CN1928028A - Method and device for producing synthesis gases by partial oxidation of slurries - Google Patents

Method and device for producing synthesis gases by partial oxidation of slurries Download PDF

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Publication number
CN1928028A
CN1928028A CNA2005101141525A CN200510114152A CN1928028A CN 1928028 A CN1928028 A CN 1928028A CN A2005101141525 A CNA2005101141525 A CN A2005101141525A CN 200510114152 A CN200510114152 A CN 200510114152A CN 1928028 A CN1928028 A CN 1928028A
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China
Prior art keywords
water
raw gas
cooled
fuel
waste heat
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Chinese (zh)
Inventor
曼弗雷德·申格尼茨
弗里德曼·梅尔霍泽
托尔斯滕·贝尔格特
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Future Energy GmbH
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Future Energy GmbH
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/52—Ash-removing devices
    • C10J3/526—Ash-removing devices for 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
    • 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
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/86—Other features combined with waste-heat boilers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/04—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
    • 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
    • C10J2300/0903—Feed preparation
    • 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
    • C10J2300/0973—Water
    • 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
    • C10J2300/0983—Additives
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Abstract

A method and a device for the gasification of solid fuels such as bituminous coal and coke such as bituminous coal, lignite, and biomass, as well as petroleum coke, that are finely ground and mixed with water or oil to make fuel-liquid suspensions, so-called slurries, and their gasification together with an oxidizing medium containing free oxygen by partial oxidation at pressures between atmospheric pressure and 100 bar, and at temperatures between 1200 and 1900 DEG C, in an entrained flow reactor. The method includes the steps of slurry preparation and infeed to the reactor, gasification in an entrained flow reactor with cooled reaction chamber contour, partial quenching, waste heat recovery, and wet or dry dust separation, with the crude gas being pretreated so that it can be fed to other technological steps such as crude gas conversion or desulfurization.

Description

Being used for partial oxidation by mud produces the method and apparatus of synthetic gas
Technical field
The present invention relates to a kind of by the gasification process of claim 1 preamble and the device of this method of enforcement.This method is made up of mud manufacturing, fuel input, gasification reaction, part water-cooled, gas scrubbing and these operations of partial condensation, wherein gas washing and partial condensation can replace with the mechanical type dust separation, contain CO and H to contain grey fuel by ashes shape with the partial oxidation generation of the vaporized chemical that contains free oxygen under High Temperature High Pressure 2Gas.
Background technology
In order to reach long working time, the pressure casing of gasifying reactor must protect reliably to the effect of raw gas and 1200-1900 ℃ high gasification temperature.This is by carrying out with a refrigerative shielded-plate tube limited reactions chamber and a vaporizer that is suspended in the pressure casing.Annulus between shielded-plate tube and the pressure casing is dashed to be drenched.
Fuel is brought up to vapor pressure as mud by pump delivery, and imports by burner in reactor head.Can make one or more fuel or gasification simultaneously.The slag of raw gas and liquefaction leaves vaporizer in the reactor lower end together, then partly is cooled to 700-1100 ℃ by injection water, and removes the thin soot particle of carrying secretly after reclaiming used heat, and washed subsequently raw gas flows to the subsequent disposal operation.
For many years fly gasization in known self-heating (autotherme) aspect the gas generation technique by solid, liquids and gases fuel.The ratio of fuel and oxygenousization agent is here selected like this, and feasible reason owing to the synthesis gas quality makes more carbon compound split into the synthesis gas composition fully, as CO and H 2, and inorganic integral part is discharged as liquation shape slag, sees J.Carl, and " NOELLKONVERSIONSVERFAHREN " of P.Fritz, energy and green technology, limited-liability company of EF press publishes, and 1996 years, the 33rd and 73 page.
According to systems different in the prior art data, the slag of gasifying gas and liquation shape is discharged from the reaction chamber of gasification installation separately or jointly here, as shown in DE 197 131 A1.For the inner boundary of the reaction chamber structure of gasification system both can introduce be equipped with refractory lining also can introduce the refrigerative system, see DE 4,446 803 A1.
EP 0,677 567 B1 and a kind of method of WO 96/17904 expression, wherein vaporizer is surrounded by fire brick layer.It has such shortcoming, and promptly because the molten slag that forms when gasification makes the refractory brickwork fusion, this causes rapid wearing and high repair expense.Along with this wear process of increasing of ash content is also accelerated.Therefore this gasification system only just needs to upgrade liner through limited working time.The ash content of gasification temperature and fuel is restricted in addition.Input as the fuel of carbon-grout brings significant loss in efficiency, see C.Higman and M.Van der Burgt " gasification ", U.S. ELSEVIER press published in 2003, and they can oilyly prevent or avoid as mounting medium or the preheating by carbon-grout by adopting.Introduced a kind of water-cooled or cooling system in addition, wherein high-temperature gasification gas and molten slag can be exported and introduce in the pond by a conduit that begins from the reaction chamber lower end together.The common output of gasifying gas and slag may cause conduit to stop up, thereby causes the restriction of usability.
DE 353 4015 A1 represent a kind of method, and wherein gasifying medium fine breeze and oxygen containing oxidant be by a plurality of burners input reaction chambers, make the mutual deflection of flame.Wherein gasifying gas loading fine breeze ground upwards flows, and slag flows into a slag cooling system downwards.Usually above vaporizer, be provided with one and have the indirect cooling device that used heat utilizes.But because the danger that the molten slag particle that is torn makes heat exchanger surface have deposition and be capped, this causes heat passage obstacle, causes the obstruction and the corrosion of pipeline sometimes.People overcome the danger of obstruction by the method that is used in the cooling gas cooling heat coal gas of guiding in the circulation loop.
Ch.Higman and M.van der Burgt introduce a kind of method in " gasification " that Elsevier press in 2003 publishes the 24th page, wherein high-temperature gasification gas and molten slag leave gasifier together, and directly entering a waste heat boiler that vertically is arranged on below it, raw gas and slag are utilizing used heat to cool off under the situation that steam takes place in this boiler.Slag collects in the pond, and the refrigerative raw gas leaves waste heat boiler from the side.Advantage by this system recoveries used heat is brought a series of shortcoming simultaneously.Here particularly should be mentioned that to form settling on Tube Sheet of Heat Exchanger, it causes heat passage obstacle and corrosion and corrosion, thereby causes operability to descend.
CN 200 4,200 200 7.1 introduces a kind of " powdered fuel gasifier ", the wherein pneumatic input of coal dust, and gasifying gas and molten slag are introduced the pond by a pipe core, with further cooling.This center cooling in described pipe core is stopped up easily, and it disturbs whole service and reduces the operability of entire equipment.
Summary of the invention
The objective of the invention is from this prior art, create a kind of possibility, it considers the different ash content of fuel under the situation of operation reliably, and has high operability.
This purpose is by realizing by the gasification process of claim 1 feature with by the device of claim 13.Dependent claims is represented the form of implementation that the present invention is good.
It is as follows to be used for making the feature of the gasification process that makes solid contain grey fuel gasification in the vaporizer that flies flow reactor with oxygen containing oxidant one under the pressure between barometric point and the 100bar, wherein the reaction chamber profile is surrounded by a cooling system, and wherein the pressure in the cooling system is higher than the pressure in the reaction chamber all the time.
Fuel, coal for example, bone coal and brown coal coke and biological substance coke and/or oil coke or its mixture, be crushed to＜500 μ m, especially＜200 the granularity of μ m is mixed into fuel-water or fuel-oil suspension, so-called mud under interpolation liquid such as water or oil condition.Be issued to the stable solid substance concentration of the highest 70% mass percent during as mounting medium in the situation of adding tensio-active agent at water.They bring up to the desirable vapor pressure of maximum 100bar by means of suitable pump, and flow to gasification reaction by the suitable burner that is contained in the gasifying reactor top.Monitor, measure and regulate fuel concentration and mud flow rate in the mud by measurement, adjusting and monitoring device.Comprise the oxygenant of free oxygen simultaneously to burner input, fuel mud becomes thick synthetic gas by partial oxidation.Gasification is carried out under the pressure of the highest 100bar 1200 to 1900 ℃ temperature.Reactor is equipped with a cooling screen, and it is made up of resistance to air loss welding and water-cooled pipe.
The thick synthetic gas of high temperature and leave gasifying reactor together by the molten slag that fuel ash constitutes, arrival one is arranged on the chamber under it, in this chamber, carry out the part water-cooled, that is be cooled to the temperature between 700 ℃ to 1100 ℃ by injection water or by the input cold air.Under this temperature, the fluid slag of carrying secretly is cooled to no longer can be attached on the metallic surface.After this raw gas that is cooled to 700 ℃ to 1100 ℃ temperature arrives a waste heat boiler with same refrigerative solid slag, produces steam to utilize the heat that can feel.Prevent or limit greatly the danger of residue sintering on the used heat cooling tube by this part water-cooled or part cooling in advance.The gas condensate of needed water of water-cooled or feedback is imported by nozzle, and nozzle is located immediately on the shell.The refrigerative residue collects in the pond, and the pond is arranged on the lower end of waste heat boiler.Be cooled to about 200 ℃-300 ℃ raw gas and leave waste heat boiler from the side, and arrive a raw gas washer that is suitable for making washer in the venturi.Remove the dust of carrying secretly of the most about 20 μ m granularities here.For example carry out the raw gas conversion for the catalytic process of following, this purity not enough.Here also to further consider the additional salt fog of exporting together with raw gas of in raw gas, carrying secretly that between pneumatolytic stage, from combustion ash, dissociates away.In order not only to remove＜the thin ash of 20 μ m but also remove salt fog, the raw gas after the washing flows to a condensation operation, directly cools off 5 ℃ to 10 ℃ at its inside raw gas.At this moment from containing the raw gas condensation water outlet of saturated vapor, it holds described thin ash and salt particle.In the separator of following, separate the water of condensation that comprises soot particle and salt particle.The raw gas that purifies like this can directly flow to raw gas transfer equipment or desulfurizer then.
Replace washing and condensation operation can be provided with one, can adopt separator using centrifugal force or filtering system here at 200 ℃ to 300 ℃ mechanical type dust-separating appliances of working down.
Description of drawings
Describe the present invention in detail with three accompanying drawings and an embodiment below.Accompanying drawing is represented:
Fig. 1: technology functional diagram;
Fig. 2: the gasifying reactor of band portion water cooling plant and vertically disposed waste heat boiler;
Fig. 3: the gasifying reactor of band portion water-cooled and the waste heat boiler that is arranged on the next door.
Embodiment
Have following ingredients:
C 71.5% mass percent
H 4.2% mass percent
O 9.1% mass percent
N 0.7% mass percent
S 1.5% mass percent
Cl 0.03% mass percent
Ash content is that 11.5% mass percent and water capacity are that the coal amount of the 320t/h of 7.8% mass percent will gasify under the pressure of 40bar.The calorific value of coal is 25600KJ/kg.Gasification is carried out in the time of 1450 ℃.Need 245000m in order to gasify 3The amount of oxygen of i.N./h.Coal at first flows to a milling device corresponding to prior art, inside its, be ground into the size range between 0 to the 200 μ m, so that then be mixed into stable coal dust-aqeous suspension with water, so-called mud one in by the specific equipment of Fig. 1 under the situation of adding tensio-active agent (Tenside).Solid substance concentration is 63% mass percent in this mud, and mud flow rate is 465t/h.Mud is brought up to the vapor pressure of the 100bar of hope by means of a pump that is suitable for conveying solid substance-liquid suspension, and by transfer lime 1.1 by the burner that Fig. 1 flows to gasifying reactor 2, at this moment monitor, measure and regulate flow.In order to save oxygen, mud was preheating to 400 ℃ according to vapor pressure before flowing to gasifying reactor 2.
In Fig. 2 and 3, represent gasifying reactor.Flow into the mud and the 245000m that flows into by pipeline 2.1 of the 465t/h of gasifying reactor by transfer lime 1.1 3The amount of oxygen of i.N./h carries out partial oxidation together under 1450 ℃ in vaporizer 2.3, at this moment form the 565000m of following composition 3The raw gas of i.N./h:
H 218.5% volume percent
CO 70.5% volume percent
CO 26.1% volume percent
N 22.3% volume percent
NH 30.003% volume percent
HCN 0.002% volume percent
H 2S 0.5% volume percent
COS 0.07% volume percent
Vaporizer 2.3 is surrounded by cooling screen 2.4, and it is made up of resistance to air loss piping welding, water-cooled.Raw gas and molten slag flow into through delivery port 2.5 together and are used for making raw gas part water-cooled/part to be cooled in 700 ℃-1100 ℃ the chamber 3.1 of temperature.Slag also is cooled to make it can not be deposited on by Fig. 1 to be connected in the pipe 4.1 of waste heat boiler of back except that raw gas under this temperature.The steam that produces in waste heat boiler 4 is used for the oxygen containing oxygenant of preheating or as the gasification speed reduction unit of preheating mud during the course.Slag collects in the pond 4.2, and it is positioned at the lower end of waste heat boiler, and by 4.3 discharges, raw gas leaves waste heat boiler by 4.4, and arrival is pressed in the raw gas washer 5 of Fig. 1.Waste heat boiler 4 can be set directly at gasifying reactor 2 and portion water device for cooling 3 belows by Fig. 3, but also can be arranged side by side as shown in Figure 4.Not only below portion water device for cooling 3 but also below waste heat boiler 4.6, established a slag discharger 4.3 in this case.Then the raw gas that leaves waste heat boiler 4 by opening 4.4 arrives raw gas washer 5 by Fig. 1, and it makes washer in adjustable venturi, and feeds about 100m 3The washing water of/h.Usually washing water are removed the entrained solid material and are re-entered washer in the venturi.Washing water can preheating, so that give the raw gas humidification simultaneously when cleaning.For remove＜fine dust of 20 μ m and in venturi unsegregated salt fog in the washer, the raw gas of water washing stands partial condensation 6 by Fig. 1, here raw gas cools off 5-10 ℃ indirectly.Receive the thinnest dust and salt particle by agglomerative water vapor when cooling off, thereby remove from raw gas, the raw gas that after this washes solid matter has following composition:
H 213.4% volume percent
CO 51.4% volume percent
CO 24.5% volume percent
N 21.5% volume percent
NH 30.0022% volume percent
HCN 0.0012% volume percent
H 2S 0.36% volume percent
COS 0.05% volume percent
H 2O 37.30% volume percent
Washed wet raw gas output is 775000Nm 3/ h.It can directly flow to the raw gas transfer equipment or other handle level.
The pictorial symbolization table
1 mud manufacturing and input
1.1 hydraulic fill pipeline
2 reactors
2.1 oxygen hose
2.2 burner
2.3 vaporizer
2.4 cooling screen
2.5 delivery port
3 water-cooled water coolers
3.1 water cooling chamber
3.2 the nozzle in 3
3.4 from 3 to 4 transfer lime
4 waste heat boilers
4.1 the cooling tube in the waste heat boiler 4
4.2 the pond of the band slag in 4
4.3 4 slag discharger
4.4 from 4 openings to raw gas washer 5
4.5 the pond of band slag
4.6 4 slag discharger
5 raw gas washers
6 fractional distillating tubes

Claims (21)

1. one kind is used for making for example bone coal of solid fuel such as coal and coke, brown coal, biological substance and petroleum coke in flying to flow and a kind of oxygenant that contains free oxygen by under the pressure between environmental stress and the 100bar and the method that gasifies of the temperature lower section oxidation between 1200 to 1900 ℃, it is by mud manufacturing and input, in reactor, gasify by partial oxidation with refrigerative reaction chamber profile, the part water-cooled, raw gas washing and these operations of partial condensation are formed, wherein raw gas washing and partial condensation can replace by a dry type dust removal with machine of working more than dew point, wherein:
-a kind of granularity＜200 μ m especially＜100 fuel powder of μ m are mixed into a kind of fuel-grout of solid substance concentration of the 40-70% of having mass percent with water under the situation of adding tensio-active agent in a specific equipment, and reach the vapor pressure of 100bar by pump delivery, wherein mud can preheating up to 400 ℃ temperature
-the mud that flows to reactor (2) by a transfer lime (1.1) carries out partial oxidation with a kind of oxygenant that contains free oxygen in the reaction chamber (2.3) that its profile is surrounded by a cooling screen (2.4), at this moment fuel ash melts and is input in the water cooling chamber (3.1) of water-cooled water cooler (3) by take-off equipment (2.5) with high-temperature gasification gas
-carry out the part water-cooled, raw gas is cooled to temperature between 700 to 1100 ℃,
The raw gas of-part water-cooled is cooled to the temperature between 150 to 400 ℃ under the situation that steam takes place in a waste heat boiler (4),
-after this, the refrigerative raw gas carries out raw gas washing (5) and partial condensation (6) or carries out dry type dust removal with machine by means of centrifugal force or strainer, the dust of carrying secretly with separation,
-then, will flow to the subsequent disposal operation, as raw gas conversion or desulfurization through cooling and dust separating raw gas.
2. by the method for claim 1, it is characterized by: raw gas washing (5) is designed to wash in a kind of single-stage or the multistage venturi.
3. by the method for claim 1 and 2, it is characterized by: washing is provided with the water of condensation of fresh water or feedback in the venturi, and water of condensation is subsidiary the generation when coal gas cools off.
4. by each method of claim 1 to 3, it is characterized by: waste heat boiler (4) is worked under 700 to 1100 ℃ temperature.
5. by each method of claim 1 to 4, it is characterized by: raw gas washing (5) is carried out under 150 to 300 ℃ temperature.
6. by each method of claim 1 to 5, it is characterized by: washer is supplied water by the water of condensation of recirculated water or feedback in the venturi.
7. by each method of claim 1 to 6, it is characterized by: fuel acts as a fuel-and water-slurry transportation gives reactor (2).
8. by each method of claim 1 to 7, it is characterized by: fuel flows to gasifying reactor (2) by one or more burners.
9. by each method of claim 1 to 8, it is characterized by: granular residue is discharged by one or more outlets (3.6) of water cooling chamber (3.5).
10. by each method of claim 1 to 9, it is characterized by: the raw gas of part water-cooled is by one or more coal gas output channels (3.4) leaving water cold houses (3.5).
11. by each method of claim 1 to 10, it is characterized by: one or more coals gasify simultaneously.
12. each the method by claim 1 to 11 is characterized by: measure, monitoring and regulate mud amount in the transfer lime (1.4).
13. an equipment that is used for implementing by each described method of claim 1 to 12 is characterized by:
One is used for making and gasifying reactor (2), that the device, of slurry conveyed (1) has a refrigerative reaction chamber profile is used for part and cools off water-cooled water cooler (3), a waste heat boiler (4), a raw gas washer (5) and a part of condenser (6) of raw gas, wherein raw gas washer (5) and fractional distillating tube (6) can replace or replenish by a device that is used for dry gas cleaning, said apparatus is connected mutually, wherein
-one is used for making the reactor (2) of the fuel powder of input with the oxygenant gasification that contains free oxygen, it comprises that the transfer lime (1.1) and that is used for fuel mud is used for the pipeline of oxygenant (2.1), mud and oxygenant are by means of in burner (2.2) the input reaction chamber (2.3), reaction chamber comprises that a cooling screen (2.4) and of being made up of the water-cooled pipe of resistance to air loss welding enters the interior discharger (2.5) of a water-cooled water cooler (3)
-one with the water-cooled water cooler (3) of built-in fitting, in this water cooler the inside nozzle (3.2) is set in one or more nozzle rings, sprays into the needed water of part water-cooled by these nozzles, and wherein each nozzle (3.2) is arranged on the shell of an inside with flushing,
-one is arranged on the waste heat boiler (4) of water-cooled water cooler (3) back,
-connection is used for purifying the device of coal gas in the back.
14. equipment by claim 13, it is characterized by: the reaction chamber (3.2) of water-cooled water cooler (3) directly is connected with waste heat boiler (4), wherein utilize the appreciable heat of raw gas by pipe (4.1), in order to producing steam, and be provided with in the waste heat boiler bottom and be used for raw gas (4.4) and be used to relief outlet with the residue discharger (4.3) of a pond (4.2).
15. the equipment by claim 13 and 14 is characterized by: in order to purify, the partial condensation device (6) that a raw gas washer (5) and is arranged on raw gas washer (5) back is set.
16., it is characterized by: establish in a single-stage or the multistage venturi washer as raw gas washer (5) by the equipment of claim 15.
17. the equipment by claim 13 and 14 is characterized by: establish a dry type mechanical dust collector in order to purify coal gas.
18. each the equipment by claim 13 to 17 is characterized by: be connected other coal gas with fractional distillating tube or dry type mechanical dust collector back at water scrubber (5) and handle grade, as raw gas transmodulator or desulfurizer.
19. equipment that is used for implementing by each described method of claim 1 to 12, it is characterized by: have a device (1) that is used for making and importing mud, one has the gasifying reactor (2) of refrigerative reaction chamber profile, one is used for the water-cooled water cooler (3) of part cooling raw gas, one waste heat boiler (4), one raw gas washer (5) and a part of condenser (6), wherein raw gas washer (5) and fractional distillating tube (6) can replace or replenish by a device that is used for dry gas cleaning, said apparatus is connected mutually
-one is used for making the reactor (2) of the fuel powder (1) of input with the oxygenant gasification that contains free oxygen, it comprises that the transfer lime (1.1) and that is used for fuel mud is used for the pipeline of oxygenant (2.1), fuel mud and oxygenant are by means of in burner (2.2) the input reaction chamber (2.3), reaction chamber comprises that a cooling screen (2.4) and of being made up of the water-cooled pipe of resistance to air loss welding enters the interior discharger (2.5) of a water-cooled water cooler (3)
-one water-cooled water cooler (3), part refrigerative raw gas flows to waste heat boiler (4) by transfer lime (3.4) from this water cooler in water cooling chamber (3.1),
-one waste heat boiler (4), it is equipped with vapour pipe (4.1) and utilizes the appreciable heat of raw gas to produce steam,
-one raw gas washer (5) and
-one is arranged on the partial condensation device (6) of raw gas washer (5) back, and their available mechanical filter cleaning apparatuss replace.
20. by the equipment of claim 19, it is characterized by: not only all be provided with pond (4.2), (4.5) at water cooler (3) but also in waste heat boiler (4), the refrigerative slag collects in these ponds.
21. the equipment by claim 19 and 20 is characterized by: not only go up but also on waste heat boiler (4), all be provided with the device (4.3,4.6) that is used for discharging slag at water cooler (3).
CNA2005101141525A 2005-09-07 2005-10-26 Method and device for producing synthesis gases by partial oxidation of slurries Pending CN1928028A (en)

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