US2579397A - Method for handling fuels - Google Patents
Method for handling fuels Download PDFInfo
- Publication number
- US2579397A US2579397A US487187A US48718743A US2579397A US 2579397 A US2579397 A US 2579397A US 487187 A US487187 A US 487187A US 48718743 A US48718743 A US 48718743A US 2579397 A US2579397 A US 2579397A
- Authority
- US
- United States
- Prior art keywords
- zone
- solids
- gas
- carbonization
- combustion
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/16—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form
- C10B49/20—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form
- C10B49/22—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form according to the "fluidised bed" technique
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
- C10J3/482—Gasifiers with stationary fluidised bed
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
- C10J2300/0933—Coal fines for producing water gas
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S48/00—Gas: heating and illuminating
- Y10S48/04—Powdered fuel injection
Definitions
- the present invention relates tofan improved process' for the efllcient utilization of carbonaceous solid fuels such es coal, coke.' peat andthe like, and more specifically verting such ⁇ materials in more valuable pr'oducts including fuel gases.
- The-invention will be fully understood from the following description and the drawing-
- the drawing in Fig. 1 is a. semi-diagrammatic view insectional elevation of an apparatus ⁇ for carrying out the present .process and indicates the ilow ofthe materials.
- Fig. 2 is a mmatic ilow plan showing a modification of the plan of Fig. 1.
- numeral I denotes the crusher or pulverizer which is employed to reduce a solid carbonaceous fuel to a nely divided form, for example, preferably of the order of below 50 mesh, or even less than 100 mesh although even small lumps say $4; to V2 size may be used.
- the material will be referred to as carbonization coal, but it will be understood that other materials can be used.
- the finely ground coal drops from the crusher into a dispersing chamber 2, wherein it is thoroughly dispersed in a stream of superheated steam, which is added by pipe 3.
- the coal in the dispersion is said to be in a uidized" form because capable of flowing through pipes, valves, ducts and such equipment much like -a liquid, showing both static and dynamic heads:
- the liuidized stream is passed through pipe 4 into the lower portion of a carbonization chamber 5 which is in the form of a cylinder fitted at its lower end with a conical base 6.
- a grid orl screen is located in the lower portion of the chamber conveniently at'the place where the cone Iand cylinder unite.
- a discharge pipe I I is provided to take a stream of the nuidlzed solid material from the combus- 9 and discharges it into chamber B so that the highly heated material from the combustion chamber 9, which is at a temperature of say 1800 to 2400" F., is continuously recycled to the carbonization chamber 5.
- This chamber is at the usual carbonizing temperature of say 500 to 1200 ⁇ F. and the preheat and heat of carbonization is thus substantially completely furnished by heat supplied from the combustion chamber.
- Cooler I3 may be of the indirect type shown or the direct type. as desired.
- the recovery system (not shown) need not be described in detail because such systems are well known in the art, but should provide f means for segregating the dust. tar, light oils,
- Combustion gases are taken from the chamber 9 by a pipe Ilwhich leads to a dust separator I6 and to a waste heat boiler I6 for the Vsteam generation.
- the separated dust may the chambers by a pipe I1.
- Pipe II' which is shown as branch-of pipe II, is provided to draw off a portion of the highly heated fluidized contents of chamber 9 and t0 conduct it to a gas generator I8.
- This generator is shown as a vertical cylindrical vessel with a conical base, similar to chambers 6 and 8 de ⁇ - scribed above, and it is preferably provided with a screen at its lower portion to act as a distributor.
- the fluidized solid stream is discharged into the chamber, preferably' below the screen as de scribed above and super-heated steam is added by a pipe I9.
- the generator is maintained at a temperature between about 1400 and 2000 F., suitable for the rapid reaction of carbon and steam to produce water gas by the well known reaction.
- the gas may be treated in any usual manner i'or the removal oi sulfur or other impurities, in equipment not shown, making it suitable for use as city gas or otherwise. It desired, the whole or a portion of the gas resulting from coal carbonization may be admixed with the water gas.
- a iluidized stream of solids which is now largely free from carbon is withdrawn by pipe 23 from the gas generator I8 and a portion of this ash may be returned to carbonization chamber 5 in any suitable manner, for example through line Il.
- the solids can be discharged into the chamber 24 which is blown with steam admitted by pipe 25 and is then withdrawn by pipe I9 in la highly superheated condition required for the generation of the water gas.
- a portion oi. the nuidized solid is taken from the superheating chamber 24 by a pipe 26 and may be returned to pipe 8 for recirculation to the combustion chamber 9.
- a small portion is discharged at 21 to prevent accumulation in the system.
- the combustion zone is operated at the most elevated temperature and is used to generate high temperature heat which is utilized for gas generationeither by the carbonization of the charge orby water gas generation, which processes are operated at lower temperatures. Heat is carried from the combustion chamber to the gas generation chambers by the continuously owing streams of fluidized solid. 'I'hus the process is made fully continuous.
- Ii.' coal is used as the raw material, it is preferably fed directly to the carbonizaton chamber and heat for the carbonization is supplied by i a stream of highly heated carbon flowing continuously from the combustion chamber through the pipe Il and discharging into the chamber 5.
- the temperature is capable of very careful, regulation and control and is distributed rapidly through the iluidized mass in the carbonization the high degree of agitation maintained therein.
- Chamber 5 is suillciently large to permit the complete carbonization very rapidly and the solids removed by pipe 1 are substantially free of volatile materials and are capable of rapid combustion with air in the combustin chamber 9.
- 'I'he process may be operated without the water gas generation step by closing a valve in pipe Il'. It desired.
- an inert material such as sand maybe added to the coal and circulated through the chambers i and 9 and the associated pipes 1, l and Il, so as to provide alarger volume of heat carrying solid material, but it is not required as the ash content of the coal may be allowed 'to accumulate and thus furnish any desired amount oi.' inert solid. High ash coals may thus be employed in the process.
- the apparatus of the present process is all constructed for operation at low pressure. but high temperatures arerequired. especially in the combustion zone and in the associated pipes. 'I'he equipment should be lined with high temperature tile or brick and it is found that there uidized streams is kept down in the range of 25 to 75 i'eet per second. 'Ihe operation of the reaction zones is smooth and proceeds without dimculty.
- the upward gas velocity should be of the order of 0.5 to 6 feet per second. where the solid is say to 200 mesh. and progressively higher with larger sizes say 10 to 20 i'eet per second with lumps of V4 to l/g".
- Fig. 2 there is a now plan illustrating a method which is particularly applicable to the working up of solid carbonaceous fuel materials l, particularly coal. peat, shale, tar sands and the like.
- the apparatus employed is closely similar to that shown in stage Il drogen by means of l understood by those Fig. l; but the flow plan herein contained is soliewhat more complete.
- the raw material in finely divided form enters at 3l, passing directly to the low temperature carbonization step indicated at 3i.
- Distillation products are removed from 3
- the coky residue produced as a result of the carbonization is conducted to the combustion stage of the process indicated at 33 where air is also introduced.
- the stack gases are taken olf at Il and thehot residue at 36.
- a portion o! this residue is returned to the carbonization as indicated by the line 38 in order to carry heat for carbonization, as explained pre- ⁇ viouxsly, andthe second portion of this carbonaceous residue is conducted to the water-gas .generation stage indicated at 31.
- Steam is added at 3B and ash constituents of the original fuel are collected and drawn on at 39.
- Thegas which remains is compressed at 44 and carbon dioxide is separated at 45.
- the remaining gas, which is substantially pure hydrogen, is then employed for the hydrogenation of the liquid distillation products produced from the original carbonization. This is accomplished in thehydrogenation step indicated at 46.
- the combustion and the water-gas generationV stages are conducted just as indicated in the previous description of Fig. 1, that is to say while the solid material is in a iluidized condition.
- the conversion of the CO to CO2 and hysteam is preferably effected catalytically, using asy a catalyst iron oxide or iron oxide promoted with chromium and similar materials which are well lmown in the art.
- the conversion is effected at a temperature of the order of 850 F. and low pressure is ordinarily employed.
- the hydrogenation step may be any one of a number of different types which are well known in the art. For example, it may be carried out under mild hydrogenation conditions, that is to say at relatively low temperatures and pressures so that the hydrogen does little more than to effect a purification by removal of sulfur, nitrogen and similar elements. On the other hand, the hydrogenation may be carried out under destructive conditions, above atmospheres and preferably at about 200 atmospheres and at temperature say from v '70o to 11o0 F. In this way the tarry materials are converted fully into lower boiling liquids rich in hydrogen.
- the preferred catalysts are of the sulfur immune type, especially those containing metals, oxides or suldes of the 6th group of the periodic table, either alone or in admixture with each other or with dimcultly reducible oxides such as alumina, zirconia, magnesia or lime. More readily reducible oxides such as zinc oxide can also be added to the catalyst mixtures.
- the present process is thus capable of carbonizing coal and producing a high quality fuel gas continuously.
- the advantages will be fully skilled in the art.
- the continuous process of carbonizing and gasifying finely divided solidcarbonaceous material while said material is in a uidized state which comprises continuously charging a nely divided fuel and steam into a fluidizedmass of previously carbonized finely divided solids at a solids in the said combustion fuel in a gas generating that is to say, at pressures carbonization temperature in a carbonizing zone thus-mixed solids are in a uidized state therein, thereby carbonizing said fuel, continuously circulating the hot carbonized solids from said zone to a separate combustion zone in which they are iluidized along with previously carbonized fuel.
- the continuous process'of carbonizing and .gasifying finely'divided solid carbonaceous materials which comprises. continuously charging a stream of finely divided fuel dispersed in steam into a fluidized bed of hot previously carbonized fuel in a carbonizing zone thereby carbonizing said finely divided fuel in said iluidized bed. heating a separately fluidized mass of carbonized, finely divided fuel in a separate heating zone to a gas making temperature by blasting it with a combustion supporting fluid and discharging gaseous products of combustion, generating combustible gas by passing steam through a.
- An improved process for utilizing solid carbonaceous materials which comprises continuaardse? 7 ously feeding fiuidizable, finely divided. carbonizable solids into a carbonization zone and forming a fiuidized mass of solids therein, withdrawing therefrom vaporous carbonization products and a fiuidized stream of finely divided, solid, carbon-containing carbonization residue, gasifying a portion of the carbon of said residue while the latter is in the form of a fiuidized mass of solids by a water gas reaction with steam in a gas generation zone, burning another portion of the carbon of said residue while the latter is in the form of a iiuidized mass of solids by a reaction with a combustion-supporting gas in a separate combustion zone to generate heat, heating fiuidized solids in said combustion zone, contacting solids so heated with said solids undergoing said water gas reaction to supply heat required by said water gas reaction, returning solids highly heated in said combustion zone to said carbonizationzone to supply heat required therein, and
- An improved process for utilizing solid carbonaceous materials comprising continuously feeding fiuidizable finely powdered carbonaceous solids containing volatile constituents into a carbonization zone and forming a fluidized mass of solids therein, withdrawing therefrom vaporous carbonization products and a fiuidized stream of finely divided carbonization residue, subjecting a portion of said residue while in the form of a fluidized mass of solidsI to a water gas reaction with steam in a separate gasification zone, subjecting a portion of said residue while in the form of a fluidized mass of solids to combustion in a separate gasification zone with a combustion-supporting gas to generate heat, heating fiuidized solids by said heat of combustion, oontacting solids so heated with said solids undergoing said water gas reaction to supply heat required by said water gas reaction, and returning solid powdered residue highly heated by the heat of said combustion to the carbonization zone to supply at least a portion of the heat required in said carbonization zone.
- An improved process for utilizing solid carbonizable fuel materials comprising continuously feeding fluidizable, finely divided carbonaceous solids containing volatile constituents into a carbonization zone and forming a fiuidized mass of solids therein, withdrawing vaporous carbonization products therefrom, separately withdrawing a iiuidized stream of finely divided carbonization residue, passing the same into a combustion zone and forming a fiuidized mass of solids therein, burning a portion of the carbon therein 9.
- Aprocessaceordingtoclaim'linwhichinert mineral matter is charged to the combustion zone as a heat carrier.
- An improved process for utilizing solid carbonaceous materials which comprises, continuously feeding fiuidizable finely divided carbonizable solids intn a carbonization zone and forming a fluidized mass of solids therein, withdrawing therefrom vaporous carbonization products and a iiuidized stream of finely divided solid carbon-containing carbonization residue, gasifying a portion of the carbon of said residue while the latter is in the form of a fiuidized mass of solids by an endothermicgasiiication reaction with a fluid gasifying medium in a gas generation zone.
- An improved process for utilizing solid carbonizable fuel materials comprising continuously feeding iiuidizable finely divided carbonaceous solids containing volatile constituents into a carbonization zone and forming a fiuidized mass of solids therein, withdrawing vaporous carbonization products therefrom, separately withdrawing a uidized stream of finely divided carbonization residueppassing the same into a combustion zone and forming a ⁇ uidized mass of solids therein, burning a portion of the carbon therein while in the form of a fiuidized mass of solids whereby the remainder is raised to a high temperature.
- the process for recovering vaporizable products from finely divided carbonaceous solids and for producing mixtures of hydrogen and carbon monoxide comprises introducing incandescent finely divided carbonaceous solids into a confined contacting zone, introducing a gas comprising steam into said zone and passing said gas upwardly through said zone at a rate suflicient to maintain said solids in suspended turbulent dense phase condition, maintaining said zone under conditions for effecting conversion of a substantial amount of said steam with carbon in the carbonaceous solids for producing hydrogen and carbon monoxide, continuously separating reaction products from solids in the upper part of said zone and withdrawing gasiform reaction products from the upper part of said zone, separately removing a portion of the solids from the dense turbulent suspended phase at a point below the upper level thereof, transferring at least a portion of said removed solids to a coking zone, introducing raw finely divided carbonaceous solids into said coking zone, maintaining the solids within the coking zone in a iluidized dense turbulent phase by passing a gasiform fluid upwardly there
- a method for converting coal which comprises establishing first, second and third beds of finely divided coke, passing a gas through each of said beds to maintain said finely divided coke in a fluidized state.
- the gas fed to the second bed being a combustion supporting gas and that to the third bed comprising a gasifying medium for said coke, continuously feeding coal in finely divided form to said first bed, maintaining said first bed at a carbonizing temperature, continuously feeding coke from said first bed to said second bed, subjecting said coke in said second bed to a combustion reaction in which the finely divided coke is highly heated and continuously feeding hot finely divided coke from said second bed to said first bed and said third bied.
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Combustion & Propulsion (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Dispersion Chemistry (AREA)
- Solid Fuels And Fuel-Associated Substances (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US487187A US2579397A (en) | 1943-05-15 | 1943-05-15 | Method for handling fuels |
BE460668D BE460668A (pt) | 1943-05-15 | 1945-10-13 | |
BE467126D BE467126A (pt) | 1943-05-15 | 1946-08-07 |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US487187A US2579397A (en) | 1943-05-15 | 1943-05-15 | Method for handling fuels |
Publications (1)
Publication Number | Publication Date |
---|---|
US2579397A true US2579397A (en) | 1951-12-18 |
Family
ID=23934741
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US487187A Expired - Lifetime US2579397A (en) | 1943-05-15 | 1943-05-15 | Method for handling fuels |
Country Status (2)
Country | Link |
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US (1) | US2579397A (pt) |
BE (1) | BE460668A (pt) |
Cited By (16)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2623817A (en) * | 1946-04-03 | 1952-12-30 | Standard Oil Dev Co | Production of fuel gases |
US2654698A (en) * | 1950-05-03 | 1953-10-06 | Consolidation Coal Co | Low-temperature distillation of coal |
US2697718A (en) * | 1949-09-29 | 1954-12-21 | Standard Oil Dev Co | Method of producing gasoline |
US2712495A (en) * | 1951-10-06 | 1955-07-05 | Standard Oil Co | Conversion of a carbonaceous materialwater slurry |
US2727813A (en) * | 1951-05-31 | 1955-12-20 | Universal Oil Prod Co | Production of combustible gas from hydrocarbonaceous solids, particularly bituminous coals |
US2727812A (en) * | 1951-05-31 | 1955-12-20 | Universal Oil Prod Co | Production of combustible gas from comminuted solid carbonaceous material |
US2741549A (en) * | 1952-11-01 | 1956-04-10 | Exxon Research Engineering Co | Conversion of carbonaceous solids into volatile products |
US2788314A (en) * | 1949-08-03 | 1957-04-09 | Metallgesellschaft Ag | Process for the gasification of fine grained or pulverulent fuels |
US3008815A (en) * | 1953-04-25 | 1961-11-14 | Union Rheinische Braunkohlen | Production of gases of high and low calorific value |
US3923466A (en) * | 1971-12-16 | 1975-12-02 | Krupp Gmbh | Apparatus for the production of cracked gas |
US4099933A (en) * | 1973-06-01 | 1978-07-11 | Hydrocarbon Research, Inc. | Process for the multiple zone gasification of coal |
US4274839A (en) * | 1979-12-28 | 1981-06-23 | Leas Arnold M | Process for gasification of coal and organic solid wastes |
US4439210A (en) * | 1981-09-25 | 1984-03-27 | Conoco Inc. | Method of catalytic gasification with increased ash fusion temperature |
US4700639A (en) * | 1983-03-16 | 1987-10-20 | Gerald Esterson | Utilization of low grade fuels |
US5064444A (en) * | 1986-10-16 | 1991-11-12 | Bergwerksverband Gmbh | Process for the allothermic gasification of coal |
US6312483B1 (en) * | 1993-08-18 | 2001-11-06 | Ormat Industries Ltd. | Method of and apparatus for producing combustible gases from pulverized solid fuel |
Citations (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR632466A (pt) * | 1900-01-01 | |||
GB214544A (en) * | 1923-09-17 | 1924-04-24 | Basf Ag | An improved process for the manufacture of fuel gas |
US1687118A (en) * | 1922-09-27 | 1928-10-09 | Ig Farbenindustrie Ag | Manufacturing fuel gas |
GB301975A (en) * | 1927-09-19 | 1928-12-13 | Ig Farbenindustrie Ag | Improvements in the low-temperature carbonisation of fuels and in apparatus therefor |
DE564870C (de) * | 1927-12-06 | 1932-11-24 | Werschen Weissenfelser Braunko | Verfahren und Einrichtung zur ununterbrochenen Erzeugung von Wassergas aus feinkoernigen, pulver- oder staubfoermigen Brennstoffen |
US1899887A (en) * | 1928-05-14 | 1933-02-28 | Ernest w | |
US1983943A (en) * | 1929-12-17 | 1934-12-11 | William W Odell | Process for carbonizing carbonaceous materials |
US1984380A (en) * | 1929-12-17 | 1934-12-18 | William W Odell | Process of producing chemical reactions |
US2361978A (en) * | 1942-02-28 | 1944-11-07 | Standard Oil Co | Catalytic cracking system |
US2451804A (en) * | 1940-12-27 | 1948-10-19 | Standard Oil Dev Co | Method of and apparatus for contacting solids and gases |
GB611924A (en) * | 1946-02-14 | 1948-11-05 | Standard Oil Dev Co | An improved process for gas generation from solid carbonaceous material |
US2480670A (en) * | 1942-05-02 | 1949-08-30 | Standard Oil Dev Co | Two-zone fluidized destructive distillation process |
-
1943
- 1943-05-15 US US487187A patent/US2579397A/en not_active Expired - Lifetime
-
1945
- 1945-10-13 BE BE460668D patent/BE460668A/fr unknown
Patent Citations (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR632466A (pt) * | 1900-01-01 | |||
US1687118A (en) * | 1922-09-27 | 1928-10-09 | Ig Farbenindustrie Ag | Manufacturing fuel gas |
GB214544A (en) * | 1923-09-17 | 1924-04-24 | Basf Ag | An improved process for the manufacture of fuel gas |
GB301975A (en) * | 1927-09-19 | 1928-12-13 | Ig Farbenindustrie Ag | Improvements in the low-temperature carbonisation of fuels and in apparatus therefor |
DE564870C (de) * | 1927-12-06 | 1932-11-24 | Werschen Weissenfelser Braunko | Verfahren und Einrichtung zur ununterbrochenen Erzeugung von Wassergas aus feinkoernigen, pulver- oder staubfoermigen Brennstoffen |
US1899887A (en) * | 1928-05-14 | 1933-02-28 | Ernest w | |
US1983943A (en) * | 1929-12-17 | 1934-12-11 | William W Odell | Process for carbonizing carbonaceous materials |
US1984380A (en) * | 1929-12-17 | 1934-12-18 | William W Odell | Process of producing chemical reactions |
US2451804A (en) * | 1940-12-27 | 1948-10-19 | Standard Oil Dev Co | Method of and apparatus for contacting solids and gases |
US2361978A (en) * | 1942-02-28 | 1944-11-07 | Standard Oil Co | Catalytic cracking system |
US2480670A (en) * | 1942-05-02 | 1949-08-30 | Standard Oil Dev Co | Two-zone fluidized destructive distillation process |
GB611924A (en) * | 1946-02-14 | 1948-11-05 | Standard Oil Dev Co | An improved process for gas generation from solid carbonaceous material |
Cited By (17)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2623817A (en) * | 1946-04-03 | 1952-12-30 | Standard Oil Dev Co | Production of fuel gases |
US2788314A (en) * | 1949-08-03 | 1957-04-09 | Metallgesellschaft Ag | Process for the gasification of fine grained or pulverulent fuels |
US2697718A (en) * | 1949-09-29 | 1954-12-21 | Standard Oil Dev Co | Method of producing gasoline |
US2654698A (en) * | 1950-05-03 | 1953-10-06 | Consolidation Coal Co | Low-temperature distillation of coal |
US2727813A (en) * | 1951-05-31 | 1955-12-20 | Universal Oil Prod Co | Production of combustible gas from hydrocarbonaceous solids, particularly bituminous coals |
US2727812A (en) * | 1951-05-31 | 1955-12-20 | Universal Oil Prod Co | Production of combustible gas from comminuted solid carbonaceous material |
US2712495A (en) * | 1951-10-06 | 1955-07-05 | Standard Oil Co | Conversion of a carbonaceous materialwater slurry |
US2741549A (en) * | 1952-11-01 | 1956-04-10 | Exxon Research Engineering Co | Conversion of carbonaceous solids into volatile products |
US3008815A (en) * | 1953-04-25 | 1961-11-14 | Union Rheinische Braunkohlen | Production of gases of high and low calorific value |
US3923466A (en) * | 1971-12-16 | 1975-12-02 | Krupp Gmbh | Apparatus for the production of cracked gas |
US4099933A (en) * | 1973-06-01 | 1978-07-11 | Hydrocarbon Research, Inc. | Process for the multiple zone gasification of coal |
US4274839A (en) * | 1979-12-28 | 1981-06-23 | Leas Arnold M | Process for gasification of coal and organic solid wastes |
WO1981001838A1 (en) * | 1979-12-28 | 1981-07-09 | A Leas | Integrated process for converting multi-solid fuels into clean producer gases and liquids and for recovering valuable by-products |
US4439210A (en) * | 1981-09-25 | 1984-03-27 | Conoco Inc. | Method of catalytic gasification with increased ash fusion temperature |
US4700639A (en) * | 1983-03-16 | 1987-10-20 | Gerald Esterson | Utilization of low grade fuels |
US5064444A (en) * | 1986-10-16 | 1991-11-12 | Bergwerksverband Gmbh | Process for the allothermic gasification of coal |
US6312483B1 (en) * | 1993-08-18 | 2001-11-06 | Ormat Industries Ltd. | Method of and apparatus for producing combustible gases from pulverized solid fuel |
Also Published As
Publication number | Publication date |
---|---|
BE460668A (pt) | 1946-04-13 |
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