US3746522A - Gasification of carbonaceous solids - Google Patents

Gasification of carbonaceous solids Download PDF

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US3746522A
US3746522A US00182652A US3746522DA US3746522A US 3746522 A US3746522 A US 3746522A US 00182652 A US00182652 A US 00182652A US 3746522D A US3746522D A US 3746522DA US 3746522 A US3746522 A US 3746522A
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gasification
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E Donath
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    • 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
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
    • C07C1/04—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon monoxide with hydrogen
    • C07C1/0485—Set-up of reactors or accessories; Multi-step processes
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C9/00—Aliphatic saturated hydrocarbons
    • C07C9/02—Aliphatic saturated hydrocarbons with one to four carbon atoms
    • C07C9/04—Methane
    • 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
    • C10J3/485—Entrained flow gasifiers
    • 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
    • C10J3/72—Other features
    • C10J3/78—High-pressure apparatus
    • 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
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • 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
    • 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
    • C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
    • 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
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • 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
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0979—Water as supercritical steam
    • 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1656—Conversion of synthesis gas to chemicals
    • C10J2300/1662—Conversion of synthesis gas to chemicals to methane
    • 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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
    • 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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas
    • 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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1892—Heat exchange between at least two process streams with one stream being water/steam
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/40—Ethylene production

Definitions

  • Stage 2 a charge comprising a carbonaceous solid, such as coal, is heated and reacted under methane formation With Stage l product gas and superheated steam to provide a Stage 2 product gas and char which are thereafter quenched and separated for providing gaseous and low-sulfur solid char products.
  • a part of the solid char product is Withdrawn from the process for providing a low-sulfur fuel for a boiler fuel and the remaining part is recycled to Stage 1 and there reacted with oxygen and superheated steam for providing additional Stage 1 product gases.
  • the withdrawn char product is burned in a boiler for providing process steam and the gaseous Stage 2 product is further treated for providing methane-rich fuel gas and sulfurous -by-product.
  • This invention relates to the gasification of carbonaceous solids, and more particularly to a two-stage entrained gasification process for carbonaceous solids for providing a solid, low-sulfur fuel and methane-rich gas as principal products.
  • the Lurgi process represents a typical high pressure, high temperature carbonization technique, and though providing reasonable gaseous yields, has proven somewhat unsatisfactory for efiiciently recovering heating fuels from carbonaceous solids.
  • the amount of methane rich fuel gas produced is unfavorable when compared with that produced by other processes.
  • the solid char retains most of the sulfur present in the starting material, making it unsatisfactory in many applications due, e.g., to lower heating value than a sulfur-free product.
  • large quantities of tars and oils are formed, thereby necessitating complex gas cooling systems with provisions for oil and tar separation from the gas stream.
  • the tars and oils collected must often be further treated for economical utilization of their heating value.
  • U.S. Pat. 2,662,816 teaches a process wherein a dense fiuidized bed carbonization stage is provided in connection with a gasification stage. In the carbonization stage, a carbonaceous fuel is heated in a reducing, or nonoxidizing atmosphere. Thereafter the char and gases produced vby carbonization are separated, with char passing to a gasification zone for heating and reaction with the steam and oxygen to produce a gasification product char and gases'. In that process temperatures of 1600-2000 F. are present in the gasification zone, and 900l300 F. in the carbonization zone.
  • Pat. No. 2,687,950 likewise discloses a carbonization/ gasification process for treating carbonaceous materi-als.
  • the products issuing from a fluidized bed carbonization zone wherein carbonaceous material is heated and reacted with carbon monoxide and hydrogen, comprise volatiles and a carbonaceous residue.
  • the carbonaceous residue is introduced into a gasification zone and there contacted with oxygen and steam to produce carbon monoxide, hydrogen, and methane.
  • Suggested operating conditions for the process comprise temperatures of 1000-l500 F. carbonization, 1400-2l00 Fahrenheit gasification, with an overall operating pressure of 800 pounds per square inch.
  • the char produced may be recycled, part to the gasification zone and part to the carbonization zone, or may be withdrawn for fuel purposes.
  • Pat. No. 2,680,065 discloses a gasification process for carbonaceous solids wherein heat for the gasification process is supplied by indirect heat exchange. There char product from a gasification or combined carbonization/ gasification process is completely burned to supply heat for process requirements, e.g., for gasification. In the process tars and liquid oils are produced.
  • a two-stage super-pressure coal gasification process has been developed at Bituminous Coal Research, [nc., Pittsburgh, Pa. (BCR).
  • BCR Bituminous Coal Research, [nc., Pittsburgh, Pa.
  • a carbonaceous material such as coal
  • char is recycled and reacted with steam and oxygen in a first stage to produce hot synthesis gases.
  • gases are contacted with fresh coal in the second stage whereby the coal is heated and reacted in contact with gases comprising hydrogen, carbon monoxide, and steam to produce methane, process ch-ar and additional synthesis gases.
  • That process employs a super pressure, two-stage coal gasification reactor which operates at temperatures in excess of about l600 F.
  • the BCR process for manufacturing methane may be substantially improved if a part of the char produced in the two-stage superpressure gasiiication process is withdrawn therefrom, with the remaining part being recycled to the Stage 1 gasification step of the process.
  • This invention therefore provides an improved two-stage gasification process for carbonaceous materials, especially coal, wherein principal products are produced comprising a methane-rich fuel gas and a low-sulfur solid char.
  • the invention further provides an improved twostage gasification process which may accommodate a higher proportion of raw coal than heretofore attainable, whereby increased yields of methane may [be obtained, based on coal charged to the process.
  • the invention provides an improved two-stage gasification process for carbonaceous materials which can provide, in addition to increased methane yields, a low-sulfur solid char product which provides an excellent fuel with high heating value which may be employed to efficiently and effectively provide fuel for a waste-heat boiler whereby energy is provided for maintaining the process.
  • This invention provides a two-stage gasification process for carbonaceous solids, especially coal, wherein a lowsulfur fuel char and a methane rich gas comprise the principal products.
  • the process employs two-stage coal gasification, each stage characterized by super pressures and high temperatures, and each stage further characterized in that each comprises a gasification as opposed to a conventional carbonization.
  • Stage 1 of the two-stage gasification a low-sulfur process char is reacted with oxygen and steam at an elevated temperature and pressure to provide a Stage-1 product gas.
  • time in Stage 1 is less than about two seconds, and preferably is less than about one second.
  • a charge comprising a carbonaceous solid, e.g., coal and superheated steam are heated and reacted with the Stage 1 product to provide a Stage 2 product comprising gases and a low-sulfur process char entrained therein which are thereafter cooled and separated for providing a gaseous product and low-sulfur solid char.
  • Gas residence, or contact, time in Stage 2 is less than about ten seconds, and preferably is less than about four seconds.
  • a selected part of the solid char product is withdrawn from the gasification process for providing a low-sulfur fuel and the remaining part is recycled to Stage 1 of the process and there reacted with oxygen and super-heated steam for providing Stage 1 product gases.
  • the withdrawn Stage 2 char product has a low-sulfur content and high heating value and is burned in a boiler for providing process steam and energy.
  • the Stage-2 gaseous product is preferably further treated for providing a substantially sulfur-free, methane-rich fuel gas and a sulfurous by-product. Withdrawal of the selected part of the total char product from gasification permits an increase in the raw coal charge to Stage 2 of the gasification process which results in a total overall increase in methane production based upon coal charged to the gasification process.
  • process gases from Stage 2 are passed through a water gas shift reaction unit and cooled whereby carbon monoxide is converted into carbon dioxide and hydrogen until -a hydrogen/ carbon monoxide ratio of about 3.05 is reached.
  • the gaseous product is thereafter treated with a selective solvent system to provide a concentrated hydrogen sulfide (H28) stream, with subsequent carbon dioxide removal.
  • the hydrogen sulfide stream, as formed, may pass to a Claus plant for conversion to elemental sulfur, and subsequent recovery.
  • the remaining gases are heated to 500 F. and reacted with a reducing, hydrogenating nickel catalyst for completely methanating the product gas, thus forming a methane rich product gas comprising at least about percent by volume methane.
  • FIG. l is a schematic representation of a process according to the invention.
  • FIG. 2 is a schematic representation of an alternative preferred process according to the invention.
  • carbonaceous materials is intended to designate a solid carbon-containing composition, particularly coal, which will yield a part of that carbon as volatile material upon heating.
  • carbonization is intended to designate the destructive distillation or heating of a carbonaceous material in the absence of air or other oxidizing agent in a manner whereby all or part of the volatile portion of the carbonaceous material is liberated.
  • gasification is intended to designate the heating of carbonaceous material in the presence of oxidizing agents such as steam, carbon dioxide and oxygen or mixtures thereof in a manner whereby all or part of the volatile portion of carbonaceous material is liberated, and whereby carbon in the carbonaceous material may react chemically With those oxidizing yagents or with other reactants present in the gasification process.
  • oxidizing agents such as steam, carbon dioxide and oxygen or mixtures thereof
  • coal is preheated in a conventional preheater 5 and thereafter charged with superheated steam to a two-stage gasifier 10.
  • the coal may be charged by known means such as lock hoppers or by a piston feeder and may be injected into gasifier 10 together with a process gas if desired.
  • the coal charged has a particle size small enough to be carried out of the gasifier with process gases via entrainment.
  • Gasifier 10 is of the type described hereinabove, i.e., a Bituminous Coal Research two-stage entrained coal gasifier, and has two gasifying zones, namely Stage il and Stage 2 portions, 12 and 14, respectively.
  • Coal is charged into Stage 2, and is there contacted with steam and hot process gas issuing from Stage 1 portion 12 of the gasifier.
  • gases have a temperature in excess of 1700 F. and comprise oxides of carbon, hydrogen and steam.
  • the hot gases and steam serve to heat and react with the coal charge for volatilizing volatile components of the coal and for forming methane. It is indicated that at least seventy-five percent of the hydrogen in volatile matter from the coal charge forms methane with additional h'ydrogen from Stage 1 gas with the remaining carbon in the volatile matter forming oxides of carbon, principally carbon monoxide.
  • Stage 2 portion 14 of gasier l10 operating conditions constitute extremely high temperatures and super pressures.
  • Operating temperatures in Stage 2 are at least about 1600 F. and most preferably are at least about 1700 F.
  • Pressures exceed at least about 60 ⁇ atmospheres, and most preferably exceed about 70 atmospheres.
  • the superheated steam charge to Stage 2 is generally in excess of 900 F.
  • the gases entering Stage 2 portion of the process from Stage l portion 12 have a temperature greater than about 1700 F.
  • Those gases comprise a synthesis gas including principally hydrogen and carbon monoxide, and superheated steam.
  • the steam and carbon monoxide tend to equilibrate under the water-gas shift reaction to form hydrogen and carbon dioxide.
  • the formation and synthesis of Stage 1 gases will be more fully explained hereinafter.
  • a Stage 2 product is formed and is continuously withdrawn from the top of gasifier 10.
  • That product comprises generally a gaseous portion having solid char entrained therein.
  • the gaseous portion comprises methane, carbon monoxide, carbon dioxide, hydrogen and steam.
  • hydrogen sulfide is present, having formed from sulfur present in the coal charge. It should be noted here that, due to the extremely high pressures and temperatures, and due to the presence of hydrogen and steam reactants, a large part of the sulfur present in the coal charge is removed as hydrogen sulfide gas.
  • the char produced comprises a low-sulfur char.
  • Stage 2 gases and entrained char issuing from gasier are preferably passed to a quenching zone 15 where water is injected into the process stream for cooling the process products from about 1700 F. to about 1100 F.
  • the quenched process stream is then separated into its gaseous and char components.
  • a cyclone-type separator 20 is provided for separating the process products whereby a gaseous product may be continuously withdrawn from the top of the cyclone and a solid char product may be withdrawn from the bottom.
  • Stage 1 portion 12 of gasifier 10 the recycled char is gasified by contact with superheated steam and heated oxygen which are likewise charged to Stage 1 portion 12. The reactions there are exothermic and a temperature of greater than 2500 F. is reached. There the remaining organic components of the char are substantially completely utilized by gasification. The remaining inorganic ash is withdrawn as a slag from the lower portion of gasiiier 10.
  • Process gases issuing from Stage 1 comprise synthesis gas including steam, hydrogen, and oxide of carbon as principal constituents. That gas, i.e., Stage 1 product gas, may then pass into Stage 2 portion 14 of gasier 10 for heating and reacting with fresh coal charged thereto with additional steam, as hereinabove described. There, fresh coal is partially gasified under methane formation at elevated temperatures and pressures to again institute the process cycle which is operated in continuous fashion.
  • char withdrawn from the process streamafter cyclone separator 20, that char is passed to a boiler 30 of conventional type. There the char is burned for providing steam. All or a part of the steam produced may pass to a power plant 40 for providing energy for the process and for other purposes. A part of the steam formed may pass to a conventional air separation apparatus 50 to thereby provide energy for producing process oxygen.
  • ⁇ Oxygen produced in air separation unit S0 is mixed with a portion of the steam produced -in boiler 30. Both steam and oxygen are superheated to a temperature of at least about 800 F. in heat exchanger 60, and are thereafter charged to Stage 1 portion 12 of gasiier 10.
  • Stage 1 of the process the steam, oxygen, and char are reacted to form hydrogen and oxides of carbon which ascend, together with excess steam and any entrained char, into Stage 2 portion 14.
  • the non-volatile, or slag portion of that char which has been gasied in Stage 1 is liquid at the elevated temperature of Stage 1, i.e., in excess of 2500 F. and may drop to the bottom of gasifier 10, be quenched and discarded.
  • the concentrated hydrogen sulfide stream is preferably thereafter passed to a reactor where hydrogen sulfide is converted to elemental sulfur and recovered.
  • the remaining gases are then heated to about 500 F. and enter zinc oxide containing reactor for removing any traces of remaining sulfur in the gas stream.
  • the desulfurized gas stream passes to a reactor containing a nickel hydrogenating catalyst where carbon monoxide is converted into methane. In that fashion a methane-rich product gas comprising at least about 90 percent methane is formed.
  • FIG. 2 an alternative preferred process according to the invention is shown.
  • a stageier 10 is provided as hereinabove described with respect to FIG. 1 for continuously producing a Stage 2 product gas and char which are cooled and separated in char separator 20.
  • a part of the char product is recycled to Stage 1 portion 12 of gasifier 10 and a part is withdrawn from the process cycle.
  • the withdrawn char is charged to a vessel 200 where it is fiuidized by contact and reaction at an elevated temperature with a hydrogen containing gas for further reducing the sulfur content thereof.
  • the hydrogen containing gas comprises Stage 2 product gases, and most preferably Stage 2 product gases having undergone a shift reaction as described previously herein.
  • the gas and entrained char product leaving Stage 2 of the gasifer were quenched by water injection and thereby cooled to a temperature of 1115 F.
  • the quenched process stream comprising gas and entrained char were passed into a cyclone-type separator and continuously Working sand filter. From the stream leaving Stage 2 were withdrawn 798 pounds of char. Of the total withdrawn char, 144 pounds of char having a 13.0% ash content were withdrawn from the process and cooled in a char cooler.
  • the char I was withdrawn by means of lock hoppers. The remaining 654 pounds of char were fed by means of lock hoppers into the Stage 1 portion of the two-stage gasifier together with 475 pounds of oxygen, at 800 F.
  • Process char had a sulfur content of about 0.72 percent by Weight indicating that most of the sulfur present in the raw coal charge was removed during gasification.
  • said hydrogen containing gas comprises said product gas from said second gasification zone, said gas having a hydrogen/ carbon monoxide ratio of about 3.05 therein.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
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US00182652A 1971-09-22 1971-09-22 Gasification of carbonaceous solids Expired - Lifetime US3746522A (en)

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JP (1) JPS5323323B2 (enrdf_load_stackoverflow)
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DE (1) DE2245735A1 (enrdf_load_stackoverflow)
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Cited By (67)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3844733A (en) * 1972-03-23 1974-10-29 Us Interior Two-stage downflow gasification of coal
US3904386A (en) * 1973-10-26 1975-09-09 Us Interior Combined shift and methanation reaction process for the gasification of carbonaceous materials
US3971637A (en) * 1974-12-23 1976-07-27 Gulf Oil Corporation Coal gasification process utilizing waste water from an external process
US3971638A (en) * 1974-12-23 1976-07-27 Gulf Oil Corporation Coal gasification process utilizing high sulfur carbonaceous material
US3971636A (en) * 1974-12-23 1976-07-27 Gulf Oil Corporation Condensate scrubbing of coal gasifier product
US3985519A (en) * 1972-03-28 1976-10-12 Exxon Research And Engineering Company Hydrogasification process
US3991557A (en) * 1974-07-22 1976-11-16 Donath Ernest E Process for converting high sulfur coal to low sulfur power plant fuel
US4052172A (en) * 1974-07-03 1977-10-04 Mitsubishi Jukogyo Kabushiki Kaisha Process for gasifying coal or other carbon containing material
DE2732647A1 (de) * 1976-07-19 1978-01-26 Nichols Eng & Res Corp Verfahren und vorrichtungen zur behandlung des abgases von einem ofen zur verbrennung von organischem material in einer sauerstoff-mangelatmosphaere
US4095959A (en) * 1976-03-06 1978-06-20 Kraftwerk Union Aktiengesellschaft Coal gasification apparatus
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US4099933A (en) * 1973-06-01 1978-07-11 Hydrocarbon Research, Inc. Process for the multiple zone gasification of coal
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JPS5323323B2 (enrdf_load_stackoverflow) 1978-07-14
GB1361745A (en) 1974-07-30
ZA721284B (en) 1973-10-31
DE2245735A1 (de) 1973-03-29
CA966660A (en) 1975-04-29
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FR2153442B1 (enrdf_load_stackoverflow) 1978-10-20

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