Coal liquefaction is a process of converting coal into liquid hydrocarbons: liquid fuels and petrochemicals. This process is often known as "Coal to X", where X can be many different hydrocarbon-based products. However, the most common process chain is "Coal to Liquid Fuels" (CTL).
- 1 Historical background
- 2 Methods
- 3 Environmental considerations
- 4 Research and development of coal liquefaction
- 5 Coal liquefaction plants and projects
- 6 See also
- 7 References
- 8 External links
Coal liquefaction originally was developed at the beginning of the 20th century. The best known CTL process is Fischer–Tropsch synthesis (FT), named after the inventors Franz Fischer and Hans Tropsch from the Kaiser Wilhelm Institute in the 1920s. The FT synthesis is the basis for indirect coal liquefaction (ICL) technology. Friedrich Bergius, also a German chemist, invented direct coal liquefaction (DCL) as a way to convert lignite into synthetic oil in 1913.
Coal liquefaction became an integral part of the German industry during World War II. Coal liquefaction was an important part of Adolf Hitler's four-year plan of 1936. In the mid 1930s, companies like IG Farben and Ruhrchemie initiated industrial production of synthetic fuels derived from coal. This led to the construction of twelve DCL plants using hydrogenation and nine ICL plants using Fischer–Tropsch synthesis by the end of World War II. In total, CTL provided 92% of Germany's air fuel and over 50% of its petroleum supply in the 1940s. The DCL and ICL plants effectively complemented each other rather than competed. The reason for this is that coal hydrogenation yields high quality gasoline for aviation and motors, while FT synthesis chiefly produced high quality diesel, lubrication oil, and waxes together with some smaller amounts of lower quality motor gasoline. The DCL plants were also more developed as lignite - the only coal available in many parts of Germany - worked better with hydrogenation than with FT synthesis. After the war, Germany had to abandon its synthetic fuel production as it was prohibited by the Potsdam conference in 1945.
South Africa developed its own CTL technology in the 1950s. The South African Coal, Oil and Gas Corporation (Sasol) was founded in 1950 as part of industrialization process that the South African government considered essential for continued economic development and autonomy. However, South Africa had no domestic oil reserves and this made the country very vulnerable to disruption of supplies coming from outside, albeit for different reasons at different times. Sasol was a successful way to protect the country's balance of payment against the increasing dependence on foreign oil. For years its principal product was synthetic fuel and this business enjoyed significant government protection in South Africa during the apartheid years for its contribution to domestic energy security. Although it was generally much more expensive to produce oil from coal than from natural petroleum, the political as well as economic importance of achieving as much independence as possible in this sphere was sufficient to overcome any objections. Early attempts to attract private capital, foreign or domestic, were unsuccessful, and it was only with state support that the coal liquefaction could start. CTL continued to play a vital part in South Africa's national economy, providing around 30% of its domestic fuel demand. The democratization in the 1990s has made Sasol search for products that could prove more competitive in the global marketplace, and as of the new millennium Sasol is focusing primarily on its petrochemical business, as well as on efforts to convert natural gas into crude oil (GTL) usings its expertise in Fischer–Tropsch synthesis.
CTL technologies have steadily improved since the Second World War. Technical development has resulted in a variety of systems capable of handling a wide array of coal types. However, only a few enterprises based on generating liquid fuels from coal have been undertaken, most of them based on ICL-technology. The most successful one is the South African company Sasol. CTL also received new interest in the early-2000s as a possible mitigation option for reducing oil dependence as rising oil prices and concerns over peak oil made planners rethink existing supply chains for liquid fuels.
Specific liquefaction technologies generally fall into two categories: direct (DCL) and indirect liquefaction (ICL) processes. Direct processes are based on approaches such as carbonization, pyrolysis, and hydrogenation.
Indirect liquefaction processes generally involve gasification of coal to a mixture of carbon monoxide and hydrogen, often known as synthesis gas or simply syngas. Using the Fischer–Tropsch process syngas is converted into liquid hydrocarbons.
In contrast, direct liquefaction processes convert coal into liquids directly without having to rely on intermediate steps by breaking down the organic structure of coal with application of hydrogen-donor solvent, often at high pressures and temperatures. Since liquid hydrocarbons generally have a higher hydrogen-carbon molar ratio than coals, either hydrogenation or carbon-rejection processes must be employed in both ICL and DCL technologies.
At industrial scales (i.e. thousands of barrels/day) a coal liquefaction plant typically requires multibillion-dollar capital investments.
Pyrolysis and carbonization processesEdit
A number of carbonization processes exist. The carbonization conversion typically occurs through pyrolysis or destructive distillation. It produces condensable coal tar, oil and water vapor, non-condensable synthetic gas, and a solid residue - char.
One typical example of carbonization is the Karrick process. In this low-temperature carbonization process, coal is heated at 680 °F (360 °C) to 1,380 °F (750 °C) in the absence of air. These temperatures optimize the production of coal tars richer in lighter hydrocarbons than normal coal tar. However, any produced liquids are mostly a by-product and the main product is semi-coke - a solid and smokeless fuel.
The COED Process, developed by FMC Corporation, uses a fluidized bed for processing, in combination with increasing temperature, through four stages of pyrolysis. Heat is transferred by hot gases produced by combustion of part of the produced char. A modification of this process, the COGAS Process, involves the addition of gasification of char. The TOSCOAL Process, an analogue to the TOSCO II oil shale retorting process and Lurgi–Ruhrgas process, which is also used for the shale oil extraction, uses hot recycled solids for the heat transfer.
Liquid yields of pyrolysis and Karrick processes are generally considered too low for practical use for synthetic liquid fuel production. Furthermore, the resulting liquids are generally require further treatment before they can be usable as motor fuels. Resulting coal tars and oils from pyrolysis are then further processed by hydrotreating to remove sulfur and nitrogen species, after which they are finally processed into liquid fuels.
In summary, the economic viability of this technology is questionable.
One of the main methods of direct conversion of coal to liquids by hydrogenation process is the Bergius process, developed by Friedrich Bergius in 1913. In this process, dry coal is mixed with heavy oil recycled from the process. A catalyst is typically added to the mixture. The reaction occurs at between 400 °C (752 °F) to 500 °C (932 °F) and 20 to 70 MPa hydrogen pressure. The reaction can be summarized as follows:
After World War I several plants based on this technology were built in Germany; these plants were extensively used during World War II to supply Germany with fuel and lubricants. The Kohleoel Process, developed in Germany by Ruhrkohle and VEBA, was used in the demonstration plant with the capacity of 200 ton of lignite per day, built in Bottrop, Germany. This plant operated from 1981 to 1987. In this process, coal is mixed with a recycle solvent and iron catalyst. After preheating and pressurizing, H2 is added. The process takes place in a tubular reactor at the pressure of 300 bar (30 MPa) and at the temperature of 470 °C (880 °F). This process was also explored by SASOL in South Africa.
In 1970-1980s, Japanese companies Nippon Kokan, Sumitomo Metal Industries, and Mitsubishi Heavy Industries developed the NEDOL process. In this process, coal is mixed with a recycled solvent and a synthetic iron-based catalyst; after preheating, H2 is added. The reaction takes place in a tubular reactor at a temperature between 430 °C (810 °F) and 465 °C (870 °F) at the pressure 150-200 bar. The produced oil has low quality and requires intensive upgrading. H-Coal process, developed by Hydrocarbon Research, Inc., in 1963, mixes pulverized coal with recycled liquids, hydrogen and catalyst in the ebullated bed reactor. Advantages of this process are that dissolution and oil upgrading are taking place in the single reactor, products have high H/C ratio, and a fast reaction time, while the main disadvantages are high gas yield (this is basically a thermal cracking process), high hydrogen consumption, and limitation of oil usage only as a boiler oil because of impurities.
The Nuclear Utility Services Corporation developed hydrogenation process which was patented by Wilburn C. Schroeder in 1976. The process involved dried, pulverized coal mixed with roughly 1wt% molybdenum catalysts. Hydrogenation occurred by use of high temperature and pressure synthesis gas produced in a separate gasifier. The process ultimately yielded a synthetic crude product, naphtha, a limited amount of C3/C4 gas, light-medium weight liquids (C5-C10) suitable for use as fuels, small amounts of NH3 and significant amounts of CO2. Other single-stage hydrogenation processes are the Exxon Donor Solvent Process, the Imhausen High-pressure Process, and the Conoco Zinc Chloride Process.
There are also a number of two-stage direct liquefaction processes; however, after the 1980s only the Catalytic Two-stage Liquefaction Process, modified from the H-Coal Process; the Liquid Solvent Extraction Process by British Coal; and the Brown Coal Liquefaction Process of Japan have been developed.
Shenhua, a Chinese coal mining company, decided in 2002 to build a direct liquefaction plant in Erdos, Inner Mongolia (Erdos CTL), with barrel capacity of 20 thousand barrels per day (3.2×103 m3/d) of liquid products including diesel oil, liquefied petroleum gas (LPG) and naphtha (petroleum ether). First tests were implemented at the end of 2008. A second and longer test campaign was started in October 2009. In 2011, Shenhua Group reported that the direct liquefaction plant had been in continuous and stable operations since November 2010, and that Shenhua had made 800 million yuan ($125.1 million) in earnings before taxes in the first six months of 2011 on the project.
Chevron Corporation developed a process invented by Joel W. Rosenthal called the Chevron Coal Liquefaction Process (CCLP). It is unique due the close-coupling of the non-catalytic dissolver and the catalytic hydroprocessing unit. The oil produced had properties that were unique when compared to other coal oils; it was lighter and had far fewer heteroatom impurities. The process was scaled-up to the 6 ton per day level, but not proven commercially.
Indirect conversion processesEdit
Indirect coal liquefaction (ICL) processes operate in two stages. In the first stage, coal is converted into syngas (a purified mixture of CO and H2 gas). In the second stage, the syngas is converted into light hydrocarbons using one of three main processes: Fischer–Tropsch synthesis, methanol synthesis with subsequent conversion to gasoline or petrochemicals, and methanation. Fischer–Tropsch is the oldest of the ICL processes.
In methanol synthesis processes syngas is converted to methanol, which is subsequently polymerized into alkanes over a zeolite catalyst. This process, under the moniker MTG (MTG for "Methanol To Gasoline"), was developed by Mobil in the early 1970s, and is being tested at a demonstration plant by Jincheng Anthracite Mining Group (JAMG) in Shanxi, China. Based on this methanol synthesis, China has also developed a strong coal-to-chemicals industry, with outputs such as olefins, MEG, DME and aromatics.
Methanation reaction converts syngas to substitute natural gas (SNG). The Great Plains Gasification Plant in Beulah, North Dakota is a coal-to-SNG facility producing 160 million cubic feet per day of SNG, and has been in operation since 1984. Several coal-to-SNG plants are in operation or in project in China, South Korea and India.
The above instances of commercial plants based on indirect coal liquefaction processes, as well as many others not listed here including those in planning stages and under construction, are tabulated in the Gasification Technologies Council's World Gasification Database.
Typically coal liquefaction processes are associated with significant CO2 emissions from the gasification process or as well as from generation of necessary process heat and electricity inputs to the liquefaction reactors, thus releasing greenhouse gases that can contribute to anthropogenic global warming. Especially if coal liquefaction is conducted without any carbon capture and storage technologies. There are technically feasible low-emission configurations of CTL plants.
CO2 emission control at Erdos CTL, an Inner Mongolian plant with a carbon capture and storage demonstration project, involves injecting CO2 into the saline aquifer of Erdos Basin, at a rate of 100,000 tonnes per year.[third-party source needed] As of late October 2013, an accumulated amount of 154,000 tonnes of CO2 had been injected since 2010, which reached or exceeded the design value.[third-party source needed]
For example, in the United States, the Renewable Fuel Standard and low-carbon fuel standard such as enacted in the State of California reflect an increasing demand for low carbon-footprint fuels. Also, legislation in the United States has restricted the military's use of alternative liquid fuels to only those demonstrated to have life-cycle GHG emissions less than or equal to those of their conventional petroleum-based equivalent, as required by Section 526 of the Energy Independence and Security Act (EISA) of 2007.
Research and development of coal liquefactionEdit
The United States military has an active program to promote alternative fuels use, and utilizing vast domestic U.S. coal reserves to produce fuels through coal liquefaction would have obvious economic and security advantages. But with their higher carbon footprint, fuels from coal liquefaction face the significant challenge of reducing life-cycle GHG emissions to competitive levels, which demands continued research and development of liquefaction technology to increase efficiency and reduce emissions. A number of avenues of research & development will need to be pursued, including:
- Carbon capture and storage including enhanced oil recovery and developmental CCS methods to offset emissions from both synthesis and utilization of liquid fuels from coal,
- Coal/biomass/natural gas feedstock blends for coal liquefaction: Utilizing carbon-neutral biomass and hydrogen-rich natural gas as co-feeds in coal liquefaction processes has significant potential for bringing fuel products' life-cycle GHG emissions into competitive ranges,
- Hydrogen from renewables: the hydrogen demand of coal liquefaction processes might be supplied through renewable energy sources including wind, solar, and biomass, significantly reducing the emissions associated with traditional methods of hydrogen synthesis (such as steam methane reforming or char gasification), and
- Process improvements such as intensification of the Fischer–Tropsch process, hybrid liquefaction processes, and more efficient air separation technologies needed for production of oxygen (e.g. ceramic membrane-based oxygen separation).
Since 2014, the U.S. Department of Energy and the Department of Defense have been collaborating on supporting new research and development in the area of coal liquefaction to produce military-specification liquid fuels, with an emphasis on jet fuel, which would be both cost-effective and in accordance with EISA Section 526. Projects underway in this area are described under the U.S. Department of Energy National Energy Technology Laboratory's Advanced Fuels Synthesis R&D area in the Coal and Coal-Biomass to Liquids Program.
Every year, a researcher or developer in coal conversion is rewarded by the industry in receiving the World Carbon To X Award. The 2016 Award recipient is Mr. Jona Pillay, Executive director for Gasification & CTL, Jindal Steel & Power Ltd (India). The 2017 Award recipient is Dr. Yao Min, Deputy General Manager of Shenhua Ningxia Coal Group (China).
In terms of commercial development, coal conversion is experiencing a strong acceleration. Geographically, most active projects and recently commissioned operations are located in Asia, mainly in China, while U.S. projects have been delayed or canceled due to the development of shale gas and shale oil.
Coal liquefaction plants and projectsEdit
World (Non-U.S.) Coal to Liquid Fuels ProjectsEdit
|Project||Developer||Locations||Type||Products||Start of Operations|
|Sasol Synfuels II (West) & Sasol Synfuels III (East)||Sasol (Pty) Ltd.||Secunda, South Africa||CTL||160,000 BPD; primary products gasoline and light olefins (alkenes)||1977(II)/1983(III)|
|Shenhua Direct Coal Liquefaction Plant||Shenhua Group||Erdos, Inner Mongolia, China||CTL (direct liquefaction)||20,000 BPD; primary products diesel fuel, liquefied petroleum gas, naphtha||2008|
|Yitai CTL Plant||Yitai Coal Oil Manufacturing Co., Ltd.||Ordos, Zhungeer, China||CTL||160,000 mt/a Fischer–Tropsch liquids||2009|
|Jincheng MTG Plant||Jincheng Anthracite Mining Co., Ltd.||Jincheng, China||CTL||300,000 t/a methanol from MTG process||2009|
|Sasol Synfuels||Sasol (Pty) Ltd.||Secunda, South Africa||CTL||3,960,000 (Nm3/d) syngas capacity; Fischer–Tropsch liquids||2011|
|Shanxi Lu'an CTL Plant||Shanxi Lu'an Co. Ltd.||Lu'an, China||CTL||160,000 mt/a Fischer–Tropsch liquids||2014|
|ICM Coal to Liquids Plant||Industrial Corporation of Mongolia LLC (ICM)||Tugrug Nuur, Mongolia||CTL||13,200,000 (Nm3/d) syngas capacity; gasoline||2015|
|Yitai Yili CTL Plant||Yitai Yili Energy Co.||Yili, China||CTL||30,000 BPD Fischer–Tropsch liquids||2015|
|Yitai Ordos CTL Plant Phase II||Yitai||Ordos, Zhungeer-Dalu, China||CTL||46,000 BPD Fischer–Tropsch liquids||2016|
|Yitai Ürümqi CTL Plant||Yitai||Guanquanbao, Urunqi, China||CTL||46,000 BPD Fischer–Tropsch liquids||2016|
|Shenhua Ningxia CTL Project||Shenhua Group Corporation Ltd||China, Yinchuan, Ningxia||CTL||4 million tonnes/year of diesel & naphtha||2016|
|Celanese Coal/Ethanol Project||Celanese Corporation – PT Pertamina Joint Venture||Indonesia, Kalimantan or Sumatra||CTL||1.1 million tons of coal/year to produce ethanol||2016|
|Clean Carbon Industries||Clean Carbon Industries||Mozambique, Tete province||Coal waste-to-liquids||65,000 BPD fuel||2020|
|Arckaringa Project||Altona Energy||Australia, South||CTL||30,000 BPD Phase I 45,000 BPD + 840 MW Phase II||TBD|
U.S. Coal to Liquid Fuels ProjectsEdit
|Adams Fork Energy - TransGas WV CTL||TransGas Development Systems (TGDS)||Mingo County, West Virginia||CTL||7,500 TPD of coal to 18,000 BPD gasoline and 300 BPD LPG||Operations 2016 or later|
|American Lignite Energy (aka Coal Creek Project)||American Lignite Energy LLC (North American Coal, Headwaters Energy Services)||MacLean County, North Dakota||CTL||11.5 million TPY lignite coal to 32,000 BPD of undefined fuel||Delayed/Cancelled|
|Belwood Coal-to-Liquids Project (Natchez)||Rentech||Natchez, Mississippi||CTL||Petcoke to up to 30,000 BPD ultra-clean diesel||Delayed/Cancelled|
|CleanTech Energy Project||USA Synthetic Fuel Corp. (USASF)||Wyoming||Synthetic crude||30.6 mm bbls/year of synthetic crude (or 182 billion cubic feet per year)||Planning/financing not secured|
|Cook Inlet Coal-to Liquids Project (aka Beluga CTL)||AIDEA and Alaska Natural Resources to Liquids||Cook Inlet, Alaska||CTL||16 million TPY coal to 80,000 BPD of diesel and naphtha; CO2 for EOR; 380 MW electrical generation||Delayed/Cancelled|
|Decatur Gasification Plant||Secure Energy||Decatur, Illinois||CTL||1.5 million TPY of high-sulfur IL coal generating 10,200 barrels per day of high quality gasoline||Delayed/Cancelled|
|East Dubuque Plant||Rentech Energy Midwest Corporation (REMC)||East Dubuque, Illinois||CTL, polygeneration||1,000 tpd ammonia; 2,000 BPD clean fuels and chemicals||Delayed/Cancelled|
|FEDC Healy CTL||Fairbanks Economic Development Corp. (FEDC)||Fairbanks, Alaska||CTL/GTL||4.2-11.4 million TPY Healy-mined coal; ~40k BPD liquid fuels; 110MW||Planning|
|Freedom Energy Diesel CTL||Freedom Energy Diesel LLC||Morristown, Tennessee||GTL||Undetermined||Delayed/Cancelled|
|Future Fuels Kentucky CTL||Future Fuels, Kentucky River Properties||Perry County, Kentucky||CTL||Not specified. Coal to methanol and other chemicals (over 100 million tons of coal supply)||Active|
|Hunton "Green Refinery" CTL||Hunton Energy||Freeport, Texas||CTL||Bitumen crude oil to 340,000 BPD jet and diesel fuel||Delayed/Cancelled|
|Illinois Clean Fuels Project||American Clean Coal Fuels||Coles County, Illinois||CTL||4.3 million TPY coal/biomass to 400 million GPY diesel and jet fuel||Delayed/Cancelled|
|Lima Energy Project||USA Synthetic Fuel Corp. (USASF)||Lima, Ohio||IGCC/SNG/H2, polygeneration||Three Phases: 1) 2.7 million barrels of oil equivalent (BOE), 2) expand to 5.3 million BOE (3) expand to 8.0 million BOE (47 billion cf/y), 516 MW||Active|
|Many Stars CTL||Australian-American Energy Co. (Terra Nova Minerals or Great Western Energy), Crow Nation||Big Horn County, Montana||CTL||First phase: 8,000 BPD liquids||Active (no new information since 2011)|
|Medicine Bow Fuel and Power Project||DKRW Advanced Fuels||Carbon County, Wyoming||CTL||3 million TPY coal to 11,700 BPD of gasoline||Delayed/Cancelled|
|NABFG Weirton CTL||North American Biofuels Group||Weirton, West Virginia||CTL||Undetermined||Delayed/Cancelled|
|Rentech Energy Midwest Facility||Rentech Energy Midwest Corporation (REMC)||East Dubuque, Illinois||CTL||1,250 BPD diesel||Delayed/Cancelled|
|Rentech/Peabody Joint Development Agreement (JDA)||Rentech/Peabody Coal||Kentucky||CTL||10,000 and 30,000 BPD||Delayed/Cancelled|
|Rentech/Peabody Minemouth||Rentech/Peabody Coal||Montana||CTL||10,000 and 30,000 BPD||Delayed/Cancelled|
|Secure Energy CTL (aka MidAmericaC2L||MidAmericaC2L / Siemens||McCracken County, Kentucky||CTL||10,200 BPD gasoline||Active (no new information since 2011)|
|Tyonek Coal-to-Liquids (formerly Alaska Accelergy CTL Project)||Accelergy, Tyonek Native Corporation (TNC)||Cook Inlet, Alaska||CBTL||Undefined amount of coal/biomass to 60,000 BPD jet fuel/gasoline/diesel and 200-400 MW electricity||Planning|
|US Fuel CTL||US Fuel Corporation||Perry County/Muhlenberg County, Kentucky||CTL||300 tons of coal into 525 BPD liquid fuels including diesel and jet fuel||Active|
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- The SRC-I pilot plant operated at Fort Lewis Wash in the 1970s but was not able to overcome lack of solvent balance problems (continual imports of solvent containing polynuclear aromatics were necessary). A SRC-I demonstration plant was scheduled to be built at Newman, KY but was cancelled in 1981. Based on 1913 work by Bergius it had been noted that certain minerals in coal ash had a mild catalytic activity, and this led to design work on a SRC-II demonstration plant to be built at Morgantown, WV. This too was cancelled in 1981. It appeared based on the work done so far to be desirable to separate the coal-dissolution and catalytic-hydrogenation functions to obtain a greater yield of synthetic crude oil; this was accomplished in a small+scale pilot plant at Wilsonville, AL during 1981-85. The plant also included a critical-solvent deasher to recover a maximum amount of usable liquid product. In a commercial plant, the deasher underflow containing unreacted carbonaceous matter would be gasified to provide hydrogen to drive the process. This program ended in 1985 and the plant was scrapped.Cleaner Coal Technology Programme (October 1999). "Technology Status Report 010: Coal Liquefaction" (PDF). Department of Trade and Industry. Archived from the original (PDF) on 2009-06-09. Retrieved 2010-10-23. Cite journal requires
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