harmful to the reaction of CO2 and CO32−, most of the CO2 bubbles were emitted to the atmosphere again, causing wastage and low CO2 utilization efficiency. It is also not beneficial for microalgal growth rate.

The CO2 bicarbonation absorber (CBA) has been generally adopted to produce sodium bicarbonate (NaHCO3) in industry.[23-26] A gas distributor was needed on the bottom of the CBA to provide a uniform gas flow distribution. The CO2 gas was added to the CBA from the bottom inlet hole, while the sodium carbonate mixture flowed in from the top of the CBA. The reaction pressure and temperature were strictly controlled to produce (NaHCO3) crystals at the end of the reaction. On the basis of this technology, the CBA could be combined with the RWP so that the CO2 gas can be converted to HCO3− more efficiently, because the CO2 molecule was reacted with the HCO3− in advance, which made it easier for the algal cell to absorb it. However, the CBA could not be applied to the RWP, because the HCO3− concentration was fairly high, and even crystallized. Because the algal cells only required a limited HCO3− concentration, a higher HCO3− concentration would cause a drop in pH levels and the proton gradient. Zhang et al.[27] proposed a spraying absorption tower coupled with an outdoor open RWP based on this principle to improve the CO2 utilization efficiency. The pH value was controlled by the absorption tower. The biomass productivity increased by 40.7% and CO2 fixation efficiency reached 50% compared to the conventional process where the CO2 was added through porous pipes placed at the bottom of the RWP.[27] However, the use of the proposed spraying absorption tower did not take into account the CO2 exhaust gas, which was emitted directly to the atmosphere, causing a secondary emission of CO2 gas. Also, the optimized operation parameters were not given in this study. Eloka-Eboka and Inambao[28] investigated the rate of sequestration of both total and dissolved carbon, and suggested that Dunaliella has a higher CO2 uptake rate. However, they did not give the specific method for improving the CO2 uptake rate in a real application, and the relationship of HCO3− concentration and biomass growth rate was not studied. Mokashi et al.[29] also proved that HCO3− can be an alternative inorganic carbon source for higher microalgal production. Therefore, it is necessary to develop an apparatus to convert CO2 to HCO3− efficiently. The CO2 fixation efficiency would improve considerably if CO2 was reacted to HCO3− and fixed by the algal cell.

The main purpose of this study was to find an efficient method for CO2 fixation by microalgal. A CBA was proposed which would convert the CO2 gas to HCO3−, which can be easily utilized by the microalgal cells and dramatically enhances the CO2 fixation efficiency. The exhausted CO2 gas was recycled to the inlet gas flow, which means that the CO2 gas was completely reacted to the HCO3−, so CO2 fixation efficiency was greatly enhanced. The reaction time and pressure were optimized to regulate the molar proportion of NaHCO3 in total inorganic carbon. The initial concentration of sodium carbonate (Na2CO3) in the substrate and the volume ratio of Na2CO3 solution in the CBA were optimized to regulate the NaHCO3 product and to improve the biomass growth rate. Furthermore, the metabolism pathway of photosynthesis and CO2 fixation were determined to further understand the absorption mechanism of HCO3− by the algal cell.

Materials and methods

Design of CO2 bicarbonation absorber

As shown in Fig. 1, a CBA was proposed for improving the microalgal growth rate. The CBA was made of plexiglass, which gives a maximum CO2 pressure of 1.0 MPa. The dimensions of the CBA were ∅5 × 70 cm. The CBA was used for the reaction of CO2 and Na2CO3 (Na2CO3 + CO2 + H2O → 2NaHCO3). During the reaction, the CO2 gas in the storage tank was dried by a drier and then flowed into the CBA. A check valve was installed before the CO2 inlet to prevent the backward flow of gas. A pressure valve was installed before the check valve to keep the reaction pressure within 0.1 to 0.5 MPa. Simultaneously, the Na2CO3 was dissolved in water and injected to the CBA using a pump with the Na2CO3 concentration ranging from 120 to 280 mM L−1. The initial volume ratio μ of the Na2CO3 solution in CBA was defined as the ratio of solution height h1 and reactor height h2, that is, μ = h1/h2. In order to improve the CO2 utilization efficiency, the exhaust CO2 gas was dried and returned back into the CBA. For a better distribution of CO2 gas in the CBA, there was a cavity on the bottom of the reactor, above which was a gas distributor. The gas distributor was comprised of several holes which increased the CO2 resistance time and improved the reaction efficiency of CO2 and Na2CO3. The reaction time varied from 30 to 150 min. After the reaction, the solution mixture flowed into the RWP for the cultivation of microalgal.

Fig. 1

Schematic diagram of an experimental system for a CO2 bicarbonation absorber (CBA) for improving microalgal growth rate.

Cultivation of Arthrospira platensis

The algal strain Arthrospira was mutated using nuclear irradiation and domestication in a high CO2 concentration environment[30] to obtain hereditary stability. As well as the solution mixture of NaHCO3 and Na2CO3 from CBA, the culture medium was composed of 2.5 g L−1 sodium nitrate (NaNO3), 0.5 g L−1 dipotassium phosphate (K2HPO4), 0.2 g L−1 magnesium sulfate heptahydrate (MgSO4·7H2O), 1.0 g L−1 potassium sulfate (K2SO4), 0.01 g L−1 ferrous sulfate heptahydrate (FeSO4·7H2O), 0.08 g L−1 disodium ethylenediaminetetraacetate dihydrate (Na2EDTA), 0.04 g L−1 calcium chloride (CaCl2), 3 mL hydrochloric acid (HCl) (35% w/v) and 1 mL A5. A5 refers to the micronutrients required for the growth of the microalgal, including 2.86 g L−1 boric acid (H3BO3), 1.81 g L−1 manganese(ii) chloride tetrahydrate (MnCl2·4H2O), 0.22 g L−1 zinc sulfate heptahydrate (ZnSO4·7H2O), 0.08 g L−1 copper(ii) hydrate pentahydrate (CuSO4·5H2O) and 0.01 g L−1 molybdenum trihydrate (MoO3). The algal were inoculated into RWP with a solution depth of 5 cm and absorbance value of 0.3. The dimension of the RWP was 20 × 8 × 5 cm. The solution temperature was kept at 30 ± 2 °C and light intensity on the surface of the RWP was 8000 ± 500 lux. The RWP was covered with a plastic membrane to prevent evaporation of the microalgal solution. During the experiments, the algal samples were collected at 9 : 00 and 21 : 00 every day, and the solution optical density (OD) and pH were measured. The curve fitting of the OD and cell density (C) was measured as C (g L−1) = 0.505 × OD560nm − 0.034 (R2 = 0.996). All the experiments were conducted in triplicate. The solution concentration of total inorganic carbon (TIC), NaHCO3 and Na2CO3 were measured using a double-tracer method.[31-34]

Quantitative label-free protein measurement

The direct mass spectrometry analysis of protein peptide segments was conducted using a label-free method.[35] It was effective and efficient for quantitatively determining the protein functions. The label-free method mainly included three steps:[36,37]

Total protein extraction

The sample was milled to a powder in a mortar with liquid nitrogen followed by mixing 150 mg of the powder from each sample with 1 mL of lysis buffer [2-amino-2-(hydroxymethyl)-1,3-propanediol, TRIS base, pH 8], 8 M urea and 1% sodium dodecyl sulfate with protease inhibitor cocktail in a glass homogenizer. After homogenization, the homogenate was incubated on ice for 20 min and centrifuged at 12 000 × g for 15 min at 4 °C. The supernatant was transferred to a clean tube, and the protein concentration was determined using the Bradford assay. To the supernatant, 4 volumes of 10 mM dithiothreitol (DTT) in cold acetone were added followed by placing the sample at −20 °C for 2 h to overnight for sample extraction. Samples were centrifuged and the pellet was washed twice with cold acetone. Finally, the pellet was resuspended in the dissolution buffer [Tris base (pH = 8) and 8 M urea].

Peptide preparation

The supernatant from each sample, containing precisely 0.1 mg of protein, DTT reduction and iodoacetamide alkylation, was digested using Trypsin Gold (Promega, Madison, WI, USA) at 37 °C for 16 h. After trypsin digestion, the peptide was desalted using a C18 cartridge to remove the high urea, and the desalted peptides were dried using vacuum centrifugation.

Liquid chromatography-mass spectrometry/mass spectrometry (LC-MS/MS) analysis

Each peptide sample was dissolved with loading buffer and then separated using a C18 column [75 μm inner diameter, 360 μm outer diameter × 10 cm, 1.9 μm C18, (Dr Maisch HPLC GmbH)]. Mobile phase A consisted of 0.1% formic acid in water solution, and mobile phase B consisted of 0.1% formic acid in acetonitrile solution and a series of 60 min gradients were used which were adjusted according to the hydrophobicity of the fractions eluted in the one-dimensional (1D) LC with a flow rate of 300 nL min−1. A Q-exactive HF-X hybrid quadrupole-Orbitrap MS (ThermoFisher) was operated in positive polarity mode with a capillary temperature of 320 °C. Full MS scan resolution was set to 60 000 with an automatic gain control target value of 3 × 106 for a scan range of 350–1500 m/z. The proteins found were identified using the functional database of the KEGG Pathway.[38,39]

Results and discussion

Optimizing operation conditions of CO2 bicarbonation absorber to improve the microalgal growth rate

Optimizing reaction time

Kantarci et al.[40,42] proposed, that the reaction time of Na2CO3 and CO2 in CBA was important. This is because the CO2 dissolution rate in the liquid solution is slow, so most of the CO2 gas gathered on the top of the free space causing a low contact area. In an actual application, a shorter reaction time would increase the work efficiency. Therefore, optimizing the reaction time was essential for obtaining the correct HCO3− concentration. As shown in Fig. 2(a), with an increase of reaction time from 30 min to 150 min, the TIC and NaHCO3 concentrations increased from 219 mM L−1 to 350 mM L−1, and from 98 mM L−1 to 350 mM L−1, respectively. The molar proportion of NaHCO3 in TIC (ω) increased from 45% to 100% and the CO2 absorption volume increased from 69 mM L−1 to 551 mM L−1. Lin et al.[41] also proved that increasing the reaction time was beneficial for NaHCO3 production. However, the Na2CO3 concentration, decreased from 121 mM L−1 to 0.4 mM L−1. The microalgal biomass growth rate first increased from 0.21 g L−1 d−1 to 0.55 g L−1 d−1, and subsequently decreased to 0.36 g L−1 d−1. It was found that the reaction of CO2 and Na2CO3 required enough reaction time to enhance the production of NaHCO3. When the reaction time was 150 min, the Na2CO3 was completely converted to NaHCO3. However, the solution pH was low at these conditions, which affected the active transport of NaHCO3. The algal growth was also not ideal under these conditions.

Fig. 2

Optimizing the reaction time in a CO2 bicarbonation absorber (CBA) to regulate the production of the absorption product, NaHCO3, (a) effects of reaction time, (b) dynamic changes of NaHCO3 and Na2CO3 concentrations, and (c) biomass density and pH value.

As shown in Fig. 2(b) and (c), as the reaction time increased from 30 min to 150 min, the initial solution pH decreased continually from 10.14 to 9.19. The biomass density was increased at first and then decreased, which may be a result of the ω and pH differences. When the reaction time was 90 min, the ω was 91% and the initial pH was 9.73, which was suitable for the growth of the microalgal cells. With the growth of the microalgal cells, the solution NaHCO3 in the RWP decreased gradually while the Na2CO3 concentration increased. The biomass density and pH value also increased gradually. The reaction time caused the difference in the initial NaHCO3 level in the solution, which was critical for the carbon concentrating mechanism (CCM) of the algal cells. As is known, the OH− ions were exhausted causing an increase of pH value. According to the CCM, the HCO3− passed through the plasma membrane via the translocator HLA3 and LC11, followed by passage through the chloroplast envelope via the translocator LciA and then the thylakoid membrane via the translocator LCI11. The HCO3− finally reached the thylakoid lumen, where the HCO3− was catalysed to CO2 by the CAH3 enzyme. The CO2 was fixed by the enzyme RuBisCO and was channelled into the Calvin cycle.[1,2] However, some of the HCO3− was catalysed by the CA in the periplasmic space and converted to CO2, which was diffused to the stroma and captured by the RuBisCO.[1] The HCO3− was transported by the CA in cellular stroma during the growth of algal cells, so the HCO3− concentration decreased gradually while the CO32− concentration increased. The HCO3− was the dominant carbon type to be absorbed by the algal cells. The presence of sufficient HCO3− promoted the Calvin cycle, and more adenosine triphosphate (ATP) was required, which in turn promoted photosynthesis to produce ATP. The HCO3− went through the cytoplasmic membrane by active transport, thereby enhancing the ion transport.

Optimizing reaction pressure

The reaction pressure was considered to be a key factor affecting the reaction of Na2CO3 and CO2 in CBA.[42-44] As shown in Fig. 3(a), with the increase of reaction pressure from 0.1 MPa to 0.5 MPa in CBA, the TIC and NaHCO3 concentration increased from 186 mM L−1 to 352 mM L−1 and from 5.7 mM L−1 to 351 mM L−1, respectively. The ω increased continually from 3% to 99%; while the Na2CO3 concentration decreased from 180 mM L−1 to 0.6 mM L−1. These results fully demonstrated that a higher reaction pressure promoted the production of NaHCO3. According to the Gibbs free energy theory, the reaction of CO2 and Na2CO3 was volume-reduced and was an exothermic reaction. The increase in pressure would promote the forward reaction, therefore the TIC and NaHCO3 concentrations, as well as ω and the CO2 absorption amount increased while the Na2CO3 decreased gradually. When the pressure was over 0.4 MPa, all the Na2CO3 was converted to NaHCO3. These results were similar to those reported in other studies.[43,45,46]

Fig. 3

Optimizing reaction pressure in a CO2 bicarbonation absorber (CBA) to regulate the absorption of the product, NaHCO3 (a) effects of reaction pressure, (b) biomass density and pH value.

The reacted NaHCO3 and Na2CO3 mixtures were used to cultivate microalgal. Microalgal growth rate first increased from 0.07 g L−1 d−1 to 0.42 g L−1 d−1 and then decreased to 0.38 g L−1 d−1. As shown in Fig. 3(b), with the growth of the algal cells, the biomass density and solution pH increased gradually. When the reaction pressure was 0.1 MPa, the microalgal nearly died, and the solution pH decreased slightly. That was because the solution NaHCO3 concentration was pretty low under these conditions, which were not sufficient for photosynthesis in the microalgal. However, if the solution only consisted of NaHCO3, the algal growth rate would also decrease. As the pH level was pretty low, it was not beneficial to the growth of the algal cells.

Optimizing initial sodium carbonate concentration

In the future it is hoped that it will be possible to produce more NaHCO3 with less Na2CO3 substrate to reduce the economic costs of the process. Thus, the initial Na2CO3 concentration in CBA was studied. As shown in Fig. 4(a), with an increase in the initial Na2CO3 concentration from 120 mM L−1 to 280 mM L−1, ω first increased from 88% to 92% and then decreased to 71%. The biomass growth rate first increased from 0.33 g L−1 d−1 to 0.45 g L−1 d−1 and then decreased to 0.29 g L−1 d−1, and the NaHCO3 concentration first increased from 203 mM L−1 to 273 mM L−1 and then decreased to 213 mM L−1, whereas the CO2 absorption amount decreased continually from 411 mM L−1 to 81 mM L−1. The reason for this may be that with the initial Na2CO3 concentration increasing from 120 mM L−1 to 200 mM L−1, the CO2 gas and reaction time were sufficient, so more NaHCO3 was produced, resulting in most of the Na2CO3 in the substrate being depleted, which was followed by an increase in ω. It seems that there was a saturation concentration of the NaHCO3 and Na2CO3 mixture because with a further increase in substrate Na2CO3 concentration, it was more difficult for the reaction between Na2CO3 and CO2 to occur. The ω and the concentration of the NaHCO3 produced were decreased. It was noticed that the absorbed CO2 concentration decreased continually. The reason for this may be that the accumulation rate of TIC decreased with an increase in substrate Na2CO3. The higher Na2CO3 concentration reduced the dissolution rate of CO2, thus the CO2 concentration decreased gradually. Furthermore, the biomass growth rate was increased first and then decreased, which was closely affected by the value of ω. As explained previously, the ω would promote the photosynthesis, and CO2 fixation process. The accelerated Calvin cycle promoted the production of glyceraldehyde-3-phosphate (G3P), which was converted to carbohydrate. The carbohydrate caused an accumulation of biomass, thereby increasing the biomass growth rate.

Fig. 4

Optimizing initial Na2CO3 concentration in the CO2 bicarbonation absorber (CBA), (a) effects of initial Na2CO3 concentration, (b) dynamic changes of NaHCO3 and Na2CO3 concentrations, and (c) biomass density and pH value.

The NaHCO3 and Na2CO3 reaction mixtures were used to cultivate microalgal. Fig. 4(b) and (c) show the change in microalgal density and solution TIC. This demonstrated again that the optimized ω would promote microalgal growth. With the growth of the microalgal, the biomass density and solution pH increased gradually. In 0th, the order of the solution pH was pH280 mM L> pH240 mM L> pH120 mM L> pH200 mM L = pH160 mM L. The reason behind this was that the solution pH was affected by ω which was different over the five different conditions. With the growth of algal cells, more OH− were produced and more Na2CO3 was reacted. The order of biomass density was 200 mM L−1 > 240 mM L−1 > 160 mM L−1 > 120 mM L−1 > 280 mM L−1. So the final solution pH also followed this order. Furthermore, the Na2CO3 concentration of the solution increased whereas the NaHCO3 concentration decreased (OH− + HCO3− → CO32− + H2O), as shown in Fig. 4(c).

Optimizing the volume ratio of sodium carbonate solution

The influence of volume ratio of Na2CO3 solution (μ) in the CBA on the production of NaHCO3 was investigated further. As shown in Fig. 5(a), with an increase in the relative height of the solution from 20% to 100%, the TIC and NaHCO3 concentrations decreased gradually from 311 mM L−1 to 179 mM L−1, and from 310 mM L−1 to 59 mM L−1, respectively. The ω and CO2 absorption amount decreased from 100% to 33%, and from 408 mM L−1 to 0 mM L−1, respectively, whereas the Na2CO3 concentration increased from 0.6 mM L−1 to 120 mM L−1. The dissolution rate of the CO2 gas was low and the reaction rate of CO2 and Na2CO3 was slow. Thus, a space above the solution in the CBA was required for further reaction of CO2. The gradual decrease of ω and CO2 absorption amount proved this hypothesis. In a real application, it is essential to increase both the μ and ω to produce more NaHCO3 in the mixture for large sale cultivation of microalgal.

Fig. 5

Optimization of the volume ratio of Na2CO3 solution in the CO2 bicarbonation absorber (CBA), (a) effects of volume ratio of Na2CO3 solution, (b) biomass density in microalgal growth.

The reacted solution mixture was used to cultivate the microalgal, and the biomass growth rate first increased from 0.27 g L−1 d−1 to 0.41 g L−1 d−1, and then decreased to 0.28 g L−1 d−1. As shown in Fig. 5(b), the biomass growth rate was dramatically higher when the μ in the CBA was 60% when compared with other conditions. When the μ was 100%, there was no CO2 absorbed by the Na2CO3 solution, as there was no space above the solution. Therefore, almost no NaHCO3 was produced under these conditions, however, sufficient NaHCO3 is necessary for the growth of microalgae.

Promoting the photosynthesis and carbon fixation metabolism pathway

It was noticed that the reaction pressure was essential for NaHCO3 production, which further affects the biomass growth rate. The results in Fig. 3 show that the biomass growth rate under a CBA pressure of 0.3 MPa increased by 5.0 times compared with that obtained in 0.1 MPa. The ω was 92% when the reaction pressure was 0.3 MPa in CBA, which is ideal for the growth of algal cells. In order to investigate the molecular mechanism behind the improvement of microalgal growth rate under these conditions, label-free proteomics was conducted. The total number proteins identified in the Arthrospira platensis cells cultivated with the NaHCO3 product converted from Na2CO3 solution at pressure of 0.1 MPa and 0.3 MPa, separately in the CBA was 1611. Meanwhile, the up-regulated protein number was 468 (29%), the down-regulated protein number was 541 (34%), and the insignificant-regulated protein number was 602 (37%).

As shown in Fig. 6(a), the enrichment pathway of the light reaction is shown along the electron transport chain. The light reaction of photosynthesis includes four stages: photosystem II (PSII), cytochrome b6/f complex (b6/f), photosystem I (PSI) and ATP synthase. The overall reaction formula is:

Fig. 6

Improved photosynthesis and carbon fixation pathways in Arthrospira platensis cells cultivated with the NaHCO3 product at a pressure of 0.3 MPa in the CO2 bicarbonation absorber, (a) improved photosynthesis pathway, (b) improved carbon fixation pathway (coloured boxes are Arthrospira specific enzymes, red boxes represent the up-regulated proteins, blue boxes represent the down-regulated proteins, and yellow boxes represent the uncertain-regulated proteins).

In the PSII stage, an H2O molecule was disintegrated by the high light energy, and the H+ proton gradient was established along the thylakoid membrane, and a high energy electron was released to the plastoquinone (Pq). This electron was transported to the b6/f, which also produced the H+ proton and transferred it to the ATP synthase. The PSI reaction centre was P700, and the activated electron from P700 was transferred consecutively to the primary accepter (A0), secondary acceptor (A1), iron-sulfur protein and ferredoxin (Fd). The NADP reductase (FNR) then restored the NADP+ to NADPH. At the same time, the H+ produced in PSII and the b6/f was transferred to the ATP synthase, during which the phosphate ion (Pi) and ADP were consumed, and ATP was produced. As shown in Table 1, the D1 (PsbA) and D2 (PsbD) protein increased by 1.4 and 1.5 times, respectively. The PSII reaction centre proteins of CP43 (PsbC) and CP47 (PsbB) increased by 1.8 and 1.5 times, respectively. The PSI reaction centre (PsaL and PsaE) and iron-sulfur (PsaC) proteins increased by 96% and 93%, respectively. The PSI plastocyanin (PsaF) protein increased by 76%. The cytochrome proteins of b6 (PetB), f (PetA), ferredoxin (PetF) and c6 (PetJ) increased by 2.1, 1.4, 1.7 and 4.0 times, respectively. The ATP synthase subunit proteins of beta (atpD) and b (atpF) increased by 2.1 and 2.6 times, respectively, whereas the subunit a (atpB) decreased by 40%. The reason for this may be that the HCO3− concentration, at 0.3 MPa, of the CBA was higher than that at 0.1 MPa, which was beneficial for the photosynthesis of the algal cells. As is known, the HCO3− ion can cross the cell membrane through active transportation, and was then catalysed to CO2 by the inorganic carbon transporters (such as LC11 and HLA3).[1,2] However, CA catalyses the extracellular HCO3− ion to CO2, the CO2 is diffused to the thylakoid membrane and fixed by the enzyme RuBisCO. Therefore, both of these methods required the participation of HCO3−. The higher HCO3− concentration required abundant ATP for the active transportation and dark reaction, the up-regulated ATP synthase subunit proteins of beta atpD, b atpF, and so on promoted the generation of ATP. In addition, the higher ATP consumption rate promoted the electron transport rate, thus, PSI and PSII were accelerated. The cytochrome complex, which was the electron carrier, was an essential protein in the electron transport chain. The up-regulated cytochrome proteins, such as b6 (PetB), f (PetA), ferredoxin (PetF) and c6 (PetJ) also contributed to the light reaction. Once again, the higher HCO3− concentration promoted the generation of ATP, which was beneficial for the electron transport chain. The up-regulated cytochrome proteins and accelerated electron transport rate co-contributed to the reaction of PSI and PSII.

The significant expressed proteins of photosynthesis in Arthrospira platensis cells cultivated with the NaHCO3 product in the CO2 bicarbonation absorber. FC: fold change

Protein name	Gene	FC	log2FC	State
Photosystem II D1 protein	PsbA	2.42	1.28	Up
Photosystem II D2 protein	PsbD	2.45	1.29	Up
Photosystem II CP43 reaction centre protein	PsbC	2.75	1.46	Up
Photosystem II lipoprotein	Psb27	3.27	1.71	Up
Photosystem II CP47 reaction centre protein	PsbB	2.50	1.32	Up
Photosystem II CP47 reaction centre protein	Psb28	1.93	0.95	Up
Cytochrome b559 subunit alpha	PsbE	3.94	1.98	Up
Photosystem II reaction centre protein	PsbH	5.83	2.54	Up
Photosystem II 12 kDa extrinsic protein	PsbU	3.15	1.66	Up
Cytochrome c-550	PsbV1	2.21	1.14	Up
Photosystem II cytochrome	PsbV2	4.36	2.12	Up
Photosystem II manganese-stabilizing protein	PsbO	2.49	1.31	Up
Photosystem II oxygen evolving complex protein	PsbP	1.80	0.85	Up
Photosystem I P700 chlorophyll a apoprotein A2	PsaB	1.59	0.67	Up
Photosystem I iron-sulfur center	PsaC	1.93	0.95	Up
Photosystem I protein	PsaD	1.93	0.95	Up
Photosystem I reaction center subunit XI	PsaL	1.96	0.97	Up
Photosystem I reaction center subunit IV	PsaE	1.96	0.97	Up
Putative plastocyanin docking protein	PsaF	1.76	0.82	Up
Cytochrome b6	PetB	3.06	1.61	Up
Cytochrome b6-f complex subunit 4	PetD	3.00	1.58	Up
Cytochrome f	PetA	2.39	1.25	Up
Cytochrome b6-f complex iron-sulfur subunit	PetC	3.17	1.66	Up
Ferredoxin	PetF	2.66	1.41	Up
Cytochrome c6	PetJ	4.98	2.32	Up
ATP synthase subunit beta	atpD	3.14	1.65	Up
ATP synthase subunit alpha	atpA	1.91	0.93	Up
ATP synthase gamma chain gamma	atpG	2.36	1.24	Up
ATP synthase subunit delta	atpH	1.82	0.87	Up
ATP synthase epsilon chain epsilon	atpC	2.43	1.28	Up
ATP synthase subunit a	atpB	0.58	−0.79	Down
ATP synthase subunit b	atpF	3.57	1.84	Up

The enriched carbon fixation pathway is shown in Fig. 6(b). In the Calvin cycle, the CO2 was catalysed by RuBisCO and was reacted with ribulose diphosphate (RuBP) to produce phosphoglycerate (PGA). The PGA reacted with ATP and NADPH to produce G3P that was transferred to carbohydrate and RuBP. The specific reaction formula is:

The higher HCO3− concentration mainly improved the expression of RuBisCO, as shown in Table 2, the RuBisCO (rbcL) and RuBisCO (cbbL) large chain increased by 3.5 and 2.4 times, respectively, improving the generation of G3P. The enzyme RuBisCO was important for the Calvin cycle, which determined the carbon assimilation rate of the photosynthesis. The up-regulated RuBisCO promoted the dark reaction of the algal cell, which accelerated the accumulation of biomass. In addition, the other proteins such as phosphoribulokinase (prkB), ribose-5-phosphate isomerase A (rpiA) and transketolase (tktA) were increased by 80%, 70% and 60%, respectively. These are helpful to the metabolism of pentose phosphate.

The significant expressed proteins of carbon fixation in Arthrospira platensis cells cultivated with NaHCO3 product in the CO2 bicarbonation absorber

Protein name	Gene	FC	log2FC	State
Ribulose-bisphosphate carboxylase (RuBisCO)	rbcL	4.50	2.17	Up
Ribulose-phosphate 3-epimerase	RPE	4.09	2.03	Up
Fructose-bisphosphate aldolase class II	ALDO	3.65	1.87	Up
RuBisCO large chain	cbbL	3.35	1.74	Up
Transketolase domain protein	tktB	2.98	1.57	Up
d-fructose 6-phosphate phosphoketolase	xfp	2.16	1.11	Up
Phosphoribulokinase	prkB	1.80	0.85	Up
Ribose-5-phosphate isomerase A	rpiA	1.68	0.74	Up
Transketolase	tktA	1.59	0.67	Up
Glyceraldehyde-3-phosphate dehydrogenase	gapA	0.67	−0.59	Down
Probable phosphoketolase	xpk	0.63	−0.67	Down
Fructose-1,6-bisphosphatase class 1	fbp	0.50	−0.99	Down

Practical applications of the CO2 bicarbonation absorber and the raceway pond

The CBA-RWP has broad application prospects in engineering. The CO2 gas added directly to the RWP caused a low CO2 utilization efficiency. A huge amount of CO2 gas was wasted and released to the atmosphere, causing secondary pollution. The NaHCO3 was also used to cultivate the microalgal. However, the chemical NaHCO3 was expensive. The price of Spirulina powder was around 1000–7000 $ per ton, whereas the NaHCO3 was about 300–700 $ per ton with a consumption of 0.9–1.2 ton per ton algal powder, this accounted for a huge percentage of the operation costs. Combining CO2 gas with Na2CO3 to cultivate microalgal has the potential to save on the operation costs and to reduce the CO2 emission. Pure CO2 gas was inexpensive, about 70–100 $ per ton. The Na2CO3 was 10–20 $ per ton and which can also be found in natural alkali lakes. During the later cultivation period, the Na2CO3 solution can be replaced by the wasted algal solution, as it contained a high sodium carbonate concentration. Also, the algal cell efficiently fixed CO2 gas without any secondary pollution. Therefore, optimizing the CBA-RWP to cultivate microalgal was both economically and environmentally friendly.

Conclusions

A CO2 bicarbonation absorber was proposed to efficiently convert CO2 gas and Na2CO3 solution to produce NaHCO3, which was easier to dissolve and remained for a longer time in the culture medium for promoting the microalgal growth rate. The CO2 gas reacted with the Na2CO3 solution (initial concentration = 200 mM L−1 and the volume ratio in the CBA = 60%) for 90 min at 0.3 MPa to give the optimized molar proportion (92%) of the NaHCO3 product in total inorganic carbon to increase the microalgal growth rate by 5.0 times. Expression levels of the PSII reaction centre protein (PsbH) and PSII cytochrome (PsbV2) in the photosynthesis pathway increased by 4.8 and 3.4 times, respectively, whereas that of the RuBisCO enzyme (rbcL) in the carbon fixation pathway increased by 3.5 times in Arthrospira platensis cells cultivated with the NaHCO3 product at 0.3 MPa in the CBA. However, development of continuous flow is needed for the NaHCO3 product, which would greatly improve the transfer efficiency, and would then be applicable for large-scale cultivation.

Conflicts of interest

There are no conflicts to declare.