Coal liquefaction and catalysis

Derbyshire, F.J.; Hager, Todd

doi:10.1016/0016-2361(94)90242-9

Cited by 45 publications

(38 citation statements)

References 14 publications

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“…DCL grew out of work conducted in Germany prior to World War II. In the original Bergius-IG hydroliquefaction process, which used nonrecycled iron oxide or molybdenum catalysts (Derbyshire and Hager, 1994), conditions were quite severe. Pressures were up to around 10,000 psig (700 atm), residence times were close to 90 minutes, and H 2 consumption was roughly double that of comparable processes developed since the 1970s (McMillen et al, 1987).…”

Section: Processingmentioning

confidence: 99%

“…In either the H-Coal or the CTSL process, neither the capital cost nor the cost of catalyst seems to have been greatly reduced compared to processes using disposable iron-based catalyst, as evidenced by the fact that Shenhua has chosen to go back to iron-based catalysts. This is because iron-based catalysts are so much cheaper than molybdenum-based catalysts such as CoMo or NiMo that they can be justifiably disposed of after a single pass (Derbyshire and Hager, 1994).…”

Section: Reducing Capital Costs With Improved Catalystsmentioning

confidence: 99%

“…One option for increasing catalyst activity and reducing costs would be to use catalysts in which metals are dispersed as either water-or oil-soluble liquids (Derbyshire and Hager, 1994;Ruether et al, 1987;Zhan and Givens, 1999;Demirel and Givens, 2000a), allowing the metals to deposit and interact directly on coal surfaces. Dispersed catalysts are reported to give higher liquid yields and require lower catalyst loadings than do supported catalysts Givens, 1998, 2000a, b;Ni et al, 1994).…”

Section: Reducing Capital Costs With Improved Catalystsmentioning

confidence: 99%

“…This was the approach used in the Dow coal liquefaction process, which used a fine micron-scale powdered molybdenum catalyst (Probstein and Hicks, 1982;Derbyshire and Hager, 1994;Moll et al, 1981). Solid products (ash, coke, and unreacted coal) were separated from the liquid products using hydrocyclones.…”

Section: Reducing Capital Costs With Improved Catalystsmentioning

confidence: 99%

“…Indeed, when the EDS process was tested using subbituminous coals and lignites, yields were consistently low (Probstein and Hicks, 1982). Results such as these led many researchers to the general conclusion that low-rank coals react more slowly than higher-rank coals and give lower yields (Derbyshire and Hager, 1994). It is also generally assumed that oxygen is detrimental to liquefaction (Burke et al, 2001), because reducing oxygen to water will require higher hydrogen consumption (Probstein and Hicks, 1982).…”

Section: Optimizing Processes and Catalysts For Lignitementioning

confidence: 99%

See 4 more Smart Citations

Subtask 3.3 - Feasibility of Direct Coal Liquefaction in the Modern Economic Climate

Oster¹,

Strege²,

Kurz³

et al. 2009

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Section: Processingmentioning

confidence: 99%

Section: Reducing Capital Costs With Improved Catalystsmentioning

confidence: 99%

Section: Reducing Capital Costs With Improved Catalystsmentioning

confidence: 99%

Section: Reducing Capital Costs With Improved Catalystsmentioning

confidence: 99%

Section: Optimizing Processes and Catalysts For Lignitementioning

confidence: 99%

See 3 more Smart Citations

Subtask 3.3 - Feasibility of Direct Coal Liquefaction in the Modern Economic Climate

Oster¹,

Strege²,

Kurz³

et al. 2009

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Coal Liquefaction

Kaneko¹,

Derbyshire²,

Makino³

et al. 2001

Ullmann's Encyclopedia of Industrial Chemistry

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Coal Liquefaction

Kaneko

Derbyshire

Makino³

et al. 2012

Ullmann's Encyclopedia of Industrial Chemistry

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The article contains sections titled: 1. Introduction 1.1. Commercial Development 1.2. Historical Background 2. Indirect Coal Liquefaction 2.1. Preparation of Synthesis Gas 2.1.1. Coal Gasification 2.1.2. Water–Gas Shift 2.1.3. Synthesis Gas Purification 2.2. Fischer–Tropsch Synthesis 2.2.1. Mechanisms 2.2.2. Product Selectivity and Characteristics 2.2.3. Catalytic Selectivity 2.2.4. Refining of Crude Products 2.2.5. Integrated Plant Configurations 2.2.6. Commercial Practice at SASOL 2.2.7. New and Developing Technologies 2.2.8. Advanced Systems 2.3. Methanol and Methanol to Gasoline (MTG) 2.4. Dimethyl Ether (DME) 2.5. Environmental Protection 2.6. Economic Aspects 3. Direct Coal Liquefaction 3.1. Mechanisms 3.2. Liquefaction Products 3.3. Solvents 3.3.1. Hydrogen Donors 3.3.2. Coal Conversion and Hydrogen Transfer 3.3.3. Interactive Solvent Effects 3.3.4. Side Reactions of Solvents 3.4. Coal Composition 3.4.1. Coal Rank 3.4.2. Bituminous Coal 3.4.3. Low‐Rank Coal 3.4.4. Coal Drying and Oxidation 3.5. Gaseous Hydrogen 3.6. Liquefaction in COH 2 O and COH 2 H 2 O 3.7. Catalysis 3.7.1. Mechanisms 3.7.2. Disposable Catalysts 3.7.3. Supported Catalysts 3.7.4. Molten Halide Catalysts 3.8. Process Description 3.9. Commercial Processes 3.9.1. Kohleoel (Ruhrkohle‐Veba Oel) Process 3.9.2. NEDOL Process 3.9.3. Solvent‐Refined Coal (SRC‐I and SRC‐II) Processes 3.9.4. Exxon Donor Solvent Process 3.9.5. H‐Coal Process 3.9.6. Catalytic Two‐Stage Process 3.9.7. HTI Coal Process 3.9.8. BCL Process 3.9.9. Liquefaction Solvent Extraction Process 3.10. Environmental Considerations 3.11. Economic Aspects

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Coal liquefaction and catalysis

Cited by 45 publications

References 14 publications

Subtask 3.3 - Feasibility of Direct Coal Liquefaction in the Modern Economic Climate

Subtask 3.3 - Feasibility of Direct Coal Liquefaction in the Modern Economic Climate

Coal Liquefaction

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