US3817724A - Gasification of solid carbonaceous waste material - Google Patents

Gasification of solid carbonaceous waste material Download PDF

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US3817724A
US3817724A US00252449A US25244972A US3817724A US 3817724 A US3817724 A US 3817724A US 00252449 A US00252449 A US 00252449A US 25244972 A US25244972 A US 25244972A US 3817724 A US3817724 A US 3817724A
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gasification
gases
zone
gas
gasification zone
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J Ellis
F Franklin
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Chevron USA Inc
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Chevron Research and Technology Co
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Priority to JP48051531A priority patent/JPS5239602B2/ja
Priority to CA170,978A priority patent/CA998530A/en
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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
    • 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
    • C10J3/845—Quench rings
    • 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
    • C10J2300/0956—Air or oxygen enriched air
    • 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
    • C10J2300/0976—Water as 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
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • C10J2300/0996—Calcium-containing inorganic materials, e.g. lime
    • 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
    • C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
    • C10J2300/1606—Combustion processes
    • 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
    • C10J2300/1671—Integration of gasification processes with another plant or parts within the plant with the production of electricity
    • 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
    • C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen only
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/12—Heat utilisation in combustion or incineration of waste
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
    • Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]

Definitions

  • the process of the present invention can also be advantageously used for gasification of solid carbonaceous matter in general; however, certain modifications, such as in the reaction zone quench are preferably made when feeding lignite, coal, peat or the like to the gasification zone.
  • the present invention relates to gasification of solid carbonaoeous material, especially waste material.
  • process gas is obtained from coal by distillation comprising passing the gas-making material between heated walls in a finely divided condition and While separated and distributed in a substantially non-oxidizing medium and distilling the material during such passage and regulating the motion of the material and said medium by imparting thereto a vertical motion by jets of heated gas directed along the heated walls transversely to the direction of passage.
  • coal distillation is not gasification. Distillation drives off volatile matter already present; gasification creates volatiles not originally present.
  • part of the material left after eduction of oil from the shale feed is burned to ashes with the resulting hot gas then being used to educt gas and oil from the shale feed material.
  • U.S. Pat. 3,361,644 gases and oil are educted from shale by passing oxygen-free hot gas countercurrent to downowing shale particles.
  • the hot gas is obtained by heating a portion of the gas efliuent from the eduction zone. Temperature is maintained below about 1800 F. in the eduction zone to avoid clinker formation by fusion of ash constituents.
  • the process of U.S. Pat. 3,361,644 is largely a pyrolysis-distillation process which is not based on a gasification reaction such as reacting H2O with carbonaceous material.
  • Partial oxidation processes are described, for example, in U.S. Pat. Nos. 1,977,684; 2,592,377; 2,657,986; 2,633,- 417; 2,727,812; 2,987,387; 2,657,124; and 3,025,149.
  • U.S. Pat. No. 2,660,521 is directed to partial oxidation of gases with expansion of the resultant hot gases through a turbine and thereby generating power and obtaining a cooled synthesis gas. Temperature in the reaction zone is controlled by carbon dioxide recycle. The carbon dioxide is a diluent and also lowers temperature by virtue of the endothermic reaction of carbon dioxide with hydrocarbon to form carbon monoxide and hydrogen.
  • Combustible gases produced by the present invention may be utilized in processes which burn the gas and produce energy by expanding the resultant hot gases through a turbine.
  • Gas turbines are now operating on fuel gas (natural and refinery), blast-furnace gases, fuel oils (including heavy residuals), and at least one gas turbine burning gas generated from coal is operating.
  • the gases After purification of the gases from the gasification step, the gases are heated in exchange with incoming air, expanded through a turbine which drives the second stage air compressor, then combusted with air, and then expanded through a gas turbine which turbine is used to drive an electricity generator and first stage air compressor.
  • the amount of air introduced to the combustor chamber is just that required to burn the gases. Heat is removed from the combustor by steam generation so that the inlet temperature to the gas turbine is about 820 C. (1508 F.).
  • the Rudolph report is directed to the gasification of coal and also mentions that other gasification plants are used to gasify similar material such as sub-bituminous coal and lignite.
  • the Rudolph process calls for injection of oxygen directly to the gasification zone and also the injection of steam to aid in controlling the temperature in the reaction zone.
  • a process for converting solid carbonaceous waste material to combustible gases which comprises:
  • the present invention is based on the combination of carbonaceous waste solids gasification with temperature control in the gasification zone obtained by partially or wholly burning a portion of the efiiuent gases from the gasification zone and then recycling the hot gases thus obtained to the gasification zone. It is critical in the process of the present invention that gasification reactions are carried out in the gasification zone to generate hydrogen from hydrocarbonaceous matter in the gasification zone and also to generate hydrogen from the H2O which is added to the reaction zone via the recycled hot gases.
  • the present invention is also based on a critically important third feature or concept which is that the present process is extremely attractive for the conversion of solid carbonaceous wastes to combustible gas.
  • solid carbonaceous waste material is used herein to connote municipal garbage, industrial or agricultural vvastes which are organic, such as cellulosic solids, dried or partially dried sewage, and like solid carbonaceous waste'materials.
  • Still another critical aspect of the present invention is the reuse of H2O which is vaporized by reactor effluent scrubbing or quenching.
  • the temperature in the gasification zone can, of course, be controlled pursuant to the present invention by controlling both the amount of hot recycle gas and the temperature of the recycle gas. Usually both of these will be adjusted to an optimum level for the process of the present invention so as to achieve desired reaction rates of solids in the gasication zone at minimum energy requirement for recycle gas compression, but yet to maintain temperatures in the gasification zone below the ash fusion temperature, erg., below about 2000 F.
  • the partial burning of the recycle gas to the gasification zone can be carried out, for example, by an in-line burner.
  • the gases obtained from the gasification zone are preferably cooled and cleansed lby a water quench. This water in part finds its way back to the gasification zone via that portion of the gases which are recycled to supply heat and reactant gases to the gasification zone. Additional water is supplied to the gasification zone from the solids fed to the gasification zone, as the solids fed invariably will have at least some moisture content. Additional water and carbon dioxide are produced by partial burning of the recycle Igas. Thus, there will be H2O and CO2 present in the gasification zone for conversion of carbon and hydrocarbons into hydrogen and carbon monoxide according to well known reactions such as The portion of the gasification zone gases which are not recycled to the gasification zone are preferably utilized in a manner previously described by the Rudolph report.
  • the process of the present invention can also be advantageously used for gasification of solid carbonaceous matter in general; however, certain modifications, such as in the reaction zone quench, are preferably made when feeding lignite, peat, coal or the like to the gasification zone.
  • the raw hot gases from the gasification zone are preferably not immediately quenched with water, but instead are first quenched with an oil stream to remove particulate matter and thereby allow advantageous heat recovery from a portion of the gasification zone efiiuent without incurring severe heat exchanger fouling.
  • FIG. 1 A schematic process ow diagram illustrating preferred embodiments of the present invention as applied to gasification of municipal waste type feedstocks (FIG. 1) and as applied to gasification of lignite, coal, peat or the like (FIG. 2).
  • solid wastes are introduced via line 1 to gasification zone 2.
  • the solid wastes can be chosen from a variety of feeds such as municipal garbage (paper, orange peels, grease, bones, plastics, etc.); agricultural wastes (corn stalks, etc.); sewage, preferably in dried form; and the like.
  • the solids can be considered to undergo a series of steps of reactions in the gasification zone including, for example, H2O distillation, oil distillation, pyrolysis, and gasification reactions such as previously mentioned. In the present invention there must be gasification reactions in the gasification zone.
  • a gaseous stream is withdrawn from the gasification zone as indicated by line 4. This gas stream is quenched and scrubbed to remove particles by water introduced to quench drum 6 via line 7 and recycle line 8.
  • Make-up water and alkali carborate is introduced via line 5 to react with strong acids such as HC1 that may form in the gasifier and to also vaporize most of the water for efficient use in the gasifier.
  • a small portion of the makeup water is ultimately recycled as a solids-containing sludge via lines 9 and 10 to gasifier 2.
  • the water preferably carries reacted alkali carbonate to the gasifier which also provides catalytic benefits for the reaction of solid waste material in gasifier 2 as is further described in the commonly assigned application of R. J'. White, titled Catalytic Hydrogen Manufacture, filed May 5, 1970, Ser. No. 34,844.
  • Heavy sludge material and water are withdrawn from quench drum 6 via line 9 and passed to settler 11.
  • Oily sludge material, water and preferably reacted alkali carbonate is passed to gasifier 2 via line 10 from the settler.
  • a clarified oil stream is withdrawn from an intermediate point from settler 11 via line 12.
  • the hot gases withdrawn from gasifier 2 via line 4 are at a temperature of about ⁇ 600 F., and the water scrub in the quench drum results in them being cooled to a temperature of about 350 F. to 450 F. before they are removed -via line 13.
  • the gaseous material in line ⁇ 13 is then split into two streams; first stream 14 for alternate recycle 'back to the gasification zone, and a second stream 15 which can be referred to as a product gas stream.
  • the product gas stream is preferably introduced to zone 16 for power generation preferably using a gas turbine system similar to that referred to in the Rudolph report previously and/ or steam generation.
  • the product gas in line 15 can be used in other manners as a low B.t.u. fuel or as feed to synthesis gas processes,
  • Recovered oil is shown as being passed from the settler to the power generation system via line 12.
  • the recovered oil can be removed as a product as indicated by line 21.
  • Electric power is preferably generated in zone 16 by an electrical generator driven by a gas turbine, which gas turbine is in turn driven by combusted product gases and combusted recovered oil, as desired, introduced via lines 1S and 12, respectively.
  • the electric power is schematically indicated as withdrawn via line 18. Flue gas resulting from burning the product gas, to supply power in zone 16, is shown as Withdrawn via line 19.
  • a portion of the power generated by the gas turbine in zone 16 is preferably used for driving an air compressor to provide compressed air for combustion in zone l16 and, as indicated by line 20, for use in recycle combustor 24. Air to the compressor is shown entering zone 16 via line 17.
  • recycle gases from quench drum Y6 are passed to the recycle combustor via recycle compressor 22 and then line 23.
  • Compressed air or pressurized oxygen is introduced to recycle combustor 24 via line 20.
  • Recycle combustor 24 is preferably an in-line burner device.
  • the partially combusted recycle gas is withdrawn from recycle combustor 24 usually at a temperature of about 1700 F. and passed via line 25 to the bottom of gasification zone 2 to supply reactive gases and temperature control as well as the necessary heat for gasification zone 2.
  • carbonaceous solids are introduced via line 1 to gasification zone 2.
  • the carbonaceous solids can be chosen from a variety of Vfeeds such as lignite, or peat, or coal, or wood, or cellulose, or other solid carbonaceous materials. IHowever, the solids are not a wide ranging mixture as in the previously described embodiment relating to a waste material feed such as municipal waste.
  • the carbonaceous solids are in pulverized form to increase the reactability of the solids and permit more uniform flow into the apparatus.
  • the solids can be considered to undergo a series of steps or reactions in the gasification zone including, for example, H2O distillation, oil distillation, pyrolysis, and gasification reactions such as previously mentioned. In the present invention there must be gasification reactions in the gasification zone.
  • a gaseous stream is withdrawn from the gasification zone as indicated by line 4. This gas stream is quenched and scrubbed to remove particles by oil introduced to quench drum 5 vi-a line 6 and recycle line 7. Heavy sludge material is withdrawn from oil scrubber 5 via line 8 and returned to the gasifier via line 9 for further conversion to product combustible gases.
  • a clarified oil stream is withdrawn from an intermediate point from oil scrubber 5 via line 10. This clarified oil stream is recirculated via pump 11 and then lines 12 and 6 to the upper part of the oil scrubber where it is introduced to scrub the hot gases which are introduced to the scrubber via line 4. The hot gases are introduced to the scrubber at a temperature of about 1000 F., and the oil scrubbing process results in them being cooled to a temperature of about 700-800 F. before they are removed via line 13.
  • the gaseous material in line 13 is then split into two streams; a first stream 14 for alternate recycle back to the gasification zone, and a second stream 1S which can be referred to as a product gas stream.
  • the product gas stream is introduced to a heat recovery and/or steam generation zone 16 wherein steam can be generated l'as indicated by line 17 leaving zone 16.
  • product gas is Withdrawn via line l18 from the heat recovery zone 16. This product gas is then passed to further processing and use, for example, further processing.
  • Recovered oil is also withdrawn from zone 16 as indicated by line 19.
  • the recovered oil can be used within the process as indicated by line 20, or the recovered oil can be removed as a product as indicated by lines 21 and 22.
  • Recovered water (waste water) is removed from zone 16 via line 23 and preferably is used internally in the process of the present invention as can be seen by reference to boiler 24.
  • Makeup water which may be necessary in the process of the present invention can also be added to boiler 24 as indicated by lines 2S and 23.
  • junction 28 receives oil that has been withdrawn, for example, via lines 10 and 29 from oil scrubber 5, and oil may also be added to the recycle gas 'at junction 28 via lines 30 and 31 from boiler '24 as shown in the drawing.
  • the recycle stream containing oil which has been sprayed into the stream at yjunction 28 is introduced via line 26 to quench pot 27 wherein the hot recycle gas is further cooled, preferably by vaporization of hot blowdown Water (waste Water) from boiler 24 which is introduced to the quench pot via line 32.
  • hot blowdown water to quench the hot recycle gases is a particularly preferred mode of carrying out the present invention as it contributes to a relatively high efficiency for the overall process of the present invention, while eliminating waste disposal problem.
  • Oil is withdrawn from the bottom of the quench pot via line 33 and is pumped via pump 34 to the boiler 24 via line 35.
  • Quenched recycle gases are removed at a temperature of about 350 to 500 F. via line 36 yfrom the quench pot containing a sufficient amount of Water vapor for the gasification reaction in zone 2, including water which is formed by combustion in combustor 37 to achieve the temperature control of the gasification reaction in zone 2.
  • the amount of recycle gas, as well as the temperature of the recycle gas leaving recycle combustor 37, is the primary variable in controlling the maximum temperature and reaction rate in gasification zone 2.
  • the amount of water vapor in the recycle gas to the gasifier can be augmented by steam from boiler 24 with the steam being added to the recycle gas as shown by line 38. Additional steam may also be produced from boiler 24 via line 43.
  • the amount of H2O fed to the gasifier is controlled in the process of the present invention by the amount of water vaporized into the recycle gas in quench pot 27; secondly, by the amount of steam introduced into the recycle gas via line 38; and, thirdly, by the amount of gases combusted and the temperature of combustion in recycle combustor 37.
  • recycle gases from quench pot 27 are passed to the recycle combustor via recycle compressor 39 and then line 40.
  • Compressed air or pressurized oxygen, depending on the ultimate use for the product gas, is introduced to recycle combustor 37 via line 41.
  • Recycle combustor 37 is preferably an in-line burner device.
  • the partially combusted recycle gas is withdrawn from recycle combustor 37, usually at a temperature of about 1900 F. and passed via line 42 to the bottom of gasification zone 2 to supply reactive gases and temperature control as well as the necessary heat for gasification zone 2.
  • a process for converting solid carbonaceous Waste material to combustible gases which comprises:
  • a process for converting solid carbonaceous material to combustible gases which comprises:
  • a process for converting solid carbonaceous waste material into combustible gases which comprises:
  • said quenched gases are at a temperature in the range from about 350 F. to 450 F.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Coke Industry (AREA)
US00252449A 1972-05-11 1972-05-11 Gasification of solid carbonaceous waste material Expired - Lifetime US3817724A (en)

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US00252449A US3817724A (en) 1972-05-11 1972-05-11 Gasification of solid carbonaceous waste material
JP48051531A JPS5239602B2 (enrdf_load_stackoverflow) 1972-05-11 1973-05-09
CA170,978A CA998530A (en) 1972-05-11 1973-05-10 Gasification of solid carbonaceous waste material

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JP (1) JPS5239602B2 (enrdf_load_stackoverflow)
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Cited By (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3907519A (en) * 1972-05-11 1975-09-23 Chevron Res Gasification of solid carbonaceous materials to obtain high BTU product gas
US4005994A (en) * 1975-12-22 1977-02-01 Syngas Recycling Corporation Process and apparatus for converting solid wastes to pipeline gas
US4206186A (en) * 1975-02-06 1980-06-03 Holter Gesellschaft Fur Patentverwertungsverfahren Mbh Refuse pyrolysis
DE3121206A1 (de) * 1980-05-29 1982-02-04 Union Carbide Corp., 10017 New York, N.Y. Verfahren zum beseitigen von festem abfall
US4638629A (en) * 1984-11-05 1987-01-27 Westinghouse Electric Corp. Process for electric power production using a biogas
GB2244548A (en) * 1990-05-10 1991-12-04 Brian Reginald Harfield Incinerating waste
US5425792A (en) * 1992-05-07 1995-06-20 Hylsa, S.A. De C.V. Method for gasifying organic materials
US5656044A (en) * 1992-05-07 1997-08-12 Hylsa S.A. De C.V. Method and apparatus for gasification of organic materials
US5851246A (en) * 1992-05-07 1998-12-22 Hylsa, S.A. De C.V. Apparatus for gasifying organic materials
US20050155288A1 (en) * 2003-08-04 2005-07-21 Rogers Michael W. Gasification apparatus and method
US20060249021A1 (en) * 2003-08-04 2006-11-09 Rogers Michael W Gasification apparatus
DE102006056480A1 (de) * 2006-11-28 2008-05-29 Berthold, Hermann Verfahren und Anlage zur Energiegewinnung durch Müllvergasung
DE102008010919A1 (de) 2008-02-25 2009-09-03 Markus Franssen Abfallverwertungsanlage zur Erzeugung von Energie
DE102009014410A1 (de) 2008-03-31 2009-10-01 Etag Production Gmbh Abfallverwertungsanlage zur Erzeugung von Energie
US20110209478A1 (en) * 2009-03-11 2011-09-01 Minoru Morita Method of power generation by waste combustion and waste combustion system
US20130067763A1 (en) * 2010-05-12 2013-03-21 Woongjin Coway Co., Ltd. Method of controlling the finishing of operation of a drying furnace assembly in a food waste disposer
JP2013544946A (ja) * 2010-12-08 2013-12-19 エスケー イノベーション シーオー．， エルティーディー． 二酸化炭素の排出が低減されるガス化方法
EP2706103A1 (fr) * 2012-09-05 2014-03-12 Commissariat A L'energie Atomique Et Aux Energies Alternatives Procédé de gazéification de charge de matière carbonée à rendement amélioré
US11215360B2 (en) * 2015-08-18 2022-01-04 Glock Ökoenergie Gmbh Method and device for drying wood chips

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* Cited by examiner, † Cited by third party
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JPS5648285A (en) * 1979-09-26 1981-05-01 Imamura Seisakusho:Kk Treating apparatus for content of vessel in treating tank
JPS59500275A (ja) * 1982-03-01 1984-02-23 ザ　エナジ−　イクイツプメント　カンパニ−　リミテツド 可燃性ガス発生装置
JPS58225191A (ja) * 1982-06-24 1983-12-27 Nippon Kokan Kk <Nkk> 流動層による石炭のガス化方法及びその装置

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US3511194A (en) * 1968-03-25 1970-05-12 Torrax Systems Method and apparatus for high temperature waste disposal

Cited By (27)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3907519A (en) * 1972-05-11 1975-09-23 Chevron Res Gasification of solid carbonaceous materials to obtain high BTU product gas
US4206186A (en) * 1975-02-06 1980-06-03 Holter Gesellschaft Fur Patentverwertungsverfahren Mbh Refuse pyrolysis
US4005994A (en) * 1975-12-22 1977-02-01 Syngas Recycling Corporation Process and apparatus for converting solid wastes to pipeline gas
DE3121206A1 (de) * 1980-05-29 1982-02-04 Union Carbide Corp., 10017 New York, N.Y. Verfahren zum beseitigen von festem abfall
US4638629A (en) * 1984-11-05 1987-01-27 Westinghouse Electric Corp. Process for electric power production using a biogas
GB2244548B (en) * 1990-05-10 1994-12-21 Brian Reginald Harfield Waste disposal process
GB2244548A (en) * 1990-05-10 1991-12-04 Brian Reginald Harfield Incinerating waste
US5425792A (en) * 1992-05-07 1995-06-20 Hylsa, S.A. De C.V. Method for gasifying organic materials
US5656044A (en) * 1992-05-07 1997-08-12 Hylsa S.A. De C.V. Method and apparatus for gasification of organic materials
US5851246A (en) * 1992-05-07 1998-12-22 Hylsa, S.A. De C.V. Apparatus for gasifying organic materials
US7964026B2 (en) * 2003-08-04 2011-06-21 Power Reclamation, Inc. Gasification apparatus
US20050155288A1 (en) * 2003-08-04 2005-07-21 Rogers Michael W. Gasification apparatus and method
US20060249021A1 (en) * 2003-08-04 2006-11-09 Rogers Michael W Gasification apparatus
DE102006056480A1 (de) * 2006-11-28 2008-05-29 Berthold, Hermann Verfahren und Anlage zur Energiegewinnung durch Müllvergasung
WO2008064661A3 (de) * 2006-11-28 2008-09-25 Hermann Berthold Verfahren und anlage zur nutzenergieerzeugung durch müllvergasung
US20100307392A1 (en) * 2006-11-28 2010-12-09 Hermann Berthold Method and installation for the generation of effective energy by gasifying waste
DE102006056480B4 (de) * 2006-11-28 2008-09-04 Berthold, Hermann Verfahren und Anlage zur Nutzenergiegewinnung durch Müllvergasung
DE102008010919A1 (de) 2008-02-25 2009-09-03 Markus Franssen Abfallverwertungsanlage zur Erzeugung von Energie
EP2110520A2 (de) 2008-02-25 2009-10-21 Markus Franssen Abfallverwertungsanlage zur Erzeugung von Energie
DE102009014410A1 (de) 2008-03-31 2009-10-01 Etag Production Gmbh Abfallverwertungsanlage zur Erzeugung von Energie
US20110209478A1 (en) * 2009-03-11 2011-09-01 Minoru Morita Method of power generation by waste combustion and waste combustion system
US8893498B2 (en) * 2009-03-11 2014-11-25 Tsukishima Kankyo Engineering Ltd. Method of power generation by waste combustion and waste combustion system
US20130067763A1 (en) * 2010-05-12 2013-03-21 Woongjin Coway Co., Ltd. Method of controlling the finishing of operation of a drying furnace assembly in a food waste disposer
JP2013544946A (ja) * 2010-12-08 2013-12-19 エスケー イノベーション シーオー．， エルティーディー． 二酸化炭素の排出が低減されるガス化方法
EP2650258A4 (en) * 2010-12-08 2015-03-25 Sk Innovation Co Ltd GASIFICATION METHOD FOR REDUCING EMISSIONS OF CARBON DIOXIDE
EP2706103A1 (fr) * 2012-09-05 2014-03-12 Commissariat A L'energie Atomique Et Aux Energies Alternatives Procédé de gazéification de charge de matière carbonée à rendement amélioré
US11215360B2 (en) * 2015-08-18 2022-01-04 Glock Ökoenergie Gmbh Method and device for drying wood chips

Also Published As

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CA998530A (en) 1976-10-19
JPS5239602B2 (enrdf_load_stackoverflow) 1977-10-06
JPS4961203A (enrdf_load_stackoverflow) 1974-06-13

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