CN1782037A - Apparatus and method for coal gasification - Google Patents
Apparatus and method for coal gasification Download PDFInfo
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- CN1782037A CN1782037A CN200510125052.2A CN200510125052A CN1782037A CN 1782037 A CN1782037 A CN 1782037A CN 200510125052 A CN200510125052 A CN 200510125052A CN 1782037 A CN1782037 A CN 1782037A
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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
- C10J3/72—Other features
- C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/36—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents
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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
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/20—Apparatus; Plants
- C10J3/34—Grates; Mechanical ash-removing devices
- C10J3/40—Movable grates
- C10J3/42—Rotary grates
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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
- C10J3/72—Other features
- C10J3/74—Construction of shells or jackets
- C10J3/76—Water jackets; Steam boiler-jackets
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- 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
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- 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
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- 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
- C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
- C10K3/001—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by thermal treatment
- C10K3/003—Reducing the tar content
- C10K3/005—Reducing the tar content by partial oxidation
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- 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
- C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
- C10K3/001—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by thermal treatment
- C10K3/003—Reducing the tar content
- C10K3/008—Reducing the tar content by cracking
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
- C01B2203/0255—Processes for making hydrogen or synthesis gas containing a partial oxidation step containing a non-catalytic partial oxidation step
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1235—Hydrocarbons
- C01B2203/1247—Higher hydrocarbons
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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
- C10J2200/00—Details of gasification apparatus
- C10J2200/15—Details of feeding means
- C10J2200/156—Sluices, e.g. mechanical sluices for preventing escape of gas through the feed inlet
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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
- 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
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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
- 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
Abstract
A process and apparatus for converting a coal into a substitute natural gas generates raw gas in a conventional coal gasification unit and passes at least a portion of the raw gas into a partial oxidation unit to convert the at least portion of the raw gas into a secondary raw synthesis gas substantially devoid of higher hydrocarbons. Optionally, the raw gas is quenched and only the resulting condensate is passed to the partial oxidation unit for conversion to the secondary raw synthesis gas.
Description
Technical field
The present invention relates to coal is converted into the equipment and the method for instead of natural gas.More specifically, the present invention relates to pass through non-catalytic partial oxidation, to be converted into the secondary synthetic gas from the phlegma of elementary gasification, and cause all byproduct stream basically are used for producing other crude synthesis gas, thereby the unwanted effluent that this gasification process is produced be minimum.
Background technology
Coal Gasification Technology is well-known method, for example drops into commercial use for many years in South Africa.The most frequently used coal gasifier is developed by Lurgi Kohle und Mineraloeltechnik GmbH.The Lurgi method adopts fixed bed gasifiers, and the coal of selected particle diameter and the air-flow adverse current of steam and oxygen are imported this gasifier.
Supervene the by product that mainly comprises oil, tar and phenols in the coal gasification course.Handle these by products and cause tangible environment and economic problems.
Therefore, this area needs a kind of apparatus and method, all by products basically of gasification can be used for producing more thick gas, the synthetic gas maximization that gasification process is produced.
Summary of the invention
Therefore, a kind of coal is converted into the method for instead of natural gas, comprises following step: the coal raw material is dropped into coal gasification apparatus, be in vaporized chemical and heating down by making the coal raw material, to small part coal raw material generating gasification.Outlet at coal gasification apparatus obtains elementary thick gas, and this thick gas of at least a portion fed non-catalytic partial oxidation device, retaining part oxygenant and certain temperature make at least that this part primary raw materials cyclostrophic turns to the secondary crude synthesis gas, avoid producing higher hydrocarbon basically.
The present invention relates to the method that coal is converted into instead of natural gas on the other hand, and this method comprises: the coal raw material is dropped into coal gasification apparatus, in coal gasification apparatus by the coal raw material is under vaporized chemical and the heating, to small part coal raw material generating gasification.Outlet at coal gasification apparatus obtains elementary thick gas, and carries out quenching, therefrom separates the condensed fluid of hydrocarbonaceous.Then, in the presence of the partial oxidation agent, this liquid carries out non-catalytic partial oxidation being enough to be converted under the temperature of secondary crude synthesis gas, avoids producing other hydrocarbon except that carbon monoxide, carbonic acid gas and methane basically.
Another aspect of the invention relates to the equipment that coal is converted into instead of natural gas, and this equipment comprises a plurality of coal gasification apparatus, and each device all can move at least a portion generating gasification that makes the coal raw material of sending into this device, produces elementary thick gas in the gasification installation outlet.The import of quench system is connected to the outlet of each gasification installation, accepts the elementary thick gas of gasification installation, and carries out liquid being transported to the liquid exit of quench system from the operation of elementary thick gas delivery condensable hydrocarbons.The import of partial oxidation device is connected the liquid exit of quench system, makes the liquid hydrocarbon of acceptance be enough to make under its temperature that is converted into the secondary crude synthesis gas in this this device and carries out partial oxidation, avoid producing hydrocarbon basically in the outlet of partial oxidation device.
Description of drawings
By the detailed description below in conjunction with accompanying drawing, target of the present invention and feature are conspicuous.In the accompanying drawing:
Shown in Figure 1 is FB(flow block) according to gasification system of the present invention.
Shown in Figure 2 is the sketch of elementary gasification installation and the partial oxidation device that is connected by optional quench system.
Shown in Figure 3 is the general flow chart of example of the gasification factory of partial oxidation device of employing of arranging according to the present invention and four elementary coal gasification apparatus and a multistage quench system.
Embodiment
In this manual, term " higher hydrocarbon " refers to consist of C
nH
mHydrocarbon, wherein n and m are 2 or bigger integer.
Referring to Fig. 1, be depicted as the fundamental block diagram of optional arrangement of the present invention.Elementary gasifier 102 makes thick gas be delivered to quenching and liquid separating appts 106 by pipeline 110A in its outlet 10, or is delivered to non-catalytic partial oxidation device 104 by pipeline 110B.If use pipeline 110B, then the input material to partial oxidation device 104 is gas form substantially.If use quenching and liquid separating appts 106, then the input material 116 to partial oxidation device 104 is a liquid form, is the condensation product that produces when cooling off in 106 installing.
Will be apparent to those skilled in the art, only some thick gas 110 is transfused to partial oxidation device 104 by optional pipeline 110B.
When thick gas 110 goes to carry out quenching by pipeline 110A, then during the oxidizer 104 of importation, the secondary synthetic gas that produce in outlet 114 turn back to the import of quench system 106, further cooling by pipeline 114A.Otherwise if do not carry out quenching before partial oxidation, the secondary crude synthesis gas 114 can be by the outlet 112 of pipeline 114B to system.
The difference of the present invention and known gasification is to comprise a non-catalytic partial oxidation device 104.Device 104 is produced other crude synthesis gas from the thick air-flow 110 of gas form or tar that exists and oil its liquid form charging 116.Therefore, all byproduct stream are used to produce thick gas, and the refuse that this method is produced is minimum.
Partial oxidation device 104 is converted into carbon monoxide and hydrogen with higher hydrocarbon, and some seldom measures (inadvertent) carbonic acid gas.This is under high-temperature very, adopts directly to contact with the hot flame burner in being lower than stoichiometric oxygen atmosphere and carries out, and can prevent that like this carbon monoxide that produces is converted into carbonic acid gas in a large number.
In the final product of instead of natural gas, do not need to exist in those application of methane, can directly import thick gas 110 by pipeline 110B.Yet, when adopting quenching and liquid separation system 106, have only the liquid of generation to feed the partial oxidation device, rather than the thick gas in the pipeline 110.In such application, methane is the required component in the synthesis gas of system outlet 112 normally, can directly needn't arrive partial oxidation device 104 by system 106.
Referring to Fig. 2, shown in be the basic arrangement of elementary gasifier, non-catalytic partial oxidation device and optional quench system 212.
When lock coal bunker 204 was in gasifier pressure, bottom cone was opened, and coal begins to flow into gasifier 206 by sparger 208, and sparger better comprises an eddy flow sleeve.When 204 emptying of lock coal bunker, bottom cone is closed, and is used for reinforced again.
Gasifier 206 is a kind of double-walled pressurizing vessels.The feed water of high-duty boiler remains in the chuck that is formed by double-walled, to limit the temperature of chuck and gasifier wall.The high-duty boiler feed water is circulated by chuck by outfall sewer.During operation, a large amount of heats are transferred to the chuck from the fuel bed.Make the interior steam of chuck be increased to high pressure steam, total steam and oxygen are with the mixed of 0.4 pound of steam/SCF oxygen.This vaporized chemical enters this gasifier fuel bed by rotation grate 209.As a result, grate 209 is cooled off by vaporized chemical.Grate 209 is driven by alternating current machine, at first is used for making vaporized chemical to be distributed in the cross section part of gasifier 206 by the vaporized chemical annular space.Finish this distribution at ash bed.
Secondly, grate 206 to lock ash bucket 210, helps the ash band to pulverize grey accumulation and becomes (make grey do not stop up cone) overall dimension with the ashes piece.At last, grate 209 can keep the motion of fuel bed.
Grate 209 comes automatic control velocity by Oxygen Flow, makes ash discharge adaptive with the generation of ash.Also can manual synchronizing grate speed.The production capacity of grate 209 is by being inserted in the pears sheet quantity below the stove and the speed decision of grate 209.Grate 209 moves continuously, and only the short period of time stops when 210 cyclical operations of lock ash bucket begin.
Oxygen in vaporized chemical such as the pipeline 233 and the steam mixture in the pipeline 231 are by the following reaction zone of reactor 206.
In ash bed 206A, vaporized chemical is left overheated 0 hypothesis of combustion zone 206B by the lime-ash under about 2730 temperature and has set up enough ash bed 206A, and lime-ash is cooled to the temperature higher than vaporized chemical, and vaporized chemical is heated at the inlet that enters reactor 206 simultaneously.
At combustion zone 206B, carbon and oxygen are converted into carbonic acid gas and heat.The air-flow upwards and the temperature of downward sedimentary lime-ash (carbon content about 2%) are brought up near 2700 °F.
The air-flow that makes progress from combustion zone 206B is mainly by carbonic acid gas and vapor composition, and in the 206C of gasification zone, reacts under about 1560 medial temperature.The principal reaction of gasification zone 206C is that carbon and water are converted into carbon monoxide, hydrogen and heat.Methanation reaction is very little to the gas composition influence of leaving gasification zone 206C.
At dry distillation area 206D, discharge the fugitive constituent in producing coal.Dry distillation reactor is heat dissipation reaction.As a result, the gasified raw material air-flow that makes progress from gasification zone 206C must heat downward coal, and the heat that provides destructive distillation to use.In addition, at dry distillation area 206D, the powdery coke tar cracking of recirculation is oil and coke.
The grate 209 of operation is discharged to the lime-ash that gasifier 206 produces in the lock ash bucket 210 by hydraulically powered top cone continuously, and this feed hopper bottom cone is closed under gasifier pressure.In case lock ash bucket 210 is filled, and stops grate 209.After the top cone of lock ash bucket was closed and sealed, grate 209 was restarted.
Then, the pressure that reduces lock ash bucket 210 is to normal atmosphere, and its bottom cone is opened, and lime-ash flows out to the tank 253 from this hopper, is delivered to the lime-ash workshop by cancellation and by hydraulic pressure.
The thick gas that gasifier device 206 produces is expelled to optional quench system 212 by pipeline 235, and this system outlet 237 contains the condensed fluid from quench process.Perhaps, at direct feed system, do not use quench system 212, thick gas is transfused to partial oxidation device 216.
In optional scrubbing/cooling apparatus 212, isolate excessive water, some condensable hydrocarbons and small amount of solid in the flow of feed gas from pipeline 235.Liquid stream in the pipeline 235 is as the raw material to partial oxidation device 216.
In non-catalytic partial oxidation device 216, the reaction in the presence of as the steam of the conditioning agent of crude synthesis gas of this raw material and oxygen.The water that directly injected of thick gas of heat at quench tube 218 and expander 220 by water cooling.Separator 222 is discharged slag from its outlet 249.
Non-catalytic partial oxidation device 216 is at about 2500 and about 435psig pressure lower section oxidation heavy fraction.Steam in oxygen in the pipeline 239 and the pipeline 241 joins in pipeline 237 incoming stock by partial oxidation combustion unit 214.This combustion unit 214 is guaranteed the charging thorough mixing, and this is that to generate required crude synthesis gas with high conversion necessary.
In the injection region of reactor 216, charging is partial oxidation in the flame of burner 214.Total reaction in the device 216 divides two stages basically higher hydrocarbon to be converted into carbon monoxide and hydrogen.
In first heating and the cleavage stages, raw material and oxygen are leaving burner 214 under the preheating temperature separately.Before Actual combustion, reactant is further heated by heat and container 216 scorching hot laying bricks that flame reflects.Higher hydrocarbon in the raw material is cracked into free radical.
Next, in step of reaction, reaching kindling temperature, a part of hydrocarbon and oxygen generation thermopositive reaction form carbonic acid gas and water.In fact, getable oxygen is in this stage total overall reaction.Hydrocarbon is oxidized portion and steam reaction not, and reaction product mainly is carbon monoxide and hydrogen.
As previously described, raw material, oxygen and steam enter reactor 216 by burner 214, and burner 214 is installed in the top of reactor 216.Burner 214 better is designed to four nozzles, a pipe core is arranged as starting burner.During startup, pipe core is responsible for the startup burner of a little fighting, and this burner is equipped with flame control transmitter.Be reactor heating 216, in pipeline 243, factory air and fuel gas be added to this startup burner.Under comparatively high temps, when the higher heating load of needs, air and fuel gas also can be by four nozzle inputs of this burner.When the self-ignition temperature of temperature of reactor, in the time of common about 1470 °F, remove this startup burner, and substituted by the pipe of a steaming out apparently higher than fuel gas.When finally being heated to about 2200 °F, fuel gas and air are by four nozzle inputs of this burner.
For making the volume gas deliverability maximum of partial oxidation reactor 216, can also fine coal be added in the liquid starting material by spray gun burner 214.
Burner 214 usefulness water coolants and the media cooling of passing through therein.This reactor outlet to quench tube 218 also can cool off, and makes in the refractory materials wearing and tearing of this position minimum.
In the reactor 216 of lining, carry out the conversion of hydrocarbon partial oxidation with refractory materials.Refractory materials is selected according to the ash content of coal and the ash character of raw material.Ash must fusion under the service temperature of reactor, flows freely into quench vessel 220 to guarantee molten ash from reactor 216, and can avoid stopping up reactor 216 and quench tube 218.
Come second crude synthesis gas of the heat of autoreactor 206 to be transported to quench vessel 220 by quench tube 218.By injecting water, second synthetic gas is cooled to about 430 equilibrium temperature from about 2470 °F immediately.Liquid slag stream is consolidated into particle by this synthetic gas.Particle is by acidity or alkaline medium lixiviate.Gas separates with slag granules with the water of surplus in quench tube 218 below and the quench vessel 220.Gas is extracted out by other nozzle, and the slag water of collection is transported to slag separator 222 by tank level control.In having the slag system of slag separation vessel 222, slag and the coal ash water sepn of leaving expander by pipeline 251.Heavy slag granules sedimentation from coal ash water in slag separation vessel 222, and be collected in the cone base that is used to discharge by pipeline 249.
Coal ash and the lime-ash collected are mixed into the coal ash slurry, send into the calx recovery system, in this system, coal ash in slurry tank flash distillation to normal atmosphere.Filter this slurry, obtain filter cake and can be used for the clean water of quenching and scrubbing operation.
Shown in Figure 3 is the general flow chart that adopts the gasification factory of a non-catalytic partial oxidation device and four elementary coal gasification apparatus.Such arrangement has only utilized the pyrolysis product of the thick gas that produces from elementary gasification installation by the fact of partial oxidation.At this, only need the partial oxidation device that can be used for a plurality of (maximum 5) primary fixed bed degasser device.
As shown in Figure 3, the coal source 301a-d that gasifies is sent into each chute 350 of four fixed-bed gasification furnace 302a-d respectively.Coal is interlocked with vapourizing furnace to reinforced lock coal bunker 352,352 from charging chute 350.In the ingress, near the top of vapourizing furnace, eddy flow sleeve 354 helps the coal feed distribution by this vapourizing furnace of flowing downward is become with the vaporized chemical stream from source of oxygen 305 and vapour source 307 respectively to become adverse current, and vaporized chemical is supplied with the import of each vapourizing furnace 320a-d.Rotation grate 356 distribution vaporized chemicals are also being handled lime-ash by Fig. 2 in the described system.
303a-d collects the thick gas of this process in outlet, and these outlets are connected on the pipeline 313 together, as the gas feed of quench system 306.As mentioned above, vaporized chemical is oxygen and steam mixture.
Quench system 306 comprises placed in-line 5 heat exchanger units 308,310,312,314 and 316.308 and 310 of front end is accepted the gas input of relatively-high temperature, and produces high pressure steam from heat exchanging process.Condensation product from 308 and 310 is discharged from these devices at liquid exit 309a and 309b, and these condensation products mainly comprise stiff tar and lime-ash.
The subsequent stage of quench system produces middle pressure steam and condensed light oil.As shown in Figure 3, the pneumatic outlet in each stage is connected to the gas feed of last stages, and to the last the stage 316, its output 311 forms the Entry-level System output that has the refrigerative instead of natural gas.
At this, pneumatic outlet 317 is connected to the import of heat exchanger 310, and its pneumatic outlet is connected to the import of heat exchanger 312.312 pneumatic outlet 321 is connected to the import of device 313, and the outlet 323 of device 314 is connected to the import of final stage heat exchanger unit 316.
Liquid exit 309a-e links together at a liquid exit 309 of elementary quench system.
Liquid hydrocarbon in the pipeline 309 is connected to the import of non-catalytic partial oxidation device 304.In addition, from the source 305 oxygen and from the source 307 steam is connected to the import of device 304, the secondary crude synthesis gas that mainly comprises hydrogen and carbon monoxide is discharged from installing 304 by pipeline 315, turns back to the import 313 of quench system 306, with further cooling.
Therefore, the device output 311 thick instead of natural gas that contain in about 392 quenchings, it is substantially free of the pyrolysis product that produces in elementary gasifier 302a-d.
Embodiment
With the highest unreacted coal that is about 50 weight % of ash (promptly, contain coal greater than about 30% uninflammability impurity) import in the elementary vapourizing furnace of arranging shown in Fig. 2 or 3, the elementary thick gas composition following (volume %) that in this elementary vapourizing furnace output, produces: 28.2% carbonic acid gas, 0.05% hydrogen sulfide, 0.69% higher hydrocarbon, 22.66% carbon monoxide, 38.51% hydrogen, 9.5% methane and 0.39% nitrogen.Then, the thick gas that as above produces is sent into quench system, in this system, pyrolysis product and the condensation from gas stream of other liquid, and be sent to the import of non-catalytic partial oxidation device, this device is operated under about 2578 temperature of reaction.Then, the reformation in this partial oxidation device of the thick gas of autopneumatolysis device, cracking and hydrolysis, under gasification reaction conditions, carry out this process, representative gases component (% represents with volume) below the outlet of partial oxidation device produces: 1.9% carbonic acid gas, 0.08% hydrogen sulfide, 52% carbon monoxide, 45.1% hydrogen, 0.3% methane and 0.62% nitrogen.
Described the application referring to embodiment, these embodiments only are used for example.Scope and spirit of the present invention are determined by claims.
Claims (23)
1. one kind is converted into the method for instead of natural gas with coal, and this method comprises:
The coal raw material is dropped into coal gasification apparatus;
By the coal raw material is under vaporized chemical and the heating, to small part coal raw material generating gasification;
Outlet at coal gasification apparatus obtains elementary thick gas;
And at least a portion primary raw materials gas fed non-catalytic partial oxidation device, and add a kind of partial oxidation agent, keep certain temperature, make the elementary thick gas of at least a portion effectively be converted into the secondary crude synthesis gas, avoid producing higher hydrocarbon basically.
2. the method for claim 1, this method also comprises: add the secondary crude synthesis gas in elementary thick gas.
3. the method for claim 1 is characterized in that, the elementary thick gas of at least a portion carries out quenching, therefrom separate condensable hydrocarbon, be transported to the non-catalytic partial oxidation device, condensable hydrocarbon be converted into secondary be used for synthetic gas, keep away the generation higher hydrocarbon basically.
4. the method for claim 1 is characterized in that, the partial oxidation agent comprises oxygen-containing gas and steam mixture.
5. the method for claim 1 is characterized in that, the cleaved and hydrolysis in the non-catalytic partial oxidation device of all higher hydrocarbons basically in the elementary thick gas of at least a portion.
6. method as claimed in claim 3 is characterized in that, in the cleaved and hydrolysis in the non-catalytic partial oxidation device of all higher hydrocarbons basically from the condensable liquid of elementary thick gas delivery.
7. the method for claim 1 is characterized in that, all elementary thick gases are transfused to the non-catalytic partial oxidation device basically.
8. method as claimed in claim 3 is characterized in that, all elementary thick gases carry out quenching basically, then isolated condensable hydrocarbons are transported to the non-catalytic partial oxidation device.
9. one kind is converted into the method for instead of natural gas with coal, and this method comprises:
The coal raw material is dropped into coal gasification apparatus;
By making the coal raw material in coal gasification apparatus, be under vaporized chemical and the heating at least a portion coal raw material generating gasification;
Outlet at coal gasification apparatus obtains elementary thick gas;
Make elementary thick quenching of gases, therefrom separate the liquid that contains condensable hydrocarbon;
In the presence of the partial oxidation agent, being enough to that described liquid is converted under the temperature of secondary crude synthesis gas, make this liquid carry out non-catalytic partial oxidation, avoid producing the hydrocarbon except that carbon monoxide, carbonic acid gas and methane basically.
10. method as claimed in claim 9, this method also are included in and add the secondary crude synthesis gas in the elementary thick gas.
11. method as claimed in claim 9 is characterized in that, the partial oxidation agent comprises oxygen and steam.
12. method as claimed in claim 9 is characterized in that, the temperature that liquid suffers can make abundant cracking of all higher hydrocarbons and hydrolysis basically in this liquid.
13. method as claimed in claim 12 is characterized in that, liquid carries out partial oxidation under about 2372-2732 temperature.
14. method as claimed in claim 12 is characterized in that, liquid carries out partial oxidation under about 2578 temperature and about 400psig pressure.
15. method as claimed in claim 9 is characterized in that, the coal raw material is made up of the coal that comprises at least about 30 weight % uninflammability impurity.
16. method as claimed in claim 15 is characterized in that, elementary thick gas comprises about 28 volume % carbonic acid gas, less than the hydrocarbon of about 1 volume %, and about 23 volume % carbon monoxide, the methane of about 38.5 volume % hydrogen and about 9.5 volume %.
17. method as claimed in claim 16 is characterized in that, the secondary crude synthesis gas comprises less than about 2 volume % carbonic acid gas, greater than about 50 volume % carbon monoxide with greater than the hydrogen of about 45 volume %.
18. method as claimed in claim 9 is characterized in that, the coal raw material is made up of the coal that comprises ash and maximum about 50 weight % uninflammability impurity.
19. method as claimed in claim 9 is characterized in that, the coal raw material is made up of the coal of the maximum about 3 weight % of oxygen level.
20. coal is converted into the equipment of instead of natural gas, comprises:
A plurality of coal gasification apparatus, each installs operation, makes at least a portion generating gasification of the coal raw material of sending into this device, produces primary raw materials gas in the gasification installation outlet;
Quench system, has the import that is connected to each gasification installation outlet, accept elementary thick gas, and carry out the operation of from elementary thick gas, isolating condensable hydrocarbons, liquid is transported to the liquid exit of quench system, and the thick gas of refrigerative is sent to the pneumatic outlet of quench system as synthetic natural gas;
The partial oxidation device has the import that is connected the quench system liquid exit, makes the liquid hydrocarbon of acceptance be enough to make under its temperature that is converted into the secondary crude synthesis gas in this device and carries out partial oxidation, avoids producing hydrocarbon basically in the outlet of partial oxidation device.
21. equipment as claimed in claim 20 is characterized in that, the outlet of partial oxidation device is connected to the quench system import.
22. equipment as claimed in claim 20 is characterized in that, each gasification installation comprises a fixed-bed gasification furnace, and this vapourizing furnace has:
Reinforced lock coal bunker is connected with and accepts import and the outlet that the coal raw material is used;
Pressurizing vessel, be connected with the coal import of accepting coal from the outlet of reinforced lock coal bunker, in pressurizing vessel, be connected to the coal distribution eddy flow sleeve of coal import, rotation grate with the combustion zone that is positioned at this container, be used for the part of coal of burning, and, ash is distributed to outlet of container, and be connected the gasification import that this rotation grate is used for accepting vaporized chemical;
The lock ash bucket has the import that is connected to this container solid relief outlet.
23. equipment as claimed in claim 20 is characterized in that, quench system also comprises:
A plurality of placed in-line heat exchanger units, each interchanger have the import of accepting input gas, and be used to carry from the condensation product outlet of the liquid of input condensation of gas and be used to carry pneumatic outlet by the gas of heat exchanger cooling,
Wherein, the condensation product outlet of a plurality of heat exchanger units links together, form the liquid exit of quench system, except last heat exchanger unit in this series connection, the pneumatic outlet of each heat exchanger unit is connected to the import that gas is used of accepting of next heat exchanger unit, and the pneumatic outlet of last heat exchanger comprises the pneumatic outlet of quench system.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US10/991,293 | 2004-11-17 | ||
| US10/991,293 US20060101715A1 (en) | 2004-11-17 | 2004-11-17 | Apparatus and method for coal gasification |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1782037A true CN1782037A (en) | 2006-06-07 |
Family
ID=36384645
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200510125052.2A Pending CN1782037A (en) | 2004-11-17 | 2005-11-17 | Apparatus and method for coal gasification |
Country Status (5)
| Country | Link |
|---|---|
| US (1) | US20060101715A1 (en) |
| CN (1) | CN1782037A (en) |
| AU (1) | AU2005203534A1 (en) |
| CA (1) | CA2521982A1 (en) |
| MX (1) | MXPA05008871A (en) |
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| CN102021037A (en) * | 2009-09-14 | 2011-04-20 | 新奥科技发展有限公司 | Method and apparatus for preparing methane by catalytic gasification of coal |
| CN102041120A (en) * | 2010-12-15 | 2011-05-04 | 新奥科技发展有限公司 | Method for generating synthetic natural gas |
| CN102443439A (en) * | 2010-10-15 | 2012-05-09 | 中国石油化工股份有限公司 | Method for preparing synthetic gas by gasifying on fixed bed under increased pressure |
| CN102443440A (en) * | 2010-10-15 | 2012-05-09 | 中国石油化工股份有限公司 | Stationary bed pressurizing and gasifying device for preparing synthesis gas |
| CN102911739A (en) * | 2012-11-16 | 2013-02-06 | 华东理工大学 | Method for preparing synthesis gas by coupling fixed bed gasification and non-catalytic partial oxidation |
| CN103031154A (en) * | 2011-09-30 | 2013-04-10 | 上海国际化建工程咨询公司 | Method and device for preparing synthesis gas or hydrogen by direct connection of non-catalytic partial oxidation furnace with BGL gasifier or crushed coal pressurized slag gasifier |
| CN103857772A (en) * | 2011-05-16 | 2014-06-11 | 普莱克斯技术有限公司 | Partial oxidation of methane and higher hydrocarbons in syngas streams |
| CN105392868A (en) * | 2013-05-16 | 2016-03-09 | 林德股份公司 | Process and plant for at least partial gasification of solid organic input material |
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| US20100175426A1 (en) * | 2009-01-09 | 2010-07-15 | Hunton Energy Holdings, LLC | Power Management For Gasification Facility |
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-
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- 2005-08-09 AU AU2005203534A patent/AU2005203534A1/en not_active Abandoned
- 2005-08-19 MX MXPA05008871A patent/MXPA05008871A/en unknown
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- 2005-11-17 CN CN200510125052.2A patent/CN1782037A/en active Pending
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| CN102021037A (en) * | 2009-09-14 | 2011-04-20 | 新奥科技发展有限公司 | Method and apparatus for preparing methane by catalytic gasification of coal |
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| CN102041120A (en) * | 2010-12-15 | 2011-05-04 | 新奥科技发展有限公司 | Method for generating synthetic natural gas |
| CN102041120B (en) * | 2010-12-15 | 2013-06-12 | 新奥科技发展有限公司 | Method for generating synthetic natural gas |
| CN103857772A (en) * | 2011-05-16 | 2014-06-11 | 普莱克斯技术有限公司 | Partial oxidation of methane and higher hydrocarbons in syngas streams |
| CN103031154A (en) * | 2011-09-30 | 2013-04-10 | 上海国际化建工程咨询公司 | Method and device for preparing synthesis gas or hydrogen by direct connection of non-catalytic partial oxidation furnace with BGL gasifier or crushed coal pressurized slag gasifier |
| CN102911739A (en) * | 2012-11-16 | 2013-02-06 | 华东理工大学 | Method for preparing synthesis gas by coupling fixed bed gasification and non-catalytic partial oxidation |
| CN105392868A (en) * | 2013-05-16 | 2016-03-09 | 林德股份公司 | Process and plant for at least partial gasification of solid organic input material |
Also Published As
| Publication number | Publication date |
|---|---|
| MXPA05008871A (en) | 2006-05-19 |
| CA2521982A1 (en) | 2006-05-17 |
| AU2005203534A1 (en) | 2006-06-01 |
| US20060101715A1 (en) | 2006-05-18 |
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