EP0115094A2 - Verfahren und Vorrichtung zur Herstellung von Synthesegas - Google Patents

Verfahren und Vorrichtung zur Herstellung von Synthesegas Download PDF

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Publication number
EP0115094A2
EP0115094A2 EP83201705A EP83201705A EP0115094A2 EP 0115094 A2 EP0115094 A2 EP 0115094A2 EP 83201705 A EP83201705 A EP 83201705A EP 83201705 A EP83201705 A EP 83201705A EP 0115094 A2 EP0115094 A2 EP 0115094A2
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EP
European Patent Office
Prior art keywords
synthesis gas
crude synthesis
slag
evaporator
gasifier
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.)
Ceased
Application number
EP83201705A
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English (en)
French (fr)
Other versions
EP0115094A3 (de
Inventor
Günter Klaus Eckstein
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
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 Shell Internationale Research Maatschappij BV filed Critical Shell Internationale Research Maatschappij BV
Publication of EP0115094A2 publication Critical patent/EP0115094A2/de
Publication of EP0115094A3 publication Critical patent/EP0115094A3/de
Ceased legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • 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
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/485—Entrained flow gasifiers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/86—Other features combined with waste-heat boilers
    • 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
    • C10K1/02—Dust removal
    • C10K1/026—Dust removal by centrifugal forces
    • 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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen only

Definitions

  • the invention also relates to an apparatus for carrying out the process described hereinbefore, which apparatus is characterized in that it comprises the following components:
  • carbonaceous fuel means any combustible material consisting of at least 50% by weight, of carbon.
  • the fuel may contain oxygen, sulphur and/or nitrogen.
  • a feedstock includes, e.g., lignite, anthracite, bituminous coal, coke, shale oil, mineral oils or oil fractions, tar sand oil or natural gas.
  • the feedstock, if solid, should be in a powdered form so that it can readily react with oxygen in the gasifier.
  • the size of solid carbonaceous fuel is such that 70%, by weight, of the fuel has a particle size smaller than 200 mesh (A.S.T.M.).
  • the oxidant includes air and oxygen diluted with steam, carbon dioxide, nitrogen and/or argon.
  • the oxidant is preheated before it is reacted with the carbonaceous fuel.
  • the preheating of the oxidant is suitably carried out indirectly by heat exchange with any heat source, e.g., the hot product gas obtained in the present process.
  • the oxidant is preferably preheated to a temperature in the range of 150 to 1300°C, depending on the type of oxidant.
  • the hot oxidant is advantageously mixed with carbonaceous fuel and the oxidant/fuel mixture is introduced, preferably as one or more jets into the gasifier.
  • a process for the production of a hydrogen- and carbon monoxide-containing gas from a carbonaceous fuel ccnprises reacting air or oxygen with the carbonaceous fuel in a gasifier which is preferably kept at an average temperature within the range 1200 to 1700°C and an average pressure within the range 2 to 200 bar, the residence time in said gasifier being preferably from 1 to 10 seconds.
  • a moderator is also supplied to the gasifier.
  • the purpose of the moderator is to exercise a moderating effect on the temperature in the gasifier. That is achieved by means of an endothermic reaction between the moderator and the reactant and/or products of the synthesis gas preparation.
  • Suitable moderators are steam and carbon dioxide.
  • the gasifier in which the synthesis gas is prepared has the shape of a vertical cylinder.
  • the gasifier has substantially the shape of a circular cylinder.
  • the carbon-containing fuel and the oxygen-containing gas can be supplied through the bottom of the gasifier. It is also possible for one of the reactants to be supplied through the bottom of the gasifier and one or more other reactants through the side-wall of the gasifier. Preferably, however, both the fuel as well-as the oxygen-containing gas and the moderator are supplied through the side-wall of the gasifier. This is advantageously effected by means of at least two burners positioned symmetrically in relation to the gasifier axis in a low-lying part of the side-wall. These burners protrude through the vertical cylindrical outer pressure shell and the water tube wall structure.
  • a proportion of the slag is entrained as small droplets by the hot crude synthesis gas leaving the gasifier flowing substantially vertically upwards via the gas discharge at the top, preferably at an average linear velocity in the range fran 1 to 15 m/s.
  • the presence of slag droplets in the gas may be inconvenient.
  • the hot crude synthesis gas is first passed upwards through a radiation chamber where it is cooled, preferably to a temperature in the range from 600 to 1200 °C.
  • the average linear velocity of the hot crude synthesis gas in the radiation chamber is preferably in the range from 1 to 15 m/s.
  • the gasifier and the radiation chamber have both the form of cylinders, preferably circular cylinders and are positioned vertically on top of each other. Preferably the internal diameters of the gasifier and of the radiation chamber are equal. This design which does not apply an outlet nozzle at the top of the gasifier is much simpler than the conventional designs.
  • the gasifier and the radiation chamber are internally defined by the lower and an intermediate part respectively of the tube wall structure. Through this tube wall structure cooling water is passed, which is evaporated by the heat radiation from the hot crude synthesis gas generated in the gasifier. In order to cool the hot crude synthesis gas leaving the top of the gasifier even better and quicker this gas is preferably quenched. The quench is advantageously carried out by injecting cold gas, steam and/or water into the hot crude synthesis gas. Recycled cold purified synthesis gas is very suitable for this purpose since it substantially does not change the composition of the gas to be cooled.
  • the present apgaratus is preferably provided with two to 20 quench nozzles protruding through the vertical cylindrical outer pressure shell and the water tube wall structure. These nozzles are suitably situated in a quench section between the gasifier and the radiation chamber, which advantageously has the same internal diameter as the gasifier and the radiation chamber, In the quench section the hot crude synthesis gas is preferably cooled to a temperature in the range from 600 to 1200°C.
  • the hot gas leaves the gasifier at the top end and then flows upwards through the optional quench section and the radiation chamber, preferably at an average linear velocity ranging from 1 to 15 m/s.
  • a gas recovered by partial oxidation consists for the greater part of H 2 and CO, and possibly further of CO 2 , CH 4 , H 2 0, N 2 , H 2 S and Ar, and entrains sticky slag droplets and/or particles (dependant on the gas temperature and the nature of the inorganic components of the carbon-containig material to be combusted) from the gasifier.
  • the content of said sticky slag droplets and/or particles of the gas usually ranges from 1 to 15% by weight.
  • a quantity of 0.2-2 kg of a cold, clean gas is advantageously injected into 1 kg of the hot gas.
  • the cold, clean gas preferably has a temperature ranging from 50 to 300°C and suitably has the same composition as the hot gas to be cooled down rapidly, so that the gas mixture obtained by injecting cold, clean gas into the hot gas preferably has a composition that does not deviate substantially from the original hot gas, the temperature of said gas mixture advantageously ranging from 600 to 1200°C.
  • the cold, clean gas is in any case injected through openings in the wall of the substantially vertical quench section which is connected to the outlet of the reactor.
  • the quench section and the radiation chamber suitably contain means by which the gas mixture can be indirectly cooled.
  • Said means consist of the tube wall structure which is located on the inside of the quench section and radiation chamber. Through this membrane wall coolant, for example evaporating water and steam, flow.
  • the further reduction in temperature of the crude synthesis gas is achieved by passing it in an upward direction through the superheater which is situated above the radiation chamber and defined by the upper part of the water tube wall structure.
  • the superheater has advantageously about the same internal diameter as the radiation chamber and it contains at least one tube bank in which steam produced in the evaporator and/or the radiation chamber is superheated thereby indirectly cooling the upflowing crude synthesis gas to the desired temperature in the range from 400 to 600°C.
  • the average linear velocity of the gas in the superheater is preferably in the range from 3 to 15 m/s.
  • the pipe connecting the top of the vertical cylindrical outer pressure shell with the top of the evaporator preferably contains means for separating solidified slag from the crude synthesis gas.
  • Such means consist very suitably of one or more impingement separators, bend separators or cyclones in which at least the relatively coarse slag particles are separated from the crude synthesis gas, cyclone(s), being preferred. Slag particles are discharged from the bottom of the cyclone(s), the partially purified synthesis gas being removed from the top of the cyclone(s) and passed to the top of the evaporator.
  • the gas mixture On its route through the connecting pipe the gas mixture is advantageously further cooled, preferably by indirect heat exchange and to a temperature ranging from 200 to 350°C.
  • the connecting pipe is suitably provided with means by which the gas can be cooled indirectly.
  • coolant for example water and/or steam, can flow are most suitable and are therefore preferred.
  • the vertically arranged evaporator is preferably of a type in which the gas to be cooled is conducted substantially vertically downwards around cooling pipes through which coolant, suitably consisting of water, flows, which is to be transferred to steam.
  • the average linear velocity of the gas in the evaporator is preferably in the range from 3 to 15 m/s.
  • the crude synthesis gas is advantageously cooled in the evaporator to a temperature in the range fran 200 to 350°C.
  • slag particles are separated therefrom in order to purify it further.
  • This separation is carried out in means for separating slag particles iron the cooled crude synthesis gas.
  • These means suitably consist of at least one cyclone, impingement separator or bend separator and they are connected with the bottom of the evaporator by a pipe.
  • one or more cyclones are preferred.
  • the pipe connecting the radiation chamber and the evaporator preferably contains means for separating relatively coarse slag particles from the crude synthesis gas.
  • the separated slag particles are suitably caught in a receiving vessel for slag particles which is connected by a pipe with the means for separating the relatively coarse slag particles from the crude synthesis gas.
  • the receiving vessel is connected by a pipe with the bottom of the evaporator or with the pipe connecting the bottom of the evaporator with the means for separating slag particles from the cooled crude synthesis gas caning from the evaporator. Since on its way through the evaporator the crude synthesis gas is somewhat reduced in pressure, the pressure in the pipe connecting the bottom of the evaporator with the means for separating slag particles is somewhat lower than the pressure in the receiver. Therefore the relatively coarse slag particles caught in the receiver can be easily passed from the receiver to the pipe connected to the bottom of the euaporator, a solid pump not being necessary for this purpose.
  • the relatively coarse slag particles having been removed from the crude synthesis gas before it enters into the evaporator are thus united with this gas after it has been passed through the evaporator.
  • erosion of the evaporator by the relatively coarse particles is obviated ultimately and moreover the relatively coarse particles are very effectively cooled so that they can be sluiced out of the system in an easy way.
  • the relatively coarse slag particles as the other slag particles are removed from the cooled crude synthesis gas.
  • the relatively coarse slag particles caught in the receiving vessel are taken up in water, thus forming a slurry. This can be done by spraying water over the slag particles in the. receiving vessel, the receiving vessel containing means for supplying water at the top and an outlet for slurxy at the bottan..
  • the slurry formed in the receiving vessel is preferably depressurized before it is discharged fran the system.
  • the outlet for slurry at the bottom of the receiving vessel for slag particles is suitably connected with a receiving vessel for slurry, which is intermittently filled with slurry and depressurized, whereafter the depressurized slurry is passed through a pipe to a settler for slurry.
  • the depressurized slurry is advantageously separated into solid material and water and at least part of the water is used again for the uptake of slag particles.
  • the settler preferably comprises an outlet for wet slag particles at the bottom and an outlet for water at its upper part, the latter outlet being connected by a pipe with the means for supplying water to the receiving vessel for slag particles.
  • hot liquid slag is removed from the bottom of the gasifier.
  • This hot liquid slag drips down into a water bath contained in the bottom of the outer pressure shell, where it cools down rapidly and solidifies thus forming more or less big lumps of glassy material. These lumps are sometimes too big to be handled easily.
  • the bottom of the vertical cylindrical outer pressure shell is suitably connected with a slag crusher which is joined by means of a pipe with a receiving vessel for crushed slag in water.
  • the slag lumps are passed together with the surrounding water through the slag crusher wherein they are ground and the mixture of ground slag and water is then passed into the receiving vessel. Thereafter it is depressurized and removed from the system.
  • means are preferably connected to the radiation chamber, the superheater, the evaporator and/or the connecting pipe (s) to remove slag deposits from the inner walls of said components.
  • Said means may be of various types, for example, acoustic, mechanical and/or electrical means.
  • mechanical jogging means are preferably connected for said purpose.
  • the radiation chamber, superheater, connecting pipes and/or the evaporator are preferably designed in such a manner that there is some clearance between the above-mentioned membrane walls, on the inside of which slag particles can settle, and insulating layers suitably arranged against the inside of the (steel) outer walls of said components of the apparatus according to the invention, which outer walls are preferably kept relatively cool, since they must be capable of absorbing forces resulting from the high pressure, for example 30 bar, at which the process according to the invention is preferably carried out.
  • Figure 1 of the drawings represents a simple embodiment of the process according to the invention especially suitable for the conversions of low ash coals i.e. coals having an ash content in the range from 1 to 5%wt.
  • a mixture of ponderous coal oxygen-containing gas and steam is passed into a gasifier 2 where it is converted to an H 2 and CO-containing crude synthesis gas by partial combustion.
  • the gasifier 2 is defined by the lower part of a membrane wall 3 consisting of water tubes through which boiling water is circulated being transferred into high pressure steam.
  • the membrane wall 3 is positioned within a vertical cylindrical outer pressure shell 4.
  • a water bath 5 is present for catching and solidifying liquid slag dropping down from the gasifier 2 through an outlet 6 for liquid slag at the bottom of the water tube wall 3.
  • Liquid slag caught in the water bath 5 solidifies.
  • This material is removed therefrom through an outlet 7 for solidified slag in water. It is passed to a slag crusher 8 where it is crushed to particles with a diameter of at most 50 mm and withdrawn from the system via an outlet 9 together with a volume of water.
  • the proper level of the water in the slag bath 5 is maintained by supplying water to it through a line 10.
  • the hot crude synthesis gas generated in the gasifier 2 contains liquid slag droplets.
  • a quench section 11 which has substantially the same internal diameter as the gasifier 2.
  • the ascending gas is rapidly cooled down by injecting water, steam and/or cold recycle gas into it through nozzles 12.
  • the temperature and the amount of water, steam and/or cold recycle gas are preferably chosen such that the ascending hot crude synthesis gas is cooled down to a temperature at which the entrained slag droplets solidify to slag particles.
  • the crude synthesis gas is passed upwards through a radiation chamber 13, which is defined by an intermediate part of the water tube wall structure 3 and has about the same internal diameter as the quench section 11.
  • the crude synthesis gas is further cooled because it loses heat by radiating it to the tubes of the tube wall structure 3 in which water is converted to steam.
  • solid slag particles which may be sticky at the entrance of the chamber 13 lose their stickyness.
  • the crude synthesis gas is then passed through a superheater 14 in order to cool it still further. It enters the superheater 14 at its bottom and leaves it through an outlet at its top.
  • This superheater 14 is defined by the upper part of the tube wall structure 3 and has about the same internal diameter as the radiation chamber 13.
  • the water enters the tube banks 21 via an inlet 22 at its bottom and the steam leaves the tube banks via an outlet 23 at its top. Heat is transferred by convection to the tube banks 21, the crude synthesis gas being passed from the top to the bottom of the evaporator 20 and being further cooled during its course through the evaporator 20.
  • the cooled crude synthesis gas leaves the evaporator 20 via an outlet 24 which is connected by a pipe 25 to a cyclone 26.
  • a cyclone 26 slag particles are separated from the crude synthesis gas, cooled purified synthesis gas being discharged from the system via a line 27 and separated slag particles being withdrawn from the system via an outlet 28.
  • Figure 2 represents a preferred embodiment of the process and apparatus according to the invention and in the process and apparatus outlined in this figure essentially the same constructional parts are used as depicted in figure 1.
  • the crude synthesis gas being transferred in pipe 18 from the top of superheater 14 to the inlet 19 of the evaporator 20 is firstly introduced into a relatively low efficiency cyclone 29, where relatively coarse slag particles are removed from the synthesis gas. These particles fall down through a pipe 30 into a receiving vessel 31 for slag particles, from which vessel they are discharged via an outlet 32.
  • the synthesis gas fran which the relatively coarse particles have been removed is transferred through a pipe 33 to the inlet 19 of the evaporator 20 and further treated as has been described hereinbefore with regard to figure 1.
  • Figure 3 represents a further extension of the preferred embodiment according to figure 2 in which the outlet 32 of the receiving vessel 31 for relatively coarse particles is connected by a line 34 with the line 25 connecting the outlet 24 of the evaporator 20 with the high efficiency cyclone 26. Therefore in this embodiment not only relatively fine slag particles but also the relatively coarse slag particles are removed from the system via the outlet 28 of cyclone 26 in which they have been separated from the synthesis gas.
  • the advantage of the embodiment according to figure 3 over that according to figure 2 consists in the need of only one sluicing system operating at a relatively low temperature (not shown in both figures) in order to depressurize the slag particles which have been obtained fran the cyclones 31 and 26 at about the relatively high pressure at which the present process is operated.
  • FIG. 4 gives an alternative extension of the preferred embodiment according to figure 2.
  • the receiving vessel 31 is now provided with a sprinkle installation 36 through which water being supplied through a line 35 is sprayed on the slag particles contained in the receiving vessel 31.
  • a slurry of slag particles in water is withdrawn through the outlet 32 and passed via a line 37 to a receiving vessel 38 for slurry.
  • Via a line 39 the slurry is transferred to a sluicing system (not shown) where it is depressurized.
  • the depressurized slurry may be separated by settling and/or filtration into clear water and wet slag particles. The latter are withdrawn from the system.
  • the former can be recycled via the line 35 to the sprinkle installation 36.
  • the coal powder had an average particle size of 50 and, on a dry and ash-free basis, had the following composition:
  • the ash content was 8% by weight and the moisture content 1% by weight.
  • the oxygen-containing gas had the following composition:
  • the pressure in the gasifier was 30 bar and the temperature 1450°C.
  • the quantity of slag drained via the slag discharge 6 was 280 kg/h.
  • the crude synthesis gas was cooled down to a temperature of 900°C by injecting 9000 kg/h cleaned synthesis gas of substantially the same gas composition as the crude gas but having a temperature of 40°C.
  • the synthesis gas was further cooled to a temperature of 800°C in the radiation chamber 13 and still further to 500°C by passing it through the superheater 14.
  • the gas On its way through the evaporator 20 the gas was lowered in temperature to 300°C. It was finally passed through the cyclone 26 where 200 kg/h slag was separated from the gas.
  • the cooled and purified gas leaving the top of the cyclone contained only 0.1%wt. slag which was removed by a water wash.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Industrial Gases (AREA)
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EP83201705A 1982-12-29 1983-11-30 Verfahren und Vorrichtung zur Herstellung von Synthesegas Ceased EP0115094A3 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3248551 1982-12-29
DE3248551 1982-12-29

Publications (2)

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EP0115094A2 true EP0115094A2 (de) 1984-08-08
EP0115094A3 EP0115094A3 (de) 1985-05-22

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EP83201705A Ceased EP0115094A3 (de) 1982-12-29 1983-11-30 Verfahren und Vorrichtung zur Herstellung von Synthesegas

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EP (1) EP0115094A3 (de)
JP (1) JPS59133292A (de)
AU (1) AU2273683A (de)
ZA (1) ZA839538B (de)

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0150533A2 (de) * 1984-01-11 1985-08-07 Shell Internationale Researchmaatschappij B.V. Verfahren und Vorrichtung zur Herstellung von Synthesegas
US4950308A (en) * 1988-07-16 1990-08-21 Krupp Koppers Gmbh Apparatus for producing a product gas from a finely-divided carbon-bearing substance
EP0616022A1 (de) 1993-03-16 1994-09-21 Krupp Koppers GmbH Verfahren für die Druckvergasung von feinteiligen Brennstoffen
US5445658A (en) * 1993-03-16 1995-08-29 Krupp Koppers Gmbh Gasification apparatus for a finely divided combustible material
US5803937A (en) * 1993-01-14 1998-09-08 L. & C. Steinmuller Gmbh Method of cooling a dust-laden raw gas from the gasification of a solid carbon-containing fuel
WO2009080334A2 (de) * 2007-12-22 2009-07-02 Uhde Gmbh Entfernung von flüssigasche und alkalien aus einem synthesegas
EP2336276A1 (de) * 2009-12-12 2011-06-22 KOPF SynGas GmbH & Co. KG Gaskühler mit Klopfvorrichtung
CN105936836A (zh) * 2016-06-07 2016-09-14 广东工业大学 小型生物质气化燃烧系统

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH0653878B2 (ja) * 1988-03-08 1994-07-20 バブコツク日立株式会社 石炭ガス化炉のスラグ回収装置
CN102851080B (zh) * 2011-06-30 2015-08-26 通用电气公司 整体气化联合循环发电系统和气化反应器以及方法

Citations (6)

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Publication number Priority date Publication date Assignee Title
DE1421655B (de) * Badische Anilin- & Soda-Fabrik Ag, 6700 Ludwigshafen Schachtofen zum Vergasen feinkörniger Brennstoffe in der Wirbelschicht
FR1070615A (fr) * 1951-12-12 1954-08-03 Babcock & Wilcox France Générateur de vapeur combiné à un appareil de production de gaz de synthèse
GB783054A (en) * 1955-03-15 1957-09-18 Koppers Gmbh Heinrich Installation for utilising the sensible heat of gases to generate steam
GB793466A (en) * 1954-09-08 1958-04-16 Koppers Gmbh Heinrich Apparatus for the gasification of finely divided solid fuels
GB837307A (en) * 1955-11-16 1960-06-09 Koppers Gmbh Heinrich Process and apparatus for gasifying finely divided fuels
US4188915A (en) * 1975-12-05 1980-02-19 Dr. C. Otto & Comp. G.M.B.H. Water-cooled, high-temperature gasifier

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1421655B (de) * Badische Anilin- & Soda-Fabrik Ag, 6700 Ludwigshafen Schachtofen zum Vergasen feinkörniger Brennstoffe in der Wirbelschicht
FR1070615A (fr) * 1951-12-12 1954-08-03 Babcock & Wilcox France Générateur de vapeur combiné à un appareil de production de gaz de synthèse
GB793466A (en) * 1954-09-08 1958-04-16 Koppers Gmbh Heinrich Apparatus for the gasification of finely divided solid fuels
GB783054A (en) * 1955-03-15 1957-09-18 Koppers Gmbh Heinrich Installation for utilising the sensible heat of gases to generate steam
GB837307A (en) * 1955-11-16 1960-06-09 Koppers Gmbh Heinrich Process and apparatus for gasifying finely divided fuels
US4188915A (en) * 1975-12-05 1980-02-19 Dr. C. Otto & Comp. G.M.B.H. Water-cooled, high-temperature gasifier

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0150533A3 (en) * 1984-01-11 1986-06-11 Shell Internationale Research Maatschappij B.V. Process and apparatus for the production of synthesis gas
EP0150533A2 (de) * 1984-01-11 1985-08-07 Shell Internationale Researchmaatschappij B.V. Verfahren und Vorrichtung zur Herstellung von Synthesegas
US4950308A (en) * 1988-07-16 1990-08-21 Krupp Koppers Gmbh Apparatus for producing a product gas from a finely-divided carbon-bearing substance
US5803937A (en) * 1993-01-14 1998-09-08 L. & C. Steinmuller Gmbh Method of cooling a dust-laden raw gas from the gasification of a solid carbon-containing fuel
EP0616022A1 (de) 1993-03-16 1994-09-21 Krupp Koppers GmbH Verfahren für die Druckvergasung von feinteiligen Brennstoffen
US5445658A (en) * 1993-03-16 1995-08-29 Krupp Koppers Gmbh Gasification apparatus for a finely divided combustible material
US5441547A (en) * 1993-03-16 1995-08-15 Krupp Koppers Gmbh Method for gasification of a finely divided combustible material
WO2009080334A2 (de) * 2007-12-22 2009-07-02 Uhde Gmbh Entfernung von flüssigasche und alkalien aus einem synthesegas
WO2009080334A3 (de) * 2007-12-22 2010-02-25 Uhde Gmbh Entfernung von flüssigasche und alkalien aus einem synthesegas
AU2008340600B2 (en) * 2007-12-22 2013-07-04 Thyssenkrupp Uhde Gmbh Removal of liquid ash and alkalis from a synthesis gas
RU2490314C2 (ru) * 2007-12-22 2013-08-20 Тиссенкрупп Уде Гмбх Удаление жидкого шлака и щелочей из синтез-газа
CN101910376B (zh) * 2007-12-22 2017-04-05 蒂森克虏伯伍德有限公司 从合成气中去除液态灰和碱的方法
EP2336276A1 (de) * 2009-12-12 2011-06-22 KOPF SynGas GmbH & Co. KG Gaskühler mit Klopfvorrichtung
CN105936836A (zh) * 2016-06-07 2016-09-14 广东工业大学 小型生物质气化燃烧系统
CN105936836B (zh) * 2016-06-07 2023-09-15 广东工业大学 小型生物质气化燃烧系统

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ZA839538B (en) 1984-08-29
JPS59133292A (ja) 1984-07-31
EP0115094A3 (de) 1985-05-22
AU2273683A (en) 1984-07-05

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