EP2013317A1 - Système de gazéification et son utilisation - Google Patents

Système de gazéification et son utilisation

Info

Publication number
EP2013317A1
EP2013317A1 EP07728328A EP07728328A EP2013317A1 EP 2013317 A1 EP2013317 A1 EP 2013317A1 EP 07728328 A EP07728328 A EP 07728328A EP 07728328 A EP07728328 A EP 07728328A EP 2013317 A1 EP2013317 A1 EP 2013317A1
Authority
EP
European Patent Office
Prior art keywords
synthesis gas
gas
water
gasification
mist
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Withdrawn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
EP07728328A
Other languages
German (de)
English (en)
Inventor
Robert Erwin Van Den Berg
Franciscus Gerardus Van Dongen
Thomas Paul Von Kossak-Glowczewski
Hendrik Jan Van Der Ploeg
Pieter Lammert Zuideveld
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
Priority claimed from PCT/EP2006/061951 external-priority patent/WO2006117355A1/fr
Application filed by Shell Internationale Research Maatschappij BV filed Critical Shell Internationale Research Maatschappij BV
Priority to EP07728328A priority Critical patent/EP2013317A1/fr
Publication of EP2013317A1 publication Critical patent/EP2013317A1/fr
Withdrawn legal-status Critical Current

Links

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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • 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
    • C10J3/78—High-pressure apparatus
    • 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
    • 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
    • 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
    • C10K1/16—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids
    • 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 system for preparing mixture comprising of carbon monoxide and hydrogen from a carbonaceous stream using an oxygen containing stream.
  • the gasification system comprises a gasification reactor and a synthesis gas cooling vessel.
  • the invention is also directed to a process to prepare a mixture comprising of carbon monoxide and hydrogen in a system according to the invention. Background of the invention 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
  • 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, heat exchange surfaces, 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 .
  • WO-A-2004/005438 describes a gasification system comprising a gasification reactor and a synthesis gas cooling vessel.
  • 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. In the tubular part a quench gas is injected into the hot synthesis gas.
  • This publication also describes a separate cooling vessel provided with three banks of heat exchange heating surfaces located one above the other .
  • US-A-5803937 describes a gasification reactor and a syngas cooler within one pressure vessel.
  • a tubular part is fluidly connected to an open upper end of a combustion chamber.
  • 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.
  • US-A-4836146 describes a gasification system for a solid particulate comprising a gasification reactor and a synthesis gas cooling vessel as in WO-A-2004/005438.
  • a method and apparatus is described for controlling rapping of the heat exchange surfaces as present in the separate cooling vessel. Rapping is required to avoid deposits to accumulate on the surfaces of the heat exchangers.
  • 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.
  • the present invention is directed to an improved reactor of the type where slag flows downwardly and is discharged at the bottom end of the reactor and wherein synthesis gas flows upwardly and is discharged at the upper end of said reactor.
  • Gasification system comprising a gasification reactor and a synthesis gas cooling vessel, wherein the gasification reactor comprises:
  • synthesis gas cooling vessel comprises an inlet for hot synthesis gas, an outlet for cooled synthesis gas and means to, in use, directly contact liquid water with the hot synthesis gas as formed in the gasification reactor.
  • 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 the gasification system according to the invention.
  • the solid carbonaceous feed is partially oxidized 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, and a pressure of between 20 and 100 bar, cooling said gas mixture in the connecting conduit to a temperature of between 500 and 900 0 C by injecting a gaseous or liquid cooling medium and subsequently further cooling the gas in the synthesis gas cooling vessel to below 500 0 C by contacting with water .
  • 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 longitudinal cross- section of a preferred gasification system consisting of a reactor vessel and a cooling vessel.
  • Figure 3 schematically shows a possible further embodiment for the cooling vessel.
  • 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 preferably cooled, in a first cooling step.
  • the gas is further cooled to preferably below 500 0 C.
  • 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
  • coal (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) .
  • Oxygen may contain some steam. Steam acts as moderator gas in the gasification reaction.
  • the ratio between oxygen and steam is preferably from 0 to 0.3 parts by volume of steam per part by volume of oxygen.
  • 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 feed is preferably dried before use.
  • 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 an oxygen.
  • a pair of burners is here meant two burners, which are directed horizontal and diametric into the gasification chamber. This results in a pair of two burners in a substantially opposite direction at the same horizontal position.
  • the reactor may be provided with 1 to 5 of such pairs of burners . The upper limit of the number of pairs will depend on the size of the reactor.
  • 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 to prepare hydrogen methanol and/or dimethyl ether or as feed gas of a Fischer-Tropsch synthesis.
  • the synthesis gas discharged from the gasification reactor comprises at least H 2 , CO, and CO2.
  • the hot synthesis gas is first cooled in a first cooling step to a temperature of between 500 and 900 0 C before it enters the separate cooling vessel.
  • This first cooling step is preferred to achieve a gas temperature below the solidification temperature of the non-gaseous components present in the hot synthesis gas.
  • the solidification temperature of the non-gaseous components in the hot 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 is preferably performed in the connecting conduit that fluidly connects the gasification chamber and the cooling vessel.
  • Cooling 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. Examples of suitable quench gases are recycle synthesis gas and steam.
  • this first cooling and/or the cooling performed in the cooling vessel 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. 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 liquid.
  • Even more preferably the process condensate of an optional downstream water shift reactor is used as the liquid.
  • hot synthesis gas is meant the gas mixture as directly obtained in the gasification chamber.
  • 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, more preferably under an angle.
  • the mist is injected from the wall of the connecting conduit or from the wall of the cooling vessel in the direction of the flow of hot synthesis gas and under an angle of between 30-60°, more preferably about 45°, with respect to a plane perpendicular to the longitudinal axis of the connecting conduit or cooling vessel.
  • the injection of the mist in the cooling vessel may be performed by injecting the mist in the same, suitably downwardly, direction as the flow path of the synthesis gas .
  • 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 CO2, synthesis gas, steam and a combination thereof.
  • the amount of injected mist is selected such that the raw synthesis gas leaving the cooling vessel 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 cooling vessel, 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 cooling vessel is saturated with water.
  • the weight ratio of the raw synthesis gas and water injection can be 1:1 to 1:4.
  • Overquench type process conditions may be achieved by injecting a large amount of water into the flow path of the synthesis gas, by passing the flow of synthesis gas through a water bath positioned at the lower end of the cooling vessel or combinations of these measures.
  • the synthesis gas or a part thereof, 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 CO 2 and H 2 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 chamber (2) .
  • gasification chamber (2) a raw synthesis gas and a slag is obtained.
  • several burners (not shown) are present in the gasification chamber (2) .
  • the partial oxidation in the gasification chamber (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 produced raw synthesis gas is fed via a connecting conduit (5) to a cooling vessel (9);
  • a connecting conduit (5) water (17) in the form of a mist is injected, wherein the synthesis gas is cooled to below 500 0 C, for example to about 400 0 C.
  • the ash components as are present in most of the preferred feeds will form a so-called liquid slag in gasification chamber (2) at these temperatures.
  • the slag will preferably form a layer on the inner side of the wall of gasification chamber (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 partly cooled synthesis gas (8) enters a cooling vessel (9).
  • cooling vessel (9) the synthesis gas (8) is contacted with an amount of water (6) in an overquench process mode to obtain a with water saturated synthesis gas (10) .
  • Water saturated synthesis gas (10) is directly fed 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) .
  • Part of the scrubbed gas (21) may by-pass the shift converter (13) .
  • This gas and stream (20) may be combined, optionally after both streams have been subjected to a further gas treating (not shown).
  • 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) or (6) .
  • the synthesis gas (10) is suitably fed to a dry-solids removal unit to at least partially remove dry ash.
  • Preferred solids removal units are cyclones or filter units as for example described in EP-A-551951 and EP-A-1499418.
  • the stream in line (16) may be fed to an indirect heat exchanger (19) , for indirect heat exchange with the stream in line (17) .
  • 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 CO depleted synthesis gas leaving the indirect heat exchanger (19) in line (20) may be further processed, if desired, for further heat recovery and gas treatment .
  • FIG. 1 shows a longitudinal cross-section of a gasification system, which may be part of the system 1 of Figure 1.
  • Figure 2 shows the gasification reactor (43) of Figure 1 of WO-A-2004/005438 in combination with a downstream cooling vessel or quench vessel (44) fluidly connected by a connecting conduit, i.e. transfer duct (45) .
  • Shown in Figure 2 is the gasification chamber (47), which is connected to a tubular part (51), which connects, by means of a connecting conduit, gasification chamber (47) via an upper wall part (52) to the interior of cooling vessel (44) .
  • injecting means (48) are present for injecting a liquid or gaseous cooling medium.
  • Cooling vessel (44) is further provided with an outlet (49) for cooled synthesis gas.
  • the system of Figure 2 differs from the system disclosed in Figure 1 of WO-A-2004/005438 in that the cooling vessel 3 of said Figure 1 is omitted and replaced by a simple vessel comprising means (46) to add liquid water.
  • injecting means (48) may be suited for injecting a mist of liquid water.
  • the wall of the gasification chamber (43) and/or the wall of the connecting conduit (51) are provided with cooling means.
  • the cooling means are an arrangement of water-cooled tubes, more preferably in the form of a membrane wall.
  • Figure 2 also shows a burner (50) .
  • the burner configuration may suitably be as described in EP-A- 0400740, which reference is hereby incorporated by reference.
  • the various other details of the gasification reactor (43) and the transfer duct (45) as well as the upper design of the cooling vessel (44) are preferably as disclosed for the apparatus of Figure 1 of WO-A-2004/005438.
  • the embodiment of Figure 2 is preferred when retrofitting existing gasification reactors by replacing the syngas cooler of the prior art publications with a cooling vessel (44) or when one wishes to adopt the process of the present invention while maintaining the actual gasification reactor of the prior art.
  • the invention is thus preferably directed to a system, wherein the inlet for receiving hot synthesis gas of the cooling vessel is at its upper end and the outlet for cooled synthesis gas is at its lower end, such that in use, a substantially downwardly directed flow path of synthesis gas will result and wherein in the flow path downwardly directed injecting means are present, said injecting means suited to inject a mist of water.
  • Figure 3 shows the upper end of gasification reactor
  • Injecting means (48) are present to inject a gaseous or liquid quenching medium in accordance with the process of the present invention.
  • a dip tube (54) is present to create a downwardly directed flow path for synthesis gas.
  • injecting means (46) are present to inject a mist of liquid water into the synthesis gas.
  • the dip-tube is partly submerged in a water bath (55) .
  • the synthesis gas will flow through water bath (55) to an annular space (56) as present between dip-tube (54) and the wall of the cooling vessel (53). From said annular space (56) the water saturated synthesis gas is discharged from said cooling vessel via conduit (57) .
  • Figure 3 also shows a pump (58) to recirculate water (59), providing a bleed stream (60) and a supply stream (61) for fresh water.
  • the invention is thus also directed to a system, wherein the synthesis gas cooling vessel has an opening for receiving hot synthesis gas at its upper end and an outlet for cooled synthesis gas defining a flow path for synthesis gas there between, and wherein a water bath is present in the flow path of the synthesis gas.
  • the invention is directed to a system, wherein in the connecting conduit injecting means are present for injecting a liquid or gaseous cooling medium into the synthesis gas. Even more preferably wherein the injecting means are injecting means for injecting a liquid cooling medium in the form of a mist of water droplets.

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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)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

La présente invention concerne un système de gazéification et son utilisation, ledit système de gazéification comprenant un réacteur (43) de gazéification et un récipient (44) de refroidissement de gaz de synthèse. Le réacteur (43) de gazéification présente une coque étanche permettant de garder une pression supérieure à la pression atmosphérique; un bain de scories situé dans une partie inférieure de la coque étanche; une paroi de gazéifieur disposée à l'intérieur de la coque étanche définissant une chambre (47) 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 avec le bain de scories et une extrémité supérieure ouverte de la paroi du gazéifieur en communication fluidique avec le récipient de refroidissement de gaz de synthèse via un conduit (51) de connexion. Le récipient (44) de refroidissement de gaz de synthèse comprend une entrée de gaz de synthèse chaud, une sortie (49) de gaz de synthèse refroidi et des moyens (46) destinés, en cours d'utilisation, à mettre en contact direct l'eau liquide avec le gaz de synthèse chaud formé dans le réacteur de gazéification.
EP07728328A 2006-05-01 2007-04-27 Système de gazéification et son utilisation Withdrawn EP2013317A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP07728328A EP2013317A1 (fr) 2006-05-01 2007-04-27 Système de gazéification et son utilisation

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
PCT/EP2006/061951 WO2006117355A1 (fr) 2005-05-02 2006-05-01 Procede et systeme de production de gaz synthetique
EP06123313 2006-11-01
EP07728328A EP2013317A1 (fr) 2006-05-01 2007-04-27 Système de gazéification et son utilisation
PCT/EP2007/053869 WO2007125046A1 (fr) 2006-05-01 2007-04-27 Système de gazéification et son utilisation

Publications (1)

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EP2013317A1 true EP2013317A1 (fr) 2009-01-14

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EP (1) EP2013317A1 (fr)
JP (1) JP5559532B2 (fr)
KR (1) KR101367691B1 (fr)
CN (2) CN101432400B (fr)
AU (1) AU2007245731B2 (fr)
BR (1) BRPI0710627A2 (fr)
CA (1) CA2650604C (fr)
RU (1) RU2441900C2 (fr)
WO (1) WO2007125046A1 (fr)

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CN101432400A (zh) 2009-05-13
RU2441900C2 (ru) 2012-02-10
CN101432401B (zh) 2012-11-14
KR101367691B1 (ko) 2014-02-27
CN101432400B (zh) 2012-11-14
AU2007245731B2 (en) 2010-08-12
CA2650604A1 (fr) 2007-11-08
CN101432401A (zh) 2009-05-13
JP2009543890A (ja) 2009-12-10
BRPI0710627A2 (pt) 2011-08-23
RU2008147138A (ru) 2010-06-10
KR20090012255A (ko) 2009-02-02
CA2650604C (fr) 2015-04-07
JP5559532B2 (ja) 2014-07-23
AU2007245731A1 (en) 2007-11-08
WO2007125046A1 (fr) 2007-11-08

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