Optimization of Biochar Production by Co-Torrefaction of Microalgae and Lignocellulosic Biomass Using Response Surface Methodology

: Co-torrefaction of microalgae and lignocellulosic biomass was evaluated as a method to process microalgae sludge produced from various efﬂuents and to obtain biochars with suitable properties for energy or material valorization. The inﬂuence of four independent variables on biochar yield and properties was evaluated by a set of experiments deﬁned by response surface methodology (RSM). The biochars were characterized for proximate and ultimate composition, HHV, and methylene blue adsorption capacity. HHV of the biochars was positively correlated with carbonization temperature, residence time, and lignocellulosic biomass content in the feed. Co-torrefaction conditions that led to a higher yield of biochar (76.5%) with good caloriﬁc value (17.4 MJ Kg − 1 ) were 250 ◦ C, 60 min of residence time, 5% feed moisture, and 50% lignocellulosic biomass. The energy efﬁciency of the process was higher for lower temperatures (92.6%) but decreased abruptly with the increase of the moisture content of the feed mixture (16.9 to 57.3% for 70% moisture). Biochars produced using algal biomass grown in contaminated efﬂuents presented high ash content and low caloriﬁc value. Dye removal efﬁciency by the produced biochars was tested, reaching 95% methylene blue adsorption capacity for the biochars produced with the least severe torrefaction conditions. This study intends to evaluate the co-torrefaction of microalgae sludge with lignocellulosic biomass as a simple and low-cost technology to process algal sludges obtained from the bioremediation of industrial or agro-industrial efﬂuents. The co-torrefaction process was also selected as a technology to promote the elimination of nitrogen, therefore improving the fuel quality of algal biomass by decreasing its potential to generate NOx emissions. Nitrogen is eliminated during devolatilization and char conversion processes The inﬂuence of process parameters (carbonization temperature, residence time, concentration of lignocellulosic biomass in the and the moisture of the feed) in the yields of carbonization products and properties of the biochars were studied using a series of experiments deﬁned by RSM (response surface methodology). Moreover, this work also tested the co-torrefaction of microalgae used in the bioremediation of an aquaculture efﬂuent and a landﬁll leachate as examples of real case scenarios and provides insights on the use of the produced biochars as low-cost adsorbents.


Introduction
Microalgae are efficient agents for the bioremediation of animal production effluents due to their high capacity to remove nitrogen and phosphorus, two important contributors to the chemical oxygen demand (COD) of such effluents [1][2][3]. The robustness of microalgae makes them suitable to treat recalcitrant effluents with high levels of organic or inorganic contaminants, that are difficult to remediate with aerobic or anaerobic bacteria [3][4][5]. After bioremediation, the algal biomass must be separated from the treated effluent and ideally valorized as raw material for fuels and/or specialty chemicals. Separation of the algal biomass has been studied using membrane technology [6], electrocoagulation [7,8], radiofrequency [9], and coagulation with polymers [10], but these techniques involve complex equipment and additional costs that are compatible only with large scale systems with the subsequent valorization of the algal biomass in multiple applications. A possible alternative is the decantation of the sedimented biomass, in the form of an algal sludge that can be further dried or mixed with other biomass feedstocks to be used in energy or material applications. For example, mixing wet algal biomass (80% moisture) with yard This study intends to evaluate the co-torrefaction of microalgae sludge with lignocellulosic biomass as a simple and low-cost technology to process algal sludges obtained from the bioremediation of industrial or agro-industrial effluents. The co-torrefaction process was also selected as a technology to promote the elimination of nitrogen, therefore improving the fuel quality of algal biomass by decreasing its potential to generate NOx emissions. Nitrogen is eliminated during devolatilization and char conversion processes [39]. The influence of process parameters (carbonization temperature, residence time, concentration of lignocellulosic biomass in the feed, and the moisture of the feed) in the yields of carbonization products and properties of the biochars were studied using a series of experiments defined by RSM (response surface methodology). Moreover, this work also tested the co-torrefaction of microalgae used in the bioremediation of an aquaculture effluent and a landfill leachate as examples of real case scenarios and provides insights on the use of the produced biochars as low-cost adsorbents.

Biomass Feedstocks Characterization
Microalgal biomass (Cv) and lignocellulosic material (Lc) were used as raw materials in this study. The Cv sample corresponded to dried Chlorella vulgaris biomass obtained from a commercial source (Allmicroalgae-Natural Products S.A.). The Lc sample was composed of waste pine biomass used for pellet production and was supplied by CMC Biomassa. The Lc sample was further milled in a coffee grinder (Bosch TSM6A011W) and sieved by a 10 mesh (= 2 mm) sieve. Both biomasses were oven-dried until a moisture content of 5% was achieved. Proximate analysis of ash content (Ash), volatile matter (VM), and moisture (MC) was determined gravimetrically, for both biomass materials, according to the methods described in BS EN 15403:2011, 942-2007, and ISO 665:2020, respectively. Fixed carbon (FC) was determined by difference in a dry basis (db). Ultimate analysis (carbon, hydrogen, nitrogen, and sulfur contents) was performed using an elemental analyzer (Thermo Finnigan-CE Instruments Model Flash EA 112 CHNS series). Oxygen content was determined by difference on a dry ash free basis (daf).
High heating values (HHV) of the feedstocks were calculated using a correlation established by Huang and Lo [40] After process optimization, microalgae biomass obtained from the remediation of an aquaculture effluent [4] and a landfill leachate [3] were subjected to the co-torrefaction process with lignocellulosic material (0, 50, and 100%) at 250 • C and 60 min, without water addition, that is, with 5% feed moisture. The aquaculture microalgae biomass was produced over 34 days in 1.5 L reactors using un effluent with 9600 mg O 2 L −1 of COD, 3266 mg N L −1 , and 23 mg P L −1 and reaching biomass productivity of 880 mg L −1 d −1 . The landfill leachate microalgae biomass was produced over 27 days in 2 L reactors using un effluent with 5200 mg O 2 L −1 of COD, 738 mg N L −1 , and 22 mg P L −1 (pretreated with biomass ash) and reaching a biomass productivity of 40 mg L −1 d −1 . Biochars obtained in the experiments with microalgae produced in aquaculture wastewater and landfill leachate were analyzed following the same methodology used for biochars obtained with commercial dry microalgae (Section 2.4).

Torrefaction Experiments
The torrefaction tests were performed on a glass reactor placed in a gas chromatography furnace (Thermo Finnigan Trace GC with FID), under oxygen-limited conditions, as described byŞen et al. [41]. For each experiment, selected masses of dry algal biomass, lignocellulosic material, and added water were introduced in the reactor in order to achieve the values of Lc incorporation rate and feed moisture defined in the experimental design, as shown in Table S1 (Supplementary Materials). A total of 39 initial compositions were  considered, with incorporations of 0, 25, 50, 75, and 100% of lignocellulosic material and  feed moisture contents of 5, 15, 30, 45, and 70%. The samples were placed in 250 mL glass  flasks and heated up to the final torrefaction temperatures (200, 225, 250, 275, or 300 • C)  while the conditions were kept isothermal for 15, 30, 45, or 60 min. In the end, the furnace was cooled to 35 • C, with a cooling rate equal to the heating rate that varied between 11 and 14 • C/min.
The liquid phase was collected in a cooling trap and the mass yields of biochar and liquid phase were determined with an analytical scale (Mettler Toledo AB204-S). The gas yield was determined by difference. Biochar samples were stored in dry conditions until further analysis and liquid phase samples were stored at −4 • C to avoid chemical and biological degradation.

Torrefaction Products Characterization
The biochars were characterized using the methods described in Section 2.1. The HHV of the produced biochars was determined through the correlation established by Parikh et al. [42]: where FC, VM, and Ash are the fixed carbon, volatile matter, and ash content of the biochar, respectively, expressed in wt.%, db. The aqueous phase of the torrefaction process was analyzed for pH (Crison MicropH 2001), conductivity (Mettler Toledo MC226 Conductivity Meter), chemical oxygen demand (COD) through the high range dichromate method (Hanna Instruments test kits), total phenolics content (TPC), and reducing sugars (RS). Total phenolics were quantified by the Folin-Ciocalteu method, as proposed by Singleton et al. [43], and total reducing sugars content was determined by the DNS method, as described by Miller [44]. All the analyses were performed in triplicate, and the presented results correspond to average values.

Process Performance
The mass and energy yields of the produced biochars were calculated using Equations (3) and (4), respectively: Energy yield (%) = Mass yield × HHV biochar HHV raw material × 100 (4) where m biochar and HHV biochar are the mass (kg) and high heating value of biomass char (MJ Kg −1 ) and m raw material and HHV raw material are the mass and high heating value of raw biomass material. Process energy efficiency (PEE) compares the energy contained in the biochars with the sum of the energy in the original raw biomass plus the energy required for the torrefaction process. This parameter was calculated through Equation (5) [45]: where Q input is the total energy requirements of the torrefaction process, in MJ. Q input was determined as the sum of the different energy requirements of the process, as follows: where Q 1 represents the energy needed to heat the feedstock from room temperature to process temperature (∆T). The specific heat of the biomass sample (Cp raw material) was evaluated using the values of 4.1 × 10 −3 MJ Kg −1 K −1 for algal biomass and of 1.7 × 10 −3 MJ Kg −1 K −1 for lignocellulosic material, used by Artan et al. [46], and taking into account their relative concentrations in the initial feedstock. Q 2 represents the energy needed for heating the water present in the reactor (m H2O ) from room temperature to 100 • C (∆T), considering the specific heat of water as Cp H2O = 4.1379 × 10 −3 MJ Kg −1 K −1 .
Q 3 is the latent heat of water vaporization (L = 2.26 MJ Kg −1 ), corresponding to the energy needed for water evaporation at 100 • C.
Q 4 corresponds to the heat of reaction for the torrefaction process itself. This parameter was inferred from the values obtained by Ohliger et al. [47], for different temperatures, residence times, and moisture.
Q 5 are the thermal losses connected to the diffusion losses through the reactor walls and heat loss from the biochar and produced gas exiting the reactor. These thermal losses were assumed to be 45% at 300 • C and 60 min and 25% at 200 • C and 15 min; the other values for all the combinations of temperature and residence time were interpolated [45].

Response Surface Methodology
For the study, four independent variables (temperature, residence time, incorporation rate of lignocellulosic material, and moisture content of algal biomass) were considered, using four or five levels for each variable ( Table 1). Selection of the experimental conditions was based on the RSM model and Design-Expert ® Software version 12-Stat-Ease (12.0.0.6), yielding a total of 39 experimental runs including 29 trials for model determination, 5 trials for lack of fit, and 5 replicates for pure error estimation as described in Table S1 (Supplementary Materials). The operational variables of the process were optimized considering the results obtained. The p-value confidence level used to assess the model terms was 95%. To verify the adequacy of the model, the value of the determination coefficient (R 2 ) was compared to the adjusted value of R 2 . The three-dimensional surface graphics generated by the software served to evaluate the interaction between the process variables and their effect on the output response.

Adsorption Experiments
Methylene blue (MB), a synthetic dye often present in industrial wastewaters, was used as a model compound to evaluate the biochar adsorption capacity towards cationic contaminants. The adsorption of MB by the produced biochars was measured with a quick adsorption method based on the work of Correia et al. [48]. The biomass or biochar samples were milled and sieved to less than 500 µm diameter before use in the adsorption experiments. A small mass of each sample (25 mg) was added to a test tube containing 5 mL of a MB aqueous solution (100 mg L −1 ) and the tube was shaken for 3 s (Heidolph top shaker) and then centrifuged at 3000 rpm for 5 min (Hettich EBA 20). The supernatant was transferred to another tube and the concentration of dye was determined by UV-VIS spectrophotometry (Biochrom Libra S4) at 664 nm. The adsorption capacity (q) was determined using Equation (7): where C i and C f are the initial and final concentrations (mg L −1 ) of dye in the aqueous solution.

Biomass Feedstock Characterization
The characterization of the original feedstocks and the mixtures of microalgae and lignocellulosic biomass used in the torrefaction tests are presented in Table 2. Samples Cv and Lc presented significant differences in their proximate and ultimate compositions: Cv presented higher ash, nitrogen, and volatile matter contents while Lc showed higher concentrations of fixed carbon and oxygen. The lower ash content of Lc may be related to a higher HHV, and its lower nitrogen content reduces the potential for harmful NOx emissions in case of energy recovery. Han et al. [49] determined the elemental analysis of the C. vulgaris biomass, obtaining values (C: 47.4%; O: 27.9%; N: 10.9%; H: 9.9%; and S: 0.7%) in line with those obtained in the present study, and confirming the tendency of high nitrogen concentrations in algal biomass.
The advantage of mixing lignocellulosic biomass with algal biomass is primarily to decrease the ash and nitrogen contents of algal biomass, improving its fuel quality. Furthermore, in real conditions, algal biomass can be obtained in the form of a decanted sludge, with high moisture content and the mixing with dried biomass residues can facilitate the process of sludge drying, even at atmospheric conditions. Microalgae coming from effluent treatments are not typically used in food or cosmetic applications and therefore do not undergo the same treatments as commercial microalgae (spray drying). Therefore, in this work, different mixtures of Cv and Lc biomasses were considered as a substrate for co-carbonization, and the moisture of the biomass mixtures was adjusted to controlled values by the addition of selected volumes of water. The purpose of this approach was to simulate the mixing of dried lignocellulosic biomass and decanted microalgae sludge and the direct use of the mixture as feed for biochar production. As seen in Table 2, additions of Lc of 25%, 50%, and 75% of the feed were considered, and this approach had a significant effect on the ash content and nitrogen content of the feed, reaching values of 3.78% for ash content and 3.09% for nitrogen content for the mixture with 75% Lc.

Characterization of Torrefaction Products
The conditions of the co-torrefaction experiments were selected according to a response surface methodology, in order to evaluate the influence of the following parameters: carbonization temperature, residence time, incorporation of lignocellulosic biomass in the feed, and moisture of the feed. A total of 39 experiments were performed and the solid and liquid products obtained were characterized for composition and relevant properties.

Biochars
The appearance of the biochars obtained by the torrefaction of microalgae and lignocellulosic biomass mixtures, with 50% Lc, at different temperatures and residence times is shown in Figure 1. The variation in color intensity is clearly a function of the final torrefaction temperature. At the temperatures of 200 • C, regardless of the residence time, there were no significant changes in the colors of biochars that were similar to the color of the feed mixture. This suggests that, at such mild conditions, the torrefaction process had minor effects on feedstock composition and structure, with changes restricted to the loss of water and volatile matter. Higher temperatures and longer residence times yielded darker biochars, indicating some degree of decomposition and rearrangement of the feedstock. The color of the biochars produced at 250 • C was influenced by the residence time while all biochars produced at 300 • C presented a homogeneous black color. As such, torrefaction temperature showed a larger impact on biochar color than torrefaction time, thus being responsible for a higher degree of decomposition and molecular rearrangement of the tested samples.
The proximate and ultimate compositions of the biochars were determined, as well as their HHV and MB adsorption capacity (q MB ), to evaluate their suitability for energy or material applications (Table 3). Biochars obtained at higher temperatures and residence times presented a higher amount of fixed carbon and less volatile matter. The incorporation of lignocellulosic biomass decreased the ash content of the biochars (12.6 to 4.8%) because of the higher ash content of the Cv sample. The HHVs of the biochars presented the lowest and highest values of 14.8 and 21.4 MJ Kg −1 , for 0% Lc and 100% Lc, respectively. This parameter was significantly improved for samples subjected to more severe torrefaction conditions and decreased for a greater amount of water in the feedstock. In particular, HHVs higher than 18 MJ Kg −1 were obtained for mixtures with the incorporation of Lc from 0% to 50% at the temperatures of 275 • C and 300 • C. Similar conclusions were drawn by Chen et al. [22] for biochars produced from sawdust, wheat straw, pine, and microalgae. In general, the biochars with better fuel properties were those subjected to a torrefaction process at temperatures above 275 • C and residence time above 45 min, which shows that nitro-gen elimination and deoxygenation reactions played a major effect on the biochar final properties [50].
The variation of the elemental composition of the biochars relative to the feedstocks, expressed as their H/C and O/C atomic ratios, is shown in a van Krevelen diagram ( Figure 2). As can be seen, the biochars produced at 200 • C and 225 • C evidenced some degree of deoxygenation, expressed as a decrease of the O/C ratio relative to the raw materials Cv and Lc, but no significant structural rearrangements were detected since the H/C ratio was comparable to the feedstocks. As the torrefaction temperature increases the deoxygenation reactions become more relevant leading to biochars with O/C ratios between those of lignite and anthracite, demonstrating the upgrading effect on fuel quality [52]. For torrefaction temperatures higher than 250 • C, a temperature-dependent decrease of the H/C ratio also occurred, indicating that the rearrangement of the carbonaceous structure takes place with increasing formation of aromatic structures [53].
In contrast, the adsorption capacity for methylene blue (q MB ) was negatively influenced by the torrefaction capacity, since q MB values higher than 60% were obtained for biochars produced at 250 • C or lower (Table 3). Since methylene blue is a cationic dye, this behavior agrees with the adsorption of the dye due to ion exchange, hydrogen bonding, and electrostatic interactions with the carboxyl groups from the feedstock, which are partially retained in the biochar surface if the carbonaceous structure is not strongly modified, that is, for the lower torrefaction temperatures [48]. Severe torrefaction conditions lead to more significant rearrangement in the lignocellulosic structure of biochars with Lc, altering the surface porosity, by removing the binding-OH groups [54,55]. The biochars with the highest adsorption capacity were obtained at 200 • C, 30 min, and 25% of lignocellulosic material incorporation and 15% moisture, reaching 95% adsorption. Some biochars showed a better adsorption efficiency than the original biomasses' feedstocks (59.2% for Cv and 18.3% for Lc), which may be the result of an increase of hydroxyl and carboxyl groups generated on the biochar surface by hydrolysis reactions at low torrefaction temperatures. Relative to the raw biomasses, biochars also have the advantage of being less susceptible to chemical or microbial degradation, because of their lower moisture content [56].
The q MB of the biochars was not influenced by the percentage of Lc incorporation, probably because both feedstocks present anionic groups in their surface that may be involved in the adsorption process [57,58].
The adsorption capacity of a commercial activated carbon is close to 100% for several contaminants, including MB, because it involves porous adsorption, a more effective and extensive adsorption mode. Nevertheless, activated carbon production is expensive, energy-demanding, and generates contaminated effluents; thus, its use should be reserved for specific high-value applications, while low-cost biochars may be used for the preliminary treatment of highly contaminated effluents produced in high volumes [59]. Thus, by choosing the operational conditions it is possible to obtain biochars with characteristics more adequate for use as an alternative adsorbent for cationic species or to incorporate in solid fuels. The incorporation of Lc biomass is more relevant for the energy application, allowing the moisture of the feedstock mixture to be reduced and the composition of the biochar product to be improved.

Aqueous Phase
The torrefaction process yields a liquid by-product mainly composed of water recovered from the feedstock moisture and dehydration reaction. This aqueous phase contains various organic products produced during the decomposition of the feedstock and distilled at the reaction temperature. Those volatile organic products are either dissolved in the aqueous phase (if they have moderate to high dipole moment) or in the form of suspended droplets or particles (if they are non-polar compounds with low solubility in water). In some of the torrefaction conditions, the concentration of non-polar organic products was high enough to form a water immiscible organic phase (bio-oil) that separated from the aqueous phase upon cooling of the condensated liquid products. This bio-oil product was separated by decantation before the characterization of the aqueous phase. The presence of dissolved or suspended organic compounds confers specific properties to the aqueous phase, namely, influences its pH conductivity, total phenolic components, total sugars, and chemical oxygen demand. Characterization of the aqueous phases from all torrefaction tests was performed to evaluate the influence of operational parameters in these properties and is presented in Table 4.  As expected, torrefaction trials with higher temperature and residence time led to aqueous phase samples with a greater load of organic components, resulting in higher COD (766 g O 2 L −1 ), reducing sugars (54,000 mg L −1 ), and total phenolics (40,547 mg L −1 ). The increase in phenolic compounds concentration is largely due to the degradation of lignin and hemicellulose that occurs to a greater extent at higher temperatures, such as 275 and 300 • C [60]. Moreover, at temperatures of 250 • C and higher, cellulose suffers decomposition reactions leading to the formation of acids and alcohols and aldehydes and ketones such as acetic acid, oxalic acid, acetone, acetaldehyde, and propanoic acid [38].
The increase in moisture led to a significant decrease in the total phenolic content (from 40,547 to 22 mg L −1 ), COD (from 766 g L −1 to 0.8), and reducing sugars (from 54,000 mg L −1 to n.d.), potentially related to a dilution effect [38]. On the other hand, decreasing the incorporation of lignocellulosic material resulted in a reduction in total phenolics and reducing sugars, but a slight increase in COD, which may be related to the fact that microalgae may yield lower amounts of reducing sugars and phenolic compounds than lignocellulosic biomass, but their decomposition generates other organic analytes, such as simple sugars, organic acids, and amino acids, that contribute to the COD value [38].
Conductivity and pH were also higher in the situations of greater reaction severity, because of the dissolution of polar and acidic organic products. According to Cahyanti et al. [61], biomass torrefaction condensates produced below 300 • C are potential inhibitors of microbiological processes due to their concentrations in phenolic compounds, furans, and polycyclic aromatic hydrocarbons (PAHs), whose concentration increases with the severity of the torrefaction process [61]. For this reason, the use of the aqueous phases of the torrefaction process has been studied in agriculture as an herbicide and pest repellent [61]. This product is also known as pyroligneous acid, and it is known for its effect as an antimicrobial agent, insecticide, antioxidant, and for having properties to promote seed germination and plant growth. It mostly consists of aromatic, aliphatic, and naphthenic hydrocarbons and other oxygenated compounds such as aldehydes, alcohols, furans, ketones, acids, phenols, and ethers [62].

Torrefaction Process Performance
The torrefaction process converted the feedstocks to solid, liquid, and gas products at yields that were determined gravimetrically and are shown in Table 5. The condensates included two immiscible phases (aqueous phase and bio-oils) that were separated by decantation for individual accounting and characterization.  Biochar yield decreased from 90.5 to 23.0% with increasing temperature or residence time due to a higher thermal decomposition of the raw materials, leading to an increase of the aqueous phase yields (0.7 to 57.5%), bio-oil (0 to 35.8%), and gas products (1.0 to 24.5%).
As expected, biochar yields also decreased with increasing water content of the feed due to lower availability of carbonaceous components [31]. Initial feed moisture had a positive correlation with the yields of the aqueous phase and gas products because it contributes to a net water volume and may increase the extension of some hydrothermal oxidation reactions [63]. Generally, high biochar yields indicate that most of the feedstock carbon was recovered in the solid products, while high yields of condensates and gases may be related to their availability in the feed but also a higher degree of decomposition reactions. The loss of feedstock mass as volatile components was positively correlated with a decrease in the O/C and H/C ratios of the biochars, confirming an upgrading effect by the thermochemical process of torrefaction.
Bio-oil yield showed a linear correlation with operating temperature because of the increase in the formation of organic by-products through pyrolytic processes involving covalent bond breaking and deoxygenation processes [62]. The influence of residence time in the bio-oil yield was more evident for tests performed at more than 30 min, probably due to kinetic limitations of the thermal degradation processes [64]. At comparable temperatures, bio-oil yields were lower for higher moisture contents (>5%), which may be related to the increase of aqueous phase volume and consequent dissolution of higher amounts of bio-oil components such as aromatic hydrocarbons (e.g., naphthalene) and carboxylic acids (e.g., acetic acid) [65].
The incorporation of lignocellulosic material did not show a clear correlation with product yields because both feedstocks are susceptible to thermal degradation in the range of operating conditions used.
Biochar yields higher than 80% were obtained for the tests performed with 5% of moisture at 200 to 250 • C and with the incorporation of at least 50% lignocellulosic material.
It is known that torrefaction increases the hydrophobicity of the torrefied material, as well as its energy density, whilst reducing biomass tenacity [61]. Torrefaction makes the product more energy-dense due to the elimination of oxygen in the pyrolytic degradation reactions. Zhang et al. [66] studied the torrefaction of microalgae and assigned decarbonization, dehydrogenation, and deoxygenation levels of 20, 60, and 93%, respectively, for the biochar product obtained at 300 • C and 60 min, while at milder torrefaction conditions of 200 • C and 15 min, estimated values were 0.7, 10, and 17%, for the same thermal degradation processes.
To evaluate the performance of the torrefaction process, the energy yield and the process energy efficiency (including process energy requirements) were determined and are detailed in Table 6.  The energy yield, expressed as the amount of energy contained in the raw material that is retained in the biochar, reached the highest value (99.8%) at 200 • C, 60 min, 5% moisture, and 0% lignocellulosic material incorporation. Energy yield decreased with increasing temperature and moisture because both parameters were negatively correlated with biochar yield. According to Zhang et al. [51], biochars produced by torrefaction of microalgae residues (1.8% moisture) had energy yields that ranged from 77% (300 • C and 60 min) to 93% (200 • C and 15 min) in a nitrogen environment. In the present study, comparable energy yields were obtained for feedstocks with 5% or 15% of initial moisture and temperatures up to 250 • C. At higher temperatures, the biochar yields obtained were lower than 70%, probably because torrefaction was performed in oxygen-deficient conditions but not under a nitrogen flow, which limits autothermal decomposition reactions.
The determination of the heat requirements is challenging because there are considerable differences in the magnitude of thermal losses, in the specific heat of raw materials and the heat of reaction, depending on the configurations and dimensions of the reactors [67]. Q 1 (energy required for feedstock heating) increases with increasing process temperature. In this study, there was also an increase in Q 1 when the feedstock was mostly lignocellulosic material, with a when algal biomass was incorporated because the Cp of lignocellulosic material is higher (Cp lignocellulosic = 1.7 KJ Kg −1 K −1 [68]) than that of algal biomass (Cp microalgae = 1.58 KJ Kg −1 K −1 [69]). Q 2 and Q 3 , which are energy requirements for heating and evaporation of the water in the system [45], increased with moisture. Q 4 is the heat of reaction that decreases with the increasing temperature and residence time because the magnitude of exothermic reactions is increased by the process severity [38]. Q 5 represents thermal losses, and it increases with the process temperature and residence time. The thermal losses were evaluated as in Nobre et al. [45]. The PEE and energy yield were higher in mild torrefaction conditions because, under these conditions, less mass loss occurred. However, the HHVs of these biochars were lower because of their high O/C and H/C ratios, and therefore their fuel quality was negatively affected.
The relation between the torrefaction process energy efficiency (PEE, %) and the high heating value of the produced biochars (HHV, MJ Kg −1 ) is represented in Figure 3.
For the energy valorization pathway to be viable, it is necessary to choose conditions in which the process energy efficiency is higher than 50%, that is, the energy recovered in the products is higher than the sum of the process energy with the heat of combustion of the feedstock. On the other hand, to produce a biochar with a good fuel quality, process conditions that lead to biochars with the highest HHV should be selected.
As seen in Figure 3, the biochars produced at 200 • C and 250 • C presented HHVs lower than 18 MJ Kg −1 , regardless of the corresponding PEE value, while at 300 • C, it was possible to obtain biochars with HHVs higher than 18 MJ Kg −1 for most conditions tested and particularly for PEE values higher than 60%.

Response Surface Methodology (RSM) Analysis
RSM has been widely applied to process improvement and optimization, reducing the number of experimental runs needed to evaluate the influence of several independent variables in the critical properties to be studied [70]. For the quadratic model suggested by the RSM, the non-significant terms, with p > 0.05 (except those that support the modelnon-significant linear terms: A, B, C, D) were removed. This operation resulted in a reduced equation for each answer, which describes the adjustment to the experimental data. The equations for product yields with significant terms are found in (Supplementary Materials) and for biochar characterization in Table S3 (Supplementary Materials). The equations for process performance and HHV are presented in Table 7, except for Q input and Q output (Table S4, Supplementary Materials).   Note: p-value model is always 0.01%, and it means that there is only a 0.01% chance that an F-value this large could occur due to noise. The lack of fit is not significant (<4). ** Where T, t, M, and I mean temperature, residence time, moisture, and incorporation rate of algal sludge, respectively.
For all the analyzed responses, R 2 , adjusted R 2 , and predicted R 2 were high and the difference between adjusted R 2 and predicted R 2 was less than 0.2, which suggests a good fit of the model to the obtained data. R 2 (coefficient of determination) represents the ratio of the total changes in the predicted response. The adequate precision measures the signal to noise ratio and has values well above 4, which is the minimum desirable value.
To study how the different variables interact in the process and their effects on the response (energy yield and HHV), three-dimensional (3D) response surface plots were made for any two independent process variables, keeping the others at their average level. Figures 4 and 5 present the 3D surface plots with the interactions between the energy yield and HHV and their respective output responses.
Energy yield was higher for lower temperatures and residence times (Figure 4), especially when associated with low values of feedstock moisture and Lc incorporation rate; this behavior reflects the influence of the biochar mass yield on the energy yield. The negative correlation of the energy yield with initial moisture and Lc incorporation rate is corroborated in Figure 4E,F for different torrefaction temperatures.
When looking at the influence of the different variables and the interactions between the variable pairs, it is possible to conclude that the HHV of the biochar ( Figure 5) is positively correlated with the torrefaction temperature and negatively correlated with the feedstock moisture, while time and Lc incorporation rate have less influence on this parameter.
Increasing temperature has the effect of increasing the thermochemical decomposition and of removing oxygen and nitrogen, favoring the formation of aromatic carbonaceous structures, but reducing biochar yield. In contrast, the increase in residence time favors the carbon content biochar yield because it benefits reactions of recombination and adsorption to the biochar itself. The water content always removes energy from the reaction, but it can have a hydrothermal effect as it is an oxidizing agent. Comparing Figure 4A,B, the negative effect of introducing more water is visible.
HHV increased with the incorporation of lignocellulosic biomass for low temperatures but followed an opposite trend at high temperatures. These different behaviors may result from a higher degree of aromatization of the Lc biomass at temperatures above the cellulose and hemicellulose thermal decomposition threshold. The increase in water content decreased the HHV of the obtained biochar, but this decrease was only evident for the most severe torrefaction conditions ( Figure 5A,B); in the case of low temperatures, regardless of residence time, the biochars' HHV was not affected by the addition of water.

Biochars from Wastewater Microalgae Biomass
To evaluate the effect of torrefaction on algal biomass produced in contaminated effluents (aquaculture wastewaters and landfill leachate), biomass samples from Chlorella vulgaris grown in these effluents were used as torrefaction feedstocks with and without the addition of lignocellulosic material. For these experiments, the product yields were determined, and the biochar samples were characterized. Table 8 presents the product yields, proximate analysis, high heating value (HHV), and adsorption capacity of the produced biochar samples. Biochar yields varied in the range of 73.0% to 84.2% and were comparable for the torrefaction of C. vulgaris (Cv) biomass grown in contaminated effluents, mixtures of those biomasses with 50% Lc, or the lignocellulosic material alone (100% Lc). When the feed included Cv biomass produced in landfill leachate, the biochar yield was higher (79% and 84%) than for the tests using Cv grown in aquaculture effluents, which may reflect the accumulation of non-volatile contaminants of the landfill leachate in the microalgae biomass.
On the other hand, condensate yield and gas products yields were higher for the tests including Cv biomass grown in aquaculture effluents or 100% Lc, indicating a higher abundance of organic volatile components in these feedstocks.
These observations agree with the high ash contents detected in Cv-leachate biochar, an indication that mineral components from the landfill leachate were bioaccumulated in the algal biomass. The high concentration of minerals associated with a low content of fixed carbon resulted in an HHV of only 5.6 MJ/kg for this biochar.
The Cv aquaculture biochar had lower ash content and higher concentrations of volatile matter and fixed carbon mixture, which resulted in an HHV of 12.0 MJ/kg, significantly higher than that of the Cv-leachate biochar. These results indicate that not only the nature of the microalgae but also the composition of the effluent may have a strong influence on the composition of the algal biomass and consequently the yield and composition of the correspondent biochar. In both cases, the incorporation of 50% Lc material had a positive effect on the fuel quality of the biochars by reducing ash content and increasing volatile matter, fixed carbon, and HHV.
Microalgae produced in landfill leachate usually have a high amount of ash in their biomass [3]. This occurs because these organisms tend to assimilate minerals from the environment inside their cells and landfill leachate has a high mineral concentration [71]. Also, microalgae produced in saltwater (or aquaculture effluents) tend to have a high ash content, as found by Fakayode et al. [72].
The O/C and H/C ratios of raw materials (0.47 and 1.21 for algae and 1.71 and 1.51 for lignocellulosic biomass, respectively) were reduced with the torrefaction process, giving rise to a biochar with characteristics close to lignite and better than a peat. The torrefaction process is considered an upgrading process, because it increases the hydrophobicity and the energy density of the torrefied material and reduces the need for biomass grinding energy [61]. The production of biochar from microalgae has the advantage of greater stability and density of the final material, which also translates into lower transport costs [72]. Furthermore, it results in a material that can be easily used in agriculture as a soil amendment, releasing nutrients (N and P) slowly into the soil due to the presence of functional groups with oxygen on the surface of the biochar.
These biochars also reveal potential to be further explored as bioadsorbents reaching an adsorption capacity value for MB of 58.1%, without any activation process. Some experiments have revealed that torrefied algal biomass has a quite different structure than that of the original microalgae, becoming irregular and compact, which tends to increase its adsorption capacity [73]. In addition, the biomass that originated the biochars had already treated a landfill leachate or an aquaculture effluent, and thus this process can be integrated into a circular economy concept.

Conclusions
Torrefaction can be seen as a process with low energy requirements resulting in a biochar that is more stable and denser when compared to the original feedstock. Biochars have several applications, including energy valorization, soil amendment, and bioremediation of contaminated effluents.
In this work, RSM has proven to be a useful tool to optimize process parameters observed in the experimental data. A quadratic model has been recommended as a good model for predicting the production of biochar with high calorific value.
Moreover, the conditions that lead to greater biochar production with increased HHV were 250 • C, 60 min of residence time, 5% moisture, and 50% lignocellulosic biomass as feedstock. However, the incorporation of lignocellulosic biomass had more influence on HHV and fixed carbon content rather than on biochar yield. Mixing algal biomass with lignocellulosic biomass was shown to be beneficial by improving the quality of the obtained biochars. Under optimum conditions, it is possible to obtain a biochar yield of 76.5% with an HHV of 17.4 MJ Kg −1 .
Results showed that it is feasible to lower the torrefaction temperature to 250 • C without significantly affecting biochar yield and quality, provided that the residence time is maintained at 60 min. Alternatively, it is also possible to reduce residence time to 30 min, maintaining the temperature at 300 • C, without significantly affecting biochar yields.
Adding water to the feedstock considerably reduces the efficiency of the torrefaction process. Therefore, for biomass with higher moisture levels, a greater amount of lignocellulosic biomass should be incorporated to compensate for this issue.
The evaluation of the torrefaction process performance showed that using moderate torrefaction conditions (temperature and residence time) leads to better energy performance of the process with higher mass yields. However, biochars obtained under these conditions have lower HHV because of the high O/C and H/C ratios, so their fuel qualities were not enhanced.
Biochars produced in this work presented good adsorption capacities towards MB. Furthermore, the use of microalgae previously used in effluent treatment as feedstock in biochar production, also present good adsorption capacities compared to biochars obtained from commercial algal biomass. However, these algal biomass samples usually present a high levels of salts (situation verified for microalgae produced in aquaculture effluent and landfill leachate), and as such, the obtained biochars presented high ash contents resulting in a decrease in their HHV. Even with lower HHVs than those of the model biochar samples, these biochars can be used as low-cost adsorbents and further studies should be conducted to validate their use in soil amendment applications.
Supplementary Materials: The following are available online at https://www.mdpi.com/article/ 10.3390/en14217330/s1, Table S1: Experimental design matrix using the RSM modeling technique, Table S2: Equations generated by RSM software, with R2, adjusted R 2 , predicted R 2 , and adequate precision for product yields; Table S3: Equations generated by RSM software, with R2, Adjusted R 2 , Predicted R 2 and Adequate Precision for biochar characterization; Table S4: Equations generated by RSM software, with R2, adjusted R 2 , predicted R 2 , and adequate precision for energy densification index, Qinput and Qoutput.