US3817725A - Gasification of solid waste material to obtain high btu product gas - Google Patents

Gasification of solid waste material to obtain high btu product gas Download PDF

Info

Publication number
US3817725A
US3817725A US00252450A US25245072A US3817725A US 3817725 A US3817725 A US 3817725A US 00252450 A US00252450 A US 00252450A US 25245072 A US25245072 A US 25245072A US 3817725 A US3817725 A US 3817725A
Authority
US
United States
Prior art keywords
gases
gasification
zone
gas
gasification zone
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
Application number
US00252450A
Inventor
R Sieg
R White
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Chevron USA Inc
Original Assignee
Chevron Research and Technology Co
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Chevron Research and Technology Co filed Critical Chevron Research and Technology Co
Priority to US00252450A priority Critical patent/US3817725A/en
Priority to US475061A priority patent/US3907519A/en
Application granted granted Critical
Publication of US3817725A publication Critical patent/US3817725A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/08—Production of synthetic natural 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
    • 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
    • C10J2300/18—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

Definitions

  • the present invention relates to gasification of solid 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 vortical motion by jets of heated gas directed along the heated walls transversely to the direction of passage.
  • coal distillation is not gasification. Distillation drives ofl? 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 downflowing shale particles.
  • the hot gas is obtained by heating a portion of the gas eflluent 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 H O 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.
  • the present invention is based on the combination of waste solids gasification with the methanation and recycling of a portion of the combustible gas efliuent from the gasification zone.
  • temperature control in the gasification zone is preferably obtained by partially or wholly burning a second portion of the effluent gases from the gasification zone and then recycling the hot gases thus obtained to the gasification zone.
  • gasification reactions are carried out in the gasification zone to generate hydrogen and carbon oxides from hydrocarbonaceous matter in the gasification zone and also to generate hydrogen from the H 0 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 wastes to high B.t.u. gas.
  • high B.t.u. gas is used herein to mean gas having a B.t.u. value of at least B.t.u. per cubic foot and preferably above 300 B.t.u. per cubic foot.
  • B.t.u. content would be closer to 300 B.t.u./ft. and with both CO removal from the product gas and use of purified oxygen (instead of air) for the burning of said recycled second portion, the B.t.u. content would be about 400-800 B.t.u./ftfi.
  • solid waste material is used herein to connote municipal garbage, industrial or agricultural wastes which are organic, such as cellulosic solids, dried or partially dried sewage, and such as cellulosic solids, dried or partially dried sewage, and like solid waste materials.
  • methanation is used herein to mean conversion of carbon oxides and H to methane by reaction of the carbon oxides with H
  • methanation is used herein to mean conversion of carbon oxides and H to methane by reaction of the carbon oxides with H
  • the methanation reaction is exothermic, and this exothermic heat of reaction is integrated into the process of the present invention to supply a portion of the heat required for the endothermic reactions in the gasification zone.
  • the temperatures in the gasification zone are highly advantageously controlled by means of adjusting the temperature and/or amount of methanated gases recycled to the gasification zone and preferably also by means of adjusting external to the gasification zone the temperature and/or amount of a second hot recycle gas stream to the gasification zone.
  • the temperatures in the gasification zone can be controlled pursuant to the present invention by controlling both the amount of each hot recycle gas stream and the temperature of each recycle gas.
  • all four of these variables 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 gasification zone at minimum energy requirement for recycle gas compression, but yet to maintain temperatures in the gasification zone below about 2000 F.
  • One of the particular advantages of the present invention is that the recycle of methanated gases allows an added means for temperature control in the gasification zone.
  • the main means of heat input and temperature control in the gasification zone is by the second hot recycle gas stream.
  • the advantageous services which are afiorded by the integrated methanation step include the following:
  • the methanated gases are introduced at a central position along the length of said gasifier, feed waste material is introduced at an upper position along the length of said gasifier and heating gases are introduced at a lower position along the length of said gasifier.
  • the gases obtained from the gasification zone are preferably cooled and cleansed by 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 reactive 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 gas. Thus, there will be H and CO present in the gasification zone for conversion of carbon and hydrocarbons into hydrogen and carbon monoxide according to well known reactions such as 4 BRIEF DESCRIPTION OF THE DRAWING
  • the drawing is a schematic process flow diagram illustrating a preferred embodiment of the present invention.
  • 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.
  • Other solid feeds e.g. carbonaceous f'eeds such as coal, peat, lignite or the like, can be fed to the process of the present invention, but a critical concept for the preferred embodiment of the present invention is the use of the process of present invention to convert solid waste material to high B.t.u. gas.
  • the solids can be considered to undergo a series of steps or reactions in the gasification zone including, for example, H O 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. Makeup water and preferably an alkali carbonate catalyst is introduced via line 5. The water serves to quench the gasifier effluent, and the hot gasifier efiiuent gases serve to heat water for efiicient subsequent use in the gasifier. The heated water is ultimately recycled via lines 9 and 10 to gasifier 2.
  • the water preferably carries alkali carbonate catalyst to the gasifier to catalyze 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 is withdrawn from quench drum 6 via line 9 and passed to settler 11 via line 9.
  • Oily sludge material, water, and preferably alkali catalyst 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 introduced to the quench drum at a temperature of about 600 F., and the water scrub in the quench drum cools the gases to a temperature of 350 '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 recycle back to the gasification zone, and a second stream 15 which can be referred to as a product gas stream.
  • recycle gases from quench drum 6 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 2000 F. and passed via line 25 to the bottom of gasification zone 2 to supply reactive gases and temperature control as well as heat for gasification zone 2.
  • recycle gas is passed via lines 23 and 27 to methanation zone 28.
  • methane is formed by reacting carbon oxides with hydrogen.
  • the carbon oxidesand hydrogen are present in the recycle gas due to gasification reactions inticianier 2.
  • the methanation reaction is carried out catalytically over a methanation catalyst.
  • Such catalysts are known in the art and typically contain nickel.
  • sulfur removal should be effected before the recycle gases are introduced to the methanator.
  • Sulfur compounds can be removed by many known methods, such as by use of a bed of solid particles containing zinc oxide.
  • the gases fed to the methanation zone will be preheated to about 500700 F and, due to the exothermic heat of the methanation reaction, the methanated gases leaves the methanator at about 650-1000 F.
  • One of the advantageous features of the present invention is the utilization of this exothermic heat of reaction in the solid wastes gasification reaction zone.
  • the methanated gases are passed via lines 29 and 31 to gasifier 2.
  • Stream 15 can be the entire product stream, but advantageously a portion or all of the product gases are withdrawn, after methanation, from methanation zone 28 via lines 29, 31 and 33. Gases withdrawn from the methanation step have a higher B.t.u. content than the gases in line 15, and thus the process of the present invention has the advantage of adjustable B.t.u. content for the product gas by, e.g., blending various portions of stream 15 with stream 33.
  • the product high B.t.u. gas can be used as town gas in residential gas burning appliances or as a fuel gas for industrial furnaces.
  • Heat recovery zone 32 connotes recovery of heat from product gases withdraw from the methanation step; this heat recovery step is advantageously integrated into the process of the present invention as a heat input source for the feed gas to methanation zone 28.
  • a process for converting solid Waste material to combustible gases which comprises:
  • gasification zone comprises an upright cylindrical gasifier reactor vessel and the methanated gases are introduced at a central position along the length of said gasifier, feed waste material is introduced at an upper position along the length of said gasifier, and heating gases are introduced at a lower position along the length of said gasifier.
  • a process for converting solid waste material to combustible gases, said process being free of carbon dioxide removal stages which comprises:
  • a process'of claim 1 wherein a portion of the combustible gases from the gasification zone is combined with a portion of the gases from the methanation zone to form a net product combustible gas.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

(D) WITHDRAWING NET PRODUCT COMBUSTIBLE GASES FROM THE GASIFICATION ZONE OR FROM THE METHANATION ZONE.

A PROCESS FOR CONVERTING SOLID WASTE MATERIAL TO COMBUSTIBLE GASES WHICH COMPRISES: (A) HEATING AND REACTING THE WASTE MATERIAL WITH REACTIVE GASES IN A GASIFICATION ZONE TO OBTAIN SAID COMBUSTIBLE GASES AND WITHDRAWING THE COMBUSTIBLE GASES FROM THE GASIFICATION ZONE, (B) METHANATING AT LEAST A PORTION OF SAID COMBUSTIBLE GASES IN A METHANATION ZONE TO OBTAIN METHANATED GASES, (C) FEEDING AT LEAST A PORTION OF SAID METHANATED GASES TO THE GASIFICATION ZONE, AND

Description

June 18, 1974 R. P. SIEG El'AL 3,812,725 GASIFICATION OF SOLID WASTE MATERIAL TO OBTAIN HIGH B.T.U. PRODUCT GAS Filed May 11, 1972 l5 MAKE-UP WATER A +nq2 CO3 OR K2 CO3 PRODUCT HIGH BTU GAS m COMPRESSOR 7 RECYCLE GAS Cb WASTE) 4 7 GASIFIER i A SOLID WASTES QUENCH DRUM ' I RECOVERED .r PRODUCT 9 OIL HIGH BTU GAS SETTLER 33 ASH RECYCLE HEAT COMBUSTOR 2o RECOVERY 1 v A AIR 3/ 29 METHANATION Smtes Patent Ofice 3,817,725 Patented June 18, 1974 3,817,725 GASIFICATION F SOLID WASTE MATERIAL TO OBTAIN HIGH B.T.U. PRODUCT GAS Robert P. Sieg, Piedmont, and Robert J. White, Pinole,
Califi, assignors to Chevron Research Company, San
Francisco, Calif.
Filed May 11, 1972, Ser. No. 252,450 Int. Cl. C103 3/00, 3/16 U.S. Cl. 48-209 8 Claims ABSTRACT OF THE DISCLOSURE RELATED APPLICATIONS The commonly-assigned application of John R. B. Ellis and Frederick C. Franklin titled Gasification of Solid Carbonaceous Waste Material, filed concurrently with the present application, is related to this application.
BACKGROUND OF THE INVENTION The present invention relates to gasification of solid material.
Previous gasification methods for solids mostly fall into the classifications of eduction processes or partial oxidation processes.
Eduction type processes are described in U.S. Pat. No. 1,055,334, Process of Making Gas; U.S. Pat. No. 2,640,- 014, Oil-Shale Eduction Process and Apparatus; and U.S. Pat. No. 3,361,644, Shale Retorting Process.
According to the U.S. Pat. No. 1,055,334, 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 vortical motion by jets of heated gas directed along the heated walls transversely to the direction of passage.
It can be noted, however, that coal distillation is not gasification. Distillation drives ofl? volatile matter already present; gasification creates volatiles not originally present.
In the process of U.S. Pat. 2,640,014, 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.
According to U.S. Pat. 3,361,644, gases and oil are educted from shale by passing oxygen-free hot gas countercurrent to downflowing shale particles. The hot gas is obtained by heating a portion of the gas eflluent 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 H O 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.
These processes all involve injection of oxygen into the reaction zone. Also, steam is usually injected into the reaction zone.
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.
Production of hydrogen and other combustible gases from waste substances produced in the manufacture of paper from wood chips and the like has been discussed in the literature, as, for example, in U.S. Pat. 3,317,292. In the manufacture of paper, wood chips are digested, for example, with an aqueous calcium sulfide liquid thereby forming calcium lignin sulfonate Waste product in solution, leaving wood pulp behind. As disclosed in U.S. Pat. 3,317,292, the waste substances containing ligninderived organic components can be converted to a gas mixture comprising hydrogen by contacting the waste material with steam in a reaction zone at an elevated temperature at least of the order of several hundred degrees centigrade.
Both US. Pat. 1,777,449, titled Process of Producing Gas From Garbage, and U.S. Pat. 3,471,275, titled Method of Disposal of Refuse, are directed to producing combustible gases in an externally heated retort rather than by introducing hot gases directly into the retort vessel.
SUMMARY According to the present invention a process is provided for converting solid waste material to combustible gases which comprises:
(a) Heating and reacting the Waste material with reactive gases in a gasification zone to obtain said combustible gases and withdrawing the combustible gases from the gasification zone,
(b) Methanating at least a portion of said combustible gases in a methanation zone to obtain methanated gases,
(c) Feeding a portion of said methanated gases to the gasification zone, and
(d) Withdrawing net product combustible gases from the gasification zone or from the methanation zone.
The present invention, among other features, is based on the combination of waste solids gasification with the methanation and recycling of a portion of the combustible gas efliuent from the gasification zone. Also, temperature control in the gasification zone is preferably obtained by partially or wholly burning a second portion of the effluent 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 and carbon oxides from hydrocarbonaceous matter in the gasification zone and also to generate hydrogen from the H 0 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 wastes to high B.t.u. gas.
The term high B.t.u. gas is used herein to mean gas having a B.t.u. value of at least B.t.u. per cubic foot and preferably above 300 B.t.u. per cubic foot. With CO removal from the product gas of the present invention the B.t.u. content would be closer to 300 B.t.u./ft. and with both CO removal from the product gas and use of purified oxygen (instead of air) for the burning of said recycled second portion, the B.t.u. content would be about 400-800 B.t.u./ftfi.
The term solid waste material is used herein to connote municipal garbage, industrial or agricultural wastes which are organic, such as cellulosic solids, dried or partially dried sewage, and such as cellulosic solids, dried or partially dried sewage, and like solid waste materials.
The term methanation is used herein to mean conversion of carbon oxides and H to methane by reaction of the carbon oxides with H For example:
The methanation reaction is exothermic, and this exothermic heat of reaction is integrated into the process of the present invention to supply a portion of the heat required for the endothermic reactions in the gasification zone. In the process of the present invention the temperatures in the gasification zone are highly advantageously controlled by means of adjusting the temperature and/or amount of methanated gases recycled to the gasification zone and preferably also by means of adjusting external to the gasification zone the temperature and/or amount of a second hot recycle gas stream to the gasification zone.
Thus, the temperatures in the gasification zone can be controlled pursuant to the present invention by controlling both the amount of each hot recycle gas stream and the temperature of each recycle gas. Usually all four of these variables 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 gasification zone at minimum energy requirement for recycle gas compression, but yet to maintain temperatures in the gasification zone below about 2000 F.
One of the particular advantages of the present invention is that the recycle of methanated gases allows an added means for temperature control in the gasification zone. Usually the main means of heat input and temperature control in the gasification zone is by the second hot recycle gas stream.
In the process of the present invention, the advantageous services which are afiorded by the integrated methanation step include the following:
(1) Increase B.t.u. of product gas by raising CH content of product gas.
(2) Provide heat input source for gasification reaction.
(3) Provide temperature control for gasification reaction.
To reduce the amount of reversal of the methanation reaction when the recycled methanated gases are introduced to the gasification reactor, it is preferable to introduce the methanated gases to about the middle of the reactor where the temperature is about 800-1200 F. versus about 1600-2000 F. at the bottom and ZOO-600 F. at the top. Thus, according to a preferred embodiment of the present invention wherein the gasification zone comprises an upright cylindrical gasifier reactor, the methanated gases are introduced at a central position along the length of said gasifier, feed waste material is introduced at an upper position along the length of said gasifier and heating gases are introduced at a lower position along the length of said gasifier.
The gases obtained from the gasification zone are preferably cooled and cleansed by 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 reactive 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 gas. Thus, there will be H and CO present in the gasification zone for conversion of carbon and hydrocarbons into hydrogen and carbon monoxide according to well known reactions such as 4 BRIEF DESCRIPTION OF THE DRAWING The drawing is a schematic process flow diagram illustrating a preferred embodiment of the present invention.
DETAILED DESCRIPTION OF THE DRAWING Referring more particularly to the drawing, 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. Other solid feeds, e.g. carbonaceous f'eeds such as coal, peat, lignite or the like, can be fed to the process of the present invention, but a critical concept for the preferred embodiment of the present invention is the use of the process of present invention to convert solid waste material to high B.t.u. gas.
The solids can be considered to undergo a series of steps or reactions in the gasification zone including, for example, H O distillation, oil distillation, pyrolysis, and gasification reactions such as previously mentioned. In the present invention there must be gasification reactions in the gasification zone.
Ashes are withdrawn from the bottom of the gasification zone as indicated via line 3.
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. Makeup water and preferably an alkali carbonate catalyst is introduced via line 5. The water serves to quench the gasifier effluent, and the hot gasifier efiiuent gases serve to heat water for efiicient subsequent use in the gasifier. The heated water is ultimately recycled via lines 9 and 10 to gasifier 2.
The water preferably carries alkali carbonate catalyst to the gasifier to catalyze 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 is withdrawn from quench drum 6 via line 9 and passed to settler 11 via line 9. Oily sludge material, water, and preferably alkali catalyst 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 introduced to the quench drum at a temperature of about 600 F., and the water scrub in the quench drum cools the gases to a temperature of 350 '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 recycle back to the gasification zone, and a second stream 15 which can be referred to as a product gas stream.
Preferably a portion of the recycle gases from quench drum 6 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 2000 F. and passed via line 25 to the bottom of gasification zone 2 to supply reactive gases and temperature control as well as heat for gasification zone 2.
In the present invention it is critical to methanate a portion of the recycle gases. Thus recycle gas is passed via lines 23 and 27 to methanation zone 28. In the methanation zone methane is formed by reacting carbon oxides with hydrogen. The carbon oxidesand hydrogen are present in the recycle gas due to gasification reactions in gasitier 2. Preferably the methanation reaction is carried out catalytically over a methanation catalyst. Such catalysts are known in the art and typically contain nickel.
If the methanation catalyst is sulfur sensitive, sulfur removal should be effected before the recycle gases are introduced to the methanator. Sulfur compounds can be removed by many known methods, such as by use of a bed of solid particles containing zinc oxide.
Usually the gases fed to the methanation zone will be preheated to about 500700 F and, due to the exothermic heat of the methanation reaction, the methanated gases leaves the methanator at about 650-1000 F. One of the advantageous features of the present invention is the utilization of this exothermic heat of reaction in the solid wastes gasification reaction zone. Thus the methanated gases are passed via lines 29 and 31 to gasifier 2.
Previously product gas stream 15 was mentioned. Stream 15 can be the entire product stream, but advantageously a portion or all of the product gases are withdrawn, after methanation, from methanation zone 28 via lines 29, 31 and 33. Gases withdrawn from the methanation step have a higher B.t.u. content than the gases in line 15, and thus the process of the present invention has the advantage of adjustable B.t.u. content for the product gas by, e.g., blending various portions of stream 15 with stream 33. The product high B.t.u. gas can be used as town gas in residential gas burning appliances or as a fuel gas for industrial furnaces.
Heat recovery zone 32 connotes recovery of heat from product gases withdraw from the methanation step; this heat recovery step is advantageously integrated into the process of the present invention as a heat input source for the feed gas to methanation zone 28.
Although various embodiments of the invention have been described, it is to be understood that they are meant to be illustrative only and not limiting. Certain features may be changed without departing from the spirit or scope of the present invention. It is apparent that the present invention has broad application to gasification of solid wastes with methanation of recycle gases to the gasification zone. Accordingly, the invention is not to be construed as limited to the specific embodiments discussed, but only as defined in the appended claims or substantial equivalents of the claims.
What is claimed is:
1. A process for converting solid Waste material to combustible gases which comprises:
(a) heating and reactingthe waste material with reactive gases in a gasification zone to obtain said combustible gases and withdrawing the combustible gases from the gasification zone,
(b) methanating at least a portion of said combustible bases in a methanation zone to obtain methanated gases, and
(c) feeding a portion of said methanated gases through the gasification zone thereby increasing the methane content and B.t.u. value of said combustible gases and transferring the sensible heat from said methanated gases to said gasification zone.
2. A process in accordance with claim 1 wherein the gasification zone comprises an upright cylindrical gasifier reactor vessel and the methanated gases are introduced at a central position along the length of said gasifier, feed waste material is introduced at an upper position along the length of said gasifier, and heating gases are introduced at a lower position along the length of said gasifier.
3. A process in accordance with claim 1, which comprises the further steps of (d) partially or wholly burning a portion of said combustible gases in a recycle gas combustion zone to obtain hot recycle gas containing essentially no oxygen, and
(e) passing the hot recycle into the gasification zone to supply heat and said reactive gases to the carbonaceous material.
4. A process in accordance with claim 3 wherein the temperature in the gasification zone is controlled to below about 2000 F. by means of adjusting the temperature of, or amount of, said hot recycle gas to the gasification zone.
5. A process for converting solid waste material to combustible gases, said process being free of carbon dioxide removal stages, which comprises:
I (a) heating and reacting the waste material with reactive gases in a gasification zone to obtain said combustible gases and withdrawing the combustible gases from the gasification zone,
(b) partially or wholly burning a portion of said withdrawn combustible gases in a recycle gas combustion zone to obtain hot recycle gas containing essentially no oxygen,
(c) passing the hot recycle gas into the gasification zone to supply heat and at least a portion of said reactive gases to the carbonaceous material,
(d) methanating at last a portion of said combustible gases in a methanation zone to obtain methanated gases, and
(e) feeding a portion of said methanated gases through the gasification zone thereby increasing the methane content and B.t.u. value of said combustible gases and transferringthe sensible heat from said methanation gases to said gasification zone.
6. A process in' accordance with claim 5 wherein the temperature in the gasification zone is controlled to below about 2000 F. by means of adjusting the temperature of or amount of said hot recycle gas to the gasification zone.
7. A process'of claim 1 wherein a portion of the combustible gases from the gasification zone is combined with a portion of the gases from the methanation zone to form a net product combustible gas.
8. A process of claim 5 wherein a portion of the combustible gases from the gasification zone is combined with a portion of the gases from the methanation zone to form a net product combustible gas.
References Cited UNITED STATES PATENTS 2,840,462 6/ 1958 Gorin 48-202 X 3,194,644 7/ 1965 Gorin et al 48202 X 3,471,275 10/ 1969 Borggreen 48l97 X 3,503,724 3/1970 Benson 48202 X 3,671,209 6/1972 Teichmann et a1. 48--215 2,238,367 4/ 1941' Mohr et al. 48-197 R 3,511,194 5/1970 Stookey 46-209 UX 3,702,039 11/1972 Stookey et a1 48209 X MORRIS O. WOLK, Primary Examiner R. E. SERWIN, Assistant Examiner US. Cl. X.R. 48-197 R
US00252450A 1972-05-11 1972-05-11 Gasification of solid waste material to obtain high btu product gas Expired - Lifetime US3817725A (en)

Priority Applications (2)

Application Number Priority Date Filing Date Title
US00252450A US3817725A (en) 1972-05-11 1972-05-11 Gasification of solid waste material to obtain high btu product gas
US475061A US3907519A (en) 1972-05-11 1974-05-31 Gasification of solid carbonaceous materials to obtain high BTU product gas

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US00252450A US3817725A (en) 1972-05-11 1972-05-11 Gasification of solid waste material to obtain high btu product gas

Publications (1)

Publication Number Publication Date
US3817725A true US3817725A (en) 1974-06-18

Family

ID=22956058

Family Applications (1)

Application Number Title Priority Date Filing Date
US00252450A Expired - Lifetime US3817725A (en) 1972-05-11 1972-05-11 Gasification of solid waste material to obtain high btu product gas

Country Status (1)

Country Link
US (1) US3817725A (en)

Cited By (51)

* 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
FR2534926A1 (en) * 1982-10-25 1984-04-27 Charbonnages Ste Chimique Process for the manufacture of fuel gas or synthesis gas from divided biomass.
US20090217584A1 (en) * 2008-02-29 2009-09-03 Greatpoint Energy, Inc. Steam Generation Processes Utilizing Biomass Feedstocks
WO2009124017A2 (en) * 2008-04-01 2009-10-08 Greatpoint Energy, Inc. Processes for the separation of methane from a gas stream
US20090260287A1 (en) * 2008-02-29 2009-10-22 Greatpoint Energy, Inc. Process and Apparatus for the Separation of Methane from a Gas Stream
US20090324459A1 (en) * 2008-06-27 2009-12-31 Greatpoint Energy, Inc. Three-Train Catalytic Gasification Systems
US20100076235A1 (en) * 2008-09-19 2010-03-25 Greatpoint Energy, Inc. Processes for Gasification of a Carbonaceous Feedstock
US20100179232A1 (en) * 2008-10-23 2010-07-15 Greatpoint Energy, Inc. Processes for Gasification of a Carbonaceous Feedstock
US20100287835A1 (en) * 2009-05-13 2010-11-18 Greatpoint Energy, Inc. Processes for Hydromethanation of a Carbonaceous Feedstock
US20110062722A1 (en) * 2009-09-16 2011-03-17 Greatpoint Energy, Inc. Integrated hydromethanation combined cycle process
US20110062721A1 (en) * 2009-09-16 2011-03-17 Greatpoint Energy, Inc. Integrated hydromethanation combined cycle process
US20110088896A1 (en) * 2009-10-19 2011-04-21 Greatpoint Energy, Inc. Integrated enhanced oil recovery process
US20110207002A1 (en) * 2010-02-23 2011-08-25 Greatpoint Energy, Inc. Integrated Hydromethanation Fuel Cell Power Generation
US8123827B2 (en) 2007-12-28 2012-02-28 Greatpoint Energy, Inc. Processes for making syngas-derived products
US8192716B2 (en) 2008-04-01 2012-06-05 Greatpoint Energy, Inc. Sour shift process for the removal of carbon monoxide from a gas stream
US8268899B2 (en) 2009-05-13 2012-09-18 Greatpoint Energy, Inc. Processes for hydromethanation of a carbonaceous feedstock
US8286901B2 (en) 2008-02-29 2012-10-16 Greatpoint Energy, Inc. Coal compositions for catalytic gasification
US8297542B2 (en) 2008-02-29 2012-10-30 Greatpoint Energy, Inc. Coal compositions for catalytic gasification
US8349039B2 (en) 2008-02-29 2013-01-08 Greatpoint Energy, Inc. Carbonaceous fines recycle
US8361428B2 (en) 2008-02-29 2013-01-29 Greatpoint Energy, Inc. Reduced carbon footprint steam generation processes
US8366795B2 (en) 2008-02-29 2013-02-05 Greatpoint Energy, Inc. Catalytic gasification particulate compositions
US8479833B2 (en) 2009-10-19 2013-07-09 Greatpoint Energy, Inc. Integrated enhanced oil recovery process
US8502007B2 (en) 2008-09-19 2013-08-06 Greatpoint Energy, Inc. Char methanation catalyst and its use in gasification processes
US8557878B2 (en) 2010-04-26 2013-10-15 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock with vanadium recovery
US8647402B2 (en) 2008-09-19 2014-02-11 Greatpoint Energy, Inc. Processes for gasification of a carbonaceous feedstock
US8648121B2 (en) 2011-02-23 2014-02-11 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock with nickel recovery
US8653149B2 (en) 2010-05-28 2014-02-18 Greatpoint Energy, Inc. Conversion of liquid heavy hydrocarbon feedstocks to gaseous products
US8652222B2 (en) 2008-02-29 2014-02-18 Greatpoint Energy, Inc. Biomass compositions for catalytic gasification
US8652696B2 (en) 2010-03-08 2014-02-18 Greatpoint Energy, Inc. Integrated hydromethanation fuel cell power generation
US8728182B2 (en) 2009-05-13 2014-05-20 Greatpoint Energy, Inc. Processes for hydromethanation of a carbonaceous feedstock
US8733459B2 (en) 2009-12-17 2014-05-27 Greatpoint Energy, Inc. Integrated enhanced oil recovery process
US8734547B2 (en) 2008-12-30 2014-05-27 Greatpoint Energy, Inc. Processes for preparing a catalyzed carbonaceous particulate
US8734548B2 (en) 2008-12-30 2014-05-27 Greatpoint Energy, Inc. Processes for preparing a catalyzed coal particulate
US8748687B2 (en) 2010-08-18 2014-06-10 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock
US9012524B2 (en) 2011-10-06 2015-04-21 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock
US9034058B2 (en) 2012-10-01 2015-05-19 Greatpoint Energy, Inc. Agglomerated particulate low-rank coal feedstock and uses thereof
US9034061B2 (en) 2012-10-01 2015-05-19 Greatpoint Energy, Inc. Agglomerated particulate low-rank coal feedstock and uses thereof
US9127221B2 (en) 2011-06-03 2015-09-08 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock
US9234149B2 (en) 2007-12-28 2016-01-12 Greatpoint Energy, Inc. Steam generating slurry gasifier for the catalytic gasification of a carbonaceous feedstock
US9273260B2 (en) 2012-10-01 2016-03-01 Greatpoint Energy, Inc. Agglomerated particulate low-rank coal feedstock and uses thereof
US9328920B2 (en) 2012-10-01 2016-05-03 Greatpoint Energy, Inc. Use of contaminated low-rank coal for combustion
US9353322B2 (en) 2010-11-01 2016-05-31 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock
EP3156519A1 (en) * 2015-10-16 2017-04-19 Volkswagen Aktiengesellschaft Method and appartus for producing a hydrocarbon
US10344231B1 (en) 2018-10-26 2019-07-09 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock with improved carbon utilization
US10435637B1 (en) 2018-12-18 2019-10-08 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock with improved carbon utilization and power generation
US10464872B1 (en) 2018-07-31 2019-11-05 Greatpoint Energy, Inc. Catalytic gasification to produce methanol
US10618818B1 (en) 2019-03-22 2020-04-14 Sure Champion Investment Limited Catalytic gasification to produce ammonia and urea
US11097283B2 (en) 2018-10-30 2021-08-24 New Planet Energy Development Llc Systems and methods for municipal solid waste recycling facility
US11286436B2 (en) 2019-02-04 2022-03-29 Eastman Chemical Company Feed location for gasification of plastics and solid fossil fuels
US11447576B2 (en) 2019-02-04 2022-09-20 Eastman Chemical Company Cellulose ester compositions derived from recycled plastic content syngas
US11939406B2 (en) 2019-03-29 2024-03-26 Eastman Chemical Company Polymers, articles, and chemicals made from densified textile derived syngas

Cited By (65)

* 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
FR2534926A1 (en) * 1982-10-25 1984-04-27 Charbonnages Ste Chimique Process for the manufacture of fuel gas or synthesis gas from divided biomass.
US8123827B2 (en) 2007-12-28 2012-02-28 Greatpoint Energy, Inc. Processes for making syngas-derived products
US9234149B2 (en) 2007-12-28 2016-01-12 Greatpoint Energy, Inc. Steam generating slurry gasifier for the catalytic gasification of a carbonaceous feedstock
US8361428B2 (en) 2008-02-29 2013-01-29 Greatpoint Energy, Inc. Reduced carbon footprint steam generation processes
US8366795B2 (en) 2008-02-29 2013-02-05 Greatpoint Energy, Inc. Catalytic gasification particulate compositions
US20090260287A1 (en) * 2008-02-29 2009-10-22 Greatpoint Energy, Inc. Process and Apparatus for the Separation of Methane from a Gas Stream
US8349039B2 (en) 2008-02-29 2013-01-08 Greatpoint Energy, Inc. Carbonaceous fines recycle
US8297542B2 (en) 2008-02-29 2012-10-30 Greatpoint Energy, Inc. Coal compositions for catalytic gasification
US8286901B2 (en) 2008-02-29 2012-10-16 Greatpoint Energy, Inc. Coal compositions for catalytic gasification
US8709113B2 (en) 2008-02-29 2014-04-29 Greatpoint Energy, Inc. Steam generation processes utilizing biomass feedstocks
US20090217584A1 (en) * 2008-02-29 2009-09-03 Greatpoint Energy, Inc. Steam Generation Processes Utilizing Biomass Feedstocks
US8652222B2 (en) 2008-02-29 2014-02-18 Greatpoint Energy, Inc. Biomass compositions for catalytic gasification
WO2009124017A3 (en) * 2008-04-01 2010-01-14 Greatpoint Energy, Inc. Processes for the separation of methane from a gas stream
US8999020B2 (en) 2008-04-01 2015-04-07 Greatpoint Energy, Inc. Processes for the separation of methane from a gas stream
US8192716B2 (en) 2008-04-01 2012-06-05 Greatpoint Energy, Inc. Sour shift process for the removal of carbon monoxide from a gas stream
WO2009124017A2 (en) * 2008-04-01 2009-10-08 Greatpoint Energy, Inc. Processes for the separation of methane from a gas stream
US20090324459A1 (en) * 2008-06-27 2009-12-31 Greatpoint Energy, Inc. Three-Train Catalytic Gasification Systems
US8647402B2 (en) 2008-09-19 2014-02-11 Greatpoint Energy, Inc. Processes for gasification of a carbonaceous feedstock
US8328890B2 (en) 2008-09-19 2012-12-11 Greatpoint Energy, Inc. Processes for gasification of a carbonaceous feedstock
US20100076235A1 (en) * 2008-09-19 2010-03-25 Greatpoint Energy, Inc. Processes for Gasification of a Carbonaceous Feedstock
US8502007B2 (en) 2008-09-19 2013-08-06 Greatpoint Energy, Inc. Char methanation catalyst and its use in gasification processes
US8202913B2 (en) 2008-10-23 2012-06-19 Greatpoint Energy, Inc. Processes for gasification of a carbonaceous feedstock
US20100179232A1 (en) * 2008-10-23 2010-07-15 Greatpoint Energy, Inc. Processes for Gasification of a Carbonaceous Feedstock
US8734548B2 (en) 2008-12-30 2014-05-27 Greatpoint Energy, Inc. Processes for preparing a catalyzed coal particulate
US8734547B2 (en) 2008-12-30 2014-05-27 Greatpoint Energy, Inc. Processes for preparing a catalyzed carbonaceous particulate
US20100287835A1 (en) * 2009-05-13 2010-11-18 Greatpoint Energy, Inc. Processes for Hydromethanation of a Carbonaceous Feedstock
US8268899B2 (en) 2009-05-13 2012-09-18 Greatpoint Energy, Inc. Processes for hydromethanation of a carbonaceous feedstock
US8728183B2 (en) 2009-05-13 2014-05-20 Greatpoint Energy, Inc. Processes for hydromethanation of a carbonaceous feedstock
US8728182B2 (en) 2009-05-13 2014-05-20 Greatpoint Energy, Inc. Processes for hydromethanation of a carbonaceous feedstock
WO2011034890A3 (en) * 2009-09-16 2011-06-30 Greatpoint Energy, Inc. Integrated hydromethanation combined cycle process
US20110062721A1 (en) * 2009-09-16 2011-03-17 Greatpoint Energy, Inc. Integrated hydromethanation combined cycle process
US20110062722A1 (en) * 2009-09-16 2011-03-17 Greatpoint Energy, Inc. Integrated hydromethanation combined cycle process
US8479834B2 (en) 2009-10-19 2013-07-09 Greatpoint Energy, Inc. Integrated enhanced oil recovery process
US8479833B2 (en) 2009-10-19 2013-07-09 Greatpoint Energy, Inc. Integrated enhanced oil recovery process
US20110088896A1 (en) * 2009-10-19 2011-04-21 Greatpoint Energy, Inc. Integrated enhanced oil recovery process
US8733459B2 (en) 2009-12-17 2014-05-27 Greatpoint Energy, Inc. Integrated enhanced oil recovery process
US20110207002A1 (en) * 2010-02-23 2011-08-25 Greatpoint Energy, Inc. Integrated Hydromethanation Fuel Cell Power Generation
US8669013B2 (en) 2010-02-23 2014-03-11 Greatpoint Energy, Inc. Integrated hydromethanation fuel cell power generation
US8652696B2 (en) 2010-03-08 2014-02-18 Greatpoint Energy, Inc. Integrated hydromethanation fuel cell power generation
US8557878B2 (en) 2010-04-26 2013-10-15 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock with vanadium recovery
US8653149B2 (en) 2010-05-28 2014-02-18 Greatpoint Energy, Inc. Conversion of liquid heavy hydrocarbon feedstocks to gaseous products
US8748687B2 (en) 2010-08-18 2014-06-10 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock
US9353322B2 (en) 2010-11-01 2016-05-31 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock
US8648121B2 (en) 2011-02-23 2014-02-11 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock with nickel recovery
US9127221B2 (en) 2011-06-03 2015-09-08 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock
US9012524B2 (en) 2011-10-06 2015-04-21 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock
US9034061B2 (en) 2012-10-01 2015-05-19 Greatpoint Energy, Inc. Agglomerated particulate low-rank coal feedstock and uses thereof
US9273260B2 (en) 2012-10-01 2016-03-01 Greatpoint Energy, Inc. Agglomerated particulate low-rank coal feedstock and uses thereof
US9328920B2 (en) 2012-10-01 2016-05-03 Greatpoint Energy, Inc. Use of contaminated low-rank coal for combustion
US9034058B2 (en) 2012-10-01 2015-05-19 Greatpoint Energy, Inc. Agglomerated particulate low-rank coal feedstock and uses thereof
EP3156519A1 (en) * 2015-10-16 2017-04-19 Volkswagen Aktiengesellschaft Method and appartus for producing a hydrocarbon
US10464872B1 (en) 2018-07-31 2019-11-05 Greatpoint Energy, Inc. Catalytic gasification to produce methanol
US10344231B1 (en) 2018-10-26 2019-07-09 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock with improved carbon utilization
US11097283B2 (en) 2018-10-30 2021-08-24 New Planet Energy Development Llc Systems and methods for municipal solid waste recycling facility
US10435637B1 (en) 2018-12-18 2019-10-08 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock with improved carbon utilization and power generation
US11286436B2 (en) 2019-02-04 2022-03-29 Eastman Chemical Company Feed location for gasification of plastics and solid fossil fuels
US11312914B2 (en) 2019-02-04 2022-04-26 Eastman Chemical Company Gasification of plastics and solid fossil fuels to produce organic compounds
US11370983B2 (en) 2019-02-04 2022-06-28 Eastman Chemical Company Gasification of plastics and solid fossil fuels
US11447576B2 (en) 2019-02-04 2022-09-20 Eastman Chemical Company Cellulose ester compositions derived from recycled plastic content syngas
US11802251B2 (en) 2019-02-04 2023-10-31 Eastman Chemical Company Feed location for gasification of plastics and solid fossil fuels
US11939546B2 (en) 2019-02-04 2024-03-26 Eastman Chemical Company Gasification of plastics and solid fossil fuels to produce organic compounds
US11939547B2 (en) 2019-02-04 2024-03-26 Eastman Chemical Company Gasification of plastics and solid fossil fuels
US10618818B1 (en) 2019-03-22 2020-04-14 Sure Champion Investment Limited Catalytic gasification to produce ammonia and urea
US11939406B2 (en) 2019-03-29 2024-03-26 Eastman Chemical Company Polymers, articles, and chemicals made from densified textile derived syngas

Similar Documents

Publication Publication Date Title
US3817725A (en) Gasification of solid waste material to obtain high btu product gas
US4597776A (en) Hydropyrolysis process
US3817724A (en) Gasification of solid carbonaceous waste material
US3746522A (en) Gasification of carbonaceous solids
US4497637A (en) Thermochemical conversion of biomass to syngas via an entrained pyrolysis/gasification process
CA1082921A (en) Method and apparatus for producing synthetic fuels from solid waste
US4699632A (en) Process for gasification of cellulosic materials
US4592762A (en) Process for gasification of cellulosic biomass
US4999030A (en) Process for producing a methane-containing fuel gas
US3759677A (en) Catalytic synthesis gas manufacture
US3194644A (en) Production of pipeline gas from
CN102076830A (en) A two-stage high-temperature preheated steam gasifier
US3874116A (en) Synthesis gas manufacture
AU2017333732A1 (en) Process for converting carbonaceous material into low tar synthesis gas
Perry The gasification of coal
Jenkins Thermal gasification of biomass—a primer
US4415431A (en) Integrated oxygasification and hydropyrolysis process for producing liquid and gaseous hydrocarbons
US4560547A (en) Production of hydrogen from oil shale
US4391612A (en) Gasification of coal
US3823227A (en) Hydrogen manufacture
US3907519A (en) Gasification of solid carbonaceous materials to obtain high BTU product gas
US10982151B2 (en) Process for converting carbonaceous material into low tar synthesis gas
US4336125A (en) Production of synthetic hydrocarbon fuels from peat
CA1199039A (en) Hydropyrolysis process
US4005994A (en) Process and apparatus for converting solid wastes to pipeline gas