US3852182A - Coal liquefaction - Google Patents

Coal liquefaction Download PDF

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Publication number
US3852182A
US3852182A US00304320A US30432072A US3852182A US 3852182 A US3852182 A US 3852182A US 00304320 A US00304320 A US 00304320A US 30432072 A US30432072 A US 30432072A US 3852182 A US3852182 A US 3852182A
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Prior art keywords
coal
liquid
promoter
distillation temperature
fraction
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US00304320A
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English (en)
Inventor
M Sze
G Snell
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Lummus Technology LLC
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Lummus Co
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Filing date
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Application filed by Lummus Co filed Critical Lummus Co
Priority to US00304320A priority Critical patent/US3852182A/en
Priority to ZA738418*A priority patent/ZA738418B/xx
Priority to BE137295A priority patent/BE806788A/xx
Priority to LU68728A priority patent/LU68728A1/xx
Priority to FR7339069A priority patent/FR2205565B1/fr
Priority to AU62149/73A priority patent/AU469568B2/en
Priority to IT70258/73A priority patent/IT999735B/it
Priority to GB5155373A priority patent/GB1452610A/en
Priority to JP48124891A priority patent/JPS521923B2/ja
Priority to CA185,196A priority patent/CA1005384A/en
Priority to SU731975277A priority patent/SU718016A3/ru
Priority to CS7300007642A priority patent/CS186779B2/cs
Priority to NLAANVRAGE7315261,A priority patent/NL172871C/xx
Priority to DE2355539A priority patent/DE2355539C3/de
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Publication of US3852182A publication Critical patent/US3852182A/en
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
    • C10G1/083—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts in the presence of a solvent
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/04—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by extraction
    • C10G1/045—Separation of insoluble materials
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/44—Hydrogenation of the aromatic hydrocarbons

Definitions

  • the 3,341,447 9/1967 B1111 et al. 208/8 promoter liquid is P P from a fraction having a 5 3,519,553 7/1970 Johanson etalum 208/10 volumepercent dlstlllation temperature of at least 3,583,900 6/I97l Gatsis 208/8
  • Coal can be converted to valuable products by subjecting coal to solvent extraction, with or without hydrogen, to produce a mixture of coal extract and undissolved coal residue, including undissolved extractable carbonaceous matter, fusain and mineral matter or ash.
  • the finely divided mineral matter or ash and unreacted coal must be separated from the coal extract, and in general, this separation step has been the principal draw-back to the successful operation of a coal extraction process.
  • the fine particle sizes encountered in coal solvation processes create numerous difficulties in attempting to use conventional separation techniques, such as filtration, centrifugation or settling. Attempts to use filtration techniques have not been particularly successful as a result of plugging of the filter pores with or without a precoat and the expense involved in providing the required filtration area.
  • Gravity settling techniques have also met with limited success as a result of low settling rates and. inefficient ash removal. Centrifugation techniques have also been generally unsuccessful as a result of high cost and the difficulty in separating the lighter finely divided materials.
  • An object of the present invention is to provide for improved coal liquefaction.
  • Another object of the present invention is to provide a new and improved process for separating finely divided insoluble material from a' coal liquefaction product.
  • a further object of the present invention is to provide aprocess for separating insoluble material from a coal liquefaction product which does not require a filtration step.
  • Still another object of the present invention is to provide an improved gravity settler for coal deashing.
  • the drawing is a simplified schematic flow diagram of a coal liquefaction process incorporating the teachings of the present invention.
  • the objects of the present invention are broadly accomplished, in one aspect, by use of a liquid which is indigenous to the coal liquefaction process, which promotes and enhances the separation of insoluble material from a coal liquefaction product.
  • the coal liquefaction product comprised of a liq-
  • the liquid which is employed to enhance and promote the separation of insoluble material from the coal liquefaction product is generally a hydrocarbon liquid having a characterization factor (K) of at least about 9.75 wherein:
  • T is the molal average boiling point of the liquid (R); and G is specific gravity of the liquid (60F./60F.).
  • the characterization factor is an index of the aromaticity/parafinicity of hydrocarbons, and petroleum fractions as disclosed by Watson & Nelson Ind. Eng. Chem. 25 880 (1933), with more parafinic materials having higher values for the characterization factor (K).
  • the promoter liquid which is employed is one which has a characterization. factor (K) in excess of 9.75 and which is also less aromatic than the liquefaction solvent; i.e., the characterization factor K of the promoter liquid has a value which is generally at least 0.25 unit higher than the characterization factor of the liquefaction solvent. 7
  • the liquid which is used to enhance and promote the separation of insoluble material is further characterized by a 5 volume percent distillation temperature of at least about 250F. and a volume percent distillation temperature of at least about 350F. and no greater than about 750F.
  • the promoter liquid preferably has a 5 volume percent distillation temperature of at least about 310F. and most preferably of at least about 400F.
  • the 95 volume percent distillation temperature is preferably no greater than about 600F.
  • the most preferred promoter liquid has'a 5 volume percent distillation temperature of at least about 425F. and a 95 volume percent distillation temperature of no greater than about 500F.
  • the 5 volume and 95 volume percent distillation temperature may be conveniently determined by ASTM Test No.
  • the amount of liquid promoter used for enhancing and promoting the separation of insoluble matter from the coal liquefaction product will vary with the particular liquid employed, the coal liquefaction solvent, the coal used as starting material and the manner in which the liquefaction is effecte'deAs should be apparent to those skilled in the art, the amount of liquid promoter used should be minimized in order to reduce the overall costs of the process. It has been found that by using the liquid of controlled aromaticity, in accordance with the teachings of the present invention, the desired separation of insoluble material may be effected with modest amounts of liquid promoter.
  • the weight ratio of liquid promoter to coal solution may range from about 0.221 to about 4.0: l with the particular amount which is employed being dependent upon the characterization factor (K) of the promoter liquid, with promoter liquids of the present invention having lower characterization factors generally requiring greater amounts of promoter liquid.
  • the hydrogenation of the fraction recovered from the coal extract to produce the promoter liquid is not effected to a degree in which the characterization factor (K )is above about 11.0; i.e., in general the characterization factor is from about 9.75 to about 1 1.0.
  • the liquid promoter is generally used in an amount from about 1:1 to about 4:1 and preferably 8S0about 1.5:1 to about, 3.0: l.
  • liquid promoter may be employed, but the use of such greater amounts is uneconomical.
  • the use of an excess of liquid promoter may result in a precipitation or separation of an excessive amount of desired coal derived products from the coal extract.
  • v as the amount of liquid promoter employed is increased a greater amount of ash containing under flow is separated from the coal solution, but such an increased separation is accompanied by an increased separation of desired coal derived products from the coal solution.
  • ash may be effec 'tively separated from the coal solution; e,g., in amounts greater than 99 percent, without an excessive loss of desired coal derived products.
  • coal such as bituminous coal
  • a moisture ash free basis may contain from about to about 10 percent of insoluble material, such as fusain, and accordingly, at a minimum, from about 5 to about 10 percent, of the MAF coal, is lost in the process.
  • the potential product loss is measured by the amount of 850F+ product which is not recovered from the coal in that it is this fraction, which includes insoluble coal material, such as fusain, which can not be recovered from the residual solid product of the coal deashing.
  • product loss of 850F+ components on a MAF coal feed basis, can be maintained at a value of no greater than about 40 percent, by weight, and preferably no greater than about percent, by weight.
  • the loss of 850F+ products, on a MAP coal basis is from about 10 to about 25 percent, by weight.
  • the net coal product (the extracted carbonaceous matter, excluding promoter liquid, liquefaction solvent and gas make), hereinafter sometimes referred to as coal product, contains less than about 1 percent insoluble material
  • insoluble material generally less than 0.1 percent insoluble material and most preferably less than 0.05 percent insoluble material, all by weight.
  • the specific amount of insoluble material which is permitted to be present in the coal product is dependent upon product standards, and the deashing is controlled in order to provide the required specifications.
  • the production of a coal product having less than 0.05 percent, by weight, insoluble material corresponds to 99+ percent ash removal, but as should be apparent to those skilled in the art, the percent ash removal to provide a coal product having the required minimum amount of insoluble material is dependent upon the initial ash content of the coal.
  • the liquid promoter is added to the coal solution in an amount, as hereinabove described, to provide a coal product in which insoluble material is present in an amount of less than about 1 percent, by weight, and most preferably of less than 0.05 percent, by weight, with the loss of 850F+ product being from about 10 to about 40 percent, by weight, preferably from about 10 to about 25 percent, by weight, on a MAP coal feed basis; i.e., from' about 60 to about percent, by weight, of the MAF coal feed is recovered as either gas make or liquid fuel product.
  • the promoter liquid which is used to promote the separation of insoluble material, as hereinabove described, is indigenous to the process and, accordingly, such promoter liquid is produced from the essentially solid free coal extract. More particularly, a fraction having a 5 volume percent distillation temperature and a volume percent distillation temperature which is required for the promoter liquid is recovered from the coal extract product as known in the art; e. g., by fractional distillation.
  • such a fraction is in excess of that required for producing the promoter liquid (product having 5 volume percentand 95 volume percent distillation temperatures identical to that of the promoter'li'quid is continuously produced from the liquefaction of coal) and, accordingly, only a portion of this fraction is used for producing the promoter liquid, with the remaining portion constituting a portion of the net liquefaction product.
  • the indigenous fraction which is to be ultimately employed as the promoter liquid must then be subjected to a controlled hydrogenation in order to produce a promoter liquid having a controlled aromaticity; i.e., a characterization factor K in excess of 9.75.
  • all or a portion of the fraction is hydrogenated, as known in the art, in order to produce a promoter liquid having the required characterization factor K.
  • such a hydrogenation is effected at a temperature from about 450F. to about 8850F.
  • a suitable hydrogenation catalyst such as nickel tungsten sulfide, nickel molybdate, nickel molybdenium sulfide and the like.
  • nickel tungsten sulfide, nickel molybdate, nickel molybdenium sulfide and the like nickel tungsten sulfide, nickel molybdate, nickel molybdenium sulfide and the like.
  • the promoter liquid produced by hydrogenation of all or a portion of the fraction of the coal liquefaction product recovered for production of the promoter liquicl may then be employed to promote and enhance the separation of solid material from the coal liquefaction product.
  • the indigenous promoter liquid of controlled aromaticity may be employed in combination with a promoter liquid from an external source, such as a kerosene fraction, provided that the resulting blend has a characterization factor as hereinabove described.
  • the separation of the insoluble material from the coal extract is generally effected at a temperature from about 300F. to about 600F., preferably from about 350F. to about 500F., and at a pressure from about 0 psig to about 500 psig, preferably at a pressure from about 0 psig to about 300 psig. It is to be understood that higher pressures could be employed, but as should be apparent to those skilled in the art, lower pressures are preferred.
  • the insoluble material is preferably separated by gravity settling with the essentially insoluble material free coal extract being recovered as'an overflow and the insoluble material as underflow. In such gravity settling, the amount of underflow should be minimized in order to minimize the loss of heavier products in the underflow.
  • the underflow withdrawal rate to obtain desired results is deemed to be within the scope of those skilled in the art. In general, such a rate is from about 20 to about 25 wt. percent of the total feed (liquefaction product and promoter liquid).
  • the residence time for such settling is generally in the order of from about 0.5 to about 6 hours, and preferably from about 0.5 to 3.0 hours.
  • ground or pulverized coal generally bituminous, sub-bituminous or lignite, preferably bituminous coal
  • in line 10 is introduced into a coal solvation and slurrying zone 11 along with a coal liquefaction solvent in line 12.
  • the coal liquefaction solvent may be any one of the wide variety of coal liquefaction solvents used in the art, including both hydrogen donor solvents, non hydrogen donor solvents and mixtures thereof. These solvents are well known in the art and, accordingly, no detailed description thereof is deemed necessary for a full understanding of the invention.
  • the coal liquefaction solvent is a 600F.900F.
  • solvent which is recovered from the coal liquefaction product and which has not been subjected to hydrogenation subsequent to the recovery thereof.
  • the solvent is added to the coal in an amount sufficient to effect the desired liquefaction, and in general, is added in an amount to provide a solvent to coal weight ration from about 1:1 to about :1, and preferably from about l.5:l to about 5:1.
  • a coal paste is withdrawn from zone 11 through line 13 and introduced into a coal liquefaction zone 14 wherein, as known in the art, the coal is converted to liquid products.
  • the liquefaction zone 14 is operated as known in the art and may be catalytic or non-catalytic and may be effected in the presence or absence of added hydrogen.
  • the hydrogenation may be effected in a fixed catalyst bed, fluidized catalyst bed or in an expanded or ebullating bed.
  • the details of the coal liquefaction step form no part of the present invention and, accordingly, no details thereof are required for a full understanding of the invention.
  • the coal liquefaction is effected in the presence of added hydrogen.
  • the hydrogenation increases the recovery of coal products and also reduces the sulfur and nitrogen content of the recovered liquid coal product.
  • the liquefaction is preferably effected in an upflow ebullated bed, as known in, the art; e.g., as described in U.S. Pat. No. 2,987,465 to Johanson.
  • the coal liquefaction zone includes means for recovering the various gaseous products.
  • a coal liquefaction product comprised of a liquid coal extract of dissolved carbonaceous matter in the coal liquefaction solvent and insoluble material (ash and undissolved coal) is withdrawn from the liquefaction zone 14 through line 15 and mixed with promoter liquid in line 21 of controlled aromaticity, i.e., the characterization factor of the promoter liquid has avalue which is generally at least 0.25 unit greater than the characterization factor of the coal liquefaction solvent.
  • the promoter liquid is a fraction which has 5 volume percent and volume percent distillation temperatures which fall within the range from about 425-500F.
  • the combined stream of coal liquefaction product and promoter liquid in line 22 is introduced into a gravity separation zone 23, comprised of a gravity settler which may be any one of those known in the art, wherein an essentially solids free overflow is separated from a solid containing underflow.
  • a gravity settler may be any one of those generally known in the art, the settler is preferably of a special type developed for the present invention as described in copending application Ser. No. 304,319 filed concurrently herewith.
  • the overflow is withdrawn from separation zone 23 through line 24 and introduced into a recovery zone 25 for recovering various fractions of the coal extract.
  • the recovery zone 25 may be comprised of one or more fractionators to distill various fractions from the product. As particularly described, the recovery zone is operated to recover a first fraction boiling up to about 425F.; a second fraction having 5 and 95 percent volume distillation temperatures of from about 425 to about 500F.; a third fraction (500600F.) which may be employed as a distillation fuel blendstock; a fourth fraction (600-900F.) a portion of which may be used as the coal liquefaction solvent in line 12 and a further portion of which may be recovered as product, and a residual product (+900F.) of low ash and reduced sulfur content which may be used as fuel or subjected to further treatment.
  • the present invention is not limited to the above representative separation in that the different fractions may be recovered as products or as the fraction to be used as a promoter liquid.
  • the promoter liquid is preferably derived from a fraction having a 5 volume distillation temperature of no lower than about 425F. and a 95 volume percent distillation temperature of no greater than about 500F.
  • the portion of the fraction (425-500F.) required to meet the promoter liquid requirements for the process is passed through line 26 and at least a portion thereof is introduced into a hydrogenation zone 27, with the .7 remaining portion, if any, being bypassed through line 28.
  • the hydrogenation zone 27, as hereinabove described, is operated to provide a promoter liquid with the required characterization factor; i.e., a blend of the hydrogenated portion and the by-passed protion has the required characterization factor.
  • a hydrogenated product is withdrawn from hydrogenation zone 27 through line29, combined with any liquid in line 28 and the combined stream in line 21 employed as the I promoter liquid. Start-up liquid or make-up blending liquid may be added through line 31.
  • the underflow containing dispersed insoluble material withdrawn from separation zone 23 through line 41 is introduced into a stripping zone 42 wherein material boiling below about 900F. is stripped therefrom and introduced into the recovery zone 25 through line 43.
  • the ash rich stripper bottoms in line 44 may then be subjected to calcination or coking. Alternatively, part of the stripper bottoms may be used as feedstock to a partial oxidation process for producing hydrogen. As a' further alternative a portion of the stripper bottoms may be used for plant fuel. These uses and other should be apparent to those skilled in the art from the teachings herein.
  • the stripper bottoms in line 44 contains from about 10 to about 40 percent, by weight, of the MAP coal.
  • EXAMPLE An aromatic distillate fraction is obtained from a coal liquefaction product. It exhibits a characterization factor of 8.8 and volume percent and 95 volume percent distillation temperature range of 425-500F. It is pumped through .a preheater admixed with preheated hydrogen and fed to a fixed bed catalytic reactor packed with a commercial'sulfided nickel-tungsten catalyst. The hydrogen stream purity is 75% H The following reaction parameters are used: LHSV 1.0hr, an operating pressure of 1,400 psig, and an inlet temperature of 650F. Hydrogen is fed to the reactor at a rate equivalent to 400 SC F of hydrogen per gallon of liquid feedstock. e
  • Reactor effluent is quickly cooled to 200 F, and routed to a high pressure gas/liquid separator which vents gas continuously under automatic pressure control. At the conclusion of the run the high Pressure is vented down to atmospheric pressure and a liquid product with a characterization factor of 9.9 is withdrawn.
  • This hydrogenated liquid is then used to remove ash from a coal liquefaction product comprised of insoluble material and carbonaceous matter dissolved in a coal liquefaction solvent (600-900F coal tar distillate).
  • a coal liquefaction solvent 600-900F coal tar distillate
  • l,200 grams of this promoter solution and 300 grams of coal liquefaction product are added to a 2 liter rocking bomb made of stainless steel and electrically heated. The contents in the bomb is heated with rocking to 500F over about 30 minuteperiod. Bomb contents are then allowed to settle vertically for about 4 hours at 500F without any rocking. At the end of the settling period, 250 grams of an ash-rich underflow stream are withdrawn through the bottom valve.
  • said liquid promoter having a 5 volume percent distillation temperature of at least about 250F., and a volume percent distillation temperature of at least about 350F. and no greater than about 750F., said liquid promoter having a characterization factor (K) of at least 9.75, said liquid promoter having a characterization factor greater than said coal liquefaction solvent and being added in an amount sufficient to produce a coal extract essentially free of insoluble material;
  • step (d) employing liquid promoter from step (d) in step 2.
  • fraction and promoter liquid have a 5 volume percent distillation temperature of no less than about 425F and a 95 volume percent distillation temperature of no greater than about 500F.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
US00304320A 1972-11-07 1972-11-07 Coal liquefaction Expired - Lifetime US3852182A (en)

Priority Applications (14)

Application Number Priority Date Filing Date Title
US00304320A US3852182A (en) 1972-11-07 1972-11-07 Coal liquefaction
ZA738418*A ZA738418B (en) 1972-11-07 1973-10-30 Process for solvent deashing of hydrofined coal solution
BE137295A BE806788A (fr) 1972-11-07 1973-10-31 Procede d'elimination des cendres d'un produit de liquefaction du charbon
LU68728A LU68728A1 (cs) 1972-11-07 1973-10-31
AU62149/73A AU469568B2 (en) 1972-11-07 1973-11-02 Process for solvent deashing of hydrofined coal solution
FR7339069A FR2205565B1 (cs) 1972-11-07 1973-11-02
IT70258/73A IT999735B (it) 1972-11-07 1973-11-06 Procedimento per la rimozione del le ceneri dal solvente di soluzioni di carbone idrosuddiviso
GB5155373A GB1452610A (en) 1972-11-07 1973-11-06 Process for solvent deashing of hydrofined coal solution
JP48124891A JPS521923B2 (cs) 1972-11-07 1973-11-06
CA185,196A CA1005384A (en) 1972-11-07 1973-11-06 Process for solvent deashing of hydrofined coal solution
SU731975277A SU718016A3 (ru) 1972-11-07 1973-11-06 Способ обеззоливани продуктов гидрогенизации угл
CS7300007642A CS186779B2 (en) 1972-11-07 1973-11-07 Method for the separation of insoluble parts from coal solutions in liquefying agent
NLAANVRAGE7315261,A NL172871C (nl) 1972-11-07 1973-11-07 Werkwijze voor het afscheiden van onoplosbaar materiaal uit een bij het vloeibaar maken van kool verkregen produkt.
DE2355539A DE2355539C3 (de) 1972-11-07 1973-11-07 Abtrennung von unlöslichem Material aus einem Kohleverflüssigungsprodukt

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US00304320A US3852182A (en) 1972-11-07 1972-11-07 Coal liquefaction

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US3852182A true US3852182A (en) 1974-12-03

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US00304320A Expired - Lifetime US3852182A (en) 1972-11-07 1972-11-07 Coal liquefaction

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US (1) US3852182A (cs)
JP (1) JPS521923B2 (cs)
AU (1) AU469568B2 (cs)
BE (1) BE806788A (cs)
CA (1) CA1005384A (cs)
CS (1) CS186779B2 (cs)
DE (1) DE2355539C3 (cs)
FR (1) FR2205565B1 (cs)
GB (1) GB1452610A (cs)
IT (1) IT999735B (cs)
LU (1) LU68728A1 (cs)
NL (1) NL172871C (cs)
SU (1) SU718016A3 (cs)
ZA (1) ZA738418B (cs)

Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3947346A (en) * 1974-09-20 1976-03-30 The Lummus Company Coal liquefaction
US3954595A (en) * 1974-03-18 1976-05-04 The Lummus Company Coal liquefaction
US3997425A (en) * 1974-12-26 1976-12-14 Universal Oil Products Company Process for the liquefaction of coal
US4075080A (en) * 1976-02-18 1978-02-21 Continental Oil Company Coal liquefaction process with removal of agglomerated insolubles
US4172024A (en) * 1978-06-15 1979-10-23 The Lummus Company Catalyst withdrawal and addition in a coal liquefaction process
US4189372A (en) * 1978-05-22 1980-02-19 Kerr-Mcgee Corporation Process for the hydroconversion of coal
US4255248A (en) * 1979-09-07 1981-03-10 Chevron Research Company Two-stage coal liquefaction process with process-derived solvent having a low heptane-insolubiles content
US4264430A (en) * 1979-10-22 1981-04-28 Chevron Research Company Three-stage coal liquefaction process
US4264429A (en) * 1979-10-18 1981-04-28 Chevron Research Company Two-stage coal liquefaction process with process-derived solvent
US4331531A (en) * 1979-10-22 1982-05-25 Chevron Research Company Three-stage coal liquefaction process
US4347116A (en) * 1977-06-08 1982-08-31 Mobil Oil Corporation Two-stage coal liquefaction
US4350582A (en) * 1979-10-18 1982-09-21 Chevron Research Company Two-stage coal liquefaction process with process-derived solvent
US4358359A (en) * 1979-09-07 1982-11-09 Chevron Research Company Two-stage coal liquefaction process with process-derived solvent having a low heptane-insolubles content
WO1982004060A1 (en) * 1981-05-13 1982-11-25 Zandona Oliver J Progressive flow cracking of coal/oil mixtures with high metals content catalyst
US4374725A (en) * 1977-06-08 1983-02-22 Electric Power Research Institute Process for coal liquefaction
US4402821A (en) * 1981-11-13 1983-09-06 Mobil Oil Corporation Process for liquefaction of coal
US4410414A (en) * 1980-01-18 1983-10-18 Hybrid Energy Systems, Inc. Method for hydroconversion of solid carbonaceous materials
EP0087965A3 (en) * 1982-02-27 1984-01-11 Sandwell & Company Limited Process for separation of solids from liquid hydrocarbons
US4510037A (en) * 1983-12-23 1985-04-09 Hri, Inc. Hydrogenation process for solid carbonaceous feed materials using thermal countercurrent flow reaction zone
US4610777A (en) * 1984-08-15 1986-09-09 Mobil Oil Corporation Coal liquefaction with Mn nodules

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1543456A (en) * 1976-06-01 1979-04-04 Kerr Mc Gee Chem Corp Coal deashing process
GB2071132A (en) 1979-10-19 1981-09-16 Coal Industry Patents Ltd Fuel oils from coal

Citations (12)

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US3954595A (en) * 1974-03-18 1976-05-04 The Lummus Company Coal liquefaction
US3947346A (en) * 1974-09-20 1976-03-30 The Lummus Company Coal liquefaction
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US4075080A (en) * 1976-02-18 1978-02-21 Continental Oil Company Coal liquefaction process with removal of agglomerated insolubles
US4347116A (en) * 1977-06-08 1982-08-31 Mobil Oil Corporation Two-stage coal liquefaction
US4374725A (en) * 1977-06-08 1983-02-22 Electric Power Research Institute Process for coal liquefaction
US4189372A (en) * 1978-05-22 1980-02-19 Kerr-Mcgee Corporation Process for the hydroconversion of coal
US4172024A (en) * 1978-06-15 1979-10-23 The Lummus Company Catalyst withdrawal and addition in a coal liquefaction process
US4255248A (en) * 1979-09-07 1981-03-10 Chevron Research Company Two-stage coal liquefaction process with process-derived solvent having a low heptane-insolubiles content
US4358359A (en) * 1979-09-07 1982-11-09 Chevron Research Company Two-stage coal liquefaction process with process-derived solvent having a low heptane-insolubles content
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NL172871B (nl) 1983-06-01
DE2355539C3 (de) 1987-06-19
FR2205565A1 (cs) 1974-05-31
DE2355539B2 (de) 1980-07-10
AU469568B2 (en) 1976-02-19
BE806788A (fr) 1974-02-15
CA1005384A (en) 1977-02-15
AU6214973A (en) 1975-05-08
JPS521923B2 (cs) 1977-01-19
ZA738418B (en) 1974-09-25
FR2205565B1 (cs) 1978-08-11
NL7315261A (cs) 1974-05-09
GB1452610A (en) 1976-10-13
LU68728A1 (cs) 1974-01-08
CS186779B2 (en) 1978-12-29
SU718016A3 (ru) 1980-02-25
JPS4998402A (cs) 1974-09-18
IT999735B (it) 1976-03-10
NL172871C (nl) 1983-11-01
DE2355539A1 (de) 1974-05-16

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