Renewable Energy Integration: Economic Assessment of Solar Energy to Produce Biodiesel at Supercritical Conditions.
Increasing human demand for energy from fossil fuels has generated important environmental consequences worldwide. In several countries, programs have been implemented to mix fossil fuels with biofuels to reduce dependence on fossil fuels and to obtain environmental benefits, including mitigation of climate change. One of the most promising renewable fuels as an alternative to diesel is biodiesel, which consists of a mixture of monoalkyl esters of long-chain fatty acids derived from renewable lipids such as vegetable oils or animal fats .
Biodiesel is a biofuel that presents a sustainable alternative to the use of fossil fuels because it can be produced from renewable resources and its implementation in diesel engines does not require significant modifications. However, the costs of producing biofuels and energy consumption have been the primary obstacles in its industrialization and commercialization, and this has led to the investigation of various raw materials, reaction media, and designs in biodiesel production processes, seeking to increase yields and make energy consumption more efficient. All of this contributes to achieving competitive production costs and increasing the inclusion of biodiesel in the market. Using waste vegetable oils to obtain biodiesel can reduce the cost of production from 60% to 90% .
Waste vegetable oils (WVO) are considered the most promising source material for biodiesel production despite some disadvantages, such as its high free fatty acid content (FFA), which require pretreatment to be used in biodiesel produced by alkaline route. Research on noncatalytic methods for biodiesel production has recently increased, where working with WVO and the absence of catalyst simplifies the processes of biodiesel purification. One of the main noncatalytic processes studied is the supercritical condition process (SCP) . The most common SCP consists of the transesterification of triglycerides contained in vegetable oils and the simultaneous esterification of FFA at pressures of 8.4 MPa to 35MPa and temperatures of 320[degrees]C to 350[degrees]C . The high consumption of alcohol and energy to maintain the appropriate conditions of pressure and temperature in the reaction directly affects the viability of the SCP. However, the stages of biodiesel purification and recovery of methanol are more straightforward, allowing to reduce the total energy consumption by approximately 25% compared to alkaline methods .
Solar energy has enormous potential for exploitation due to its abundance, and its use has been increasing, for example, in domestic heating water, air conditioning, energy supply to industrial processes, and even in the electric power generation [6-8]. By harnessing the energy provided by the sun, it is possible to reduce the energy consumption of industrial processes, usually produced from fossil fuels. Due to the high energy consumption of the SCP, the implementation of solar energy as the main source of energy would imply great benefits for the process. In the present work, a series of simulations were performed that represent the process of production of biodiesel in supercritical conditions, with WVO as raw material, in which solar collectors were used in supplying energy to the process.
The current study is focused on the production of biodiesel under supercritical conditions and the viability of solar energy as a source of thermal energy for the process. In Figure 1, the diagram that describes these processes can be seen.
In previous studies, a methodology was developed for the evaluation of the coupling of solar energy to a biodiesel production process. Where the energy loads were determined from the biodiesel production simulation in Aspen Plus, an array of solar collectors was structured through TRNSYS to supply the required energy in the recovery of methanol for the process . This work starts with the previously developed methodology, but the study explores not only the application of solar energy in the recovery of solvents but also in the reaction conditions.
2.1. Raw Material. The raw material used for the production of biodiesel consists of WVO which have been widely used in various studies [10-12]. Triolein has been extensively used as a representative compound of a vegetable oil and methyl oleate as the biodiesel produced from this oil. However, there are various components in vegetable oil that should be taken into account in a simulation.
Canola oil is one of the most consumed vegetable oils in Mexico , and it was therefore selected for this analysis. Based on data reported in the literature, the main triglycerides and FFAs that formed canola oil were determined . It proposed a model of components to represent a more accurate and near to real composition of canola oil.
The percentage of FFA is used to symbolize the level of degradation of vegetable oil due to its use in cooking food. The composition of the WVO utilized in the simulation is exposed in Table 1.
2.2. Biodiesel SCP. Conventionally, the biodiesel production consists of the transesterification of triglycerides through basic or acid catalysis where glycerol is produced as a byproduct. In a biodiesel SCP, the triglycerides and FFA of oil are simultaneously transformed into biodiesel, without the need for catalysts due to the operating conditions. Recent research has indicated that it is possible to produce up to an additional 10% biofuel if the glycerol formed by the transesterification reaction is completely decomposed into 1,2,3-trimethyl glycerol triether. Thus, certain properties of biodiesel could be improved, favouring the cetane number . Therefore, in this research, it was considered that all glycerol is decomposed into 1,2,3-trimethyl glycerol triether and incorporated into the biodiesel. Equations (1) and (2) indicate the reactions from which the biodiesel production was simulated. Equation (1) is the overall transesterification reaction for triglycerides while (2) is the esterification reaction for FFA. Due to the presence of FFA in the WVO, both reactions were considered simultaneously.
The production of biodiesel was simulated in Aspen Plus and was designed to process 100 kg/h of WVO. The process consists of four main stages, which are described below.
First, the oil and methanol are brought to a pressure of 150 bar. Subsequently, its temperature is raised to 350[degrees]C in a series of heat exchangers. Once the appropriate pressure and temperature conditions have been reached, the reactants enter into a stoichiometric reactor. In which, five simultaneous reactions are carried out: two transesterification reactions for each of the triglycerides and three esterification reactions for the different FFAs. Both transesterification and esterification reactions have a yield of 98% and a molar ratio of methanol-triglycerides and methanol-FFA of 9: 1.
[C.sub.3][H.sub.5][(OCOR).sub.3] + 6C[H.sub.3]OH [left and right arrow] 3RCOOC[H.sub.3]
+ [C.sub.3][H.sub.5][(OC[H.sub.3])sub.3] + 3[H.sub.2]O (1)
RCOOH + C[H.sub.3]OH [left and right arrow] RCOOC[H.sub.3] + [H.sub.2]O (2)
Purification of the biodiesel is carried out in a flash separation tank, under conditions of 1 bar and 95[degrees]C. Finally, the outlet steam enters a distillation column, where the main objective is to recover the excess of methanol. The distillation is carried out in an 8-stage column, with feed in step four and a reflux ratio of 1.5.
In the simulation, two systems of thermodynamic properties were used, RK-Aspen for the stages that operate in supercritical conditions and UNIFAC-LL for the stages of purification of biodiesel and recovery of methanol.
2.3. Solar Thermal Energy Collection and Supply System. The supply of thermal energy through solar energy is used to maintain the temperature conditions suitable for the reaction and in the recovery of methanol. Due to the high operating temperatures required by the process, parabolic trough collectors (PTCs) were selected for the capture of solar energy. PTCs have been used extensively in the generation of electricity because they can reach temperatures above 400[degrees]C . The capture of solar energy was simulated in TRNSYS, considering the climatic conditions for the city of Mexicali, located in the northwest region of Mexico, whose annual average solar radiation has been determined as suitable for the exploitation of solar resources .
The system of supply and storage of the thermal energy necessary for the continuous operation of the process is carried out through the solar heating of a heat transfer fluid (HTF). From the HTF at high temperature, it is possible to generate process steam. The HTF selected for the transport of thermal energy was thermal oil, a eutectic mixture of biphenol and diphenol oxide, the trade name of which is Therminol[R] VP-1 .
The system diagram for HTF heating and storage is exhibited in Figure 2. The energy storage system consists of a storage tank for the fluid prior to heating (tank 1) and one for the heated fluid (tank 2). The heating is effected by the arrangement of the solar collectors and a series of heat exchangers, which represent the stages of the steam generation that provide thermal energy to the biodiesel production process.
For the sizing of the array of solar collectors, the annual solar fraction was utilized, which is a commonly used parameter in the design and optimization of solar energy capture systems [19, 20]. The solar fraction is a better indicator of the performance of a solar energy system compared to other parameters such as the efficiency of the collectors or the heat factor removed because it shows an overall performance of the system and not a single individual component . The solar fraction is described as the relation between the contributions of solar energy to the total energy required by the process:
f = [Q.sub.s]/[Q.sub.s] - [Q.sub.Aux] (3)
where f is the solar fraction, [Q.sub.s] is the heat contributed by the solar energy to the process, and [Q.sub.Aux] is the auxiliary thermal energy required. As the solar fraction increases in a solar energy system, the amount of fossil energy used for auxiliary heating is lower . The solar fraction, as a parameter, is used to analyze the variation of it with different system components, such as collection areas, various working fluids, volumes of storage tanks, and building materials. When a system is properly designed, for example, when the energy demand of the process is almost entirely covered, the addition of more collectors does not lead to an increase in the use of solar energy. In periods of high solar radiation, the system produces excess heat, which leads to not only to higher heat losses in the collectors but also to lower efficiency. Overdimensioning of solar systems involves higher costs than the benefits of energy collection. Moreover, during periods of low solar radiation, the uptake of energy is higher but the total annual energy captured is lower than in the original system .
3. Results and Discussion
Simulating biodiesel SCP was possible. In the simulation, 100kg/h of canola WVO is processed. The simulation diagram and streams of importance are displayed in Figure 3 and Table 2, respectively.
According to the results of the simulation, in the biodiesel SCP, a production of 107.17 kg/h can be maintained which represents a 95.4% yield in the final biodiesel production. The B-diesel stream is composed of 97.75% biodiesel. Also, according to the information of the R-MET stream, it is possible to recover 87.6% of the unreacted methanol in stream 6. Stream 11 is mostly composed of 42% water and 39% trimethyl triether. However, this stream is considered as waste due to the low mass flow of 12.86 kg/h and the trimethyl triether could be purified if a large scale plant is planned. The energy demand of the process is presented in Table 3.
Through Aspen Plus, it was estimated that a flow of 220 kg/h of thermal oil at 320[degrees]C is necessary to generate the process steam. Under these conditions, the HTF can only generate enough steam to supply 22.9 kW of the required power to the exchanger (B3), which represents 76.5% of the energy necessary by the B3 module.
Thermal energy storage and supply system were structured through TRNSYS which can be seen in Figure 4. For a constant flow of 220 kg/h of HTF at 320[degrees]C is required a cold HTF storage tank of 6 [m.sup.3] and a hot HTF storage tank of 4 [m.sup.3]. Due to the intermittency of the solar resource, different outflows for tank 1 and tank 2 were considered, 660 kg/h and 220 kg/h, respectively. In this way, the HTF necessary for the continuous operation of the biodiesel process is brought to the appropriate temperature for approximately 8 h.
For the determination of the array of collectors adequate to meet the needs of the process, a group of arrangements of solar collectors was compared according to the annual solar fraction of the solar thermal storage system. Figure 5 reveals the annual solar fraction contributed by different arrays in series and parallel.
From the analysis of solar fraction, it can be observed that the use of solar energy increases as the number of collectors in series and parallel increases. Figure 5 displays the effect on the solar fraction for each proposed arrangement, where each line represents the number of collectors in series arranged by collectors in parallel according to the horizontal axis. The annual solar fraction used by different arrangements studied ranges from 0.81 to 0.82.
Also, it can be observed that the variation in the solar fraction is considerably reduced from 13 collectors in parallel and 6 in series. As a result of the study of the thermal energy storage system for the biodiesel SCP, the collector arrangement was obtained and is presented in Table 4.
Due to thermal energy losses in tank 2, activation of the auxiliary heating system is required. Figure 6 illustrates the energy savings provided by the solar thermal storage system to the biodiesel production process, as well as the energy consumed by the same system. The energy saving is given by the energy obtained from the solar collectors. And the energy consumed by the system consists of the auxiliary heating required and the energy consumed by the system pumps.
The proposed collector array coupled with the SCP biodiesel reduces the energy consumption produced by the burning of fossil fuels.
Figure 7 displays the monthly solar fraction provided by the array of solar collectors.
It can be observed that the most significant contribution of solar energy to the process occurs in the months that comprise from March to September, where there is an input of solar energy superior to 69.5% of the thermal energy required by the biodiesel process, with a peak supply of 69.7% in June.
Figure 8 displays the different energy inputs to the biodiesel production process annually, where the 69.49% of the energy required for the process is supplied by the array of solar collectors.
3.1. Economic Analysis. An economic analysis of the biodiesel production process in supercritical condition, considering the use of solar collectors for the energy supply, was performed.
The economic analysis consisted the building of the biodiesel production process and the solar power storage system, with the specifications obtained through the performed simulations. For the analysis, the installation, operation, and maintenance costs of the process were considered, as well as the income and outcome.
The economic study was carried out in a ten-year period of operation, in which an annual average inflation of 5.5% and a recovery value of zero at the end of ten years were considered. The economic feasibility of the biodiesel production processes was compared considering the internal rate of return (IRR) of the investment, the number of periods in which the investment is paid, and the net present value of the project.
In Table 5, the quantities and unit costs of the raw materials are described, as well as the required energy and its unit cost for the industrial sector of low voltage in Mexicali, Baja California.
The characteristics of the process in supercritical conditions do not require raw materials as catalysts or water for the biodiesel washing.
The required energy for biodiesel production in supercritical conditions is considerably higher than other processes. However, it must be taken into consideration that the required energy is considered as auxiliary power because the main energy source is thermal energy, which comes from the solar system.
Table 6 presents the required equipment for the process and its estimated costs. Due to the simplicity of the process, it does not require an esterification reactor, decanter, or neutralizer, for the absence of catalysts makes more straightforward purification of biodiesel. However, for the reaction conditions, a more sophisticated and expensive transesterification reactor is required. The high energy consumption to maintain the operation process conditions in supercritical conditions requires an extensive collector's array that represents an important part of the initial investment of the project. The total cost of the investment and the operation cost are listed in Table 7.
According to the working capital, which represents the expenditures needed for the operation of the plant, and the production volume established by the performed simulations, it is possible to determine the monthly production cost and the production cost by a biofuel liter. Table 8 displays a comparison of the production costs for the proposed process and other similar processes mentioned in the literature. It also indicates the trade prices of biodiesel and diesel in Mexico and the USA.
The production costs of the proposed process exceed some of the similar processes found in the literature. However, the determined location for the project allows the production cost to be competitive if compared with other current prices of fossil fuels in the north of Mexico and the USA border with Mexico, which permits offering a competitive price in the market.
For the economic analysis in the ten-year period, it was considered an interbank interest annual average rate of 6.5%. The economic analysis revealed that the process has an annual IRR of 31.7% which allows an investment recovery before the fifth year of operation and a positive NPV of USD 1,643,955. It demonstrates that the proposed process would have economic and environmental benefits.
The production processes of biodiesel are highly benefited by the use of WVO as a raw material, due to its low cost compared to new oils, impacting the final cost of production. The biodiesel production processes in supercritical conditions have become an option of high relevance since they operate without the need of catalysts. The formation of soaps is avoided in the SCP when the amount of FFA is high and facilitates the processes of purification of biodiesel. Also, due to the lack of catalyst, the waste stream generation is diminished. The simulation in Aspen Plus allowed evaluating the energy demand of the biodiesel SCP. With this information, a solar energy capture system was modelled in TRNSYS, which allowed to supply as much energy as possible to the process. By using an array of parabolic trough collectors for the energy supply to the biodiesel production process, the burning of fossil fuels is reduced, increasing the sustainability of the process. The proposed arrangement, six collectors in series and 13 in parallel with a single collection area of 10 [m.sup.2], can provide 82% of the energy required by the exchanger (B3) and the reboiler of the column (B6), which represents the 69.45% of the energy needed for the entire process annually. The estimated production cost for the proposed process is of USD 0.778/l and represents a competitive cost for a plant located on the border with the USA and the current prices of fossil fuels. The recovery of the investment takes place before finishing the fifth year, with an IRR of 31.7% and obtaining a positive NPV of USD 1,643,955. The integration and implementation of clean technologies are significant for the development and growth of biofuels and sustainable development.
This article is based on the integration of the results obtained from the simulations developed in the Aspen Plus and TRNSYS software. The Aspen Plus license agreement signed by the Universidad Autonoma de Baja California states that "The customer will not transfer all or part of the results of the use of the software". For this reason, access to the data is restricted.
Conflicts of Interest
The authors declare that there is no conflict of interests regarding the publication of this paper.
The authors thank the Engineering Institute of the Universidad Autonoma de Baja California for the facilities to develop this project and PFCE-2017 for the financial support for the publication of this paper.
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Jose A. Leon (iD), (1,2) Gisela Montero (iD), (1) Marcos A. Coronado (iD), (1) Conrado Garcia, (1) Hector E. Campbell (iD), (1) Jose R. Ayala (iD), (1,2) Daniela Montes (iD), (1) and Carlos A. Sagaste (iD) (1,2)
(1) Instituto de Ingenieria, Universidad Autonoma de Baja California, Blvd. Benito Juarez y Calle de la Normal S/N, Col. Insurgentes Este, 21280 Mexicali, BC, Mexico
(2) Facultad de Ingenieria, Universidad Autonoma de Baja California, Campus Mexicali, Blvd. Benito Juarezy Callede la Normal S/N, Col. Insurgentes Este, 21280 Mexicali, BC, Mexico
Correspondence should be addressed to Gisela Montero; firstname.lastname@example.org
Received 21 March 2018; Accepted 5 July 2018; Published 22 July 2018
Academic Editor: Juan M. Coronado
Caption: Figure 1: Process for the production of biodiesel in supercritical conditions powered by solar energy.
Caption: Figure 2: Block diagram of the solar thermal energy storage system.
Caption: Figure 3: Aspen Plus diagram of the biodiesel production process at supercritical conditions.
Caption: Figure 4: Simulation diagram in TRNSYS of the solar thermal energy storage system.
Caption: Figure 5: Comparison of solar collector arrangements.
Caption: Figure 6: Saving and monthly energy consumption of the solar thermal energy storage system.
Caption: Figure 7: Monthly solar fraction of the solar thermal energy storage system.
Caption: Figure 8: Annual energy contributions to the biodiesel production process at supercritical conditions.
Table 1: Representative composition of canola WVO. Component 10% FFA Mass fraction Triolein 0.720 Trilinolein 0.180 Oleic acid 0.060 Linoleic acid 0.030 Linolenic acid 0.010 Table 2: Operating conditions and mass compositions of simulation streams. Stream WVO Methanol 6 Mass flow (kg/h) 100 39.59 139.5 T ([degrees]C) 25 25 350 P (bar) 1.01 1.01 100 Triolein 0.72 0 0.010 Trilinolein 0.18 0 0.003 Methanol 0 1 0.138 Oleic acid 0.06 0 0.001 Linoleic acid 0.03 0 0.000 Linolenic acid 0.01 0 0.000 M-oleate 0 0 0.552 M-linoleate 0 0 0.149 M-linolenate 0 0 0.007 G-M-E 0 0 0.096 [H.sub.2]O 0 0 0.043 Stream B-diesel MET-REC 11 Mass flow (kg/h) 109.64 17.09 12.86 T ([degrees]C) 95 75.5 178.4 P (bar) 1.01 1.01 1.01 Triolein 0.000 0.000 0.112 Trilinolein 0.000 0.001 0.027 Methanol 0.017 0.987 0.042 Oleic acid 0.001 0.000 0.000 Linoleic acid 0.001 0.000 0.000 Linolenic acid 0.000 0.000 0.000 M-oleate 0.703 0.000 0.000 M-linoleate 0.190 0.000 0.000 M-linolenate 0.009 0.000 0.000 G-M-E 0.076 0.000 0.396 [H.sub.2]O 0.003 0.012 0.423 Table 3: Energy demand of the biodiesel production process under supercritical conditions. Component Power (kW) Pump (B1) 6.935 Pump (B2) 0.928 Heat exchanger (B3) 30.037 Column (B8) 13.502 Total 51.402 Table 4: Parameters of the array of parabolic trough collectors. Arrangement of PTC Collectors in series 6 Collectors in parallel 13 Individual collection area 10 [m.sup.2] Total collection area 780 [m.sup.2] Azimuth orientation 0[degrees] Tilt Solar tracking on a single axis Table 5: Operation costs for a month. Raw material t Unit cost (USD/t) Methanol 21.28 540.5 WVO 53.76 265.67 Water process 7.91 25.46 HTF 3.2 86.04 Auxiliary power MWh USD/MWh Electricity 5.92 81 Total 998.67 Table 6: Cost of the required equipment for process. Equipment Thousand of USD Transesterification reactor 243.24 Flash separator 54.05 Distillation column 108.11 Tanks 7.62 Pumps 44.61 Heat exchangers 24.43 Solar collectors 421.62 Total 903.68 Table 7: Estimated investment and operation cost. Thousand of USD Direct costs Including Civil work 932.28 Machinery and equipment Indirect costs Including Licenses and official permits 394.20 Total investment 1326.48 Operation cost Including Consumables Leasing services 673.37 Maintenance Salary Table 8: Comparison of production costs and the biodiesel trade prices (USD/l). Proposed    process Costs 0.778 0.7525 0.507 0.623 Biodiesel, Biodiesel, Diesel, Diesel, MX USA  MX  USA  Prices -- 0.892 1.005 0.969
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|Title Annotation:||Research Article|
|Author:||Leon, Jose A.; Montero, Gisela; Coronado, Marcos A.; Garcia, Conrado; Campbell, Hector E.; Ayala, Jo|
|Publication:||International Journal of Photoenergy|
|Date:||Jan 1, 2018|
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