Lipid and biodiesel productivity of various feedstocks [7].
\\n\\n
More than half of the publishers listed alongside IntechOpen (18 out of 30) are Social Science and Humanities publishers. IntechOpen is an exception to this as a leader in not only Open Access content but Open Access content across all scientific disciplines, including Physical Sciences, Engineering and Technology, Health Sciences, Life Science, and Social Sciences and Humanities.
\\n\\nOur breakdown of titles published demonstrates this with 47% PET, 31% HS, 18% LS, and 4% SSH books published.
\\n\\n“Even though ItechOpen has shown the potential of sci-tech books using an OA approach,” other publishers “have shown little interest in OA books.”
\\n\\nAdditionally, each book published by IntechOpen contains original content and research findings.
\\n\\nWe are honored to be among such prestigious publishers and we hope to continue to spearhead that growth in our quest to promote Open Access as a true pioneer in OA book publishing.
\\n\\n\\n\\n
\\n"}]',published:!0,mainMedia:null},components:[{type:"htmlEditorComponent",content:'
Simba Information has released its Open Access Book Publishing 2020 - 2024 report and has again identified IntechOpen as the world’s largest Open Access book publisher by title count.
\n\nSimba Information is a leading provider for market intelligence and forecasts in the media and publishing industry. The report, published every year, provides an overview and financial outlook for the global professional e-book publishing market.
\n\nIntechOpen, De Gruyter, and Frontiers are the largest OA book publishers by title count, with IntechOpen coming in at first place with 5,101 OA books published, a good 1,782 titles ahead of the nearest competitor.
\n\nSince the first Open Access Book Publishing report published in 2016, IntechOpen has held the top stop each year.
\n\n\n\nMore than half of the publishers listed alongside IntechOpen (18 out of 30) are Social Science and Humanities publishers. IntechOpen is an exception to this as a leader in not only Open Access content but Open Access content across all scientific disciplines, including Physical Sciences, Engineering and Technology, Health Sciences, Life Science, and Social Sciences and Humanities.
\n\nOur breakdown of titles published demonstrates this with 47% PET, 31% HS, 18% LS, and 4% SSH books published.
\n\n“Even though ItechOpen has shown the potential of sci-tech books using an OA approach,” other publishers “have shown little interest in OA books.”
\n\nAdditionally, each book published by IntechOpen contains original content and research findings.
\n\nWe are honored to be among such prestigious publishers and we hope to continue to spearhead that growth in our quest to promote Open Access as a true pioneer in OA book publishing.
\n\n\n\n
\n'}],latestNews:[{slug:"stanford-university-identifies-top-2-scientists-over-1-000-are-intechopen-authors-and-editors-20210122",title:"Stanford University Identifies Top 2% Scientists, Over 1,000 are IntechOpen Authors and Editors"},{slug:"intechopen-authors-included-in-the-highly-cited-researchers-list-for-2020-20210121",title:"IntechOpen Authors Included in the Highly Cited Researchers List for 2020"},{slug:"intechopen-maintains-position-as-the-world-s-largest-oa-book-publisher-20201218",title:"IntechOpen Maintains Position as the World’s Largest OA Book Publisher"},{slug:"all-intechopen-books-available-on-perlego-20201215",title:"All IntechOpen Books Available on Perlego"},{slug:"oiv-awards-recognizes-intechopen-s-editors-20201127",title:"OIV Awards Recognizes IntechOpen's Editors"},{slug:"intechopen-joins-crossref-s-initiative-for-open-abstracts-i4oa-to-boost-the-discovery-of-research-20201005",title:"IntechOpen joins Crossref's Initiative for Open Abstracts (I4OA) to Boost the Discovery of Research"},{slug:"intechopen-hits-milestone-5-000-open-access-books-published-20200908",title:"IntechOpen hits milestone: 5,000 Open Access books published!"},{slug:"intechopen-books-hosted-on-the-mathworks-book-program-20200819",title:"IntechOpen Books Hosted on the MathWorks Book Program"}]},book:{item:{type:"book",id:"716",leadTitle:null,fullTitle:"Clinical Use of Local Anesthetics",title:"Clinical Use of Local Anesthetics",subtitle:null,reviewType:"peer-reviewed",abstract:"Local anesthetics are being increasingly applied in different surgeries. 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\r\n\tPalm oil is an edible vegetable oil extracted from the mesocarp of the oil palm fruit, mainly the Elaeis guineensis African oil palm and to a lesser degree, from the American oil palm Elaeis oleifera and the maripa palm Attalea maripa. Oil palm is the most profitable crop of vegetable oil per unit area and is important to economy of developing countries such as Malaysia and Indonesia. However, due to the impact it has on biodiversity, it is also extremely controversial. The expansion of oil palm plantations in Malaysia and Indonesia, includes the conversion of forests, and other forms of land in the landscapes that provide the livelihoods of clan members. The way this expansion takes place makes it important to understand the variables associated with why businesses are looking for frontier lands and what externalities are created during both the periods of land acquisition and plantation growth. We find that investors are encouraged to profit from timber harvested from plantation land clearing, an operation promoted by the local government. Also land acquisition and plantation growth have resulted in externalities to indigenous landowners in the form of time and money wasted. The reduced health of people due to the loss of livelihoods and the effect on food security are other externalities.
\r\n\r\n\tPalm oil, like all fats, is composed of fatty acids, esterified with glycerol. Palm oil has an especially high concentration of saturated fat, specifically the 16-carbon saturated fatty acid, palmitic acid, to which it gives its name. Monounsaturated oleic acid is also a major constituent of palm oil. Unrefined palm oil is a significant source of tocotrienol, part of the vitamin E family. Palm oil sludge or palm oil mill effluent (POME) is wastewater generated by processing oil palm and consists of various suspended materials. POME has a very high biochemical oxygen demand (BOD) and chemical oxygen demand (COD), which is 100 times higher than municipal sewage. The effluent also contains a high concentration of organic nitrogen, phosphorus, and other nutrient contents. POME is a colloidal suspension consisting of 95–96% water, 0.6–0.7% oil and 4–5% total solids, including 2–4% suspended solids originating from a mixture of sterilizer condensate, separator sludge and hydrocyclone wastewater.
\r\n\r\n\tIn terms of production, export, trade, and consumption, palm oil is the leading edible oil globally. With the bulk of palm oil used in foods, its role is well known in human nutrition. In addition to being a source of calories, the oil palm is a source of useful micronutrients, including β-carotene and tocotrienols (vitamin E isomers), due to its position as dietary fat. Energy-efficient usage is the key issue for our low-carbon society in future. The importance of the development of innovative energy materials and processes were well recognized for efficient energy systems. These, after extraction, have been extensively studied. In addition, to tackle vitamin A deficiency, unrefined "red palm oil" has been used. A water-soluble fraction of palm oil that is phenolic-rich has been available over the last decade and has also been the subject of more recent studies
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He earned PhD in Civil Engineering in the field of Environmental Engineering at Universiti Teknologi Malaysia (UTM). He was awarded the Young Water Professional Awards by International Water Association (IWA-YWP) in 2014 at Taipei, Taiwan. Moreover, He received an outstanding Reviewer Award in the Journal of Cleaner Production (Elsevier) and Clean Technologies Environmental Policy (Springer) in 2017. He was appointed as the Junior Board Member in the Journal of Cleaner Production, Elsevier (IF: 7.246) following his active paper review role. Also, he was appointed as managing guest editor in Energy Journal, Elsevier (IF: 6.082). He has a chair in IWA Emerging Water Leader (EWL). 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Venkateswarlu",coverURL:"https://cdn.intechopen.com/books/images_new/371.jpg",editedByType:"Edited by",editors:[{id:"58592",title:"Dr.",name:"Arun",surname:"Shanker",slug:"arun-shanker",fullName:"Arun Shanker"}],productType:{id:"1",chapterContentType:"chapter",authoredCaption:"Edited by"}},{type:"book",id:"878",title:"Phytochemicals",subtitle:"A Global Perspective of Their Role in Nutrition and Health",isOpenForSubmission:!1,hash:"ec77671f63975ef2d16192897deb6835",slug:"phytochemicals-a-global-perspective-of-their-role-in-nutrition-and-health",bookSignature:"Venketeshwer Rao",coverURL:"https://cdn.intechopen.com/books/images_new/878.jpg",editedByType:"Edited by",editors:[{id:"82663",title:"Dr.",name:"Venketeshwer",surname:"Rao",slug:"venketeshwer-rao",fullName:"Venketeshwer Rao"}],productType:{id:"1",chapterContentType:"chapter",authoredCaption:"Edited by"}},{type:"book",id:"4816",title:"Face Recognition",subtitle:null,isOpenForSubmission:!1,hash:"146063b5359146b7718ea86bad47c8eb",slug:"face_recognition",bookSignature:"Kresimir Delac and Mislav Grgic",coverURL:"https://cdn.intechopen.com/books/images_new/4816.jpg",editedByType:"Edited by",editors:[{id:"528",title:"Dr.",name:"Kresimir",surname:"Delac",slug:"kresimir-delac",fullName:"Kresimir Delac"}],productType:{id:"1",chapterContentType:"chapter",authoredCaption:"Edited by"}}]},chapter:{item:{type:"chapter",id:"71530",title:"Potential of Microalgal Biodiesel: Challenges and Applications",doi:"10.5772/intechopen.91651",slug:"potential-of-microalgal-biodiesel-challenges-and-applications",body:'Today’s scientific reports revealed that the world’s commercial primary energy needs are mostly coming from fossil fuel sources. It is forecasted that the primary energy demand by 2035 will increase to 54% and still fossil fuels contribute 82% of the global need [1]. Besides, an increase in the world population and their anthropogenic activities, such as transportation, land use, deforestation, industrialization, waste generation, etc., has been changing the natural structure of the earth. These activities lead to severe global climate problems in the present scenario. A remarkable change in the lifestyle of human beings is also building extra pressure on the production market to fulfill the demands and desires of society.
Nevertheless, the recent production and consumption models mainly rely on fossil fuel resources, which are affecting the environment and natural resources adversely and irreversibly. It has been reported that the majority of the global CO2 emissions are due to the transport sector and the number of light motor vehicles is estimated to increase to over 2 billion by 2050 [2]. Hence, to address the significant issues such as energy depletion and hazardous gas emission, there is an urgent need for a substantial displacement of fossil fuel usage.
In this context, biofuels produced from biomass rather than fossil source are considered as a potential solution to address these challenges. Currently, researchers have been exploring various types of biofuel production such as solid (biochar), liquid (ethanol, vegetable oil, and biodiesel), and gaseous (biogas, bio-syngas, and biohydrogen), and they were categorized based on the type of feedstock used. It has been reported that the first-generation liquid biofuels which are produced using edible feedstock such as corn, soybean, sugarcane, and rapeseed have directly competed with food production. Meanwhile, food production is the other most critical challenge to society [3]. The second-generation biofuel production has been developed using the nonedible feedstock such as Jatropha, Switchgrass, etc.; however, these nonedible feedstocks also compete with food production [4]. Mainly the second-generation biofuel production relies on arable land, freshwater, and nutrients for their cultivation.
Therefore, to solve these critical issues, researchers have explored a third and fourth generation of biofuels using microalgae and macroalgae (third generation) and metabolic engineering of photosynthetic organisms to produce biofuels (fourth generation) [5]. In this regard, algae have received considerable attention in recent years because of their robust growth and potential to accumulate a high amount of lipid, carbohydrate, and protein, and these can be easily converted into various biofuels (biodiesel, bioethanol, and biogas). Table 1 shows the potential applications of microalgal species for biodiesel production compared with other biomass sources. Besides, microalgae are the potential candidate for CO2 sequestration, self-purification, and effective land utilization with high environmental benefits. Also, the cultivation and utilization of microalgae do not compete with food production for land, freshwater, and nutrient sources. Many studies have reported that microalgae offer a wide variety of bioproducts that can be utilized by various sectors, such as energy (biodiesel, biohydrogen, and bioethanol), pharmaceuticals, nutraceuticals, and feed and food supplements [6]. In the past few years, a large number of research work have been focused on microalgae for the potential biofuel production.
Feedstocks | Lipid content (% dry weight basis) | Biodiesel productivity (tons/year/ha) |
---|---|---|
Corn/maize (Zea mays) | 44 | 0.152 |
Hemp (Cannabis sativa) | 33 | 0.321 |
Soybean (Glycine max) | 18 | 0.562 |
Jatropha (Jatropha curcas) | 28 | 0.656 |
Camelina (Camelina sativa) | 42 | 0.809 |
Canola/rapeseed (Brassica napus) | 41 | 0.862 |
Sunflower (Helianthus annuus) | 40 | 0.946 |
Castor (Ricinus communis) | 48 | 0.156 |
Palm oil (Elaeis guineensis) | 36 | 4.747 |
Microalgae (low lipid-yielding strains) | 30 | 51.927 |
Microalgae (high lipid-yielding strains) | 70 | 12.110 |
Lipid and biodiesel productivity of various feedstocks [7].
Nevertheless, the life cycle and techno-economic analysis have revealed that the biofuels derived from microalgae are not cost-competitive in comparison with conventional petrochemical fuels. Mostly 70% of the cost will be invested for cultivation and biomass harvesting [8]. However, a possible way to reduce the cost is to integrate the microalgal cultivation system with wastewater treatment. Generally, wastewater is rich in nutrients and other bioresources. It was reported that wastewater can produce 6.5 MJ/kL of energy, which constitutes 1% of the total world energy [9].
The nutrients presenting in the form of carbon, nitrogen, and phosphorous can be turned into an economic opportunity by feeding them to microalgae [10]. Microalgae can utilize the organic carbon in wastewater and tailor it into biomass. The use of wastewater for microalgal cultivation in mixotrophy and heterotrophy cultivation mode can balance the respiratory losses, improve energy budget, and give a boost to the biomass productivity. Earlier reports have shown that the utilization of nutrients and water from wastewater and industrial flue gas (CO2) helps to decrease the cost and makes the algal biofuels commercially viable [11]. In addition, the recovery of other value-added bioproducts, rare earth metals, etc. can compensate for the cost involved during algal cultivation. Besides, the wastewater used for algal cultivation does not require any additional treatment to meet the ecological and environmental regulations. Therefore, the utilization of a large quantity of wastewater for microalgal cultivation could promote waste-free, carbon-neutral, and environmentally sustainable technology.
The previous studies have explored that the microalgal species, such as Botryococcus braunii, Scenedesmus obliquus, Chlorella vulgaris, Chlamydomonas reinhardtii, and Nannochloropsis oculata, are recognized as promising species for biofuel production [12, 13]. Nevertheless, the biofuels produced from highly potential microalgal feedstock need a powerful downstream processing technology. This book chapter is aimed to provide knowledge about the latest research and development of microalga-based biofuel and its challenges.
Microalgae are simple microscopic heterotrophic or autotrophic photosynthetic organisms, and these organisms are also named phytoplankton. Generally, they are found in fresh, marine, and brackish water, and they utilize photonic energy (light sources), carbon dioxide (CO2), and water for their growth. Microalgae are classified as green algae (Chlorophyceae), blue-green algae (Cyanophyceae), red algae (Rhodophyceae), brown algae (Phaeophyceae), and diatoms (Bacillariophyceae). The microalgal growth contains five different phases: (1) lag phase, initial growth period, where the microalgae take time to adapt themselves into a new environment; (2) log/exponential phase, here rapid cell division occurs, and growth is faster; (3) decline phase, this phase contains limiting cell division; (4) stationary phase, the cell density of microalgae is stable because of the limiting factors; and (5) death phase, in this stage almost the cell growth is stopped due to lack of nutrients. Besides, microalgae are easy to be cultivated because they can tolerate a broad range of pH, salinity, and temperature. Some researchers have reported that a lipid content of microalgae is usually between 20 and 50% on a dry weight basis [14], whereas in some microalgal species (e.g., Botryococcus braunii), the lipid production can be reached up to 75% on a dry weight basis. Microalgae are not only a good source of lipids, it is also a vital source of producing the bioproducts, such as polysaccharides, pigments, proteins, vitamins, bioactive compounds, and antioxidants.
Generally, according to the growth nutrient modes, the microalgal cultivation can be divided into three categories, which are autotrophic, heterotrophic, and mixotrophic cultivation. In autotrophic mode, the inorganic carbon and light/solar are the primary sources of energy for microalgal growth. The heterotrophic cultivation mode mainly uses organic carbon and energy from the Krebs cycle. On the other hand, in mixotrophic cultivation mode, the carbon sources for microalgal growth can be supplied by both inorganic and organic forms.
In microalgal cultivation, large-scale biomass production can be performed by two major methods, such as open raceway and closed photobioreactor (PBR). The open pond is the traditionally used system for large cultivation of microalgal species, which is economically superior in comparison to PBR. In an open cultivation system, the sunlight and atmospheric CO2 are used as sources for carbon production to achieve higher biomass productivities. On the other hand, the PBR method is suitable for axenic cultures, and this type of cultivation is widely used for the production of high value-added bioproducts (e.g., pharmaceuticals). Basically, an open raceway pond cultivation system consists of a simple water tank or bigger earthen pond in which the nutrients are added from outsourcing. Besides, the open pond is usually designed in a raceway or track configuration attached with paddle wheel to provide circulation and mixing of the algal cells and growth nutrients. The low-cost open raceway pond is typically made from poured concrete, or they are dug into the earth and lined with a plastic liner to avoid the groundwater. The growth medium is added in front of the paddle wheel for proper mixing and absorption.
PBR is the most common system used for the closed cultivation method. It is designed based on several basic features, including liquid circulation, illumination surface area, and gas exchange to supply CO2 to PBR [15]. Generally, researchers use the PBR cultivation method for the production of high biomass with a controlled environment and to avoid contamination. This type of cultivation makes it easier to optimize the biomass productivity of selected algal species. Usually, PBR is designed by using glass or plastic, coupled with a gas exchanger to pass the nutrients and CO2. This system contains an airlift pump usually used to circulate the microalgal culture grown in PBR, which helps to keep the culture in suspension state and improve the CO2 dissolution. Researchers have identified various types of PBR design, such as polyethylene bags, glass fiber cylinder, tubular inclined, segmented glass plate, flat modular photobioreactor, and annular photobioreactor. In the PBR cultivation method, several studies have been carried out on catalyst improvement, shaping of the PBR, controlling environmental parameters, and axenic culture. During the cultivation period, the operational parameters, such as pH, temperature, and gas diffusion, are a crucial issue, and it should be adequately addressed in PBR [11].
Some studies have been performed to recycle the nutrients from wastewater sources, which is considered as a step-in treatment of industrial wastewater using microalgal species. As the world’s population continuously increases day by day, wastewater discharge also increased. Thus, the utilization of this harmful wastewater as a source of microalgal growth nutrients is highly recommended for the environmentally friendly high production of biomass and lipid. Nevertheless, to make microalgal biodiesel production at commercial scale, an integrated biorefinery approach of wastewater utilization will strongly influence the future sustainability by addressing high-energy production, reducing greenhouse gas (GHG) emission, and lowering the production cost.
Generally, two types of cultivation techniques are followed, i.e., batch and semicontinuous or continuous cultivation mode. During the cultivation period, biomass will be harvested and processed. It has been reported that the biomass harvesting accounts for approximately 20 and 30% of the total cost of microalgal downstream processes [16]. Therefore, the harvesting cost is one of the major hurdles, which makes the algal cultivation unsuccessful at commercial scale. Hence, many researchers are finding more effective techniques for microalgal cell harvesting to overcome this issue. The microalgal harvesting process is expensive and energy-consuming because the density of algal cells in the culture medium is generally low and most of the microalgal cells carry a negative charge, which makes the cells in a suspension state. To achieve a maximum biomass production during the harvesting process, researchers explored several types of harvesting methods, such as filtration, centrifugation, sedimentation ultrasound, and floatation [14]. Nevertheless, these methods are not as efficient as flocculation because of their high cost and lower efficiency. The flocculation harvesting method is much more comfortable, with higher efficiency, than other methods; however, still, a lot of challenges are needed to be addressed. On the other hand, the harvesting of microalgal biomass using flocculants can contaminate the slurry concentrate; thus, it reduces the algal biomass market value, lipid conversion into biodiesel via transesterification process, and the application of this biomass for food industry and animal feeds. Therefore, the feasible way to minimize harvesting costs is only by improving the harvesting technologies. Besides, the suitable method for biomass harvesting mostly depends on the algal species.
The lipid accumulation differs from species to species; besides, it depends on the algal cultivation methods. It has been reported that the microalgal species, such as Dunaliella, Chlorella, Isochrysis, Nannochloris, Scenedesmus, Tetraselmis, and Nannochloropsis, accumulate the average lipid content of 15–60% on a dry weight basis (Table 2). Due to their relatively high lipid accumulation, the microalgal species are considered as a promising feedstock for biodiesel production [17]. The lipids obtained from microalgae are chemically similar to the conventional vegetable oils and so have been considered as a promising source for biodiesel [18]. The microalgal triglycerides can easily be converted into biodiesel, which is renewable, biodegradable, and environmentally friendly when compared to fossil fuel sources [19]. Besides, the microalga-derived biodiesel has a higher heating value (HHV) of 39–41 MJ/kg; thus, it is considered as a potential alternative for displacement of liquid transport fuels derived from petroleum crude [20]. Generally, microalgae produce a high level of triacylglycerols (TAG), which are accumulated in the plastids or found in the cytoplasm in the form of lipid bodies. It was observed that in algal species, during cultivation, the nitrogen starvation and other stressful situations, such as salinity, temperature, CO2 concentration, and light intensity, stimulate the lipid biosynthesis, resulting in an enhanced lipid production [21, 22]. A study reported that the microalga Haematococcus pluvialis produces a high amount of neutral lipids when it is under a stressful environment (i.e., high light intensity and nitrogen starvation) [23].
Division | Microalgae | Volumetric productivity of biomass (g/L/day) | Lipid content (% dry weight biomass) |
---|---|---|---|
Freshwater microalgae | |||
Green microalgae | Ankistrodesmus sp. | — | 24–31 |
Botryococcus braunii | 0.02 | 20–75 | |
Chlorella emersonii | 0.036 | 25–63 | |
Chlorella protothecoides | 2 | 14–57 | |
Chlorella sorokiniana | 0.23–1.7 | 19–22 | |
Chlorella vulgaris | 0.02–0.2 | 5–58 | |
Chlorella pyrenoidosa | 2.9 | 2 | |
Neochloris | 29–65 | — | |
Chlorococcum sp. | 0.28 | 19.3 | |
Haematococcus pluvialis | 0.06 | 25 | |
Scenedesmus obliquus | 0.74 | 11–55 | |
Scenedesmus quadricauda | 0.19 | 1.9–18 | |
Scenedesmus sp. | 0.26 | 19–21 | |
Blue-green microalgae | Spirulina platensis | 0.6–4 | 4–16 |
Spirulina maxima | 0.21–0.25 | 4–9 | |
Red microalgae | Porphyridium cruentum | 0.36–1.5 | 9–18.8 |
Marine microalgae | |||
Green microalgae | Dunaliella salina | 0.22–0.34 | 6–25 |
Dunaliella primolecta | 0.09 | 23 | |
Dunaliella tertiolecta | 0.12 | 16.7–70 | |
Nannochloropsis sp. | 0.17–1.4 | 12–53 | |
Tetraselmis suecica | 0.12–32 | 8.5–23 | |
Tetraselmis sp. | 0.3 | 12.6–14.7 | |
Pavlova salina | 0.16 | 30.9 | |
Pavlova lutheri | 0.14 | 35.4 | |
Isochrysis sp. | 0.08–0.17 | 7.1–33 | |
Diatoms | |||
Nitzschia sp. | — | 16–47 | |
Skeletonema sp. | 0.9 | 13.3–31 | |
Skeletonema costatum | 0.8 | 13.5–51 |
Microalgal species and its productivity [25].
Thus, the microalgae accumulate a higher amount of lipids, especially TAG, which enhance a potential production of biodiesel. In microalgae, however, the biomass and lipid production plays a crucial role in biodiesel production at commercial scale; the quality of the lipids depends on algal species which greatly influences the biodiesel property. Nascimento et al. [24] investigated 12 algal species for potential biodiesel production, and results revealed that Chlorella and Botryococcus species accumulated high-level lipid content, which can be easily converted into biodiesel. Some studies showed that the biodiesel obtained from the microalgae Scenedesmus obliquus and Chlamydomonas sp. contains a high level of saturated fatty acids (SFA) and has the highest cetane number (CN) of 63 along with enhanced oxidation stability. The lipids of some microalgal species, such as Ankistrodesmus fusiformis, Kirchneriella lunaris, Ankistrodesmus falcatus, and Chlamydocapsa bacillus, are rich in polyunsaturated fatty acids (PUFA), and the obtained biodiesel has low oxidation stability, high iodine value (IV), and low CN (42.5). The microalgal lipids with a high content of SFA and monounsaturated fatty acids (MUFA) give biodiesel with improved quality. Besides, the CN value is significantly correlated with a ratio of SFA to PUFA, which can be used to evaluate the delay between compression and ignition. Mostly, the algal biodiesel has higher CN value than that of the fossil fuels, which helps to shorten the delay in the ignition and complete combustion of the algal biodiesel.
An earlier study has reported that Amphora sp., a marine and freshwater diatom, produces a significant amount of MUFA, which can be considered as a potential feedstock to produce high-quality biodiesel [26]. Among several algal strains, such as Phormidium sp., S. obliquus, C. vulgaris, and Dunaliella tertiolecta, grown in a bubble PBR for biodiesel production, Chlorella vulgaris produces a significant amount of biomass and lipid. Besides, it is considered as the best choice for CO2 sequestration at a rate of 17.8 mgL− 1min−1. In addition, the alga Chlorella vulgaris biodiesel meets the ASTM 675 and EN 14214 standards because the lipids of these strains are rich in SFA of 43.5% and MUFA of 41.5% [27]. The microalga Scenedesmus abundans lipid is a rich source of MUFA (76%), which enhances the quality of resulting biodiesel to meet the European biodiesel standard (EN 14214), South African standard (SANS1935), and Germany’s standard (DIN 51606) [28]. Some recent studies investigated different microalgal groups, such as green algae Chlorella sp., Scenedesmus sp., and Selenastrum sp.; red algae Batrachospermum sp.; diatoms Navicula sp. and Phaeodactylum sp.; and blue-green algal species (Lyngbya sp., Isochrysis sp., and Prymnesiophytes sp.), and observed that Scenedesmus sp., Chlorella sp., and Isochrysis sp. produce a significant amount of lipids, which are considered as a promising feedstock for biodiesel production [29]. A previous study isolated 96 microalgal strains from Singapore coastal area, which was then well screened for growth, biomass, and lipid productivity. The results revealed that the marine microalga Nannochloropsis sp. was found to be the most promising biomass material for biodiesel production because of its high lipid accumulation of 45% on a dry weight basis [29]. Islam et al. [30] investigated several microalgal species, such as Ankistrodesmus sp., Botryococcus sp., Chlorella sp., Chlamydomonas sp., Coelastrum sp., Desmodesmus sp., and Scenedesmus sp., for biodiesel production. The author observed that Botryococcus sp. produced a high lipid yield and the quality of the resulting biodiesel met the ASTM 6751-02 and EN 14214 standards. The quality of biodiesel obtained from different microalgal species, such as Nannochloropsis sp., Scenedesmus sp., and Dinoflagellate, was explored [31]. The biodiesel properties included density, kinematic viscosity, acid value, phosphorous content, sulfated ash content, and sulfur content, according to the Chinese National Standards (CNS). The results showed that the biodiesel characteristics were almost in the same range as fossil oil; nevertheless, the oxidative stability of those microalgal biodiesel was lower than that of the CNS standard. Also, they demonstrated that the oxidative stability of microalga-derived biodiesel could be improved by hydrogenation catalyzed over carbon-supported palladium (Pd/C). Some researchers reported that the microalga Botryococcus sp. produces lower biomass yield and higher lipid productivity, up to 75% on a dry weight basis, than other microalgal species, such as Nannochloropsis sp., Nitzschia sp., Neochloris sp., Porphyridium sp., Dunaliella sp., Isochrysis, and Chlorella sp., with a lipid content ranging from 20 to 50% but appropriate biomass yield.
In the present scenario, rapid population growth and extensive fossil fuel usage increase the energy demand and significant environmental-related problems, which lead to global warming. Therefore, researchers have seriously searched for an alternative and sustainable solution to overcome those issues. In this context, microalgae are considered a promising candidate for an alternative fuel source and an excellent option for cleansing the environment. The previous studies have shown that the cost of biodiesel produced from microalgae is estimated at $20.53 and $9.84 per gallon using a PBR and open raceway pond cultivation method, respectively. This shows that microalgal biodiesel is a promising avenue for sustainable energy production. From the literature survey, it is clearly noted that even though several microalgal species are available for biodiesel production, only a few algal species are considered as the best choice because of its quality and quantity of lipid accumulation. Raja et al. [32] reported that, on earth, more than 25,000 microalgal species are available; however, only a few species are in use.
At present, the utilization of microalgae as a feedstock for the production of bioenergy and bioproducts still faces a lot of limitations and challenges, and we must be addressing these issues by improving the technologies from laboratory scale to commercial scale. The most critical problems are to improve the algal biomass productivity, dewatering and biomass productivity, pretreatment and extraction, and biodiesel production. Despite several advanced technologies are available for a large-scale biomass production and lipid conversion into biodiesel, still, microalgal biodiesel is too costly since the cultivation system design requires temperature and growth limiting condition control (viz., CO2, water sources, nutrient source, and optimization). The other most crucial obstacle is biomass dewatering because this process is energy-intensive and so costly.
Generally, in a large-scale algal cultivation, the closed PBR system is more expensive than the open raceway ponds. The PBR system also faces major operating challenges, such as overheating and fouling, due to gas exchange limitation. In microalgal cultivation, open ponds, especially mixed raceway ponds, are much cheaper to be built and operated and are easily scaled up to several hectares, which make them the right choice for commercial-scale biomass production. About 95% of commercial microalgal biomass production is performed using open raceway ponds even for high value-added bioproducts, which sell for prices over a hundred/thousand dollars. Nevertheless, the open cultivation methods meet several limitations, mainly due to contaminations by other microalgal species, algal grazers, fungi, amoeba, etc., and temperature. A literature survey revealed that though hundreds of research papers were published, still now, no proper information is available on cultivation designs, operations, yields, and other important aspects at the commercial level [33]. A major bottleneck in microalgal biofuel production is the high capital and operating costs. However, several research studies have focused on microalga-based biofuels, still, there is a vast technological gap that was found during commercialization. In a large-scale biomass production, there is a large demand for water, CO2, nitrogen, and phosphorous, which is believed as another major hurdle. The wastewater can be utilized as a source of nutrients; nonetheless, there is a serious concern on contamination by bacteria, pathogens, and chemical compounds presenting in wastewater. Earlier studies reported that 0.16 kg of nitrogen and 0.022 kg of phosphorous are required for producing 1 liter of algal oil [34]. Besides, for producing 1-liter algal oil, the microalgae need 3.5–9.3 kg of CO2, which implies that algae utilize a large amount of CO2 for its growth and biomass production.
Another major challenge is algal lipid extraction prior to biodiesel production. In this part, after biomass drying, the lipid extraction using expensive solvents significantly increases the production cost. Many researchers are searching for significantly advanced technologies without drying or solvent extraction of the algal slurry in order to reduce the biomass pretreatment cost.
The biodiesel production based on current methods is expensive since it requires neat lipid feedstock, free from free fatty acids (FFA), and water. For this kind of extraction technique, the biomass must be dried; however, biomass drying is another important process, and it requires a higher cost. To reduce the FFA content of lipid feedstock, the esterification process is carried out via either acidic or enzymatic route; however, this process is still at the research stage. The esterification through the enzymatic process using lipases may be considered as the best choice because it has added advantage of running even at low temperatures. Nonetheless, the primary issue in this method is glycerol formed as a by-product, which can inhibit the lipase activity. Some researchers demonstrated that using methyl acetate, as a substrate instead of methanol, avoids glycerol formation and lipase inhibition since triacetin is generated as a by-product [35].
It has been reported that the current costs in biofuel produced from microalgal biomass are approximately estimated up to 50 $/L, and thus this makes algal biofuel unsuccessful at commercial scale [36]. Nevertheless, to reduce the cost and make the algal biofuel production at commercial success, research works are still ongoing. However, the most promising and sustainable way for biofuel production is to reduce the cultivation cost, particularly growth nutrient cost. The utilization of wastewater for large-scale cultivation of algal biomass is attracted between the researchers. It is possible to grow the algae at zero nutrient cost using wastewater obtained from various sources, such as industrial, municipal, and agricultural [17]. Recent researchers are extensively investigating an integrated biorefinery concept for producing the algal biomass at zero nutrient cost; besides, it is a possible way for treating the wastewater using zero-cost technology. Some studies focused on commercial interests in a large-scale microalgal culturing using coal-fired power plants or sewage treatment facilities. This approach not only provides the raw materials for the system, such as CO2 and nutrients; besides it also produces valuable biofuels with a cleansed environment (Figure 1). Today, the price of crude oil is lower, so the biodiesel produced from microalgae is economically uncompetitive with fossil diesel [33]. From the above study, it clearly shows that low-cost biomass production is a key issue towards the commercial production of algal biodiesel. Research efforts have been devoted to address the following problems: (1) to enhance the photosynthesis efficiency, biomass, and lipid production through genetic and metabolic engineering; (2) using high-efficient and low-cost biomass production system (open raceway pond or low-cost designed PBR); (3) cultivation mode (batch or semicontinuous); (4) utilization of wastewater and industrial flue gas in algal cultivation; (5) introducing novel microalgal harvesting methods; and (6) implementing low-cost with high-efficient oil extraction and transesterification methods (e.g., simultaneous oil extraction and transesterification, using novel heterogeneous acid catalysts, etc.).
Integrated microalgal biorefinery approach.
Today, microalgae offer interesting characteristic features to qualify them as promising alternative feedstocks for various industrial and environmental applications. Nevertheless, many efforts are required to address different challenges particularly on low cost with high-efficiency biofuels, wastewater treatment, and CO2 mitigation. Based on the research data available, it is clearly found that so far, microalgal biodiesel production is mainly stuck in a cost factor. It is clearly noticed that zero nutrient cost technology for biomass production, inexpensive large-scale harvesting, and biodiesel conversion process are yet to be improved through a detailed investigation. In this point of view, this review shows a clear outlook on algal cultivation for biofuel production and what are the challenges behind with future prospects. The production of microalgal biofuel at commercial scale can play a key role in the present global energy scenario and concern towards the related environmental issues. Researchers believe that microalgal as a third-generation candidate will be satiating the energy demand and its challenges in the future. The paramount challenges in algal biodiesel production are cultivation and harvesting techniques, and the limitations with an emphasis on the cost factor are discussed. Therefore, establishing a new and innovative biorefinery-based low-cost technology should be developed to overcome these problems. Recently, the microalga-based biorefinery is the emerging technology, which is aiming to address the above severe issues and make the algal biofuels sustainable and alternative. Besides, it helps wastewater treatment at zero-cost technology, CO2 mitigation, and attractive value-added bioproducts. These economic processes could be improved by adapting various cost-cutting activities, such as utilizing wastewater and industrial flue gas as nutrient and carbon sources, respectively. Finally, the microalga-based biorefinery process seems to be the most feasible approach in the forthcoming years to compete with fossil fuels and to develop a sustainable and renewable bioenergy source.
The primary application of refrigeration system is to transfer heat from a lower temperature region to a higher temperature one. A refrigeration cycle consists of a source at low temperature, a sink at high temperature, and a device to produce the work done to transfer heat from the source to sink. For the complete circulation, the refrigeration cycle should have an expansion device to circulate the refrigerant to the source.
\nMajor refrigeration systems include vapor-compression refrigeration system (VCRS), heat pump (HP), gas refrigeration system (GRS), multi-pressure refrigeration systems (MPRS), and absorption refrigeration system (ARS), as presented in Figure 1. These systems are combined with renewable sources, such as geothermal, solar, and wind energy sources.
\nThe classifications of refrigeration systems and renewable sources.
The vapor-compression refrigeration cycle (VCRS) is the most widely used cycle for refrigerators, air-conditioning systems, and heat pumps [1, 2]. It consists of four processes, as shown in Figure 2:
1-2 Isentropic compression in a compressor
2-3 Constant-pressure heat rejection in a condenser
3-4 Throttling in an expansion device
4-1 Constant-pressure heat absorption in an evaporator
Schematic and T-s diagram for the ideal VCRS.
The refrigerant enters the compressor from state 1 at saturated vapor to be isentropically compressed from low pressure of state 1 to high pressure and temperature of state 2, which is at the superheated region. Then, the refrigerant of state 2 enters the condenser to reject heat to the warm environment and exits at the saturated liquid as state 3. The refrigerant enters an adiabatic throttling or expansion valve to drop the pressure, which equals the pressure at the compressor inlet of state 1. The refrigerant temperature at state 1 is very low so that it absorbs heat from the refrigerated space at the evaporator and heated to be saturated vapor again. The vapor refrigeration system is a closed cycle where it starts and ends at state 1. This type of refrigeration system can be used for refrigerators, inside the air conditioners as split air conditioners, and separate as in radiant cooling systems [3, 4] and air-to-air systems [1].
\nThe first and second law of Thermodynamics for steady-state flow is applied for each component and the whole system. They include the energy balance equation (EnBE) and exergy balance equation (ExBE) in this order. The energy balance equation considers the heat transfer and work produced or done crossing the control volume of a component or a system, while the exergy balance equation considers the irreversibilities of a process, which are described by the exergy destruction. For the given system of Figure 2. The refrigerant mass flow rate is constant through the cycle and denotes as \n
The power input to the compressor, \n
The heat rejection rate from the condenser, \n
The energy and exergy balance equations for the expansion valve can be expressed as Eqs. (10) and (11), respectively. The expansion valves are considered to be decreasing the pressure adiabatically and isentropically, which means no heat transfer and work done in the throttling process [6]:
\nThe energy balance for the entire refrigeration system can be given as [5]:
\nThe coefficient of performance (COP) of the refrigeration system is defined as the ratio of useful energy, which is the rate of heat removal by the evaporator to the required energy, which is the power required to operate the compressor. The COP is given as below [5]:
\nThe Carnot or reversible COP is defined as the maximum COP of a refrigeration cycle operating between temperature limits \n
An actual vapor-compression refrigeration cycle differs from the ideal one because of the irreversibilities that occur in various components, such as fluid friction (causes pressure drops) and heat transfer to or from the surroundings. The aim of exergy analysis is to determine the exergy destruction in each component of the system and to determine the exergy efficiency of the entire system. Exergy destruction in a component can be evaluated based on entropy generation and an exergy balance equation using Eq. (15) [6]:
\nwhere \n
The exergetic coefficient of performance (\n
by substituting \n
Since \n
Heat pump system (HP) is similar to VCRS since it consists of a compressor, expansion valve, and outdoor and indoor coils, which operate exchangeably as condenser and evaporator. The advantage of HP systems is the ability to provide cooling and heating for the desired space, especially for the long winter season as in Canada and north European countries. This can be achieved by adding a reversing valve, as shown in Figure 3. There are two essential modes: heating mode and cooling mode. The condenser and evaporator are exchanging during the cooling and heating season since the reversing valve is switching between two modes according to the weather condition.
\nA heat pump can be used to heat a house in winter and to cool it in summer.
The energy source for heat pump can be classified into air-source, water-source, and ground-source. The air-source system uses atmospheric air through the evaporator, while the water-source system uses well water of depth 80 m and operates from 5 to 18°C. The ground-source system uses long piping under the ground since the soil temperature is not affected by climate change. The capacity and efficiency of heat pump drop at low-temperature environment, and therefore, other auxiliary systems, such as heaters or furnaces, are used to provide sufficient heating load for residential buildings.
\nThe COP of a heat pump is defined as the ratio of the heat removed for cooling mode or added for a heating mode of the indoor coil to the compressor power. Therefore, the COPheating and COPcooling are given in Eq. (19). \n
The exergetic COP is defined as the ratio of thermal exergy rate divided by the compressor power. It is also given as the ratio of COP to the reversible COP for both heating and cooling mode. \n
The VCRS is known as a modified, reverse Rankine cycle, while the gas refrigeration system (GRS) is known as a reverse Brayton cycle using a noncondensing gas such as air. The main advantage of this system is the small size for achieving the desired cooling due to the lighter weight of air than other refrigerants. This system can be used in aircraft cabin cooling.
\nAs illustrated in Figure 4, the major elements of GRS are compressor to raise the pressure of gas from state 1 to 2, a rejecting heat exchanger (condenser), turbine or expander to decrease the gas pressure isentropically, and an absorbing heat exchanger (evaporator) to absorb the heat from the refrigerated space at constant pressure. A regenerator heat exchanger can be added to the system for heat recovery between the hot and cold paths of circulated gas. It can be located between the two heat exchangers. Air is a popular refrigerant of this system since it can be utilized as a refrigerant and air-conditioning medium in smaller equipment units as aircraft cooling systems.
\nSimple gas refrigeration cycle and T-s diagram.
The energy analysis of a gas refrigeration system is similar to that of the vapor refrigeration system except that the gaseous fluid is treated as an ideal gas. Therefore, the enthalpy and entropy equations are written as [5]:
\nwhere the subscripts i and e indicate inlet and exit states, respectively. Therefore, the energy and exergy analysis for each component of Figure 5 is listed below [5, 6].
\nA two-stage cascade refrigeration system with the same refrigerant in both stages.
Compressor:
\nHeat exchanger 2 (condenser):
\nTurbine (expander):
\nHeat exchanger 1 (evaporator):
\nFor the entire refrigeration system, the energy balance can be written as:
\nThe net power for the system becomes:
\nThe COP of the gas refrigeration system is given as:
\nThe total exergy destruction in the system can be calculated by adding exergy destructions of each component:
\nIt can also be expressed as:
\nThus, the minimum power input to accomplish the required refrigeration load \n
The VCRS is the most popular refrigeration cycle because it is simple, inexpensive, and reliable. However, the industrial refrigeration systems should be efficient by providing more refrigeration load. This can be achieved by modifying the simple VCRS into multi-pressure refrigeration systems (MPRS). The MPRS can be classified into cascade RS, multi-compression RS, and multipurpose RS.
\nSome industrial applications require low temperature below −70°C with substantially large pressure and temperature difference (−70 to 100°C). VCRS cannot achieve these applications because it can operate within a temperature range of +10 to −30°C. Therefore, a modification of VCRS can be performed by using multiple refrigeration cycles operating in series, the so-called cascade refrigeration systems. The refrigerants of each cycle can be different. The evaporator of the first refrigeration cycle is connected to the condenser of the next refrigeration system forming an interchange heat exchanger between the 2 cycles, as shown in Figure 5. Cascade refrigeration systems are mainly used for liquefaction of natural gas, hydrogen, and other gases [7, 8, 9]. The major benefit of this system is decreasing the compressor power and increasing the refrigeration load compared with a VCRS with large temperature and pressure difference, as shown in the T-s diagram of cascade system in Figure 5. Therefore, reducing system components can be fulfilled in an appropriate way [2].
\nThe net compressor power can be determined by the summation of all compressor power in all cascaded refrigeration system and written as [2]:
\nThe refrigeration load can be described as:
\nThe heat exchanger that connects the 2 cycles together has an energy balance equation as follows [5]:
\nTherefore, the COP and exergetic COP of the cascade refrigeration system can be explained as the following [5, 6]:
\nSimilar to the cascade refrigeration system, multistage compression refrigeration system is used for applications below −30°C. This requires a large-pressure-ratio compressor and cannot be performed by one compressor because of the lack of efficiency and performance. Therefore, using multistage compressors connected in series can improve the performance of the refrigeration system by increasing the pressure ratio and increasing the refrigeration load. As shown in Figure 6, a two-stage compression refrigeration cycle consists of two compressors, a condenser, an evaporator, a flash intercooler, a mixer, and two throttling valves. The compressors. The upper compressor compresses the total refrigerant mass flow rate in a vapor form from the intermediate pressure of state 9 to the high pressure of state 4. The vapor refrigerant cools down in the condenser to saturated liquid at high pressure of state 5 and then passes through the upper expansion valve to reduce the pressure to intermediate pressure. The wet refrigerant passes through the flash intercooler to split the vapor and liquid phase. The vapor phase at state 3 enters the mixer to mix with the exit superheated refrigerant of the lower compressor at state 2. The liquid phase at state 7 is expanded by the lower throttling valve to state 8, which enters the lower pressure evaporator to absorb heat from the refrigerated space. The minimum temperature can be achieved by two-stage compression at −65°C, while the three-stage compression can attain about −100°C.
\nA two-stage compression refrigeration system with a flash chamber.
The heat transfer to the evaporator can be written, according to Figure 6, as [10]:
\nwhere \n
Therefore, the COP of this system can be determined as the following [10]:
\nThe second efficiency or the exergetic COP can be calculated as [6, 10]:
\nMultipurpose refrigeration systems are also considered as a branch of MPRS. This type of system accomplishes different refrigeration loads in one system. Therefore, a modification of VCRS can be done by using multiple evaporators at different low pressure and different refrigerant capacity. Also, this system can be operated using one compressor or multistage compressor.
\nThere are different configurations of multipurpose refrigeration systems [2], as shown in Figure 7. Firstly, a system of a single compressor and individual expansion valves consists of two evaporators and single compressor with individual expansion valves for each evaporator and one compressor, as shown in Figure 7a. Operation under these conditions means the dropping of pressure from high-pressure evaporators through back pressure valves to ensure the compression of the vapor from the higher temperature evaporators through a pressure ratio. Secondly, a system of a single compressor with multi-expansion valves consists of two evaporators and a compressor with multiple arrangements of expansion valves, as shown in Figure 7b. The only advantage of the arrangement is that the flashed vapor at the pressure of the high-temperature evaporator is not allowed to go to the lower-temperature evaporator, thus improving its efficiency. Finally, a system of individual compressors with multi-expansion valves consists of a compressor for each evaporator and multiple arrangements of expansion valves, as shown in Figure 7c, to reduce the total power requirement. This amounts to parallel operation of evaporators and is called sectionalizing. There may be a separate condenser for each compressor or a common condenser for the whole plant.
\nMultipurpose refrigeration system: (a) two evaporators with individual expansion valve, (b) two evaporators and multi-expansion valve, and (c) individual compressors and multi-expansion valve.
The heat transfer to the evaporators and the net compressor power of the multipurpose refrigeration system despite the system configuration can be evaluated as [2]:
\nwhere \n
Therefore, the COP of this system can be determined as the following [5]:
\nThe second efficiency or the exergetic COP can be calculated as [6]:
\nThe absorption refrigeration system (ARS) is similar to the VCRS except that the compressor of the vapor-compression system is replaced by three elements: an absorber, a solution pump, and a generator. The ABS medium is a mixture of a refrigerant and absorbent, such as ammonia-water system (NH3 + H2O) and water-lithium bromide (LiBr2 + H2O). The solubility of refrigerant (ammonia or lithium bromide) in the absorbent (water) is satisfactory, but the difference in boiling points is significant, which may affect the purity of vaporization. Thus, a purge unit or rectifier is used in the system. The refrigerant concentration in the mixture changes according to the pressure and temperature for each step. The ABS.
\nAs shown in Figure 8, the ARS consists of a condenser, an evaporator, an absorber, a regeneration heat exchanger (HX1), heat recovery heat exchanger (HX2), a generator, two expansion valves, and a solution pump. The system includes an analyzer and a rectifier to remove the water vapor that may have formed in the generator. Thus, only ammonia vapor goes to the condenser. This system utilizes the absorbent water to release and absorb ammonia as the refrigerant. Starting from state 3, the strong solution (a high concentration of ammonia refrigerant) is heated in the high-pressure generator. This produces refrigerant vapor off the solution at state 7. The hot pure ammonia vapor is cooled in the condenser at state 8 and condenses at state 9 by passing through the HX2 before entering a throttling valve into the low pressure at state 10. Then the refrigerant liquid passes through the evaporator to remove the heat from refrigerated medium and leaves at low-pressure vapor phase of state 11. The pure ammonia is heated by the HX2 to enter the absorber and mixed with the absorbent water. The weak solution (about 24% ammonia concentration) flows down from the generator at state 4 through the regeneration heat exchanger HX1 at state 5 through a throttling valve and enters the absorber at state 6. Therefore, the weak refrigerant is absorbed by the water because of the strong chemical affinity for each other. The absorber is cooled to produce a strong solution at low pressure at state 1. The strong solution is obtained and pumped by a solution pump to the generator passing through HX1, where it is again heated, and the cycle continues. Then, the water absorbs the ammonia in the absorber at the condenser temperature supplied by the circulating water or air, and hence a strong solution (about 38% ammonia concentration) occurs. For ammonia-water ARSs, the most suitable absorber is the film-type absorber because of high heat and mass transfer rates, enhanced overall performance, and large concentration rates [11].
\nAmmonia absorption refrigeration cycle.
The energy and exergy analysis for each component is presented according to Figure 8. The partial mass balance (PMBE) is also included to determine the concentration mass of ammonia and water in the absorber and generator. That is because the ARS has two fluids as refrigerant and absorbent and their composition at different points is different, particularly in the absorber and generator. The exergy analysis of ammonia-water ARSs is to determine the exergy destruction of each component and to determine the overall exergy efficiency based on the second law of thermodynamics. The exergy analysis (ExBE) for each component is stated below [5, 6]:
\nAbsorber:
\nwhere \n
Solution pump:
\nRegeneration heat exchanger (HX1):
\nGenerator:
\nwhere \n
Condenser:
\nwhere \n
Heat recovery heat exchanger (HX2):
\nExpansion valves:
\nEvaporator:
\nwhere \n
For the entire system, the overall energy balance of the complete system can be written as follows, by considering that there is negligible heat loss to the environment:
\nThe COP of the system then becomes:
\nwhere \n
The ARS is a heat-driven system, which requires heat pump instead or required power by a compressor. That means the ARS is a combination of a heat pump and a refrigeration cycle without a compressor. Therefore, the maximum (reversible) of an ARS can be achieved by a reversible heat engine and a reversible refrigerator, as shown in Figure 9. A reversible heat pump is operating by absorbing the heat from a source at and rejecting heat to an environment of to produce a work output from the heat engine. This work is defined as the reversible efficiency of the heat pump multiplied by the heat absorber from the source, which is the heat transfer from the generator in the ARS. This work output is used by the reversible refrigerator to keep a refrigerated space at TL\n while rejecting heat to the environment at T0\n. Therefore, the reversible COP of ARS can be obtained by the thermal efficiency of a reversible heat engine and the COP of a reversible refrigerator as in Eq. (72) [10]:
\nThe maximum COP of an absorption refrigeration system.
The temperature of the heat source is taken as the average temperature of geothermal water. Then the second-law efficiency of this absorption system is determined to be [10]:
\nThe refrigeration systems require an input work to release the heat from the refrigerated space to the environment, which is called as a work-driven system. The absorption refrigeration system is based on external heat transfer from an external source, which can be classified as a heat-driven system. For industrial refrigeration systems, energy demand is high and should be provided in a secure and eco-friendly approach to reduce environmental pollution. This can be executed by fossil-based fuels such as oil, natural gas, and coal, which produce substantial carbon mono-oxide and dioxide emissions that affect global warming and climate change. Massive efforts point to renewable sources such as geothermal energy, solar energy, and wind energy, which promise a potential solution to provide the clean energy needed as work or heat to operate the refrigeration. Schematic diagram of Figure 10 shows possible ways of renewable sources for work-driven and heat-driven refrigeration system.
\nRenewable sources for refrigeration systems: (a) work-driven and (b) heat-driven source.
An integrated system of a concentrated solar power plant integrated with desalination process and absorption refrigeration cycle is utilized to supply power, freshwater, and refrigeration [12]. The system, as shown in Figure 11, consists of concentrated solar collectors connected with steam turbine power plant, a multi-effect desalination process with a parallel feed of seawater, and a single-stage ammonia-water absorption refrigeration system. The solar collectors provide thermal energy 21,030 kW to the steam power plant to deliver an electric power of 4632 kW. The refrigeration load from the absorption cooling system is 820.8 kW. The desalination system can also provide 22.79 kg/s freshwater. This cycle has obtained overall energy and exergy efficiencies to be 80.70% and 66.05%, respectively.
\nSchematic diagram of the integrated solar thermal power plant, absorption refrigeration system, and MED cycle (adopted from [12]).
Another example, a small-scale system, is designed to provide an electrical load to residential buildings [13]. This system utilizes, as shown in Figure 12, photovoltaic solar system (PV) to provide electrical power. This electric power is used for a water electrolyzer system to split the water electrochemically to produce hydrogen and oxygen gases. The hydrogen gas enters high-temperature solid oxide fuel cells (SOFC) to produce electricity and heat. The heat is transferred to an absorption cooling system by heat recovery generator. The PV system may generate excess electricity more than the demand during off-peak hours. This system is designed for a detached house in Toronto city, Canada. The PV solar system delivers maximum power of 3.35 kW. The water electrolyzer can produce 0.792 and 0.538 kg/day of gaseous hydrogen in summer and winter seasons. The SOFC fuel cell supplies 8.43 kWh per day in summer season. The maximum energy and exergy efficiencies of the photovoltaic system are 17 and 18.3%, respectively, while the maximum total energy and exergy efficiencies are obtained to be 55.7 and 49.0%, respectively.
\nSchematic of the photovoltaic-fuel cell CHIP system for residential applications (adopted from [13]).
In a similar study, a hybrid renewable system was designed to produce electricity and clean fuel such as hydrogen gas and provide cooling for a residential building in two locations Egypt and Saudi Arabia in summer season [14]. The cooling loads for a house are 18.06 and 19.3 kW in Egypt and Saudi Arabia, respectively. This system, as shown in Figure 13, depends on the photovoltaic solar system and wind turbines to provide excess electricity more than the electric grid. The excess electricity is delivered to a water electrolyzer to produce pure oxygen and hydrogen gases stored in tanks for clean fueling services. Part of the hydrogen gas is used for a proton-exchange membrane (PEM) fuel cell that can produce heat and electricity through an electrochemical process without any mechanical parts. The heat generated from the fuel cell can be utilized by a generator of an ammonia-water ARS to provide cooling. The hybrid renewable system can operate in a significant performance with water mass flow rate of 1.8 kg/s to produce hydrogen with a mass flow rate of 0.2 kg/s and ammonia mass flow rate of about 0.2 kg/s to produce cooling load between 40 and 120 kW more than the design cooling load of one house. The energy and exergy efficiencies are obtained to be about 67 and 68%, respectively. Therefore, this hybrid system can be sufficient for more than one house.
\nSchematic diagram of a hybrid renewable system (adopted from [14]).
A multigeneration system is designed by [15] and powered by geothermal energy assisted with solar energy to produce five outputs: heating air for residential building, hot domestic water, drying food, refrigeration for industry, and electricity. This multigeneration system, as shown in Figure 14, consists of a heat pump system, a single flash geothermal cycle, an absorption cooling system, thermal energy storage connected with auxiliary steam turbine and concentrated solar collectors, hot water system, and drying system. The system has achieved overall energy and exergy efficiencies to be 69.6 and 42.8%, respectively. The first and second steam turbines have the power of 10,043 and 9886 kW. The COP and COPex\n are 0.678 and 0.253 for the absorption cooling system and 2.029 and 0.1826 for heat pump system, respectively. The refrigeration load is 1787 kW. The overall energy and exergy efficiencies for the whole system are 69.6 and 42.8%, respectively.
\nSchematic diagram of the multigeneration system powered by the solar and geothermal energy (adopted from [15]).
A wind system is combined with a refrigeration system, as shown in Figure 15. Wind energy is coupled with compressed air energy storage (CAES) systems to store wind energy for long-term usage [16]. The integrated system consists of a combined gas power cycle, including compressors, intercooling heat exchangers, and gas turbine, an organic Rankine power cycle (ORC), and an absorption refrigeration system (ARS). The system objective is to provide electricity, domestic hot water, and cooling load. The system can generate electricity of 33.67 kW provided by wind turbines (83.24 kWh) and fuel combustion (258.97 kWh), cooling load of 2.56 kW, and mass flow rate of hot water of 1.82 ton per day hot. The energy efficiency of the system is achieved to be 53.94%.
\nSchematic diagram of gas power cycle with wind turbine, CAES, ORC, and ARS (adopted from [16]).
The refrigeration systems are applied in our life for preserving food, cooling air, and other industrial applications. Most refrigeration systems require external power or external heat to release the heat from the refrigerated space. Many industrial applications involve large cooling energy, which can be operated by multi-pressure refrigeration system, which requires a large amount of external power. The chapter has presented some applications with renewable sources to replace the fossil fuel-driven energy with an environmentally friendly energy source such as geothermal, solar, and wind energy so-called hybrid or integrated systems. In addition to cooling load, the hybrid systems can produce electricity, heating load, and clean fuel such as hydrogen fuel. The absorption refrigeration system is mostly-combined with hybrid system to use the heating load from solar or geothermal energy to produce cooling load.
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\n\nWe have adopted the Protocol to increase the number of readers of our publications. All our Works are more widely accessible, with resulting benefits for scholars, researchers, students, libraries, universities and other academic institutions. Through this method of exposing metadata, IntechOpen enables citation indexes, scientific search engines, scholarly databases, and scientific literature collections to gather metadata from our repository and make our publications available to a broader academic audience.
\n\nAs a Data Provider, metadata for published Chapters and Journal Articles are available via our interface at the base URL:http://www.intechopen.com/oai/?.
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\n\nYou can find out more about the Protocol by visiting the Open Archives website. For additional questions please contact us at info@intechopen.com.
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\n\nBASE - Bielefeld Academic Search Engine
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