US3341447A - Solvation process for carbonaceous fuels - Google Patents

Solvation process for carbonaceous fuels Download PDF

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US3341447A
US3341447A US426340A US42634065A US3341447A US 3341447 A US3341447 A US 3341447A US 426340 A US426340 A US 426340A US 42634065 A US42634065 A US 42634065A US 3341447 A US3341447 A US 3341447A
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solvent
slurry
coal
zone
hydrogen
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US426340A
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Willard C Bull
Lawrence G Stevenson
Dean L Kloepper
Thomas F Rogers
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Priority to US426340A priority Critical patent/US3341447A/en
Priority to GB38638/65A priority patent/GB1090556A/en
Priority to SE12021/65A priority patent/SE301988B/xx
Priority to BE669732D priority patent/BE669732A/xx
Priority to FR31746A priority patent/FR1457571A/fr
Priority to NL6512147A priority patent/NL6512147A/xx
Priority to NO159737A priority patent/NO116629B/no
Priority to ES0320700A priority patent/ES320700A1/es
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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
    • C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
    • C10G1/065—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation in the presence of a solvent
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/02—Treating solid fuels to improve their combustion by chemical means
    • C10L9/04—Treating solid fuels to improve their combustion by chemical means by hydrogenating

Definitions

  • This invention relates to the solubilizing of carbonaceous fuels, and more particularly to the upgrading of carbonaceous fuels by a solution-process into low-ash low-oxygen, low-sulfur fuels.
  • the present invention has for one of its objects to provide a novel process for essentially complete solubilization of carbonaceous fuels in solvent.
  • Another object of this invention is to provide a novel and economical process for preparing low-ash, lowoxygen, low-sulfur fuels from naturally occurring carbonaceous fuels.
  • a further object of this invention is to provide a novel, economical and improved process for the solubilization of naturally occurring carbonaceous fuels for the upgrading thereof into solid low-ash, low-oxygen, low-sulfur fuels which are commercially competitive with other fuels.
  • a still further object of this invention is to provide a novel and improved process for the production of solid low-ash, low-oxygen, low-sulfur fuels from carbonaceous fuels, which process is cyclic and does not require any substantial addition of solvent after start-up.
  • a still further object of this invention is to provide a novel process for the upgrading of naturally occurring carbonaceous fuels into novel low-ash, low-oxygen, lowsulfur fuels.
  • a still further object of this invention is to prepare commercially competitive solid low-ash, low-oxygen, lowsulfur fuels from naturally occurring carbonaceous fuels.
  • the above objects and advantages are accomplished by dissolving substantially all of the potentially available fuel fractions of naturally occurring carbonaceous fuels, such as coal, lignite, peat, and the like, using a solvent derived from the original fuel feed stock under critically controlled conditions of temperature, pressure and atmosphere together with a very critical holding period in processing temperature, at which the normally insoluble portions of the fuel are decomposed, generally, by depolymerization of the feed fuel, to fractions soluble in the solvent.
  • naturally occurring carbonaceous fuels such as coal, lignite, peat, and the like
  • the drawing illustrates a continuous embodiment of this invention in which a raw feed fuel, such as Kentucky No. 11 coal which has been ground by a suitable means, such as a hammer mill (preferably the coal is finely ground to approximately percent through 200 mesh (US. Standard), is fed by means of a conveyor or the like to an agitated tank 1 where it is mixed with solvent (obtained from previous processing) at a ratio of about 1/1 to 4/1 solvent to coal.
  • a raw feed fuel such as Kentucky No. 11 coal which has been ground by a suitable means, such as a hammer mill (preferably the coal is finely ground to approximately percent through 200 mesh (US. Standard)
  • solvent obtained from previous processing
  • the coalsolvent slurry in tank 1 may be heated to any suitable temperature which will flash off any moisture which may be present in the coal.
  • the solvent used in this invention is derived from the coal being dissolved, its composition may vary, depending on the analysis of the coal being used as feedstock.
  • the solvent employed in this invention is a highly aromatic solvent obtained from previous processing of fuel, and will generally have a boiling range of about C. to 750 C., a density of about 1.1 and a carbon to hydrogen mole ratio in the range from about 1.0 to 0.9 to about 1.0 to 0.3.
  • any good organic solvent for coal may be used as the initial start-up solvent in the process.
  • a typical solvent is, for example, middle oil obtained from coal and having a boiling range of to 300 C.
  • a solvent found particularly useful as a start-up solvent is anthracene oil or creosote oil having a boiling range of about 220 C.- 400 C.
  • the selection of a specific start-up solvent is not particularly critical since during the process dissolved fractions of the raw feed fuel .form substantial quantities of additional solvent which when added to the solvent originally fed into the system provide a total amount of solvent which is greater than the original amount put in the process. Thus, regardless of what the original solvent may have been, it will lose its identity and approach the constitution of the solvent formed by solution and depolymerization of the raw fuel fed into the process.
  • the composition of the solvent approaches that of the same general composition as the de-ashed product of the processed feed fuel but of lower molecular weight, with the actual composition in each case determined by the composition of the particular raw feed fuel employed.
  • the solvent, which is employed may be broadly defined as that obtained from a previous extraction of raw carbonaceous fuels, in accordance with this invention.
  • ratio of solvent to coal in the slurry mixed in slurry tank 1 will be in the range of 0.6/1 to 4/ l with a preferred range of 1/ 1 to 2.3/1.
  • Ratios of solvent to coal of less than 0.6/1 i.e. 0.5/1) produce slurries which are of the consistencies of tar upon dissolution of the coal in the solvent, thus rendering them difficult to move in the system and which frequently cause clogging of the system.
  • Ratios of solvent to coal greater than 4/1 may be used but provide no functional advantage in the solution process of this invention and sufferthe additional disadvantage of requiring additional energy or work for the subsequent separation of solvent from the deashed coal product for recycling in the system.
  • the slurry formed in tank 1 is then fed by means of any suitable method, for example a positive displacement pump 2, to a preheater 3 and then into a dissolver 4 which is suitably heated to maintain the slurry at its elevated temperature.
  • a positive displacement pump 2 to a preheater 3 and then into a dissolver 4 which is suitably heated to maintain the slurry at its elevated temperature.
  • hydrogen be added to the slurry ahead of the preheater 3 or dissolver 4 at a partial pressure of at least 500 p.s.i.
  • the hydrogen employed is normally that recycled from previous processing together with any fresh make-up hydrogen required to provide the necessary hydrogen content.
  • the pressures employed will normally be in the range of 500 to 1500 p.s.i., with 1000 p.s.i. preferably employed.
  • the hydrogen pressurized fuel-solvent slurry is heated in the preheaters to rapidly raise the temperature thereof to about 370 C. to about 500 C., and preferably about 375 C. to about 440 C.
  • the tubes are sized, as to diameter and length, so as to enable the flow of slurry therethrough to be heated to operating temperatures as rapidly as is practical,
  • the preheater will be designed to provide the desired rate of heating to the slurry at a heat flux of not greater than abOut 10,000 B.t.u./hour/sq. ft. of tube surface area.
  • the diameter of the tubes will be sized so as to maintain the slurry in turbulent flow through the preheater.
  • the length of time in which the solution of the hydrogen pressurized slurry is continued in dissolver 4 is critical to the success of this process.
  • the duration of treatment solution
  • the mechanics of the solution provide an accurate guide for the residence time of the slurry in dissolver 4.
  • the viscosity of the solution obtained during processing of the slurry increases with time in dissolver 4, followed by a decrease in viscosity as this solubilizing of the slurry is continued and then followed by a subsequent increase in the viscosity of the solution on extended holding in the dissolver 4.
  • One of the criterions used for determining the completion of the solution process is the relative viscosity of the solution formed which is the ratio of the viscosity of the solution to the viscosity of the solvent, as fed, to the process, both viscosities being measured at 210 F. Accordingly, the term Relative Viscosity as used herein and in the claims is restricted to and defined as the viscosity at 210 F. of the solution formed divided by the viscosity of the solvent at 210 F. fed to the system, i.e.,
  • the solubilization be allowed to proceed until the decrease in Relative Viscosity (following the initial rise in Relative Viscosity) falls to a value of at least 10 and the resultant solution separated from undissolved residue of the coal before the Relative Viscosity again rises above 10.
  • the decrease in Relative Viscosity will be allowed to proceed to a value less than 5 and preferably in the range of 1 /2 to 2.
  • the feed fuel depolymerizes in the presence of hydrogen to form fractions which are soluble in the solvent, and it was observed that the depolymerization of the coal during extraction is accompanied by the evolution of hydrogen sulfide, water, carbon dioxide, methane, propane, butane, and other higher hydrocarbons which will comprise part of the atmosphere in the dissolver 4.
  • the depolymerization, of the feed fuel consumes hydrogen up to a Weight equivalent to about 2.0 percent of the weight of the feed fuel (as received), and under preferred conditions, in an amount of about 0.5 to 1 percent of the feed fuel.
  • the resultant solution is then charged to a filter 5 for separation of the coal solution from undis'solved residue (i.e. mineral matter) of the feed fuel.
  • the filter 5, as shown in the drawing, is a conventional rotary drum pressure'filter suitably adapted for pressure let down and venting of gases. It is to be understood that although a rotary drum filter has been described as being utilized in conjunction with this embodiment, other means of separation may be employed as for example centrifuges and the like.
  • gases vented from filter are then passed through a line into a gas treating unit 6 in which hydrogen sulfide and carbon dioxide are scrubbed out in any suitable manner, as for example by caustic solutions.
  • the remaining gas may be given any further treatment desired.
  • the hydrogen sulfide and carbon dioxide free gas recovered is then recycled to the process by feeding to fresh slurry being fed to preheater 3, with all make-up hydrogen being supplied by fresh hydrogen.
  • Analysis of the recovered gases has shown that the over-all consumption of hydrogen throughout the system is quite low with the actual consumption of hydrogen being not greater than 2 percent (based on the feed fuel) and quite often as loW as 0.5 percent.
  • the filter cake or residue obtained in filter 5 is withdrawn therefrom for additional processing as desired, as for example solvent recovery, which will be discussed below.
  • further processing of the filter cake is desired since, in addition to mineral water, it may contain from between 40 to 50 percent, by weight, of solvent that can be recovered by pyrolytic distillation. Often this dried filter cake contains about 50 percent carbon and runs about 7,000 Btu. per pound.
  • the further processing of the cake is particularly significant since the coal mineral matter and included solvent may comprise about 10 to percent of the total weight of the slurry fed to the system.
  • the amount of recoverable solvent comprises between about 5 to 15 percent of the original solvent fed into the system.
  • the recovered solvent may be recycled into the system for the preparation of additional slurry for feeding into the system.
  • the filtrate from filter 5 is then pumped at a temperature of about 270 to 430 C. through suitable nozzles into a simple vacuum flash evaporator 7 for removal of the majority of the solvent.
  • the evaporator will be equipped with a demister to remove any entrained liquid in the vapor, and, also, suitable heaters will be located on the outside of the evaporator to make up for heat losses.
  • the flashed solvent from the evaporator 7 may be passed to a still 8 or recycled directly to the system.
  • the amount of solvent recovered for recycling to the system will generally comprise a quantity of about 85 to 100 percent of the amount of the solvent originally introduced into the system.
  • This recycled solvent may all come from the evaporator or may be a mixture of solvent from the evaporator and solvent recovered from the filter cake processing. It is to be understood that solvent recovery may be accomplished by a variety of methods, such as wiped film evaporators, and thus such other means may also be employed if desired for recovery of solvent.
  • the remaining product from evaporator 7, which is liquid at this point may be used as such, or it may be pumped onto a continuous rotating steel belt 15 where it is cooled and solidified.
  • This product, which solidifies upon cooling, is very brittle and breaks into flakes as it finally falls from the belt.
  • Other methods may also be used to recover the product as for example spray cooling or prilling, or, again, if desired the product may be retained in the liquid state and used as such.
  • This resultant brittle product recovered from evaporator 7 is a hydrocarbon material which has little resemblance to the feed fuel charged into the system. As with the filter cake, a substantial amount of recoverable solvent remains in the product ranging from about 15 to about percent. The nature of this product is believed readily evident from the following properties thereof Density. gms./cc..
  • the melting point of this product is influenced very strongly by the amount of volatile matter that is left in the product. For example, if a product having about 39 percent volatile matter and a softening point of 180 C. had been treated so as to leave therein approximately 50 percent volatile matter, its melting point would be down near 130 C.
  • the viscosity temperature curves of this product are very steep and allow fluidization and atomization into conventional firing systems using other fuels such as residual oils. It was found that upon heating the products of this invention to between 240 and 350 C. they become sufficiently fluid for various applications at these temperatures, i.e. fuels. The economics of the invention render the products of this invention competitive with residual oil and other fuels for many uses such as for gas turbine use, in applications such as in railroads, and the like.
  • Heating said slurry in said heating zone to a temperature in the range of about 370 C. to about 500 C.;
  • step (e) Holding the charge of step (d) in said solubilizing zone;
  • Said solvent is a solvent obtained from a previous solution of coal in accordance with said process
  • the said recovered solvent comprises at least 90% of the amount of solvent fed into said process.
  • a process for preparing a substantially ash-free and low-sulfur fuel from coal which comprises the steps of:
  • a process for preparing a solid substantially ashfree, low-sulfur fuel from coal comprising the steps of:
  • step (g) Cooling the remaining filtrate of step (f) to recover the said solid fuel thereby.
  • a continuous process for preparing substantially ash-free, low-sulphur fuel which comprises the steps:
  • Step (b) Continuously heating the slurry from Step (a) in a dissolving zone in which the slurry is heated to a temperature in the range of 370 C. to about 500 C.;
  • step (g) Recycling a portion of said hydrogen sulfide and carbon dioxide free gas to step (c);
  • step (h) Continuously filtering the liquid stream from step (d) to remove mineral matter and any undissolved coal;
  • step (i) Continuously removing solvent fractions having boiling points falling in the range of C. to about 750 C. from the filtrate of step (h) and recycling said solvent fractions to step (a),
  • step (d) has a relative viscosity of 1 /2 to 10.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Combustion & Propulsion (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Paper (AREA)
US426340A 1965-01-18 1965-01-18 Solvation process for carbonaceous fuels Expired - Lifetime US3341447A (en)

Priority Applications (8)

Application Number Priority Date Filing Date Title
US426340A US3341447A (en) 1965-01-18 1965-01-18 Solvation process for carbonaceous fuels
GB38638/65A GB1090556A (en) 1965-01-18 1965-09-09 Process for preparing substantially ash-free and low-sulphur fuel and product thereof
SE12021/65A SE301988B (enrdf_load_stackoverflow) 1965-01-18 1965-09-15
BE669732D BE669732A (enrdf_load_stackoverflow) 1965-01-18 1965-09-16
FR31746A FR1457571A (fr) 1965-01-18 1965-09-17 Procédé de préparation d'un combustible ne contenant sensiblement pas de cendres et ayant une faible teneur en soufre
NL6512147A NL6512147A (enrdf_load_stackoverflow) 1965-01-18 1965-09-17
NO159737A NO116629B (enrdf_load_stackoverflow) 1965-01-18 1965-09-17
ES0320700A ES320700A1 (es) 1965-01-18 1965-12-14 Un procedimiento para preparar un combustible revalorizado o mejorado, sustancialmente libre de ceniza.

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US426340A US3341447A (en) 1965-01-18 1965-01-18 Solvation process for carbonaceous fuels

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BE (1) BE669732A (enrdf_load_stackoverflow)
ES (1) ES320700A1 (enrdf_load_stackoverflow)
GB (1) GB1090556A (enrdf_load_stackoverflow)
NL (1) NL6512147A (enrdf_load_stackoverflow)
NO (1) NO116629B (enrdf_load_stackoverflow)
SE (1) SE301988B (enrdf_load_stackoverflow)

Cited By (25)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3642607A (en) * 1970-08-12 1972-02-15 Sun Oil Co Coal dissolution process
US3642608A (en) * 1970-01-09 1972-02-15 Kerr Mc Gee Chem Corp Solvation of coal in byproduct streams
US3852182A (en) * 1972-11-07 1974-12-03 Lummus Co Coal liquefaction
US3884794A (en) * 1974-03-04 1975-05-20 Us Interior Solvent refined coal process including recycle of coal minerals
US3884795A (en) * 1974-03-04 1975-05-20 Us Interior Solvent refined coal process with zones of increasing hydrogen pressure
US3884796A (en) * 1974-03-04 1975-05-20 Us Interior Solvent refined coal process with retention of coal minerals
US3892654A (en) * 1974-03-04 1975-07-01 Us Interior Dual temperature coal solvation process
US3990513A (en) * 1972-07-17 1976-11-09 Koppers Company, Inc. Method of solution mining of coal
JPS51135902A (en) * 1975-05-21 1976-11-25 Mitsui Cokes Kogyo Kk Process for producing coke
US3997422A (en) * 1975-06-20 1976-12-14 Gulf Oil Corporation Combination coal deashing and coking process
DE2625690A1 (de) * 1975-06-20 1977-01-13 Chemap Ag Verfahren zur anschwemmfiltration von verfluessigter kohle
US4036730A (en) * 1974-05-24 1977-07-19 South African Coal, Oil & Gas Corporation Limited Solvent-refining of coal
US4056460A (en) * 1975-12-01 1977-11-01 Malek John M Process for liquefying carbonaceous materials of high molecular weight and for separating liquefaction products
US4099932A (en) * 1977-03-28 1978-07-11 Texaco Development Corporation Conversion of solid fuels to fluid fuels
US4111786A (en) * 1975-04-16 1978-09-05 Mitsui Coke Co., Ltd. Process for liquefying coal
US4119409A (en) * 1976-05-27 1978-10-10 Nissho-Iwai Co., Ltd. Process for the preparation of synthetic coking coal
US4157305A (en) * 1975-06-20 1979-06-05 Chemap Ag Method of filtering molten coal
JPS56501205A (enrdf_load_stackoverflow) * 1979-09-27 1981-08-27
DE3208256A1 (de) * 1981-04-09 1982-11-04 International Coal Refining Co., 18001 Allentown, Pa. Verfahren zur herstellung einer kohle/oel-aufschlaemmung
WO1983000370A1 (en) * 1981-07-27 1983-02-03 Pittsburgh Midway Coal Mining Apparatus and method for let down of a high pressure abrasive slurry
US4534847A (en) * 1984-01-16 1985-08-13 International Coal Refining Company Process for producing low-sulfur boiler fuel by hydrotreatment of solvent deashed SRC
US4575381A (en) * 1984-03-01 1986-03-11 Texaco Inc. Formation of disperse-slurry of coal liquefaction residue
EP0166858A3 (en) * 1984-05-30 1986-03-19 Ruhrkohle Aktiengesellschaft Process for the production of diesel fuel from coal middle oil
CN103857774A (zh) * 2011-10-13 2014-06-11 株式会社神户制钢所 煤炭混合燃料、其燃烧方法、以及用于煤炭混合燃料的煤炭燃料
US20170320738A1 (en) * 2015-01-27 2017-11-09 Jiangsu Huadong Institute of Li-Ion Battery Co., L td. Solvothermal apparatus for making lithium iron phosphate

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2476999A (en) * 1947-07-24 1949-07-26 Orchin Milton Solvation and depolymerization of coal
US2686152A (en) * 1951-07-26 1954-08-10 Gulf Research Development Co Production of high quality lump coke from lignitic coals
US2913388A (en) * 1954-11-30 1959-11-17 John H Howell Coal hydrogenation process
US3143489A (en) * 1961-11-24 1964-08-04 Consolidation Coal Co Process for making liquid fuels from coal
US3240566A (en) * 1963-04-23 1966-03-15 Reynolds Metals Co Method of obtaining maximum separability of organic matter from ash in coal extraction processes

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2476999A (en) * 1947-07-24 1949-07-26 Orchin Milton Solvation and depolymerization of coal
US2686152A (en) * 1951-07-26 1954-08-10 Gulf Research Development Co Production of high quality lump coke from lignitic coals
US2913388A (en) * 1954-11-30 1959-11-17 John H Howell Coal hydrogenation process
US3143489A (en) * 1961-11-24 1964-08-04 Consolidation Coal Co Process for making liquid fuels from coal
US3240566A (en) * 1963-04-23 1966-03-15 Reynolds Metals Co Method of obtaining maximum separability of organic matter from ash in coal extraction processes

Cited By (27)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3642608A (en) * 1970-01-09 1972-02-15 Kerr Mc Gee Chem Corp Solvation of coal in byproduct streams
US3642607A (en) * 1970-08-12 1972-02-15 Sun Oil Co Coal dissolution process
US3990513A (en) * 1972-07-17 1976-11-09 Koppers Company, Inc. Method of solution mining of coal
US3852182A (en) * 1972-11-07 1974-12-03 Lummus Co Coal liquefaction
US3892654A (en) * 1974-03-04 1975-07-01 Us Interior Dual temperature coal solvation process
US3884796A (en) * 1974-03-04 1975-05-20 Us Interior Solvent refined coal process with retention of coal minerals
US3884795A (en) * 1974-03-04 1975-05-20 Us Interior Solvent refined coal process with zones of increasing hydrogen pressure
US3884794A (en) * 1974-03-04 1975-05-20 Us Interior Solvent refined coal process including recycle of coal minerals
US4036730A (en) * 1974-05-24 1977-07-19 South African Coal, Oil & Gas Corporation Limited Solvent-refining of coal
US4111786A (en) * 1975-04-16 1978-09-05 Mitsui Coke Co., Ltd. Process for liquefying coal
JPS51135902A (en) * 1975-05-21 1976-11-25 Mitsui Cokes Kogyo Kk Process for producing coke
US3997422A (en) * 1975-06-20 1976-12-14 Gulf Oil Corporation Combination coal deashing and coking process
DE2625690A1 (de) * 1975-06-20 1977-01-13 Chemap Ag Verfahren zur anschwemmfiltration von verfluessigter kohle
US4157305A (en) * 1975-06-20 1979-06-05 Chemap Ag Method of filtering molten coal
US4056460A (en) * 1975-12-01 1977-11-01 Malek John M Process for liquefying carbonaceous materials of high molecular weight and for separating liquefaction products
US4119409A (en) * 1976-05-27 1978-10-10 Nissho-Iwai Co., Ltd. Process for the preparation of synthetic coking coal
US4099932A (en) * 1977-03-28 1978-07-11 Texaco Development Corporation Conversion of solid fuels to fluid fuels
JPS56501205A (enrdf_load_stackoverflow) * 1979-09-27 1981-08-27
DE3208256A1 (de) * 1981-04-09 1982-11-04 International Coal Refining Co., 18001 Allentown, Pa. Verfahren zur herstellung einer kohle/oel-aufschlaemmung
US4392940A (en) * 1981-04-09 1983-07-12 International Coal Refining Company Coal-oil slurry preparation
WO1983000370A1 (en) * 1981-07-27 1983-02-03 Pittsburgh Midway Coal Mining Apparatus and method for let down of a high pressure abrasive slurry
US4534847A (en) * 1984-01-16 1985-08-13 International Coal Refining Company Process for producing low-sulfur boiler fuel by hydrotreatment of solvent deashed SRC
US4575381A (en) * 1984-03-01 1986-03-11 Texaco Inc. Formation of disperse-slurry of coal liquefaction residue
EP0166858A3 (en) * 1984-05-30 1986-03-19 Ruhrkohle Aktiengesellschaft Process for the production of diesel fuel from coal middle oil
CN103857774A (zh) * 2011-10-13 2014-06-11 株式会社神户制钢所 煤炭混合燃料、其燃烧方法、以及用于煤炭混合燃料的煤炭燃料
CN103857774B (zh) * 2011-10-13 2015-05-20 株式会社神户制钢所 煤炭混合燃料、其燃烧方法、以及用于煤炭混合燃料的煤炭燃料
US20170320738A1 (en) * 2015-01-27 2017-11-09 Jiangsu Huadong Institute of Li-Ion Battery Co., L td. Solvothermal apparatus for making lithium iron phosphate

Also Published As

Publication number Publication date
NO116629B (enrdf_load_stackoverflow) 1969-04-28
BE669732A (enrdf_load_stackoverflow) 1966-01-17
NL6512147A (enrdf_load_stackoverflow) 1966-07-19
GB1090556A (en) 1967-11-08
ES320700A1 (es) 1966-07-01
SE301988B (enrdf_load_stackoverflow) 1968-07-01

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