WO2007125047A1 - Réacteur de gazéification et son utilisation - Google Patents

Réacteur de gazéification et son utilisation Download PDF

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Publication number
WO2007125047A1
WO2007125047A1 PCT/EP2007/053871 EP2007053871W WO2007125047A1 WO 2007125047 A1 WO2007125047 A1 WO 2007125047A1 EP 2007053871 W EP2007053871 W EP 2007053871W WO 2007125047 A1 WO2007125047 A1 WO 2007125047A1
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WO
WIPO (PCT)
Prior art keywords
gas
mist
synthesis gas
pressure
annular space
Prior art date
Application number
PCT/EP2007/053871
Other languages
English (en)
Inventor
Robert Erwin Van Den Berg
Franciscus Gerardus Van Dongen
Thomas Paul Von Kossak-Glowczewski
Pieter Lammert Zuideveld
Original Assignee
Shell Internationale Research Maatschappij B.V.
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
Priority claimed from PCT/EP2006/061951 external-priority patent/WO2006117355A1/fr
Application filed by Shell Internationale Research Maatschappij B.V. filed Critical Shell Internationale Research Maatschappij B.V.
Priority to JP2009508306A priority Critical patent/JP2009535471A/ja
Priority to AU2007245732A priority patent/AU2007245732B2/en
Priority to EP07728330A priority patent/EP2016160A1/fr
Publication of WO2007125047A1 publication Critical patent/WO2007125047A1/fr

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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
    • C10J3/46—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
    • C10J3/82—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
    • 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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen only

Definitions

  • the present invention relates to an improved gasification reactor for preparing synthesis gas comprising CO, CO2 and H2 from a carbonaceous stream using an oxygen containing stream.
  • the invention is also directed to a system for preparing such a synthesis gas and to a process, which may be performed in said reactor and in said system. Background of the invention
  • synthesis gas Methods for producing synthesis gas are well known from practice.
  • An example of a method for producing synthesis gas is described in EP-A-400740.
  • a carbonaceous stream such as coal, brown coal, peat, wood, coke, soot, or other gaseous, liquid or solid fuel or mixture thereof, is partially combusted in a gasification reactor using an oxygen containing gas such as substantially pure oxygen or (optionally oxygen enriched) air or the like, thereby obtaining a.o. synthesis gas (CO and H2 ) , CO2 and a slag.
  • CO and H2 substantially pure oxygen or (optionally oxygen enriched) air or the like
  • the hot product gas in the reactor of EP-A-400740 flows upwardly.
  • This hot product gas i.e. raw synthesis gas
  • This hot product gas usually contains sticky particles that lose their stickiness upon cooling.
  • These sticky particles in the raw synthesis gas may cause problems downstream of the gasification reactor where the raw synthesis gas is further processed. This because undesirable deposits of the sticky particles on, for example, walls, valves or outlets may adversely affect the process. Moreover such deposits are hard to remove. Therefore, the raw synthesis gas is quenched in a quench section. In such a quench section a quench gas is injected into the upwardly moving raw synthesis gas in order to cool it .
  • EP-A-662506 describes a process to cool synthesis gas by injecting downwardly a cooling gas into said hot synthesis gas at the interface of a combustion chamber and a tubular part fluidly connected to the top of the combustion chamber.
  • a similar reactor as in EP-A-400740 is described in
  • WO-A-2004/005438 of the same applicant.
  • This publication describes a gasification combustion chamber and a tubular part fluidly connected to an open upper end of said combustion chamber. Both combustion chamber and tubular part are located in a pressure shell defining an annular space between said pressure shell and the combustion chamber and tubular part respectively. According to this publication measures are required to avoid dust laden raw synthesis gas as prepared in the combustion chamber to enter the annular space.
  • This publication also describes a syngas cooler having three heat exchanging surfaces located one above the other as present in a separate pressure vessel.
  • US-A-5803937 describes a gasification reactor and a syngas cooler within one pressure vessel.
  • a tubular part fluidly connected to an open upper end of a combustion chamber, both located within a pressure shell.
  • the gas is deflected 180° to flow downwardly through the annular space between tubular part and the wall of the pressure shell.
  • heat exchanging surfaces are present to cool the hot gas.
  • the afore discussed gasification reactors have in common that the synthesis gas as produced flows substantially upwards and the slag flows substantially downwards relative to the gasification burners as present in said reactors. Thus, all these reactors have an outlet for slag, which is separate from the outlet for synthesis gas. This in contrast to a class of gasification reactors as for example described in EP-A-926441 where both slag and synthesis gas flow downwardly and wherein both the outlet for slag and synthesis gas are located at the lower end of the reactor.
  • the present invention is directed to an improved reactor of the type where slag and synthesis gas are separately discharged from said reactor as in e.g. WO-A-2004/005438 and US-A-5803937.
  • a problem with the syngas cooler of WO-A-2004/005438 and also with the apparatus of US-A-5803937 is that the heat exchanging surfaces introduce a large complexity to the design of said apparatuses .
  • Another problem with the syngas cooler of WO-A-2004/005438 and also with the apparatus of US-A-5803937 is that the heat exchanging surfaces are vulnerable to fouling from feedstocks with for instance a high alkaline content. There is thus a desire to process high alkaline feedstocks as well as a desire to provide more simple gasification reactors.
  • a slag bath located in a lower part of the pressure shell; - a gasifier wall arranged inside the pressure shell defining a gasification chamber wherein during operation the synthesis gas can be formed, a lower open part of the gasifier wall which is in fluid communication with the slag bath and an open upper end of the gasifier wall which is in fluid communication with a quench zone; - a quench zone comprising a tubular formed part positioned within the pressure shell, open at its lower and upper end and having a smaller diameter than the pressure shell thereby defining an annular space around the tubular part, wherein the lower open end of the tubular formed part is fluidly connected to the upper end of the gasifier wall and the upper open end of the tubular formed part is in fluid communication with the annular space; - wherein at the lower end of the tubular part injecting means are present for injecting a liquid or gaseous cooling medium and wherein in the annular space injecting means are present to inject a liquid in the form of a mist and wherein an outlet for
  • the invention is also directed to the following system for preparing a purified mixture comprising carbon monoxide and hydrogen comprising of a gasification reactor according to the present invention, wherein the outlet for synthesis gas is fluidly connected to an inlet of a wet gas scrubber and wherein the wet gas scrubber is provided for an outlet for purified mixture comprising carbon monoxide and hydrogen.
  • the above system is advantageous because a dry solid removal process step can be omitted and the overall system can be made more simple.
  • the invention is also directed to a process to prepare a mixture comprising of carbon monoxide and hydrogen by partial oxidation of a solid carbonaceous feed in a gasification reactor according to the present invention or in a system according to the present invention.
  • a solid carbonaceous feed is partially oxidized in the gasification chamber with an oxygen comprising gas to form an upwardly moving gas mixture having a temperature of between 1200 and 1800 0 C preferably between 1400 and 1800 0 C.
  • This mixture is first cooled in the tubular part to a temperature of between 500 and 900 0 C and subsequently further cooled in the annular part to below 500 0 C by injecting a mist of liquid droplets into the gas flow.
  • Figure 1 schematically shows a process scheme for a system for preparing a purified mixture comprising carbon monoxide and hydrogen
  • Figure 2 schematically shows a process scheme for a system for preparing a purified mixture comprising carbon monoxide and hydrogen .
  • FIG. 3 schematically shows a longitudinal cross- section of a preferred gasification reactor. Detailed description of the invention
  • the gasification reactor according to the present invention is suitably used to prepare a mixture comprising of carbon monoxide and hydrogen by partial oxidation of a solid carbonaceous feed in a gasification reactor according to the present invention or in a system according to the present invention.
  • a solid carbonaceous feed is partially oxidized in the gasification chamber with an oxygen comprising gas to form an upwardly moving gas mixture having a temperature of between 1200 and 1800 0 C preferably between 1400 and 1800 0 C.
  • This mixture is cooled, in a first cooling step, in the tubular part to a temperature of between 500 and 900 0 C and subsequently further cooled, in a second cooling step, in the annular part to below 500 0 C by injecting a mist of liquid droplets into the gas flow.
  • the solid carbonaceous feed is partially oxidised with an oxygen comprising gas.
  • Preferred carbonaceous feeds are solid, high carbon containing feedstocks, more preferably it is substantially (i.e. > 90 wt . % ) comprised of naturally occurring coal or synthetic (petroleum) cokes, most preferably coal.
  • Suitable coals include lignite, bituminous coal, sub-bituminous coal, anthracite coal, and brown coal.
  • this so-called gasification is carried out by partially combusting the carbonaceous feed with a limited volume of oxygen at the elevated temperature in the absence of a catalyst.
  • initial pulverisation of the coal is preferred to fine coal particulates.
  • fine particulates is intended to include at least pulverized particulates having a particle size distribution so that at least about 90% by weight of the material is less than 90 ⁇ m and moisture content is typically between 2 and 8% by weight, and preferably less than about 5% by weight.
  • the gasification is preferably carried out in the presence of oxygen and optionally some steam, the purity of the oxygen preferably being at least 90% by volume, nitrogen, carbon dioxide and argon being permissible as impurities.
  • Substantially pure oxygen is preferred, such as prepared by an air separation unit (ASU) .
  • the feed is preferably dried before use.
  • the oxygen used is preferably heated before being contacted with the coal, preferably to a temperature of from about 200 to 500 0 C.
  • the partial oxidation reaction is preferably performed by combustion of a dry mixture of fine particulates of the carbonaceous feed and a carrier gas with oxygen in a suitable burner as present in the gasification chamber of the reactor according to the invention.
  • suitable burners are described in US-A-48887962, US-A-4523529 and US-A-4510874.
  • the gasification chamber is preferably provided with one or more pairs of partial oxidation burners, wherein said burners are provided with supply means for a solid carbonaceous feed and supply means for oxygen.
  • a pair of burners is here meant two burners, which are directed diametric into the gasification chamber. This results in a pair of two burners in a substantially opposite direction at the same horizontal position.
  • the firing direction of the burners may be slightly tangential as for example described in EP-A-400740.
  • suitable carrier gasses to transport the dry and solid feed to the burners are steam, nitrogen, synthesis gas and carbon dioxide.
  • nitrogen is used when the synthesis gas is used for especially power generation and as feedstock to make ammonia.
  • Carbon dioxide is preferably used when the synthesis gas is subjected to downstream shift reactions.
  • the shifted synthesis gas may for example be used as feed gas to a Fischer-Tropsch synthesis or to prepare hydrogen methanol and/or dimethyl ether .
  • the synthesis gas discharged from the gasification reactor comprises at least H2, CO, and CO2.
  • the raw synthesis gas is cooled in the first cooling step in the tubular part to a temperature below the solidification temperature of the non-gaseous components before performing the second cooling step.
  • the solidification temperature of the non-gaseous components in the raw synthesis gas will depend on the carbonaceous feed and is usually between 600 and 1200 0 C and more especially between 500 and 1000 0 C, for coal type feedstocks.
  • the first cooling step in the tubular part may be performed by injecting a quench gas.
  • Cooling with a gas quench is well known and described in for example EP-A-416242, EP-A-662506 and WO-A-2004/005438.
  • suitable quench gases are recycle synthesis gas and steam.
  • this first cooling is performed by injecting a mist of liquid droplets into the gas flow as will be described in more detail below.
  • the use of the liquid mist as compared to a gas quench is advantageous because of the larger cooling capacity of the mist.
  • the liquid may be any liquid having a suitable viscosity in order to be atomized.
  • Non-limiting examples of the liquid to be injected are a hydrocarbon liquid, a waste stream etc.
  • the liquid comprises at least 50% water.
  • the liquid is substantially comprised of water (i.e.
  • the wastewater also referred to as black water
  • the process condensate of an optional downstream water shift reactor is used as the liquid.
  • 'raw synthesis gas' is meant the gas mixture as directly obtained in the gasification reactor. This product stream may - and usually will - be further processed, for example in a dry solids removal system, wet gas scrubber and/or a shift converter.
  • 'mist' is meant that the liquid is injected in the form of small droplets. If water is to be used as the liquid, then preferably more than 80%, more preferably more than 90%, of the water is in the liquid state .
  • the injected mist has a temperature of at most 50 0 C below the bubble point at the prevailing pressure conditions at the point of injection, particularly at most 15 0 C, even more preferably at most 10 0 C below the bubble point.
  • the injected liquid is water, it usually has a temperature of above 90 0 C, preferably above 150 0 C, more preferably from 200 0 C to 230 0 C.
  • the temperature will obviously depend on the operating pressure of the gasification reactor, i.e. the pressure of the raw synthesis as specified further below.
  • the pressure of the raw synthesis i.e. the pressure of the raw synthesis as specified further below.
  • the mist comprises droplets having a diameter of from 50 to 200 ⁇ m, preferably from 100 to 150 ⁇ m.
  • at least 80 vol.% of the injected liquid is in the form of droplets having the indicated sizes.
  • the mist is preferably injected with a velocity of 30-90 m/s, preferably 40-60 m/s.
  • the mist is injected with an injection pressure of at least 10 bar above the pressure of the raw synthesis gas as present in the gasification reactor, preferably from 20 to 60 bar, more preferably about 40 bar, above the pressure of the raw synthesis gas. If the mist is injected with an injection pressure of below 10 bar above the pressure of the raw synthesis gas, the droplets of the mist may become too large.
  • the latter may be at least partially offset by using an atomisation gas, which may e.g. be N2, CO2, steam or synthesis gas, more preferably steam or synthesis gas.
  • atomisation gas has the additional advantage that the difference between injection pressure and the pressure of the raw synthesis gas may be reduced to a pressure difference of between 5 and 20 bar.
  • mist is injected in a direction away from the gasification reactor, or said otherwise when the mist is injected in the flow direction of the raw synthesis gas.
  • mist is injected in a partially upward direction when applied in the tubular part or in a downwardly direction when applied in the annular space.
  • the mist is injected under an angle of between 30-60°, more preferably about 45°, with respect to a plane perpendicular to the longitudinal axis of the tubular part.
  • the mist is preferably directed in a vertical downwardly direction.
  • the injected mist is at least partially surrounded by a shielding fluid.
  • the shielding fluid may be any suitable fluid, but is preferably selected from the group consisting of an inert gas such as N2 and CO 2 , synthesis gas, steam and a combination thereof.
  • the amount of injected mist is selected such that the raw synthesis gas leaving the quenching sections comprises at least 40 vol.% H 2 O, preferably from 40 to 60 vol.% H 2 O, more preferably from 45 to 55 vol.% H 2 O.
  • the amount of water added relative to the raw synthesis gas is even higher than the preferred ranges above if one chooses to perform a so-called overquench.
  • the amount of water added preferably the amount added in the annular space, is such that not all liquid water will evaporate and some liquid water will remain in the cooled raw synthesis gas.
  • Such a process is advantageous because a downstream dry solid removal system can be omitted.
  • the raw synthesis gas leaving the gasification reactor is saturated with water.
  • the weight ratio of the raw synthesis gas and water injection can be 1:1 to 1:4.
  • the capital costs can be substantially lowered, as no further or significantly less addition of steam in an optional downstream water shift conversion step is necessary.
  • capital costs is here meant the capital costs for steam boilers which are required to generate steam needed to be injected into the feed to the water shift conversion step.
  • the dry solid removal system can be omitted in the overquench operation.
  • the dry solids removal system can also be omitted in a process embodiment wherein the synthesis gas temperature at the outlet of the reactor downstream of the annular space is below 500 0 C.
  • the raw synthesis gas, and especially the synthesis gas as saturated with water, leaving the quenching section is preferably shift converted whereby at least a part of the water is reacted with CO to produce CO2 and H2 thereby obtaining a shift converted synthesis gas stream.
  • a shift converter this is not further discussed.
  • the raw synthesis gas is heated in a heat exchanger against the shift converted synthesis gas stream.
  • the liquid is heated before using the liquid injecting it as a mist in the process of the present invention.
  • heating of this liquid is performed by indirect heat exchange against the shift converted synthesis gas stream.
  • Any desired molar ratio of H2/CO may be obtained by subjecting one part of the synthesis gas to a water shift reaction obtaining a CO depleted stream and by-passing the water shift unit with another part of the synthesis gas and combining the CO depleted stream and the by-pass stream.
  • a water shift reaction obtaining a CO depleted stream and by-passing the water shift unit with another part of the synthesis gas and combining the CO depleted stream and the by-pass stream.
  • Figure 1 schematically shows a system 1 for producing synthesis gas.
  • a gasification reactor (2) a carbonaceous stream and an oxygen-containing stream may be fed via lines (3), (4), respectively to a gasification reactor (2).
  • gasification reactor (2) a raw synthesis gas and a slag is obtained.
  • several burners (not shown) are present in the gasification reactor (2).
  • the partial oxidation in the gasification reactor (2) is carried out at a temperature in the range from 1200 to 1800 0 C, preferably between 1400 and 1800 0 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 ash components as are present in most of the preferred feeds will form a so-called liquid slag at these temperatures.
  • the slag will preferably form a layer on the inner side of the wall of reactor (2), thereby creating an isolation layer.
  • the temperature conditions are so chosen that the slag will create one the one hand such a protective layer and on the other hand is still able to flow to a lower positioned slag outlet (7) for optional further processing.
  • the produced raw synthesis gas is fed via line (5) to a quenching zone (6); herein the raw synthesis gas is usually cooled to below 500 0 C, for example to about 400 0 C.
  • liquid water is injected via line 17 in the form of a mist, as will be further discussed in Figure 3 below.
  • the amount of mist to be injected in the quenching section (6) will depend on various conditions, including the desired temperature of the raw synthesis gas leaving the quenching section (6). According to a preferred embodiment of the present invention, the amount of injected mist is selected such that the raw synthesis gas leaving the quenching section (6) has a H2O content of from 45 to 55 vol.%.
  • the raw synthesis gas leaving the quenching section (6) is further processed. To this end, it is fed via line (8) into a dry solids removal unit (9) to at least partially remove dry ash in the raw synthesis gas.
  • Preferred dry solids removal units (9) are cyclones or filter units as for example described in EP-A-551951 and EP-A-1499418.
  • Dry ash is removed form the dry solids removal unit via line 18.
  • the raw synthesis gas may be fed via line (10) to a wet gas scrubber (11) and subsequently via line (12) to a shift converter (13) to react at least a part of the water with CO to produce CO2 and H2, thereby obtaining a shift converted gas stream in line (14) .
  • the wet gas scrubber (11) and shift converter (13) are already known per se, they are not further discussed here in detail.
  • Waste water from gas scrubber (11) is removed via line (22) and optionally partly recycled to the gas scrubber (11) via line (23) .
  • Part of the wastewater, black water, from gas scrubber (11) may be preferably used as liquid water as injected via line (17) . This is advantageous because any solid compounds present in the black water will be removed from the process via the dry solids removal unit (9) .
  • the stream in line (14) is first fed to the heat exchanger (15) before entering the indirect heat exchanger (19) via line (16) .
  • the heat exchanger (15) may be dispensed with, if desired, or that the stream in line (14) is first fed to the indirect heat exchanger (19) before heat exchanging in heat exchanger (15) .
  • the stream leaving the indirect heat exchanger (19) in line (20) may be further processed, if desired, for further heat recovery and gas treatment.
  • the heated stream in line (17) may also be partly used as a feed (line (21)) to the gas scrubber (H) .
  • Figure 2 schematically shows a system (101) for producing synthesis gas similar to system 1 of Figure 1. To avoid duplication only the differences between Figure 1 and 2 will be discussed in detail. Most of the process conditions and functions of the streams and process units are as in Figure 1.
  • a carbonaceous stream and an oxygen containing stream are fed via lines (103), (104), respectively to a combustion chamber (102), thereby obtaining a raw synthesis gas and a slag.
  • the produced raw synthesis gas is fed via line (105) to a quenching zone (106) as in Figure 1.
  • a quenching zone (106) as in Figure 1.
  • liquid water is injected via line (17) in the form of a mist, as will be further discussed in Figure 3 below.
  • the amount of mist to be injected in the quenching section (6) relative to the raw synthesis gas is higher than in the process of Figure 1.
  • the amount of water added is such that not all liquid water will evaporate and some liquid water will remain in the cooled raw synthesis gas.
  • Such a process is advantageous because a downstream dry solid removal system can be omitted as is shown in Figure 2.
  • the weight ratio of the raw synthesis gas and water injection can be 1:1 to 1:4.
  • the raw synthesis gas leaving the quenching section (106) is further processed in wet gas scrubber (111) and subsequently via line (112) to a shift converter (113).
  • Wastewater from gas scrubber (111) is removed via line (122) and optionally partly recycled to the gas scrubber 111 via line (123) .
  • Part of the wastewater, black water, from gas scrubber (11) may be preferably used as liquid water as injected via line (117) .
  • Raw synthesis gas in line (112) is heated in a heat exchanger (115) against the shift converted synthesis gas in line (114) that is leaving the shift converter (113) .
  • Stream in line (116) is fed to an indirect heat exchanger (119), for indirect heat exchange with the stream in line (117) .
  • the stream in line (114) is first fed to the heat exchanger (115) before entering the indirect heat exchanger (119) via line (116) .
  • the stream leaving the indirect heat exchanger (119) in line (120) may be further processed, if desired, for further heat recovery and gas treatment.
  • the heated stream in line (117) may also be partly used as a feed (line (121)) to the gas scrubber (111).
  • Figure 3 shows a longitudinal cross-section of a gasification reactor which may be used in the system 1 of Figure 1 or in the system (101) of Figure 2.
  • FIG. 3 illustrates a preferred gasification reactor comprising the following elements:
  • the lower end of the reactor may suitably be designed as described in WO-A-2005/052095.
  • Slag may be removed from the pressure shell (31) via slag bath (25) via a slag sluicing device as for example described in US-B-6755980. ;
  • a gasifier wall (32) arranged inside the pressure shell (31) defining a gasification chamber (33) wherein during operation the synthesis gas can be formed, a lower open part of the gasifier wall (32) which is in fluid communication with the outlet for removing slag (25) .
  • the open upper end (34) of the gasifier wall (32) is in fluid communication with a quench zone (35) .
  • the gasifier wall (32) is cooled by a number of conduits through which water and more preferably evaporating water flows .
  • a suitable design for such a cooled wall (32) is a so- called membrane wall.
  • Membrane walls comprise of a number of parallel and interconnected tubes, which together form a gas-tight body. The tubes are preferably positioned in a vertical direction such that evaporating water can be more easily used as the cooling medium.
  • a quench zone (35) comprising a tubular formed part (36) positioned within the pressure shell (31), open at its lower and upper end and having a smaller diameter than the pressure shell (31) thereby defining an annular space (37) around the tubular part (36).
  • the wall of the tubular part (36) is preferably cooled by a number of conduits through which water and more preferably evaporating water flows.
  • a suitable design for such a cooled wall is the membrane wall as described above.
  • the annular space (37) may have a varying width along the vertical length on said space. Suitable the width increases with the direction of the gas flowing in said space (37) .
  • the lower open end of the tubular formed part (36) is fluidly connected to the upper end of the gasifier wall (32) .
  • the upper open end of the tubular formed part (36) is in fluid communication with the annular space (37) via deflector space (38).
  • injecting means (39) are present for injecting a liquid or gaseous cooling medium.
  • the direction of said injection are as described earlier in case of liquid mist injections are applied.
  • injecting means (40) are present to inject a liquid in the form of a mist, preferably in a downwardly direction, into the synthesis gas as it flows through said annular space (37) .
  • Figure 2 further shows an outlet (41) for synthesis gas is present in the wall of the pressure shell (31) fluidly connected to the lower end of said annular space (37).
  • Reactor (31) is used to prepare a water-saturated synthesis gas as illustrated in Figure 2 a water bath (not shown) may be present in the lower end of the annular space (37) .
  • a water bath (not shown) may be present in the lower end of the annular space (37) .
  • the water- saturated synthesis gas is directly discharged from the annular space (37) .
  • the quench zone is provided with cleaning means (42) and/or (43), which are preferably mechanical rappers, which by means of vibration avoids and/or removes solids accumulating on the surfaces of the tubular part and/or of the annular space respectively.
  • cleaning means (42) and/or (43) are preferably mechanical rappers, which by means of vibration avoids and/or removes solids accumulating on the surfaces of the tubular part and/or of the annular space respectively.

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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)

Abstract

La présente invention concerne un réacteur de gazéification et son utilisation. Ledit réacteur comprend une coque étanche (31) permettant de garder une pression supérieure à la pression atmosphérique; un bain de scories situé dans une partie inférieure de la coque étanche; et une paroi (32) de gazéifieur disposée à l'intérieur de la coque étanche (31), définissant une chambre (33) de gazéification dans laquelle peut être formé, en cours d'utilisation, le gaz de synthèse, une partie inférieure ouverte de la paroi du gazéifieur en communication fluidique (7) avec le bain de scories et une extrémité supérieure ouverte (34) de la paroi (32) du gazéifieur en communication fluidique avec une zone (35) de refroidissement. Ladite zone (35) de refroidissement présente une partie tubulaire (36) positionnée dans la coque étanche (31), ouverte à ses extrémités inférieure et supérieure et d'un diamètre inférieur à celui de la coque étanche (31), définissant ainsi un espace annulaire (37) autour de la partie tubulaire (36). L'extrémité inférieure ouverte de la partie tubulaire (36) est en communication fluidique avec l'extrémité supérieure de la paroi (32) du gazéifieur et l'extrémité supérieure ouverte de la partie tubulaire est en communication fluidique avec l'espace annulaire (37). L'extrémité inférieure de la partie tubulaire (36) présente des moyens (39) d'injection d'un liquide ou d'un milieu de refroidissement gazeux et l'espace annulaire comprend (37) des moyens (40) d'injection d'un liquide sous forme de poussière, et une ouverture (41) pour le gaz de synthèse est formée dans la paroi de la coque étanche (31) en communication fluidique avec ledit espace annulaire (37).
PCT/EP2007/053871 2006-05-01 2007-04-20 Réacteur de gazéification et son utilisation WO2007125047A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
JP2009508306A JP2009535471A (ja) 2006-05-01 2007-04-20 ガス化反応器及びその使用法
AU2007245732A AU2007245732B2 (en) 2006-05-01 2007-04-20 Gasification reactor and its use
EP07728330A EP2016160A1 (fr) 2006-05-01 2007-04-20 Réacteur de gazéification et son utilisation

Applications Claiming Priority (4)

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PCT/EP2006/061951 WO2006117355A1 (fr) 2005-05-02 2006-05-01 Procede et systeme de production de gaz synthetique
EPPCT/EP2006/061951 2006-05-01
EP06123312 2006-11-01
EP06123312.8 2006-11-01

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EP1939271A1 (fr) * 2006-12-18 2008-07-02 Pratt & Whitney Rocketdyne Inc. Gazogène refroidi par fluide perdu
WO2010078256A1 (fr) 2008-12-31 2010-07-08 Shell Oil Company Procédé de fabrication d'un gaz riche en méthane
WO2010078252A2 (fr) 2008-12-30 2010-07-08 Shell Oil Company Procédé et système pour fournir un gaz de synthèse
WO2010078254A2 (fr) 2008-12-31 2010-07-08 Shell Oil Company Réacteur adiabatique et procédé et système pour produire un gaz enrichi en méthane dans un tel réacteur adiabatique
US8308983B2 (en) 2008-10-08 2012-11-13 Shell Oil Company Process to prepare a gas mixture of hydrogen and carbon monoxide
CN101735858B (zh) * 2009-12-24 2013-02-20 西北化工研究院 一种气流床反应器的混合雾化器冷却保护系统
US8461216B2 (en) 2009-08-03 2013-06-11 Shell Oil Company Process for the co-production of superheated steam and methane
US8490635B2 (en) 2008-09-01 2013-07-23 Shell Oil Company Self cleaning nozzle arrangement
US8927610B2 (en) 2009-08-03 2015-01-06 Shell Oil Company Process for the production of methane

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EP2449061A2 (fr) * 2009-06-30 2012-05-09 Shell Internationale Research Maatschappij B.V. Procédé pour la préparation d'un mélange gazeux riche en hydrogène
KR101837650B1 (ko) * 2011-09-29 2018-03-13 한국전력공사 합성가스 냉각장치가 결합된 가스화기
MY167593A (en) * 2012-06-26 2018-09-20 Lummus Technology Inc Two stage gasification with dual quench

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US20130284403A1 (en) * 2008-09-01 2013-10-31 Shell Oil Company Self cleaning nozzle arrangement
US8490635B2 (en) 2008-09-01 2013-07-23 Shell Oil Company Self cleaning nozzle arrangement
US8470291B2 (en) 2008-10-08 2013-06-25 Shell Oil Company Process to prepare a gas mixture of hydrogen and carbon monoxide
US8308983B2 (en) 2008-10-08 2012-11-13 Shell Oil Company Process to prepare a gas mixture of hydrogen and carbon monoxide
WO2010078252A2 (fr) 2008-12-30 2010-07-08 Shell Oil Company Procédé et système pour fournir un gaz de synthèse
US8470059B2 (en) 2008-12-31 2013-06-25 Shell Oil Company Process for producing a methane-rich gas
WO2010078254A2 (fr) 2008-12-31 2010-07-08 Shell Oil Company Réacteur adiabatique et procédé et système pour produire un gaz enrichi en méthane dans un tel réacteur adiabatique
WO2010078256A1 (fr) 2008-12-31 2010-07-08 Shell Oil Company Procédé de fabrication d'un gaz riche en méthane
US8461216B2 (en) 2009-08-03 2013-06-11 Shell Oil Company Process for the co-production of superheated steam and methane
US8927610B2 (en) 2009-08-03 2015-01-06 Shell Oil Company Process for the production of methane
CN101735858B (zh) * 2009-12-24 2013-02-20 西北化工研究院 一种气流床反应器的混合雾化器冷却保护系统

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EP2016160A1 (fr) 2009-01-21
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JP2009535471A (ja) 2009-10-01

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