EP2226376A1 - Konfiguration für Vergasung und Quenching - Google Patents

Konfiguration für Vergasung und Quenching Download PDF

Info

Publication number
EP2226376A1
EP2226376A1 EP09154336A EP09154336A EP2226376A1 EP 2226376 A1 EP2226376 A1 EP 2226376A1 EP 09154336 A EP09154336 A EP 09154336A EP 09154336 A EP09154336 A EP 09154336A EP 2226376 A1 EP2226376 A1 EP 2226376A1
Authority
EP
European Patent Office
Prior art keywords
gas
wall
vessel
quench
tubular
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.)
Withdrawn
Application number
EP09154336A
Other languages
English (en)
French (fr)
Inventor
Robert Erwin Van Den Berg
Wouter Koen Harteveld
Evert Johannes Van Holthoon
Thomas Paul Von Kossack-Glowczewski
Joachim Papendick
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
Original Assignee
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
Priority to EP09154336A priority Critical patent/EP2226376A1/de
Priority to CN2010201379667U priority patent/CN201785362U/zh
Publication of EP2226376A1 publication Critical patent/EP2226376A1/de
Withdrawn legal-status Critical Current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
    • C10J3/466—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
    • C10J3/72—Other features
    • C10J3/74—Construction of shells or jackets
    • C10J3/76—Water jackets; Steam boiler-jackets
    • 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
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • C10J3/845—Quench rings
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • 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
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • 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
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
    • 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
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
    • C10K1/101—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids with water 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/09—Mechanical details of gasifiers not otherwise provided for, e.g. sealing means

Definitions

  • the invention relates to a configuration for gasification and quenching.
  • the configuration comprises a vertical elongated gasification reactor having a product gas outlet at its upper end is fluidly connected to an upper end of a vertically elongated quench vessel by means of a duct.
  • WO-A-2007125046 Such a configuration is known and described in WO-A-2007125046 .
  • This publication describes a gasification system having a gasification reactor and a synthesis gas cooling vessel.
  • the gasification reactor has a pressure shell for maintaining a pressure higher than atmospheric pressure. Inside the pressure shell a gasification chamber is present wherein during operation the synthesis gas can be formed. Via a connecting conduit the gasification reactor is connected to the cooling vessel. In the cooling vessel the synthesis gas is cooled by contacting the gas with evaporating droplets of water.
  • the connecting conduit as illustrated in the Figures of WO-A-2007125046 is either an upwardly straight conduit connecting the upper part of the gasification reactor with the cooling vessel or a bended conduit.
  • a disadvantage of the design of the connecting conduits is that the bended design of Figure 3 is constructively difficult to build due to the curved parts.
  • the design of Figure 2 is disadvantageous because unwanted gas flowing regimes are found in the cooling vessel that negatively influences the cooling by the mist of water droplets.
  • It is an object of the present invention is to provide an improved configuration for gasification and quenching.
  • Configuration for gasification and quenching comprising a vertical elongated gasification reactor having a product gas outlet at its upper end, fluidly connected to an upper end of a vertically elongated quench vessel by means of a duct, wherein the upper end of the gasification reactor is provided with a gas reversal chamber having a gas outlet connected to the duct and wherein the duct is connected with the upper end of the quench vessel at a lower elevation than the gas reversal chamber.
  • the gasification reactor and the quench vessel are defined using terms in this description as upper, lower, downwardly and vertically. These terms relate to the orientation of the configuration according the invention when in use.
  • the gasification reactor is a vertical elongated gasification reactor having a product gas outlet at its upper end.
  • An example of such a gasification reactor is described in the aforementioned WO-A-2007125046 .
  • Such gasification reactors are suited to gasify ash-containing feedstocks.
  • a layer of molten slag will be present on the internal walls of the gasification reactor, wherein the molten slag slowly moves downwards to a lower slag outlet opening.
  • the synthesis gas flows upwards to a higher gas outlet.
  • the synthesis gas is thus separated from the slag before it is cooled.
  • gasification reactors are excluded which gave a quenching zone at their lower end in which quench zone synthesis gas and slag are reduced in temperature in the same cooling step.
  • a synthesis gas comprising for its majority of hydrogen and carbon monoxide.
  • the feedstock is suitably an ash containing carbonaceous feedstock.
  • feedstocks are coal, coke from coal, coal liquefaction residues, petroleum coke, soot, biomass, and particulate solids derived from oil shale, tar sands and pitch.
  • the coal may be of any type, including lignite, subbituminous, bituminous and anthracite.
  • gasification is carried out in a gasification chamber at a temperature in the range from 1200 to 1800 °C, preferably between 1400 and 1800 °C and at a pressure in the range from 1 to 200 bar, preferably between 20 and 100 bar, more preferably between 40 and 70 bar.
  • the synthesis gas is partly cooled before it is fed to the quench vessel.
  • the synthesis gas is preferably partly cooled by means of a gas or liquid quench as the gas leaves the gasification chamber.
  • the synthesis gas entering the quench vessel has a temperature between 500 and 900 °C, more preferably between 600 and 900 °C.
  • the synthesis gas will typically contain some residual ash particles, fly-ash, when an ash-containing feed is gasified.
  • the synthesis gas is cooled from an elevated temperature to a lower temperature by contacting the synthesis gas with a suitable liquid quench medium.
  • the temperature of the gas as it leaves the quench vessel is preferably between 200 and 600 °C and more preferably between 300 and 500 °C and even more preferably between 350 and 450 °C.
  • the quenching medium may be any liquid having the required cooling capacity.
  • Non-limiting examples are a hydrocarbon liquid, a waste stream as obtained in a downstream process, which uses the synthesis gas as feedstock.
  • the liquid comprises at least 50 wt% water.
  • Most preferably the liquid is substantially comprised of water (i.e. > 95 vol%).
  • the wastewater also referred to as black water, as obtained in a possible downstream synthesis gas scrubber is used as the quenching medium.
  • Contacting with the liquid quenching medium can be performed in different manners for which different types of quench vessels are preferably used.
  • the synthesis gas is passed through a water bath via a diptube.
  • droplets of liquid quench medium is injected into a stream of synthesis gas.
  • Figures 1 and 2 will show suitable quench vessels for both methods.
  • the temperature of said liquid is at most 50 °C below the bubble point at the prevailing pressure conditions at the point of injection, particularly at most 15 °C, even more preferably at most 10 °C below the bubble point.
  • the injected quenching medium is water, it usually has a temperature of above 90 °C, preferably above 150 °C, more preferably from 200 °C to 270 °C, for example 230 °C.
  • the temperature will obviously depend on the operating pressure of the gasification reactor, i.e. the pressure of the raw synthesis gas as specified further below.
  • the pressure of the raw synthesis gas as specified further below.
  • the quenching medium is injected in the form of a mist of fine liquid droplets. More preferably the mist comprises droplets having a diameter of from 50 to 200 ⁇ m, even more preferably from 50 to 150 ⁇ m. Preferably, at least 60 vol.% of the injected liquid is in the form of droplets having the indicated sizes.
  • the quenching medium is preferably injected with a mean velocity of between 10 and 60 m/s and more preferably between 20 and 50 m/s.
  • Injection is preferably performed by means of a nozzle or an arrangement of nozzles. More preferably an arrangement of more than one nozzles for atomisation and spraying liquid in a downwardly direction is used.
  • a downwardly direction is especially meant that the direction of the liquid as it is discharged from the nozzles is vertically downward. It is of course understood that the flow of quench medium as it is discharged from the nozzle will have a cone form and that the average direction of this cone will be the direction of the liquid as it is sprayed from the nozzle.
  • the nozzle can be a hydraulic nozzle. Hydraulic nozzles require a high injection pressure of typically at least 40 bar above the pressure of the synthesis gas.
  • twin fluid nozzle wherein an atomisation gas, which may e.g. be N 2 , CO 2, steam or synthesis gas atomises the fluid into fine droplets.
  • a preferred atomisation gas is synthesis gas as recycled from a downstream process step.
  • atomisation gas has the advantage that the difference between injection pressure and the pressure of the raw synthesis gas may be reduced while achieving the same droplet size and velocity.
  • twin-fluid nozzles are well known and can for example be obtained from Spraying Systems Co. Examples of suitable nozzles are described in US-A-5732885 and US-A-2004/0222317 .
  • the quenching medium is injected with an injection pressure of at least 5 bar above the pressure of the raw synthesis gas, preferably from at least 10 bar above the pressure of the raw synthesis gas and up to 20 bar above the pressure of the raw synthesis gas.
  • Figure 1 shows a configuration (1) for gasification and quenching, comprising a vertical elongated gasification reactor (2) and a vertically elongated quench vessel (6).
  • the gasification reactor (2) has a product gas outlet (3) at its upper end (4), fluidly connected to an upper end (5) of the quench vessel (6) by means of a duct (7).
  • the upper end (4) of the gasification reactor (2) is provided with a gas reversal chamber (8) having a gas outlet (9) connected to the duct (7).
  • the duct (7) is connected with the upper end (5) of the quench vessel (6) at a lower elevation than the gas reversal chamber (8).
  • the duct (7) comprises a downwardly positioned straight tubular conduit (10).
  • the straight tubular conduit (10) suitably comprises a co-axial inner conduit (11), wherein the inner conduit has a water-cooled wall, suitably a so-called membrane wall.
  • the angle ⁇ between the horizon and the tubular conduit (10) is between 40 and 70°, and more preferably from 45 to 50°, lower angles are not advantageous because fly-ash may accumulate in conduit (11). Higher angles are not advantageous because the sharp curves the gas has to make results in a high risk of erosion.
  • membrane wall is commonly known and refers to a cooled wall arrangement. Such a wall is gas tight and comprises of an arrangement of interconnected conduits. Cooling is typically accomplished by evaporating cooling water. These conduits are fluidly connected via a common distributor to a supply for cooling medium and at their other ends fluidly connected to a common header to discharge used cooling medium.
  • the gasification reactor (2) is provided with a gasification chamber (35).
  • Gasification chamber (35) is fluidly connected to a lower opening (32) for discharge of slag and fluidly connected at its upper end to a vertical transport conduit (34).
  • Transport conduit (34) is provided at its lower end with an injection ring (33) to inject a quench gas or liquid to partly cool the hot synthesis gas as formed in the gasification chamber.
  • the upper end of the vertical transport conduit is connected to gas reversal chamber (8).
  • Gas reversal chamber (8) is suitably an in-line extension of vertical transport conduit (34), closed at its upper end and provided with an opening in its vertical walls, which opening fluidly connects with inner conduit (11).
  • the carbonaceous feed and an oxygen-containing stream are fed via lines (31) to the gasification chamber (35).
  • gasification chamber (35) In gasification chamber (35) a raw synthesis gas and a slag is obtained. To this end usually several burners (not shown) are present in the gasification chamber (35).
  • the walls of the gasification chamber (35) and the walls of the transport conduit (34) are preferably water cooled, preferably by means of a membrane wall.
  • Figure 1 also shows that the quench vessel (6) is provided with an inlet (12) for gas at its upper end (5), and with an outlet (13) for cooled gas.
  • the quench vessel (6) is provided at its upper end (5) with a first internal tubular wall part (16), which wall part (16) is fluidly connected to the inlet (12) for gas.
  • the tubular wall part (16) is connected at its lower end (17) to a diptube (18) terminating in a water bath (19).
  • the internal tubular wall part (16) and the diptube (18) have a smaller diameter than the quench vessel (6) resulting in an upper annular space (21) between said internal tubular wall part (16) and the wall of quench vessel (6) and a lower annular space (22) between the diptube (18) and the wall of quench vessel (6).
  • Annular space (21) and (22) are preferably gas tight separated by sealing (23) to avoid ingress of ash particles from space (22) into space (21).
  • the tubular wall part (16) preferably has a diameter, which is smaller than the diameter of the tubular diptube (18) at the outlet opening (17) of wall part (16).
  • the tubular wall part (16) is oriented co-axial with the diptube (18) as shown in the Figure.
  • the diptube (18) is open to the interior of the quench vessel (6) at its lower end (18a). This lower end (18a) is in fluid communication with a gas outlet (13) as present in the quench vessel wall (6a).
  • the diptube (18) is partly submerged in a water bath (19).
  • a draft tube (27) is present to direct the syngas upwardly in the annular space (28) formed between draft tube (27) and diptube (18).
  • deflector plate (27a) is present to provide a rough separation between entrained water droplets and the quenched syngas.
  • Deflector plate (27a) preferably extends from the outer wall of the diptube (18).
  • the lower part (26) of the diptube (18) has a smaller diameter than the upper part (25) as shown in Figure 1 . This is advantageous because the layer of water as present on the inner wall of diptube (18) will increase in said lower end. Another result is that the annular area for the water bath (19) will increase. This is advantageous because it enables one to use a more optimized, smaller, diameter for quench vessel (6).
  • the quench vessel (6) is further provided with an outlet (20) for water containing for example fly-ash.
  • the tubular wall part (16) is preferably formed by an arrangement of interconnected parallel arranged tubes resulting in a substantially gas-tight tubular wall running from a cooling water distributor to a header.
  • the cooling of tubular wall part (16) can be performed by either sub-cooled water or boiling water.
  • the walls of the diptube (18) are preferably of a simpler design, like for example a metal plate wall.
  • a discharge conduit (30) is preferably present having an outflow opening for liquid water directed such that, in use, a film of water is achieved along the inner wall of the diptube (18).
  • Discharge conduit (30) is connected to water supply conduit (29).
  • the arrangement of more than one nozzles (47) for atomisation and spraying liquid in a downwardly direction may have any design which enables contacting of the synthesis gas flow and the liquid medium.
  • the arrangement comprises of a number of radial disposed arms extending from the wall of the quenching vessel and through openings in the wall of the divergent conical part to a central position.
  • the arms are provided with one or more downwardly directed nozzles.
  • the minimal horizontal distance between the centre of the outlet opening of the nozzles and the wall of the divergent conical part is between 0.2 and 1 m.
  • each arm may suitably have from 3 to and including 10 nozzles.
  • the nozzle closest to the central position has a slightly tilted main outflow direction between downwardly and to the central position.
  • the arms are preferably present in one horizontal plane. Alternatively the arms may be present in different planes, for example in a staggered configuration. It is believed, without wishing to be bound to the following theory, that by providing the arrangement of more than one nozzle (47) at this location, the risk that ashes deposit on the wall is further reduced.
  • the synthesis gas contains a substantial amount of non-gaseous components it may be advantageous under these conditions to provide means for supplying a shielding gas around the nozzles.
  • the arms are provided with means to avoid or remove deposits to accumulate on top of the arms.
  • Such means can be mechanical rapper means directly on the arms itself or on metal shields placed above said arm.
  • Such means can also be acoustic cleaning means.
  • Such means can also be blasting means to continuously or intermittently blast away any solid deposits or with which also remove any solid deposits.
  • the shielding and/or blasting gas may be e.g. N 2 , CO 2 , steam or synthesis gas and is more preferably of the same source as the atomisation gas.
  • the first inner wall part (43) and/or the wall (46) of the divergent conical part (45) preferably has a water-cooled membrane wall design.
  • the angle beta between the surface of the wall (46) of the divergent conical part (45) and the vertical axis is preferably between 3° to 30° and more preferably between 5° and 10°.
  • the divergent conical part (45) is preferably followed at its lower end (49) by a second tubular inner wall (50) having a lower open end (51). With followed is here meant that both parts may optionally be fixed to each other to form a gas tight connection.
  • the lower end (51) is in fluid communication with the outlet (40) for cooled gas.
  • the second tubular inner wall (50) may optionally be designed a membrane wall. Because the temperature conditions at that part of the quench vessel (6') are more moderate, a more simple design, suitably made from a high alloy steel plate, for this part is preferred.
  • the first internal tubular wall part (43), divergent conical part (45) and second tubular inner wall (51) can be provided with one or more cleaning devices (51), which can be mechanical rappers, pneumatic blasters devices or acoustic cleaning devices.
  • the internal vessel dimensions which define the pathway (42) for gas flow are so chosen to achieve a certain minimal downward gas velocity of synthesis gas for a given design throughput.
  • the gas velocity is at least 1 m/s when the gas passes the first internal tubular wall part (43).
  • the length of the second tubular inner wall (51) in the direction of the flow path for gas should be long enough to achieve the desired cooling after the quenching medium has been added in the upstream part.
  • the ratio between the internal diameter of the second tubular inner wall and its length is between 1:1 and 1:6.

Landscapes

  • 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)
EP09154336A 2009-03-04 2009-03-04 Konfiguration für Vergasung und Quenching Withdrawn EP2226376A1 (de)

Priority Applications (2)

Application Number Priority Date Filing Date Title
EP09154336A EP2226376A1 (de) 2009-03-04 2009-03-04 Konfiguration für Vergasung und Quenching
CN2010201379667U CN201785362U (zh) 2009-03-04 2010-03-04 用于气化和骤冷的装置

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP09154336A EP2226376A1 (de) 2009-03-04 2009-03-04 Konfiguration für Vergasung und Quenching

Publications (1)

Publication Number Publication Date
EP2226376A1 true EP2226376A1 (de) 2010-09-08

Family

ID=41043137

Family Applications (1)

Application Number Title Priority Date Filing Date
EP09154336A Withdrawn EP2226376A1 (de) 2009-03-04 2009-03-04 Konfiguration für Vergasung und Quenching

Country Status (2)

Country Link
EP (1) EP2226376A1 (de)
CN (1) CN201785362U (de)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2524957A1 (de) * 2011-05-18 2012-11-21 Stirling.DK ApS Biomassenvergasungssystem mit einem Steigstromvergaser
CN103820169A (zh) * 2014-03-11 2014-05-28 上海锅炉厂有限公司 一种复合式高温粗煤气冷却净化装置及方法

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102851081B (zh) * 2012-09-28 2014-12-31 中国船舶重工集团公司第七一一研究所 一种用水分级激冷的水煤浆或干煤粉气化装置

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3988421A (en) * 1972-05-10 1976-10-26 Tecnochim S.R.L. Gas cleaning process and equipment
JPS53110967A (en) * 1977-03-11 1978-09-28 Babcock Hitachi Kk Device of quencher
US4859214A (en) * 1988-06-30 1989-08-22 Shell Oil Company Process for treating syngas using a gas reversing chamber
US5732885A (en) 1994-10-07 1998-03-31 Spraying Systems Co. Internal mix air atomizing spray nozzle
WO2001057161A1 (de) * 2000-01-31 2001-08-09 Thermoselect Ag 2-stufige synthesegaskühlung
WO2004005438A1 (en) * 2002-07-02 2004-01-15 Shell Internationale Research Maatschappij B.V. Method for gasification of a solid carbonaceous feed and a reactor for use in such a method
US20040222317A1 (en) 2002-05-07 2004-11-11 Spraying Systems Co. Internal mixing atomizing spray nozzle assembly
WO2007125046A1 (en) 2006-05-01 2007-11-08 Shell Internationale Research Maatschappij B.V. Gasification system and its use

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3988421A (en) * 1972-05-10 1976-10-26 Tecnochim S.R.L. Gas cleaning process and equipment
JPS53110967A (en) * 1977-03-11 1978-09-28 Babcock Hitachi Kk Device of quencher
US4859214A (en) * 1988-06-30 1989-08-22 Shell Oil Company Process for treating syngas using a gas reversing chamber
US5732885A (en) 1994-10-07 1998-03-31 Spraying Systems Co. Internal mix air atomizing spray nozzle
WO2001057161A1 (de) * 2000-01-31 2001-08-09 Thermoselect Ag 2-stufige synthesegaskühlung
US20040222317A1 (en) 2002-05-07 2004-11-11 Spraying Systems Co. Internal mixing atomizing spray nozzle assembly
WO2004005438A1 (en) * 2002-07-02 2004-01-15 Shell Internationale Research Maatschappij B.V. Method for gasification of a solid carbonaceous feed and a reactor for use in such a method
WO2007125046A1 (en) 2006-05-01 2007-11-08 Shell Internationale Research Maatschappij B.V. Gasification system and its use

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2524957A1 (de) * 2011-05-18 2012-11-21 Stirling.DK ApS Biomassenvergasungssystem mit einem Steigstromvergaser
CN103820169A (zh) * 2014-03-11 2014-05-28 上海锅炉厂有限公司 一种复合式高温粗煤气冷却净化装置及方法
CN103820169B (zh) * 2014-03-11 2015-08-19 上海锅炉厂有限公司 一种复合式高温粗煤气冷却净化装置及方法

Also Published As

Publication number Publication date
CN201785362U (zh) 2011-04-06

Similar Documents

Publication Publication Date Title
EP2190555B1 (de) Sprühdüsenverteiler und verfahren zum abschrecken eines heissen gases unter verwendung einer derartigen anordnung
EP2197988B1 (de) Löschgefäss
US8475546B2 (en) Reactor for preparing syngas
US8960651B2 (en) Vessel for cooling syngas
EP2364345B1 (de) Behälter zum abkühlen von syngas
EP2226376A1 (de) Konfiguration für Vergasung und Quenching
US9261307B2 (en) Self cleaning nozzle arrangement

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO SE SI SK TR

AX Request for extension of the european patent

Extension state: AL BA RS

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION HAS BEEN WITHDRAWN

18W Application withdrawn

Effective date: 20110307