Optimization to Hydrothermal Liquefaction of Low Lipid Content Microalgae <i>Spirulina</i> sp. Using Response Surface Methodology

Wei, Xuan; Jie, Dengfei

doi:https://doi.org/10.1155/2018/2041812

Journal of Chemistry

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Abstract Introduction Materials and Methods Results and Discussion Conclusion Conflicts of Interest Acknowledgments References Copyright Related Articles

Research Article | Open Access

Volume 2018 | Article ID 2041812 | https://doi.org/10.1155/2018/2041812

Optimization to Hydrothermal Liquefaction of Low Lipid Content Microalgae Spirulina sp. Using Response Surface Methodology

Xuan Wei^1,2and Dengfei Jie³

Academic Editor: Albert Demonceau

Received03 Aug 2017

Accepted24 Jan 2018

Published21 May 2018

Abstract

The production and nature of the biocrude obtained from Spirulina sp. by hydrothermal liquefaction (HTL) technology is focused in this investigation. Our aim is to evaluate the interaction of different factors on the bio-oil production through HTL using microalgae that contains relatively low lipid content and high protein. Optimization of three key parameters—concentration (mass of algae per mass of solvent), reaction temperature, and holding time—was carried out by response surface methodology (RSM). In this work, we used central composite design to conduct the experiment process. Graphical response surface and contour plots were used to locate the optimum point. The final results showed that the optimum concentration, temperature, and holding time were 10.5%, 357°C, and 37 min, respectively. Under the optimum conditions established, yield of the biocrude (41.6 ± 2.2%) was experimentally obtained using the fresh microalgae. This study showed the potential of bio-oil production of Spirulina sp. by HTL technology, but it still needs more improvement of the biocrude for utilization.

1. Introduction

Microalgae, which could fast convert CO₂ into biomass, have got an increasing interesting role in biofuel production [1]. They are considered more photosynthetically efficient than any other energy plants [2].

Microalgae have shown great potential to produce a wide variety of fuel products in present studies [3, 4]: (1) hydrogen (H₂) via direct and indirect biophotolysis [5], (2) biodiesel through transesterification [6], (3) biomethane via anaerobic digestion [7], (4) bioethanol by fermentation [8], and (5) bio-oil via thermochemical conversion [9].

Usually, microalgae contain the lipid in the range of 20–50% [10]. The lipid content is dependent upon strain and growth conditions [11]. After solvent extraction or physical extraction, these lipids of microalgae can then be further transesterified to biodiesels. One of the problems of this approach is that the wet aquatic biomass requires drying before it can be processed [12]. Hydrothermal liquefaction is one of the alternatives being increasingly considered, especially at low temperatures and pressures near the water critical pressure [13]. Wet microalgae with high water content could be converted into crude bio-oil by thermally and hydrolytically decomposing the biomacromolecules such as protein and lipid into smaller compounds. The biocrude is an energy dense product that can potentially be used as a substitute for petroleum crudes [14]. Some reports showed that hydrothermal liquefaction could be widely applied to various microalgae as the oil yield usually exceeds the crude fat content of microalgae [15].

Some of the most productive microalgae in terms of biomass production are lower in lipid and contain larger amounts of protein and carbohydrate [16]. Growing these algae for biodiesel is unlikely to be economical, and the alternative-processing routes would be advantageous such as Spirulina. The Spirulina industry in China is developing rapidly as a national strategic programme [17]. By the mid-1990s, China has become the biggest country in Spirulina production in the world. Just in 2009, 3,500 t (dw) of Spirulina have been produced [18]. The supply of Spirulina as the functional food has much exceeded the demand. Some studies showed the possibility of producing bio-oil using Spirulina by liquefaction technology [19–22]. If bio-oil is to be obtained efficiently from mass-cultivated Spirulina by liquefaction, this will be one of the both promising methods for energy production and one of the Spirulina consumption.

To date, there is still lack of the studies about the interaction of multifactors on bio-oil production using Spirulina. This work focuses on the optimization of hydrothermal liquefaction condition of Spirulina sp. using response surface methodology (RSM). The influences of process variables containing feedstock concentration, temperature, and holding time have been studied. We hope to evaluate the maximum production rate and further analyze the characteristic of biocrude by using the wet microalgae as the feedstock under the optimal condition.

2. Materials and Methods

2.1. Strains and Culture Media

The Spirulina sp. strain was bought from Freshwater Algae Culture Collection at the Institute of Hydrobiology (FACHB-collection). Strains were cultured for three weeks at 25°C with a continuous illumination of 120 μ·mol·m⁻²s⁻¹ in Spirulina medium. Per 1 liter, Spirulina medium contained 13.61 g of NaHCO₃, 4.03 g of Na₂CO₃, 0.50 g of K₂HPO₄, 2.50 g of NaNO₃, 1.00 g of K₂SO₄, 1.00 g of NaCl, 0.20 g of MgSO₄·7H₂O, 0.04 g of CaCl₂·2H₂O, 0.01 g of FeSO₄·7H₂O, and 1 mL of trace metal mix A₅. The trace metal mix A₅ contained 2.86 g of H₃BO₃, 1.81 g of MnCl₂·4H₂O, 0.222 g of ZnSO₄·7H₂O, 0.039 g of NaMoO₄·2H₂O, 0.079 g of CuSO₄·5H₂O, and 0.049 g of Co(NO₃)₂·6H₂O in 1 L of distilled water.

The freeze-dried Spirulina sp. powder was got from a local microalgae cultured farm. It was kept in dryer at −4°C. We measured the moisture of the fresh Spirulina sp. after reducing most of the water by centrifugation, and then, we diluted the sludge into the specific concentration after the optimization calculation. Meanwhile, the lipid and protein content of Spirulina sp. powder and fresh (Figure 1) were measured by the Soxhlet extraction method and Dumas combustion method, respectively.

(a)

(b)

2.2. Elements Analyses and Higher Heating Value (HHV) Estimate

The basic elements of the biomass are listed in Table 1. C, H, N, and S contents of the biomass were measured using an elemental analyzer (Flash EA 1112 series, CE Instruments, Italy). All measurements were repeated in triplicate, and a mean value was reported.

Estimation of HHV from the elemental composition of fuel is one of the basic steps in performance modeling and calculations on thermal systems [23]. As HHV is an important fuel property which defines the energy content of the fuel, we calculated the biomass and biocrude by the following equations, respectively [24, 25]:where C, H, O, and S are the weight percentages of carbon, hydrogen, oxygen, and sulfur, respectively.

2.3. Apparatus and Experimental Procedure

We applied central composite design of three key factors and five levels to simulate our experiment (Design-expert, V8.0, Stat-ease, Inc., USA). 374°C is the critical temperature, a dramatic increase of biomass degradation rate could appear near this critical point owing to the hydrolyze capability of water [26]. And after some single factor trials, the parameters were set like in Table 2. Finally, we obtained sixty biocrude samples from each of the conversion process that were triple duplicated.

The hydrothermal liquefaction was performed in a reactor (2 L, Parr, USA) at heating rate of the reactor approximately 2°C·min⁻¹. In each case, different weight of microalgae was mixed in deionized water. Microalgae were added into the reactor premixed as slurry. Then, the reactor vessel was sealed and nitrogen was introduced to purge the residual air. The microalgae slurry was stirred during the whole process. The speed of magnetic stir bar was set at 100 rpm. Meanwhile, the stir was cooled down by the condense water. The reaction started by heating the autoclave with an electric furnace. After heating the autoclave up to the required temperature, the temperature was maintained constant for the desired holding time, and then, the autoclave was allowed to cool to the room temperature.

2.4. Yield

After the conversion finished, we opened the reactor and dumped the reaction mixture into a beaker. The reactor and stir bar were washed with trichloromethane, and then, they were poured into the beaker too (Figure 2). And then, the solid residue was separated by the glass microfiber filter. The trichloromethane together with the reaction solvent was separated from the water-insoluble substance, and then, the trichloromethane in the mixture was evaporated using the rotary evaporator (RV 10 digital, IKA, Staufen, German) at 60°C under a vacuum condition.

The material remaining in the flask was the biocrude. The weight of biocrude was calculated by using the overall weight of the remaining materials after evaporation subtracting the initial trichloromethane-soluble substrate. The yield of biocrude is determined on a dry basis using the following equation:

2.5. FT-IR Analysis

Infrared (IR) spectra for biocrude samples were acquired using a FT-IR spectrometer (4100, JASCO Inc., Tokyo, Japan) to determine the main organic components based on the peaks of the functional groups present. The measurement wavenumber range is 7,800 to 350 cm⁻¹ and resolution is 4 cm⁻¹, controlled by JASCO’s exclusive Spectra Manager™ cross-platform software.

2.6. Constituent Analysis of the Fresh Biomass-Based Bio-Oil

The biocrude is analyzed by GC/MS on an Agilent 6890N GC/5975B MSD. A volume of 0.5 mL was injected for each sample, and the inlet temperature and split ratio are 300°C and 3 : 1, respectively. Two minutes solvent delay was set to protect the filament. The column was initially held at 40°C for 4 min. The temperature was ramped to 300°C at 4°C·min⁻¹ and held isothermally for 4 min, giving a total runtime of about 60 min. Helium flowing at 3 mL·min⁻¹ served as the carrier gas. NIST Mass Spectra Database was used for compound identification.

3. Results and Discussion

3.1. Sample Workup and Analysis

The optimization process was carried out to determine the optimum value of bio-oil yield using the Design Expert 8.0 software. The biocrude is a dark viscous liquid. Table 3 shows the yield of each experiment. The yield of biocrude was in the range of 37.2–44.4% and the average was 40.9%. Table 4 shows that the HHV was in the range of 26.7–36.0% and the average was 32.0 MJ·kg⁻¹. The HHV are much higher than the feedstock. The oxygen content of microalgal biocrude in our study was a little higher than in some other microalgal liquefaction studies [20, 27]. The sulfur content of microalgal bio-oil was less than 1% in all cases.

We used the Design Expert software to analyze the experimental results by multiple regressions fitting analysis. Following is the quadric multiple regression equation of yield:

After that, we carried on a significance test of the regression equation. From Table 5, we can see that first degree terms of temperature and concentration are very significant (), the holding time is significant (), and quadratic terms of the three variables are very significant (). The Model value of 23.02 implies the model is significant. There is only a 0.01% chance that a “Model value” this large could occur due to noise. The “Lack of Fit value” of 2.70 implies the Lack of Fit is not significantly relative to the pure error. There is a 15.02% chance that a “Lack of Fit value” this large could occur due to noise. Nonsignificant lack of fit is good, and we want the model to fit.

3.2. Graphical Interpretation of the Response Surface Models

In order to determine the effect of the independent variables on the yield of biocrude, a three-dimensional diagram and contour plot for each response were generated as a function of two variables, while the other one variable was held constant. Figure 3 shows the response surface and contour plots for biocrude yield as a function of concentration () and temperature () with a holding time of 40 min. As can be seen from Figure 3, with the increase of temperature, the yield increases and finally tends towards stability. The yield firstly increases and then decreases with the increase of the concentration. The highest yield (44.4%) occurs when the concentration and temperature are kept at about 10.5% and 355°C, respectively.

(a)

(b)

Figure 4 shows the response surface and contour plots for biocrude yield as a function of temperature () and holding time () with the concentration of 12.5%. Under this condition, the yield firstly increases and then decreases with the increase of temperature or holding time. The yield reaches to the highest (44.4%) when the concentration and holding time are kept at about 354°C and 38.5 min, respectively.

(a)

(b)

Figure 5 illustrates the response surface and contour plots for bio-oil yield as a function of concentration () and holding time () with specific temperature. The yield also shows increase at the beginning and then decrease with the increase of concentration or holding time with the temperature of 345°C. The highest yield is 44.4% when the concentration and holding time are kept at about 11% and 38 min, respectively.

(a)

(b)

3.3. Determination of HTL Process of Fresh Spirulina sp. with Optimal Variables

According to the software optimization step, the desired goal for each operational condition (temperature, holding time, and concentration) was chosen “within the range,” while the response (the yield of biocrude) was defined as “maximum” to achieve the highest performance. The program combines the individual desirability into a single number and then searches to maximize this function. Accordingly, optimum working conditions are concentration of 10.5%, temperature of 357°C, and holding time of 37 min. The largest yield is 44.4%. In order to verify the optimal condition, we used cultured microalgae for the further experiment. The moisture of fresh microalgae was 82.1 ± 1.6% after centrifugation. We added some water to the microalgae slurry for the HTL process. The result of three replicated experiments was 41.6 ± 2.2%. The result indicated that when each of the parameters was set as the optimum value, the bio-oil yield was in agreement with the value predicted by the model. It implies that the strategy to optimize the HTL conditions using Spirulina sp. and to obtain the maximal biocrude yield by RSM in this study is feasible. Dimitriadis and Bezergianni showed that the yields from algae by HTL obtained from the literature are more dispersed, but 40% of them render a 45% oil yield [26]. Our results indicated that the bio-crude yield of Spirulina sp. is a little less than that of some microalgae by HTL, but the performance is not bad, and it is still worth for further analysis.

3.4. FT-IR Analysis

The FT-IR analysis of bio-oil provided results consistent with the GC-MS characterization and the elemental analysis. In the FT-IR analysis, the curves (Figure 6) of the bio-oil obtained under different condition showed some difference. But most of them are similar, suggesting that the same types of functional groups exist in these samples. The composition of the bio-oil is complex as there are many absorbance band and some main bands are shown in Table 6. The bio-oil showed a strong absorbance between 2850 and 3000 cm⁻¹, indicating a high content of methyl and methylene groups. There was also a strong absorbance around between 1500 and 1700 cm⁻¹, and C=O stretching indicated the presence of ketones, aldehydes, esters, or acids.

3.5. GC-MS Analysis

Specific compositions of the biocrude products were not easily identifiable by FT-IR, so the biocrude obtained from fresh Spirulina sp. by the HTL was characterized by GC-MS for identification of their chemical compositions too. For a better understanding of the properties of the biocrude, a mass spectral library and computer matching were used to facilitate compound identification. Hundreds of peaks were detected by GC-MS in this investigation. The results reveal that the HTL-based microalgal biocrude is an extremely complex mixture of numerous compounds; some major chemical categories are listed in Table 7. The compositions are far different from the bio-oil obtained from the Chlorella pyrenoidosa or Dunaliella tertiolecta cake by HTL [27–29]. Some compounds are similar with the compounds in bio-oil obtained by hydrothermal liquefaction of Chlorella vulgaris and Spirulina using alkali and organic acids as catalyst [20, 30]. The final hydrocarbon product has about 19 wt.% in naphtha range (mainly C₅–C₁₀) and 84 wt.% in diesel range (mainly C₁₀–C₂₀). The hydrocarbons have about 7 wt.% larger than C₂₀. That is probably why the biocrude was a dark viscous liquid.

4. Conclusion

In this study, bio-oil crude was produced by hydrothermal liquefaction using Spirulina sp. By RSM optimization, we got the optimal reactor condition that was 10.5% of concentration, 37 min of holding time, and 357°C of temperature and finally got the yield of 41.6 ± 2.2% using the fresh Spirulina sp. as the feedstock. Among the three variables examined in this study, temperature and concentration were the most influential factors on the product oil yield. The characteristic of the bio-crude displayed the potential ability of Spirulina sp. to be a valuable and environmentally friendly feedstock candidate for biofuels and biochemicals. As some of the compounds in biocrude, such as fatty acids and aldehydes, are directly related to the undesirable properties of bio-oil, the biocrude still needs more improvement to be used as the liquid fuel.

Conflicts of Interest

The authors declare that they have no conflicts of interest.

Acknowledgments

This study was supported by the Natural Science Foundation of Fujian (2017J05041) and Fundamental Research Funds for the Central Universities. The authors thank the project of Gaoyuan Agricultural Engineering of Fujian (712018014).

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Copyright © 2018 Xuan Wei and Dengfei Jie. This is an open access article distributed under the Creative Commons Attribution License, which permits unrestricted use, distribution, and reproduction in any medium, provided the original work is properly cited.

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