EP0349090A1 - Methode zur Umänderung der Schmutzstoffe in einem rohen Hochtemperatur-Hochdruck-Synthesegasstrom - Google Patents

Methode zur Umänderung der Schmutzstoffe in einem rohen Hochtemperatur-Hochdruck-Synthesegasstrom Download PDF

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Publication number
EP0349090A1
EP0349090A1 EP89201730A EP89201730A EP0349090A1 EP 0349090 A1 EP0349090 A1 EP 0349090A1 EP 89201730 A EP89201730 A EP 89201730A EP 89201730 A EP89201730 A EP 89201730A EP 0349090 A1 EP0349090 A1 EP 0349090A1
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EP
European Patent Office
Prior art keywords
gas
synthesis gas
particles
sticky
quench
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.)
Granted
Application number
EP89201730A
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English (en)
French (fr)
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EP0349090B1 (de
Inventor
Charles Victor Sternling
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.)
Shell Internationale Research Maatschappij BV
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Shell Internationale Research Maatschappij BV
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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
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/466—Entrained flow processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
    • 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
    • C10J2300/0953—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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1223—Heating the gasifier by burners
    • 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

Definitions

  • the invention relates to a process for the partial combustion of finely-divided solid fuel, such as pulverized coal, in which the latter is introduced together with oxygen-containing gas via a burner into a reactor or gasifier from which a stream of high-temperature raw synthesis gas is discharged together with a minor amount of contaminating material, some of which may be in the form of particles having a sticky outer surface, that tend to adhere to equipment located downstream of the reactor.
  • finely-divided solid fuel such as pulverized coal
  • Partial combustion is the reaction of all of the fuel particles with a substoichiometrical amount of oxygen, either introduced in pure form or admixed with other gases, such as a transport stream of nitrogen, whereby the fuel is partially oxidized to hydrogen and carbon monoxide. This partial combustion differs from complete combustion wherein the fuel would be completely oxidized to carbon dioxide and water.
  • the present invention is directed to a process for the partial combustion of finely divided carbonaceous fuel containing at least 1% by weight ash in a reactor or gasifier to produce a product gas (mainly carbon monoxide and hydrogen) which carries along with it, as it leaves the reactor, sticky particles of fly ash or fly slag, or ash-forming constituents which may consist of alkali metal chlorides, silicon and/or aluminium oxides or other mineral species.
  • a product gas mainly carbon monoxide and hydrogen
  • the ash is usually sticky.
  • the residence time in the gasifier or reactor is very short compared with gasification in a fluidized or moving bed process, and the temperature is very high.
  • the ash that is formed during the present gasification process is at least partly in liquid form at the conditions that prevail in the reactor, usually temperatures from 1050 to 2200 °C. If the ash particles are not fully in liquid form, they will generally consist at least partly of a molten slag or be a combustion product or residue having a partly molten consistency.
  • the high temperature of a reactor is sufficient to vaporize certain other by-products which may assume a sticky form when cooled in the process equipment.
  • the invention therefore provides a process for the production of synthesis gas wherein coal is partially oxidized at an elevated temperature by feeding substantially dry particulate coal and oxygen to a gasification zone of a reactor, the ratio of coal to oxygen being such as to maintain a reducing atmosphere, and producing raw synthesis gas, said gas also carrying with it a minor amount of at least one contaminating impurity having a sticky outer surface when in a solid particle form which tends to adhere to equipment downstream of the reactor, characterized by - the step of reducing the sticky characteristic of sticky particles of contaminants carried by the effluent stream of synthesis gas from the reactor by injecting a flow of lower temperature quench gas into the higher temperature synthesis gas stream substantially immediately upon leaving the reactor to cool the sticky contaminating particles; and - flowing the combined mixture of synthesis gas containing contaminating sticky particles and injected cooling quench gas through a substantially straight conduit under conditions of turbulent flow for a time sufficient to thoroughly mix the combined flowing stream to reduce the sticky characteristic of at least the outer surface of the particles to a form that does not interfere
  • the temperature of the product gas at this point may be, say 1400 °C for example.
  • a stream of product gas, which has been cooled several hundred degrees, is recycled from a selected point in the process and injected as a quench gas into the upstream end of the quench section of the reactor discharge duct.
  • the hot synthesis product gas and the sticky particles carried thereby are thoroughly mixed with the cooler quench gas thereby allowing the molten or sticky particles to "freeze” or at least cause the outer surfaces of the particles to become non-sticky to the extent that they do not stick to the walls of any downstream equipment or piping.
  • the invention is designed for use in a synthesis gas generation complex comprising
  • the invention provides a process for the production of synthesis gas comprising the steps of
  • the raw synthesis gas also contains minor amounts of vaporized mineral matter and said reducing step includes condensing the vaporized mineral matter by the injection of a volume of quench gas at a lower temperature than the synthesis gas stream into which it is injected.
  • the quench gas stream is injected into the raw synthesis gas stream at a plurality of points around the periphery thereof so as to form at said gas injection area a sheath of cooler quench gas around the hot stream of synthesis gas and the sticky particles carried thereby.
  • the quench gas is synthesis gas taken from a point downstream which contains a minor amount of lower temperature solid particles of the contaminating impurity, said particles being of the same composition as at least one of the impurities in the effluent raw synthesis gas stream leaving the reactor.
  • the steam generated in the gasifier shell may be passed to a heat exchange zone where it may be superheated and then sent for utilization.
  • the gasification may be carried out utilizing techniques suitable for producing a synthesis gas having a gasifier outlet temperature of from about 1050 °C to about 1650 °C.
  • the process is advantageously carried out with a gasifier comprising at least one burner.
  • a gasifier comprising at least one burner.
  • Such a process will advantageously include combustion, with oxygen, of dry particulate coal, i.e., coal having less than about 10 per cent water content. Steam may be added in some instances to assist in the combustion.
  • the type of coal utilized is not critical, but it is an advantage of the invention that lower grade coals, such as lignite or brown coal, may be used. If the water content of the coal is too high to meet the requirements mentioned, supra, the coal should be dried before use.
  • the atmosphere will be maintained reducing by the regulation of the weight ratio of the oxygen to moisture and ash free coal in the range of about 0.6 to 1.2, in particular 0.9 to 1.0.
  • the specific details of the equipment and procedures employed form no part of the invention, but those described in U.S. patent specification No. 4,350,103, and U.S. patent specification No. 4,458,607, may be employed.
  • suitable structural materials such as the Inconels and Incoloy 800, i.e., high chrome-molybdenum steels, should be employed for superheating duty for long exchanger life. It is an advantage of the invention that, by carrying out the advantageous procedure described herein, or utilizing the advantageous structural aspects mentioned, as described, a synthesis gas stream is produced free of particles of sticky material that might adhere to and/or clog flow lines or equipment.
  • the drawing is a schematic representation of the process flow type, and illustrates the efficient integration of the specialized gasifier with equipment for substantially eliminating the particles of sticky material that are produced in a gasifier. All values specified in the description relating thereto hereinafter are calculated, or merely illustrative.
  • dry particulate coal (average particle size about 30 to 50 microns and moisture content of less than about 10 per cent by weight) is fed via a line (1) to burners (2) of a gasifier (3).
  • the gasifier (3) may be a vertical oblong vessel, for example cylindrical in the burner area, with substantially conical or convex upper and lower ends, and is defined by a surrounding membrane wall structure (4) for circulation of cooling fluid.
  • the generally cylindrical reactor wall will comprise a plurality of heat exchange tubes, spaced apart from each other by "membranes" or curved plates, the tubes being connected at their extremities for continuous flow of a heat exchange fluid, such as water, and also having multiple inlets/outlets for the fluid, in a manner well known to the art.
  • a heat exchange fluid such as water
  • oxygen is introduced to the burners (2) via a line (5), the weight ratio of oxygen to moisture and ash free coal being about 0.9, for example.
  • the combustion produces a flame temperature of about 2200 °C, with a gas temperature at the outlet of the gasifier being about 1250 °C to about 1450 °C. Regulation of gasifier and outlet temperature is assisted by coolant in the membrane wall structure (4). Slag is discharged at the outlet (1a).
  • Hot raw synthesis gas with impurities leaves the gasifier (3) through a straight elongated quench line (8) of selected length the interior of which forms a quench chamber in which the raw synthesis gas and the impurities carried thereby are quenched by cooler synthesis gas through line (6) from any suitable point in the process.
  • the quench gas may be from 140 °C to about 540 °C.
  • the quench line (8) may also be jacketed for heat recovery, although this is not illustrated.
  • the quenched gas then passes to a cooler or heat exchanger (7).
  • the heat exchanger (7) is advantageously a multiple section exchanger, the quenched synthesis gas being cooled by fluid in the tubes.
  • the raw synthesis gas now cooled in the low temperature section of the heat exchanger (7) to a temperature of about 315 °C to 140 °C, passes via a line (14) to a cleanup section (15) or solids separator where particulates and various impurity gases, such as H2S, may be removed.
  • the details of the gas cleanup form no part of the invention. Steam requirements for cleanup activities may be supplied from that generated by the overall process.
  • the purified synthesis gas passes from the section (15) in the line (17), and is ready for use. Dry solids impurities are discharged at the outlet (17a).
  • the quench line (8) of Fig. 1 running horizontally from the gasifier (3)
  • the quench line (8) from the gasifier (3) in Fig. 2 is illustrated as extending vertically from the top of the gasifier for a calculated distance.
  • the length of the quench line (8) depends on many factors such as flow rates or volumes in the quench lines and the recycled quench gas supply lines, the temperatures of the raw synthesis gas from the gasifier and that of the quench gas, the nature of the vaporized impurities in the raw synthesis gas to be condensed, the nature of the sticky ash particles in the synthesis gas to be rendered non-sticky, etc.
  • Tests were conducted in a pilot operation in which 200 tons per day of finely-divided coal were burned with an equal weight of oxygen.
  • the gasifier in one test was operated at about 25 bar (10 to 100 bar range) with the product gas being discharged from the gasifier with contaminants at about 1450 °C. After being cleaned and cooled, a portion of the product gas flow stream at about 315 °C was recycled and injected as a quench gas into the upstream end of the quench section which forms substantially the first section of gas discharge line from the gasifier.
  • Equal masses of product gas and quench gas may be used although this ratio may be varied with from 0.5 to 4.0 mass of quench gas being used for each mass of product gas depending on operating conditions.
  • the length of the quench line it is necessary for the length of the quench line to be between 5 and 20 times the inner diameter of the line. It is advantageous that this minimum length of quench line have no bends in it until the particles have passed a point in the line where they are no longer sticky.
  • certain impurities such as the lower oxides of silica and many of the alkali metals are vaporized. The materials are then condensed and cooled in the quench section of the process equipment.
  • a quench section having a straight run of 14 times the section diameter handled a9 metres per sec flow of hot synthesis gas in a system burning 200 tons of coal per day.
  • Fig. 2 The remaining equipment shown in Fig. 2 are similar to the components of Fig. 1. Fig. 2 is included to show that the quench line (8) may leave the gasifier in a vertical direction and enter the heat exchanger (7) from the top, if desired.
EP19890201730 1988-06-30 1989-06-28 Methode zur Umänderung der Schmutzstoffe in einem rohen Hochtemperatur-Hochdruck-Synthesegasstrom Expired - Lifetime EP0349090B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US21341888A 1988-06-30 1988-06-30
US213418 1988-06-30

Publications (2)

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EP0349090A1 true EP0349090A1 (de) 1990-01-03
EP0349090B1 EP0349090B1 (de) 1993-03-31

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EP19890201730 Expired - Lifetime EP0349090B1 (de) 1988-06-30 1989-06-28 Methode zur Umänderung der Schmutzstoffe in einem rohen Hochtemperatur-Hochdruck-Synthesegasstrom

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EP (1) EP0349090B1 (de)
JP (1) JP2668266B2 (de)
DE (1) DE68905681T2 (de)
DK (1) DK315289A (de)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0618282A2 (de) * 1993-03-31 1994-10-05 Krupp Koppers GmbH Verfahren zur Kühlung von durch Vergasung gewonnenem Rohgas
WO2009043540A1 (de) * 2007-09-26 2009-04-09 Uhde Gmbh Verfahren zur reinigung des rohgases aus einer feststoffvergasung
CN103874749A (zh) * 2011-04-06 2014-06-18 伊内奥斯生物股份公司 合成气冷却器系统和运行方法

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103666580B (zh) * 2013-11-29 2015-07-22 武汉凯迪工程技术研究总院有限公司 一种耦合式生物质加压热解工艺及系统

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2053262A (en) * 1979-07-13 1981-02-04 Texaco Development Corp Process and Apparatus for Producing Gaseous Mixtures including H2 and CO
DE2942804A1 (de) * 1979-10-23 1981-05-07 Janich, geb.Fischer, Elsbeth, 4720 Beckum Vorrichtung und verfahren zur gaserzeugung

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3808729A1 (de) * 1988-03-16 1989-10-05 Krupp Koppers Gmbh Verfahren und vorrichtung zur abkuehlung des aus einem vergasungsreaktor austretenden heissen produktgases
DE3809313A1 (de) * 1988-03-19 1989-10-05 Krupp Koppers Gmbh Verfahren und vorrichtung zum kuehlen von partialoxidationsgas

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2053262A (en) * 1979-07-13 1981-02-04 Texaco Development Corp Process and Apparatus for Producing Gaseous Mixtures including H2 and CO
DE2942804A1 (de) * 1979-10-23 1981-05-07 Janich, geb.Fischer, Elsbeth, 4720 Beckum Vorrichtung und verfahren zur gaserzeugung

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0618282A2 (de) * 1993-03-31 1994-10-05 Krupp Koppers GmbH Verfahren zur Kühlung von durch Vergasung gewonnenem Rohgas
EP0618282A3 (de) * 1993-03-31 1994-10-12 Krupp Koppers Gmbh Verfahren zur Kühlung von durch Vergasung gewonnenem Rohgas.
WO2009043540A1 (de) * 2007-09-26 2009-04-09 Uhde Gmbh Verfahren zur reinigung des rohgases aus einer feststoffvergasung
RU2466179C2 (ru) * 2007-09-26 2012-11-10 Уде Гмбх Способ очистки сырого газа после газификации твердого топлива
AU2008306154B2 (en) * 2007-09-26 2013-02-21 Thyssenkrupp Uhde Gmbh Method for purifying the crude gas from a solid matter gasification
AU2008306154B9 (en) * 2007-09-26 2013-03-21 Thyssenkrupp Uhde Gmbh Method for purifying the crude gas from a solid matter gasification
US8529792B2 (en) 2007-09-26 2013-09-10 Uhde Gmbh Process for the purification of crude gas from solids gasification
CN103874749A (zh) * 2011-04-06 2014-06-18 伊内奥斯生物股份公司 合成气冷却器系统和运行方法

Also Published As

Publication number Publication date
JP2668266B2 (ja) 1997-10-27
DK315289D0 (da) 1989-06-26
JPH0247193A (ja) 1990-02-16
DK315289A (da) 1989-12-31
EP0349090B1 (de) 1993-03-31
DE68905681D1 (de) 1993-05-06
DE68905681T2 (de) 1993-07-08

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