US3871839A - Method of feeding solid carbonaceous material to a high temperature reaction zone - Google Patents

Method of feeding solid carbonaceous material to a high temperature reaction zone Download PDF

Info

Publication number
US3871839A
US3871839A US296959A US29695972A US3871839A US 3871839 A US3871839 A US 3871839A US 296959 A US296959 A US 296959A US 29695972 A US29695972 A US 29695972A US 3871839 A US3871839 A US 3871839A
Authority
US
United States
Prior art keywords
slurry
gasifier
solid carbonaceous
gas
carbonaceous material
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
US296959A
Other languages
English (en)
Inventor
Burton E Moody
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.)
Air Products and Chemicals Inc
Original Assignee
Air Products and Chemicals Inc
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 Air Products and Chemicals Inc filed Critical Air Products and Chemicals Inc
Priority to US296959A priority Critical patent/US3871839A/en
Priority to ZA737437*A priority patent/ZA737437B/xx
Priority to JP48111879A priority patent/JPS4974203A/ja
Priority to BE136472A priority patent/BE805825A/xx
Priority to FR7336219A priority patent/FR2202929B1/fr
Priority to DE19732350953 priority patent/DE2350953A1/de
Priority to GB4760473A priority patent/GB1407176A/en
Priority to PL1973165799A priority patent/PL96935B1/pl
Application granted granted Critical
Publication of US3871839A publication Critical patent/US3871839A/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
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/485—Entrained flow gasifiers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/50—Fuel charging devices
    • C10J3/506—Fuel charging devices for entrained flow gasifiers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0903—Feed preparation
    • C10J2300/0906—Physical processes, e.g. shredding, comminuting, chopping, sorting
    • 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
    • C10J2300/094—Char
    • 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
    • C10J2300/0943—Coke
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S48/00—Gas: heating and illuminating
    • Y10S48/07—Slurry

Definitions

  • ABSTRACT A method of feeding solid carbonaceous material to a gasifier operating under conditions of high temperature and pressure by forming a slurry of the carbonaceous material and a liquid vehicle, raising the internal pressure of the slurry to the operating level of the gas ifier, drying the carbonaceous material by entraining the carbonaceous material in a hot gas stream, and thereafter separating the carbonaceous material and feeding the carbonaceous material to the gasifier.
  • the method is adaptable to using the gasifier effluent to dry the carbonaceous material and includes using process materials such as char accumulated from the process and condensing steam to provide a portion of the source of carbonaceous materials and vehicle for the slurry.
  • Field of the Invention pertains to the feeding of solid carbonaceous material, e.g. coal, into a high-pressure, hightemperature reaction zone such as a coal gasifier.
  • a coal gasifier In coal gasification, finely pulverized coal is reacted in the presence of steam and air oxygen at elevated temperature and pressure to form an effluent gas. If the product is to be a low BTU content gas, it is subject toremoval of hydrogen sulfide and then used directly.
  • a high methane content gas is to be produced, the effluent gas is then subjected to various process steps including water shift reaction, acid gas removal and methanation thereby yielding a synthetic natural gas.
  • figsuch process is discgasgd in U.S. Pat. No. 2,840,462; another is the process referred to as the; BCR Two-Stage Super-Pressure Gasification Process developed by Bituminous Coal Research Incorporated of Monroeville, PA; and a third pertains to generation fo a synthetic gas by electrothermal hydrogasification developed by the Institute of Gas Technology of Chicago, ILL.
  • the finely divided carbonaceous material is fed to the gasification vessel by a conventional lock hopper feeding system, a piston feeder, and a hydrocarbon liquid slurry respectively after the coal has been ground to size, screened, dewatered, and stored in storage hoppers.
  • U.S. Pat. No. 3,207,102 discloses a slurry feed for a steam generating unit such as is found in a commercial electrical generating plant. Here again the slurry is not dewatered prior to injection into the furnace and the slurry is further comminuted by impingement against a breaker in the furnace zone.
  • U.S. Pat. No. 3,229,651 discloses an alternate slurry feed means for conducting a finely divided solid carbonaceous material into a steam boiler or the like.
  • coal will be fed to the gasifier by a pressurized piston feeder in conjunction with a star-wheel feeder.
  • the coal will be pressurized by the piston feeder and fed into the gasifier by the star-wheel feeder.
  • a number of lock hoppers feed coal into a highpressure surge vessel from which the coal would be fed to the gasifier.
  • the high-pressure gas in the hopper is vented to a series of receivers at different pressure levels down to atmospheric pressure. Gas is vented first to the highest pressure receiver and when pressure equalization is approached the venting is switched to the receiver at the next lower pressure and so on until the final venting is to atmospheric pressure.
  • the lock hopper is then refilled with coal then pressurized in staged from each gas receiver in turn and the receivers are maintained at constant pressure by pumping gas from the receiver at the next lowest pressure.
  • F inal pressurization is made by pumping gas from the highest pressure receiver directly into the lock hopper.
  • the coal is fed into oneof several alternating hoppers, the hopperis pressurized, the coal is injected into the gasifier and the hopper is vented for receiving the next charge.
  • the solid carbonaceous material can be dispersed in a liquid vehicle in the form of a slurry, the slurry can be raised to an elevated pressure by means of a slurry pump, the slurry can be dried using the high-temperature effluents from the gasification vessel and simultaneously entrained in a humidified gas, the solid carbonaceous materials can be separated from the gas into which it has been entrained, and fed at high pressure into the gasifier by means of a stream of hot recycled gas or stream.
  • the separated gas can be sent to the further purification steps without loss of volume of production for the overall gasification process. It is further contemplated that char separated and collected in the gasification process and condensed steam from the process or boiler feed water can be used in making up the initial slurry.
  • FIG. 1 is a schematic drawing of the method of the instant invention.
  • FIG. 2 is a schematic drawing of the method of the instant invention as applied to a process for producing a synthesis gas.
  • FIG. 1 there is shown a slurry tank with an impeller 12 mounted on shaft 14 rotated by a suitable motor or other rotating device not shown.
  • the tank 10 receives the pulverized carbonaceous material from a feed hopper or pipe that is shown by arrow 16.
  • the pulverized carbonaceous material generally is coal but can include coke, char or low grade volatile materials such as lignite.
  • Arrow l8 designates a source of supply of water which can be fresh water from utility, boiler feed water, or condensed steam from the process generally referred to as condensate.
  • the slurry tank 10 isconnected via conduit 10 to a slurry pump 22 which in turn is connected through conduits 24, 26, heat exchanger 28, and valve 30, to a mixing chamber 32.
  • the heat exchanger 28 is included in the process stream and can be bypassed if not needed as by conduit 34. If used, the heat exchanger 28 can be used to heat the slurry by means of heat exchange with steam, hot condensate, hot gas from the gasifier or hog gas from an independent gas heater (not shown).
  • the mixing chamber 32 contains an inlet conduit 36 for receiving hot gas, which in turn is connected to another conduit 38 having disposed therein temperature indicating control valve 40.
  • An outlet conduit 42 is connected to a separator 44, which in turn has an outlet gas conduit 46 and a solids removal device shown as 48. Removal device 48 in turn is connected to a coal feeder 50, which in turn is connected to a conduit 52 to a venturi nozzle 54.
  • a conduit 56 is connected to the venturi nozzle 54 in order to entrain the coal into a reactant gas for injection of the reactant and gas and coal into the gasifier.
  • solid carbonaceous material e.g. coal is fed through conduit 16 and condensate through conduit 18 into the slurry tank 10.
  • the impeller 12 is used to agitate the coal and condensate in tank 10 to form a slurry having approximately 50 percent by weight solids.
  • the slurry is then pumped under pressure to the mixing chamber 32 which chamber is maintained at the pressure of the gasifier vessel as the slurry is sprayed therein.
  • the mixing chamber 32 the slurry is contacted by the hot gasifier effluent entering through conduit 36.
  • the action of the hot gasifier effluent and the spraying of the slurry causes the water to v be driven off and the solid carbonaceous material (coalibecomes dried and entrained in the humidified hot gasifier effluent:
  • the evaporated water humidifies the effluent gas to enhance subsequent reactions in the shift convertor where the gas is used.
  • Steam conduit 38 is included to maintain the temperature of the spray drying chamber and to adjust the humidity of the effluent gas with the entrained solid carbonaceous material which is passed through conduit 42 to a cyclone separator and solid carbonaceous storage vessel 44 wherein the solid carbonaceous material is separated from the gas ans stored for use as needed with the solid carbonaceous material being withdrawn through a solids removal device, e.g., conduit 48, into feeder 50 for feeding into the gasification vessel.
  • the dried carbonaceous material is fed under pressure from conduit 52 into centuri feed nozzle 54 for pneumatic feeding to the reactor or gasifier. It may be advantageous to entrain the coal in a reactnat stream 56 which can be either hot recycled gas or steam used in the gasifier reaction vessel as in U.S. Pat. No.
  • coal can be fed through conduit 52 directly to the gasifier nozzles.
  • the gas separated in separator 44 is conducted through conduit 46 to subsequent processing steps (e.g. water gas shift reactor, acid gas removal, and methanation) in the overall gasification scheme so that none of the gasifier effluent is sacrificed in feeding the coal or other solid carbonaceous material to the gasifier.
  • the foregoing process provides a method for feeding dried preheated coal to a gasifier. It is possible to preheat the coal during drying to a temperature .of approximately 500F therebyachieving overall process economies in the production of synthetic natural gas by reducing oxygen requirements.
  • the foregoing basic method can be modified for application to other gasification schemes.
  • the gasification vessel for such a process requires heated coal at 80 atmospheres pressure for gasifier feed and requires process gasifier effluent temperature of 660F with a 1:1 steam to dry gas ratio for feed to the shift converter, which is the step after the gasifier.
  • the coal slurry is prepared as a 50 percent by weight mixture by adding coal at approximately 60F, hot condensate at approximately 212F and a low pressure steam at 50 psig and 298F into the slurry tank 10.
  • the slurry is pumped at the desired pressure (80 atmospheres) and preheated by hot condensate in heat exchanger 28.
  • the slurry is dried (32) and the coal and process gas separated in the cyclone 44.
  • the first section of the process will encompass multiple train slurry preparation consisting of makedown tanks and mixers, low-pressure, centrifigal slurry pumps, holding tansk with mixers, and circulation pumps.
  • coal sized at approximately percent less than 200 mesh and hot condensate direct from deaerators will be combined to produce a 50 weight percent coal water slurry in the make-down tanks.
  • Each tank will have a 10-minute residence time and be of 16,500 gallon capacity.
  • the slurry mixer will employ an axial flow, constant velocity discharge impeller with the shaft and impeller covered with rubber to minimize erosion. There will be provision in these tanks for steam sparging for heating of the slurry and usual circumstances where the coal may have settled to the bottom of the tank. After the slurry is throughly mixed, it will flow into a manifold from which it will be pumped to the holding tanks.
  • the next section of the process containsof the slurry pumping and hot condensate heat exchangers.
  • the slurry pumps will develop the system pressure of approximately 80 atmospheres using reciprocating singleacting Triplex plunger pumps.
  • the slurry will be discharged from the pumps at 1,200 psi and approximately 230F into a heat exchanger wherein the slurry will be raised to approximately 430F before feeding into the dryer.
  • the temperature of 430F is required in order to obtain the desired gas and coal temperature with a 1 to 1 steam to dry gas ratio in the process gas from the dryer. Care must be taken in constructing special inlet channels and distribution in the heat exchanger to prevent or minimize erosion due to the abrasive characteristics of the slurry.
  • the next section of the overall process will consist of slurry drying wherein there is employed a spray dryer, a cyclone, and a pair of coal receivers.
  • the coal slurry is dried and the water is vaporized in a spray dryer which will operate at approximately 80 atmospheres pressure with exit gas temperatures of 660F.
  • Gas used for heating the slurry will be effluent gas from the gasifier.
  • the effluent gas from the gasifier is at a temperature of 1,750F but before being used is subjected to a char separation in a cyclone separator. The char is then recycled to the gasifier.
  • a second cyclone separation is effected to eliminate the balance of the char from the gaas and lower the gas temperature to approximately 1,100F.
  • a portion of the gas from the first and second cyclone is combined with a net temperature of about 1,600F which gas is used in the spray dryers to content the slurry which is pumped into the dryer and atomized. If required, steam canbe added'to increase the atomization of the slurry or it can be added later to achieve the desired steam to dry gas ratio.
  • the dried coal and humidified gas is then taken over into a cyclone where the coal is separated and conducted into a pair of receivers, which will operate on a switching cycle to eliminate back surging through the cyclone.
  • the separated gas will be taken and fed to the carbon monoxide shift converters for further processing into the required pipeline gas. At this stage, the coal can be withdrawn from the storage hoppers under pressure and fed to the gasifier for reacting.
  • FIG. 2 There is shown in FIG. 2 a method of using a slurry feed in conjunction with a commercial partial oxidation unit.
  • the partial oxidation unit is shown in U.S. Pat. No. 2,595,234 and is used to produce a synthesis gas consisting mainly of water vapor, hydrogen, carbon dito free the mixer and impeller for start up under u'n- I oxide, and carbon monoxide, which can be subsequently shift converted to carbon dioxide and hydrogen.
  • the hydrogen is then separatedout and used for various processesincluding gasification of crude oil or as product hydrogen for other manufacturing operations.
  • the partial oxidation reactor is shown as60 in FIG. 2 and has an inlet conduit 62 for receiving the solid carbonaceous material to be reacted, a second inlet conduit 64 for receiving oxygen that reacts with the solid carbonaceous material and outlet conduit 66 for conduiting the synthesis gas out of the reactor and a bottom clean out 68 for removing slag and/or ash from the gasifier.
  • the product gas is conducted from conduit 66 to a separator 70 and from separator 70 through conduit 72 to a waste heat boiler 74, from waste heat boiler 74 through conduit 76 to a dryer 78, from dryer 78 to separator 80 and from separator 80 through to purification (shift) through conduit 81.
  • Coal is fed to the reactor 60 through conduit 82 which is in turn connected to a pneumatic injectionm device 84 which receives the coal feed from conduit 86 and carries the coal into the reactor 60 by means of steam shown by arrow 88.
  • Conduit 86 is connected in turn in reverse order to separator 80 and dryer 78.
  • a conduit 90 is connected to preheater 92 which in turn is connected to slurry pump 94 through conduit 95-for receiving the coal slurry.
  • Slurry pump 94 is connected to the slurry tank 96 by conduit 98.
  • Slurry tank 96 include'san impeller 100 and a drive shaft 102, which are connected to a suitable source of power such as a motor (not shown).
  • the slurry can be made as the result of wet grinding of the carbonaceous material in which event tank 96 is bypassed through conduit 104 directly to the slurry pump 94.
  • char, coke, or combinations thereof are introduced into the slurry tank 96 and are designated as arrow 106.
  • Condensate is added to tank 96 as indicated by arrow 108, e.g., condensate from the process in the form of boiler feed water, condensed steam, or fresh water.
  • the impeller is activated to provide the proper mixing of the solid carbonaceous material and condensate to form the slurry.
  • the slurry can be formed as the coal is wet ground to size and passed directly to the slurry pump 94 through conduit 104.
  • the preferably slurry is one that consists of 40 to 60 percent by weight water with the rest solid carbonaceous material.
  • the slurry is passed to the slurry pump 94 where its pressure is raised to that above the operating pressure of the gasifier 60 and is then preheated in heat exchanger 92 if the overall heat balance of the system requires additional heat into the system.
  • the slurry is then injected into the dryer 78 where it is contacted by the hot effluent from the waste heat boiler 74 and the water is driven off and the solid carbonaceous material is raised in temperature and entrained in a gas.
  • a source of steam can be provided through conduit 77 to control the humidity and temperature of the effluent in conduit 79 from dryer 78.
  • Waste heat boiler 74 is included in'this system to recover heat and-at the same time-to produce high-pressure steam for the overall reaction and for injecting into the gasifier itself.
  • the process provides a dry preheated carbonaceous solid fuel to the gasifier thereby increasing gasifier efficiency.-.
  • the water is evaporated without the use of additional oxygen and simultaneously provides steam required for subsequent shift operations of the effluent.
  • the process provides a method for utilizing a high-.
  • sulfur fuel such as coal, petroleum, coke or the like by producing sulfur as hydrogen sulfide because of the overall reducing atmosphere.
  • a method of feeding carbonaceous particles to a gasifier-operating at elevated temperature and pressure comprising the steps of:
  • a method of feeding solid carbonaceous particles to a gasifier operating at high temperature and high pressure comprising the steps of:
  • drying chamber introducing-the pressurized feed stream to a drying chamber, said drying chamber being separated from said gasifier, wherein it is contacted by hot gaseous effluent from the gasifier without substantial reaction so that, the water is evaporated, and the dried solid carbonaceous particles are entrained in the gaseous effluent;
  • gaseous effluent separated from the solid carbonaceous particles consists "essentially of-water vapor, carbon monoxide, and hydrogen, and issubjected to a subsequent shift step wherein carbon dioxide and hydrogen .LILAUAJU ILLA la. .1 M

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Treatment Of Sludge (AREA)
US296959A 1972-10-12 1972-10-12 Method of feeding solid carbonaceous material to a high temperature reaction zone Expired - Lifetime US3871839A (en)

Priority Applications (8)

Application Number Priority Date Filing Date Title
US296959A US3871839A (en) 1972-10-12 1972-10-12 Method of feeding solid carbonaceous material to a high temperature reaction zone
ZA737437*A ZA737437B (en) 1972-10-12 1973-09-20 Method of feeding solid carbonaceous material to a high temperature reaction zone
JP48111879A JPS4974203A (enrdf_load_stackoverflow) 1972-10-12 1973-10-04
BE136472A BE805825A (fr) 1972-10-12 1973-10-09 Procede pour amener un materiau charbonneux solide dans une zone de reaction a haute temperature
FR7336219A FR2202929B1 (enrdf_load_stackoverflow) 1972-10-12 1973-10-10
DE19732350953 DE2350953A1 (de) 1972-10-12 1973-10-11 Verfahren zum beschicken eines vergasers mit kohlenstoffhaltigem material
GB4760473A GB1407176A (en) 1972-10-12 1973-10-11 Method of feeding solid carbonaceous material to a high temperature reaction zone
PL1973165799A PL96935B1 (pl) 1972-10-12 1973-10-12 Sposob doprowadzania stalego materialu weglowego do generatora gazu

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US296959A US3871839A (en) 1972-10-12 1972-10-12 Method of feeding solid carbonaceous material to a high temperature reaction zone

Publications (1)

Publication Number Publication Date
US3871839A true US3871839A (en) 1975-03-18

Family

ID=23144271

Family Applications (1)

Application Number Title Priority Date Filing Date
US296959A Expired - Lifetime US3871839A (en) 1972-10-12 1972-10-12 Method of feeding solid carbonaceous material to a high temperature reaction zone

Country Status (8)

Country Link
US (1) US3871839A (enrdf_load_stackoverflow)
JP (1) JPS4974203A (enrdf_load_stackoverflow)
BE (1) BE805825A (enrdf_load_stackoverflow)
DE (1) DE2350953A1 (enrdf_load_stackoverflow)
FR (1) FR2202929B1 (enrdf_load_stackoverflow)
GB (1) GB1407176A (enrdf_load_stackoverflow)
PL (1) PL96935B1 (enrdf_load_stackoverflow)
ZA (1) ZA737437B (enrdf_load_stackoverflow)

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3963426A (en) * 1974-07-22 1976-06-15 Cameron Engineers, Incorporated Process for gasifying carbonaceous matter
US4153427A (en) * 1978-02-23 1979-05-08 The United States Of America As Represented By The United States Department Of Energy Apparatus and method for feeding coal into a coal gasifier
US4158552A (en) * 1977-08-29 1979-06-19 Combustion Engineering, Inc. Entrained flow coal gasifier
US4284416A (en) * 1979-12-14 1981-08-18 Exxon Research & Engineering Co. Integrated coal drying and steam gasification process
US4624684A (en) * 1985-09-03 1986-11-25 Texaco Inc. Process for feeding and gasifying solid carbonaceous fuel
EP0639220A4 (en) * 1992-05-08 1995-05-10 Victoria Elect Commission INTEGRATED METHOD AND DEVICE FOR DRYING GASIFYING FUEL.
US20010054256A1 (en) * 2000-05-09 2001-12-27 Yukuo Katayama Method for the gasification of coal
US20080216406A1 (en) * 2007-02-14 2008-09-11 Xin Wang Method of gasification burner online feeding
CN102021040A (zh) * 2009-09-14 2011-04-20 通用电气公司 用来使用蒸汽干燥固体进料的方法和装置
US20110314736A1 (en) * 2007-12-26 2011-12-29 Total Raffinage Marketing Treatment chain and process for the thermochemical conversion of a wet feed of biological material by gasification
US20120222353A1 (en) * 2002-02-05 2012-09-06 The Regents Of The University Of California Method to Produce Methane Rich Fuel Gas from Carbonaceous Feedstocks Using a Steam Hydrogasification Reactor and a Water Gas Shift Reactor
US20140054504A1 (en) * 2012-08-22 2014-02-27 Korea Institute Of Energy Research Apparatus and method for rapidly producing synthetic gas from bio-diesel by-product using microwave plasma
US9057030B2 (en) 2010-10-30 2015-06-16 General Electric Company System and method for protecting gasifier quench ring
WO2021011020A1 (en) * 2019-07-16 2021-01-21 Infiniforce, Inc. Petroleum sludge or other wastes recycle treatment system
US20240026237A1 (en) * 2020-10-26 2024-01-25 Ers Engineering S.R.L. Process for Gasifying an Organic Material and Plant for Carrying Out Said Process

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1508712A (en) * 1975-03-31 1978-04-26 Battelle Memorial Institute Treating solid fuel
DE2757918C2 (de) * 1977-12-24 1982-04-29 Davy McKee AG, 6000 Frankfurt Verfahren zum Trocknen und Einspeisen von festem Brennstoff in einen Druckvergaser
JPS59140291A (ja) * 1983-02-01 1984-08-11 Shinenerugii Sogo Kaihatsu Kiko 加圧式微粉炭ガス化法
DE3423620A1 (de) * 1984-06-27 1986-01-02 Uhde Gmbh, 4600 Dortmund Verfahren zur thermischen behandlung von kohlenstoffhaltigen stoffen, insbesondere von schlaemmen
JPS62185788A (ja) * 1986-02-10 1987-08-14 Central Res Inst Of Electric Power Ind 石炭ガス化複合発電における石炭フイ−ド方法
NL9401709A (nl) * 1994-10-17 1996-06-03 Kema Nv Werkwijze en installatie voor het vergassen van vaste brandstof.
RU2216511C2 (ru) * 2001-10-03 2003-11-20 Новиков Николай Николаевич Устройство для получения активного угля из твердых топлив

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2595234A (en) * 1949-06-15 1952-05-06 Texas Co Process for the production of fuel gas from carbonaceous solid fuels
US2946670A (en) * 1957-03-11 1960-07-26 Texaco Development Corp Manufacture of synthesis gas
US2987387A (en) * 1958-12-30 1961-06-06 Texaco Inc Method for the production of carbon monoxide from solid fuels
US3250016A (en) * 1962-11-08 1966-05-10 United States Steel Corp Method and apparatus for preparing powdered coal for injection into a blast furnace
US3384974A (en) * 1967-03-20 1968-05-28 Phillips Petroleum Co Process and apparatus for wet pellet drying
US3652454A (en) * 1968-05-27 1972-03-28 Texaco Inc High pressure water-gas shift conversion process
US3715195A (en) * 1971-06-30 1973-02-06 Texaco Inc Multihydrotorting of coal

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1030625A (fr) * 1950-10-10 1953-06-16 Texaco Development Corp Perfectionnements apportés au traitement des matières solides et friables

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2595234A (en) * 1949-06-15 1952-05-06 Texas Co Process for the production of fuel gas from carbonaceous solid fuels
US2946670A (en) * 1957-03-11 1960-07-26 Texaco Development Corp Manufacture of synthesis gas
US2987387A (en) * 1958-12-30 1961-06-06 Texaco Inc Method for the production of carbon monoxide from solid fuels
US3250016A (en) * 1962-11-08 1966-05-10 United States Steel Corp Method and apparatus for preparing powdered coal for injection into a blast furnace
US3384974A (en) * 1967-03-20 1968-05-28 Phillips Petroleum Co Process and apparatus for wet pellet drying
US3652454A (en) * 1968-05-27 1972-03-28 Texaco Inc High pressure water-gas shift conversion process
US3715195A (en) * 1971-06-30 1973-02-06 Texaco Inc Multihydrotorting of coal

Cited By (26)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3963426A (en) * 1974-07-22 1976-06-15 Cameron Engineers, Incorporated Process for gasifying carbonaceous matter
US4158552A (en) * 1977-08-29 1979-06-19 Combustion Engineering, Inc. Entrained flow coal gasifier
US4153427A (en) * 1978-02-23 1979-05-08 The United States Of America As Represented By The United States Department Of Energy Apparatus and method for feeding coal into a coal gasifier
US4284416A (en) * 1979-12-14 1981-08-18 Exxon Research & Engineering Co. Integrated coal drying and steam gasification process
US4624684A (en) * 1985-09-03 1986-11-25 Texaco Inc. Process for feeding and gasifying solid carbonaceous fuel
EP0639220A4 (en) * 1992-05-08 1995-05-10 Victoria Elect Commission INTEGRATED METHOD AND DEVICE FOR DRYING GASIFYING FUEL.
US5695532A (en) * 1992-05-08 1997-12-09 State Electricity Commission Of Victoria Integrated carbonaceous fuel drying and gasification process and apparatus
CN1039653C (zh) * 1992-05-08 1998-09-02 维多利亚州电力委员会 用于气化具有高含湿量的颗粒固体碳质燃料的方法和装置
US20010054256A1 (en) * 2000-05-09 2001-12-27 Yukuo Katayama Method for the gasification of coal
US6997965B2 (en) 2000-05-09 2006-02-14 Toyo Engineering Corporation Method for the gasification of coal
US9493721B2 (en) * 2002-02-05 2016-11-15 The Regents Of The University Of California Method to produce methane rich fuel gas from carbonaceous feedstocks using a steam hydrogasification reactor and a water gas shift reactor
US20120222353A1 (en) * 2002-02-05 2012-09-06 The Regents Of The University Of California Method to Produce Methane Rich Fuel Gas from Carbonaceous Feedstocks Using a Steam Hydrogasification Reactor and a Water Gas Shift Reactor
US7976595B2 (en) * 2007-02-14 2011-07-12 Yankuang Group Corporation Limited Method of gasification burner online feeding
US20080216406A1 (en) * 2007-02-14 2008-09-11 Xin Wang Method of gasification burner online feeding
US20110314736A1 (en) * 2007-12-26 2011-12-29 Total Raffinage Marketing Treatment chain and process for the thermochemical conversion of a wet feed of biological material by gasification
US9074150B2 (en) * 2007-12-26 2015-07-07 Total Raffinage Marketing Treatment chain and process for the thermochemical conversion of a wet feed of biological material by gasification
CN102021040B (zh) * 2009-09-14 2014-11-26 通用电气公司 用来使用蒸汽干燥固体进料的方法和装置
CN102021040A (zh) * 2009-09-14 2011-04-20 通用电气公司 用来使用蒸汽干燥固体进料的方法和装置
US9057030B2 (en) 2010-10-30 2015-06-16 General Electric Company System and method for protecting gasifier quench ring
US8999018B2 (en) * 2012-08-22 2015-04-07 Korea Institute Of Energy Research Apparatus and method for rapidly producing synthetic gas from bio-diesel by-product using microwave plasma
US20140054504A1 (en) * 2012-08-22 2014-02-27 Korea Institute Of Energy Research Apparatus and method for rapidly producing synthetic gas from bio-diesel by-product using microwave plasma
WO2021011020A1 (en) * 2019-07-16 2021-01-21 Infiniforce, Inc. Petroleum sludge or other wastes recycle treatment system
US20210017022A1 (en) * 2019-07-16 2021-01-21 Infiniforce, Inc. Petroleum sludge or other wastes recycle treatment system
US11667525B2 (en) * 2019-07-16 2023-06-06 Infiniforce, Inc. Petroleum sludge or other wastes recycle treatment system
US20240026237A1 (en) * 2020-10-26 2024-01-25 Ers Engineering S.R.L. Process for Gasifying an Organic Material and Plant for Carrying Out Said Process
US12312545B2 (en) * 2020-10-26 2025-05-27 Ers Engineering S.R.L. Process for gasifying an organic material and plant for carrying out said process

Also Published As

Publication number Publication date
FR2202929B1 (enrdf_load_stackoverflow) 1977-05-27
PL96935B1 (pl) 1978-01-31
FR2202929A1 (enrdf_load_stackoverflow) 1974-05-10
BE805825A (fr) 1974-02-01
DE2350953A1 (de) 1974-04-18
ZA737437B (en) 1974-08-28
GB1407176A (en) 1975-09-24
JPS4974203A (enrdf_load_stackoverflow) 1974-07-17

Similar Documents

Publication Publication Date Title
US3871839A (en) Method of feeding solid carbonaceous material to a high temperature reaction zone
EP0030841B1 (en) Integrated coal drying and steam gasification process
US4321151A (en) Process for wastewater treatment and wastewater sludge conversion into energy
RU2550392C2 (ru) Устройство и способ для производства синтез-газа из подготовленной биомассы путем газификации во взвешенном потоке
CA2134871C (en) Integrated carbonaceous fuel drying and gasification process and apparatus
US4678860A (en) Process of producing liquid hydrocarbon fuels from biomass
US4321150A (en) Process for wastewater treatment and wastewater sludge conversion into energy
US2694623A (en) Process for enrichment of water gas
US4380960A (en) Pollution-free low temperature slurry combustion process utilizing the super-critical state
US4002438A (en) Organic conversion system
US4427584A (en) Conversion of cellulosic fibers to mono-sugars and lignin
US4153427A (en) Apparatus and method for feeding coal into a coal gasifier
US20090208402A1 (en) Process and system for producing commercial quality carbon dioxide from fine particle limestone
US4251227A (en) Method for producing SNG or SYN-gas from wet solid waste and low grade fuels
US5000099A (en) Combination of fuels conversion and pressurized wet combustion
EP0040514A1 (en) Improved particulate coal-in-liquid mixture and process for the production thereof
US4095959A (en) Coal gasification apparatus
US20160046868A1 (en) Method for processing combustible carbon- and/or hydrocarbon-containing products and reactor for the implementation thereof
EP0366138B1 (en) Process for manufacturing fuel from ligno-cellulose material
US4930429A (en) Apparatus and process for generating steam from wet fuel
US3118746A (en) Generation of fuel gas from oil shale
US5624469A (en) Method and apparatus for recovering heat from solid material separated from gasification or combustion processes
US4556402A (en) Process of gasifying solid fuels in a moving bed and in a fluidized bed
US3953180A (en) Production of low BTU sulfur-free gas from residual oil
US4159897A (en) Producing fluid fuel from coal