CN1118544C - Two segments combined gasifying process and equipment based on coal - Google Patents
Two segments combined gasifying process and equipment based on coal Download PDFInfo
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- CN1118544C CN1118544C CN00111437A CN00111437A CN1118544C CN 1118544 C CN1118544 C CN 1118544C CN 00111437 A CN00111437 A CN 00111437A CN 00111437 A CN00111437 A CN 00111437A CN 1118544 C CN1118544 C CN 1118544C
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Abstract
The present invention provides two-stage combination type coal base gasification technology and a device thereof. Water vapor and carbon dioxide in high temperature coal gas of a one-section furnace react with coal once again in a gasification mode. The sensible heat of the coal gas in the high temperature section is recovered, and the invalid components (the water vapor and the carbon dioxide) in the coal gas are fully utilized. The purposes of improving cold coal gas efficiency and reducing investment are achieved. The one-section furnace uses water coal slurry or dry powder coal as raw materials, the cold coal gas efficiency can reach 84% to 86%, and the equipment investment is low. The present invention is coal gasification technology and a device which have wide application prospects.
Description
The invention belongs to the gasification field, relate to a kind of coal gasifying process and device thereof.
Gasification is the important channel of coal high-efficiency and clean utilization, also is to implement the strategy of sustainable development to accomplish one of gordian technique of economy and harmonious development.Gasification is converted into clean secondary energy with primary energy source, its product gas can be used as the source of combustion gas (coal gas), synthetic gas, reducing gas, hydrogen, carbon monoxide etc., the coal gasification technology is widely used in fields such as synthetic ammonia, synthesizing methanol, sponge iron production, and its potential biggest market is integrated gasification combined cycle plants (IGCC) power field.
After the crisis of early seventies international petroleum, many in the world major companies and scientific and technical personnel have researched and developed high performance air-flow bed coal-gasification technology, and commercialization so far demonstrates the high and good environment protection advantage of efficiency of carbon conversion.Representationally be that to adopt coal water slurry be the Texaco (Texaco) of raw material and be Xie Er (Shell) technology of raw material with the dry coal powder.United States Patent (USP) U.S.Pat.Nos.4,228,604,4,251,228,2,871,114,4,110,359,4,197,281 disclose Texaco Coal Gasification Process and device respectively, find in actual application, and its obvious deficiency is, efficiency of carbon conversion is lower, and about about 95%.Because be chilling process, it is suitable being used to produce synthetic gas, is used to generate electricity that then efficient is lower, and cold water power station (Cool water) clean generating efficiency only is about 36%.When being used to generate electricity, Texaco then adopts the radiation waste heat boiler to reclaim the gas heat scheme in order to improve generating efficiency.Its shortcoming is: reclaim the gas heat investment greatly, the radiant boiler investment of handling 2000 tons of device for coal a day reaches 200,000,000 Renminbi; The also often stifled slag in tower handkerchief (Tampa) power station, plant factor is low; Water vapor in the coal gas and carbonic acid gas (respectively accounting for 16% approximately) can not make full use of; The cold gas efficiency of this technology is lower, and is generally only about 74%, clean generating efficiency be about 41% (low heat value, LHV).
Patent DE P3714915.6 (publication number in China is 88102581), US738,727 (publication number in China is 86103455) disclose Xie Er dry coal powder gasification technology respectively, business-like device is the day that is built in Dutch Bu Genlun (Buggenum) to handle 2000 tons of coal gasification apparatus, its obvious deficiency is: carry the slag blocking pipe for preventing coal gas, and employing circulating gas Quench, make coal gas reduce to 900 ℃ by about 1500 ℃, this measure has increased recycle compressor and compression work thereof, the forfeiture driving force of heat transfer; For reclaiming the waste heat boiler (gas cooler) that gas heat is provided with 500 tons of weights, investment is big, and is easy to stop up.
Defective in view of above-mentioned coal gasifying process and device, branch of industry is main power industry as the coal energy particularly, wishes that urgently relevant scientific and technical personnel develop a kind of efficiency of carbon conversion height, the cold gas efficiency height is that low, the steady in a long-term Coal Gasification Technology that turns round of generating efficiency height, investment is to satisfy the needs of power industry optimization and upgrading.
One of purpose of the present invention is to overcome the deficiencies in the prior art, and disclosing a kind of efficiency of carbon conversion height, cold gas efficiency height is that generating efficiency height, investment are low, the coal-based two segments combined coal gasifying process of running steady in a long-term;
Two of purpose of the present invention is to disclose a kind of coal-based two segments combined coal gasification apparatus.
Design of the present invention is such:
Being in the gasification reaction process of raw material production coal gas with coal water slurry or dry coal powder and oxygenant, vaporized chemical, is to improve efficiency of carbon conversion, and coupled combustion reactions heat release makes the temperature out of coal gas can reach 1200～1600 ℃.In order to improve gasification efficiency, except that improving efficiency of carbon conversion, main path is the efficient recovery gas heat, and makes full use of water vapor and carbonic acid gas in the coal gas.
Because the gasification reaction of carbon is thermo-negative reaction, its reaction formula is:
Therefore, the contriver thinks and the water vapor in the coal gas of high temperature, carbonic acid gas and coal can be carried out gasification reaction again one time, two reaction process are connected mutually, need not to add oxygenant to second reaction process, utilize the gas heat of primary reformer to provide heat, can carry out gasification reaction for above-mentioned reaction.So both reclaim the gas heat of high temperature section, made full use of invalid component in the coal gas (water vapor and carbonic acid gas) again, reached the purpose that improves cold gas efficiency and reduce investment.
Adopt type of cooling recycle-water gas heat different with Texaco, Shell, the present invention adopts chemical reaction method to reclaim gas heat.
According to above-mentioned design, the contriver has proposed following technical scheme:
The said technology of the present invention mainly comprises the raw material coal gasification and realizes that by coal gasification reaction the sensible heat of coal gas of high temperature reclaims two parts:
Coal dust or coal water slurry and oxygenant, vaporized chemical are gasified in primary reformer, and vapor pressure is 0.5～12.0Mpa, by the charging proportioning gasification temperature is controlled, and makes gasification temperature reach 1200～1600 ℃.This operating process is easy to realize to one skilled in the art.The main component of outlet coal gas is: H
2=20～35%, CO=40～65%, CO
2=3～22%, water vapor=2～20%, and grey slag etc.Its reaction formula is:
Above-mentioned formula (2), (3) are thermopositive reaction, and all the other are thermo-negative reaction, and formula (4), (5) are the purpose reaction, and formula (2), (3) are its coupling reaction, promptly emit heat by it, are creating conditions of purpose reaction.Flame temperature is up to 1500～1900 ℃, and lime-ash is molten state and flows down along the furnace wall in the coal, leaves primary reformer with coal gas through outlet, and its temperature is about 1200 ℃～1600 ℃.Because of the difference of coal, processing condition, vapourizing furnace pattern, the efficiency of carbon conversion of primary reformer is 95%～99%, and cold gas efficiency is 65%～83%;
Coal gas and slag realize that by mass force both separate in coal gas and slag pipeline separator, slag flow to outlet along wall, enters slag bath after the water Quench and discharges out of the furnace;
2. the coal gas of high temperature of primary reformer then enters secondary reformer, reacts with the coal that enters secondary reformer, retrieves the sensible heat from the coal gas of primary reformer.
The coal that enters secondary reformer by from the coal gas of primary reformer in secondary reformer, temperature is warmed up to about 1350 ℃ rapidly, carries out drying, pyrolytic process simultaneously.The temperature height generates fugitive constituent and semicoke, because can not generate ring-type or polynuclear compounds such as stable tar, phenol, naphthalene.Also carry out simultaneously suc as formula (4) and the thermo-negative reaction shown in (5) temperature being reduced gradually, the lime-ash that the reaction back generates drains into the ash lock through grate with ash, and the lime-ash that carries in the coal gas then separates in gas-solid separator, and coal gas is sent to back workshop section.
The operating procedure condition of secondary reformer is such:
Feed coal is of a size of 5～50mm; Pressure is 0.3MPa～11Mpa a little less than primary reformer; Gasification temperature is different because of coal, and top is 1350～1500 ℃, and the bottom is 950～1000 ℃, can wait and regulates by add an amount of vaporized chemical such as water vapor, water or carbonic acid gas before secondary reformer; Secondary reformer coal amount accounts for 10%～25% of total coal amount; The reaction time of gasifying medium in secondary reformer is 10 seconds～20 seconds, and the residence time of coal is 1 hour～2 hours;
Coal ash fusion temperature is different because of coal, the difference great disparity, and common is 1300 ℃～1500 ℃, reaches as high as more than 1600 ℃.In order to prevent to scab,, make inlet air temperature use the ash fusion point of coal a little less than secondary reformer so before primary reformer coal gas enters secondary reformer, spray into media such as an amount of water vapor, water or carbonic acid gas by nozzle because of the coal ash fusion causes secondary reformer;
If it is raw material that primary reformer adopts dried coal powder, water vapor, carbon dioxide content are all seldom in the outlet coal gas, the two reacting weight that carries out formula (4) and (5) also is not enough to reclaim the primary reformer gas heat makes it to reduce to 950 ℃～1000 ℃, at this moment, even if the ash fusion point of secondary reformer coal is very high, also should before entering secondary reformer, primary reformer coal gas spray into media such as an amount of water vapor, water or carbonic acid gas by nozzle, so that can fully reclaim the sensible heat in the coal gas;
The secondary reformer efficiency of carbon conversion can reach more than 98%, and the transformation efficiency of water vapor and carbonic acid gas is 5～75%, and temperature can be reduced to 950 ℃～1000 ℃, has realized utilizing the primary reformer gas heat, improves CO, H
2Purpose with methane content in coal gas.In other words, in secondary reformer, do not burn (oxidation) reaction, only carry out gasification reaction, thermal source is from the primary reformer gas heat, do not need the thermopositive reaction that is coupled again, carbon major part in the coal all is converted into effective carbon monoxide and methane, and the invalid carbonic acid gas of regeneration not significantly improves cold gas efficiency.
Below will elaborate the present invention by accompanying drawing.
The said coal-based two segments combined gasifying process schema of Fig. 1.Among the figure:
1---primary reformer
2---the primary reformer feed nozzle
3---primary reformer coal gas and slag exit
4---coal gas and slag pipeline separator downtake
5---coal gas and slag pipeline separator upcast
6---nozzles
7---slag exit
8---replenish medium nozzle
9---the coal lock
10---secondary reformer
11---grate
12---the ash lock
13---the secondary reformer gas exit
14---gas-solid separator
15---gas exit
As seen from Figure 1, feed coal (water-coal-slurry or dry pulverized coal), oxidant and gasifying agent enter primary reformer 1 by primary reformer feed nozzle 2:
If take water-coal-slurry as raw material, then this water-coal-slurry and oxidant (for example contain O2=95～99% gas need not added gasifying agent) enter primary reformer 1 by primary reformer nozzle 2;
If take dry pulverized coal as raw material, then this dry pulverized coal and oxidant, gasifying agent (H2O、CO
2) enter together primary reformer 1 by primary reformer nozzle 2. Forms limited percussion flow a little more than the raw material of normal temperature by the stream thigh that primary reformer nozzle 2 penetrates in primary reformer 1, accelerate heat transfer, mass transfer and mixed process, the coal grain is along with physical and chemical processes such as the temperature rising is evaporated, pyrolysis, burning and gasification reactions;
Above-mentioned reaction is carried out under 0.5～12Mpa condition, flame temperature is 1500 ℃～1900 ℃, lime-ash is molten state and flows down along the furnace wall in the coal, leaves primary reformer 1 with coal gas through primary reformer coal gas and slag exit 3, and its temperature is about 1200 ℃～1600 ℃. Because of the difference of coal, process conditions, gasification furnace pattern, the efficiency of carbon con version of primary reformer 1 is 95%～99%, and cold gas efficiency is 65～83%. The coal gas main component is: H2＝20～35％、CO＝40～65％、CO
2=3～22%, water vapour=2～22%;
Then, coal gas and slag enter coal gas and slag pipeline separator down-comer 4 and coal gas and slag pipeline separator tedge 5 by coal gas and the slag exit 3 of primary reformer, realize that by inertia force both separate, slag flows out coal gas and slag pipeline separator down-comer 4 along wall by slag exit 7, coal gas then enters secondary reformer 10, enter secondary reformer 10 with the coal from coal lock 9 and carry out gasification reaction again, the temperature of coal gas is down to 950 ℃～1000 ℃:
The lime-ash that generates after the reaction in secondary reformer 10 is discharged by ash lock 12 by grate 11, and coal gas enters gas-solid separator 14 by the secondary reformer gas exit 13 of secondary reformer 10 bottoms, isolate ash content after, coal gas is sent to rear workshop section;
The water of adding, water vapour or carbon dioxide can be by replenishing medium nozzle 8 adding systems;
Axis at coal gas and slag pipeline separator tedge 5 is provided with nozzles 6, passes into an amount of oxidant, and preventing because of slag cooling blocking pipe, the intake of oxidant is take blocking pipe not as standard.
By Fig. 1 simultaneously as seen, above-mentioned disclosed technique can be carried out in mainly comprising the device that primary reformer 1, secondary reformer 10, primary reformer feed nozzle 2, the equipment such as medium nozzle 8, coal gas and slag pipeline separator down-comer 4 and coal gas and slag pipeline separator tedge 5 that replenish consist of.
That said primary reformer 1 can adopt is conventional, business-like coal gasifier, preferably adopt the air flow bed under slag and coal gas and the flow direction, but " multi-nozzle opposed water-coal-slurry or the pulverized coal gasification furnace " that can preferably adopt the inventor in Chinese patent CN1186840A, to provide;
Said secondary reformer 10 is a moving bed, and the top is provided with a coal lock 9 that is used for coal; The bottom is provided with a rotatable grate 11, and said grate 11 has ash discharge, break, the time of staying of adjusting coal in furnace and the effect of uniform air-flow;
Be connected with slag pipeline separator tedge 5 with coal gas with slag pipeline separator down-comer 4 with coal gas between the primary reformer coal gas of the bottom of primary reformer 1 and slag exit 3 and the secondary reformer 10, the slag of primary reformer 1 is discharged primary reformers 1 by the slag exit 7 that is arranged on coal gas and slag pipeline separator down-comer 4 bottoms;
The coal gas and the slag pipeline separator tedge 5 that close on secondary reformer 10 are provided with additional medium nozzle 8, are used for the cooling of primary reformer 1 coal gas of high temperature or replenish required water, water vapour or the carbon dioxide of secondary reformer 10 reactions;
Same axis at coal gas and slag pipeline separator tedge 5 is provided with nozzles 6, is used for passing into an amount of oxidant, to prevent because of slag cooling blocking pipe;
Coal adds from the coal lock 9 at secondary reformer 10 tops, with the coal gas from primary reformer 1 that enters secondary reformer 10, flow from top to bottom, react, reacted lime-ash enters ash lock 12, the coal gas that generates then is sent to gas-solid separator 14 by the gas exit 13 of secondary reformer 10, tell ash content after, coal gas is sent to postorder workshop section by gas exit 15.
The said coal gasification of in said apparatus, carrying out, no matter primary reformer is raw material with water-coal-slurry or dried coal powder, cold gas efficiency all will significantly increase, depending on coal and differently can reach 84% even 86%, exceed 5～8 percentage points than existing commercialization air flow bed device (Texaco, Xie Er), and equipment investment is low, is a kind of coal gasifying process and device with broad prospect of application.
Below will the present invention is further illustrated by embodiment.
With the coal water slurry is primary reformer gasified raw material two segments combined gasifying process.
Adopt coal ultimate analysis (quality %) as follows:
C 76.996
H 5.286
N 1.218
S 2.989
O 4.935
Ash 8.576
The processing condition that adopt are as follows:
Coal-water fluid concentration (solid content) 65.7%, coal slurry density 1174kg/m
3, oxygen purity 99% (volume), vapor pressure: 3.0Mpa, it is 677.3Nm that the ton coal adds the oxygen amount
3The gas temperature of primary reformer (multi-nozzle opposed type coal slurry gasifier) 1 outlet 3 is 1345 ℃, and the gas composition of primary reformer 1 outlet is: H
2O=12.33%, H
2=33.58%, CO=39.31%, CO
2=13.16%, H
2S=0.76%, COS=0.04%, CH
4=0.1%, NH
3=0.18%, N
2+ Ar=0.54%, efficiency of carbon conversion is 98%, cold gas efficiency is 75.5% (HHV), and the slag that carries in the coal gas is about 95% separated in coal gas and slag pipeline separator downtake 4 and coal gas and slag pipeline separator upcast 5, and slag is discharged through slag exit 7; Because of the temperature of coal gas before entering secondary reformer 10 is 1345 ℃, and moisture vapor 0.323Nm
3/ kg, CO
2Be 0.345Nm
3/ kg, so need not to add any material, nozzle 8 no longer is provided with under this condition.Above-mentioned gas carries out physical and chemical processes such as drying, pyrolysis, gasification with the coal that adds from coal lock 9 in secondary reformer 10, gas temperature reduces gradually, and exporting 13 place's temperature is 1000 ℃, and pressure is about 2.6Mpa, gaseous constituent (butt) H
2=39.37%, CO=47.65%, CO
2=10.22%, H
2S=0.84%, COS=0.04%, CH
4=1.12%, N
2+ Ar=0.55%, NH
3+ HCN=0.21%.Cold gas efficiency is 84.1% (HHV), has improved 8.6 percentage points than primary reformer 1, and the secondary reformer efficiency of carbon conversion is 98%, and the steam reforming rate is 60%, CO
2Transformation efficiency is 29.7%.Be 60% and CO of water vapor in the primary reformer coal gas
229.7% in secondary reformer, carry out gasification reaction, reach and reclaim its sensible heat purpose, make its temperature reduce to 1000 ℃ by 1345 ℃.
With the dry coal powder is primary reformer raw material two segments combined gasifying process.
Coal is identical with example 1, and going into stove coal water content is 2%, and oxygen purity is 95%, and the oxygen coal is than being 0.650Nm
3/ kg steams steam oxygen ratio 0.1974kg/Nm
3The gas temperature of primary reformer (multi-nozzle opposed type coal slurry gasifier CN1186840A) 1 outlet 3 is 1500 ℃, and efficiency of carbon conversion is 99%, and wet basis gas composition (volume) is: H
2=28.77%, CO=58.35%, CO
2=2.76%, H
2S=0.85%, COS=0.07%, CH
4=0.01%, N
2=3.16%, Ar=0.88%, NH
3=0.19%, H
2O=4.96%, cold gas efficiency are 80.5% (HHV).
CO in the above-mentioned coal gas
2, vapour content is very little, is not enough to reclaim the sensible heat of coal gas more than 1000 ℃ by gasification reaction formula (4) and (5) heat absorption.Before advancing secondary reformer 10, adopt the scheme add water vapor, with secondary reformer 10 be benchmark with coal, its mass ratio is 1.016kg/kg, makes into the mixed gas temperature of secondary reformer 10 reduce to 1350 ℃, satisfiedly simultaneously prevents the slag requirement that scabs.Mixed gas also flows from top to bottom with the coal that adds secondary reformer 10, carries out drying, pyrolysis, gasification reaction.Temperature of gas is 1000 ℃ when going out secondary reformer 10, and efficiency of carbon conversion is 98%, and the steam reforming rate is 69%, CO
2Transformation efficiency be 19.6%, gas composition (butt) is: H
2=32.08%, CO=59.03%, CO
2=2.29%, H
2S=0.89%, COS=0.05%, CH
4=1.82%, N
2=2.85%, Ar=0.78%, NH
3+ HCN=0.21%.Cold gas efficiency reaches 86.1%.Cold gas efficiency than primary reformer has improved 5.6 percentage points.
Claims (7)
1. coal-based two segments combined gasifying process mainly comprises the raw material coal gasification and realizes that by coal gasification reaction the sensible heat of coal gas of high temperature reclaims two parts, is characterized in that:
Temperature is that 1200 ℃～1600 ℃ primary reformer (1) coal gas leaves primary reformer (1) with slag by primary reformer coal gas and slag exit (3), enter coal gas and slag pipeline separator downtake (4) and coal gas and slag pipeline separator upcast (5), slag flows out coal gas and slag pipeline separator downtake (4) along wall by slag exit (7), coal gas then enters secondary reformer (10), enters secondary reformer (10) with the coal from coal lock (9) and carries out gasification reaction again;
The lime-ash that secondary reformer (10) reaction back generates is discharged by ash lock (12) by grate (11), and coal gas enters gas-solid separator (14) by the secondary reformer gas exit (13) of secondary reformer (10) bottom, isolate ash content after, be sent to back workshop section;
Secondary reformer (10) working pressure is lower than primary reformer (1), and the working pressure of secondary reformer (10) is 0.3MPa～11Mpa, and the top gasification temperature is 1350 ℃～1500 ℃, and the bottom is 950～1000 ℃, and the gasifying medium reaction time is 10 seconds～20 seconds; The residence time of coal is 1～2 hour, and the add-on of secondary reformer (10) coal is 10%～25% of a coal total amount.
2. technology as claimed in claim 1 is characterized in that, can by replenish medium nozzle (8) add water, water vapor or (with) carbonic acid gas.
3. technology as claimed in claim 1 is characterized in that, feeds oxygenant by nozzles (6).
4. a coal-based two segments combined gasifying device is characterized in that mainly comprising primary reformer (1), secondary reformer (10), primary reformer feed nozzle (2), replenishes medium nozzle (8), coal gas and slag pipeline separator downtake (4) and coal gas and slag pipeline separator upcast (5);
That said primary reformer (1) can adopt is conventional, the air flow bed under business-like, slag and the coal gas and the flow direction;
The top of said secondary reformer (10) is provided with a coal lock (9) that is used for coal, and the bottom is provided with a rotatable grate (11);
Be connected with slag pipeline separator upcast (5) with coal gas with slag pipeline separator downtake (4) with coal gas between the primary reformer coal gas of the bottom of said primary reformer (1) and slag exit (3) and the secondary reformer (10), the bottom of coal gas and slag pipeline separator downtake (4) is slag exit (7); The gas exit (13) of secondary reformer (10) is connected with gas-solid separator (14).
5. device as claimed in claim 4 is characterized in that, the coal gas and the slag pipeline separator upcast (5) that close on secondary reformer (10) are provided with additional medium nozzle (8).
6. device as claimed in claim 4 is characterized in that, is provided with nozzles (6) on the same axis of coal gas and slag pipeline separator upcast (5).
7. device as claimed in claim 4 is characterized in that: " multi-nozzle opposed type coal water slurry or the pulverized coal gasification furnace " that provides among the Chinese patent CN1186840A is provided said primary reformer (1).
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| CN00111437A CN1118544C (en) | 2000-01-13 | 2000-01-13 | Two segments combined gasifying process and equipment based on coal |
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|---|---|---|---|
| CN00111437A CN1118544C (en) | 2000-01-13 | 2000-01-13 | Two segments combined gasifying process and equipment based on coal |
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| CN1262309A CN1262309A (en) | 2000-08-09 |
| CN1118544C true CN1118544C (en) | 2003-08-20 |
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| CN00111437A Expired - Fee Related CN1118544C (en) | 2000-01-13 | 2000-01-13 | Two segments combined gasifying process and equipment based on coal |
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Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100543116C (en) * | 2005-08-19 | 2009-09-23 | 中国科学院过程工程研究所 | The oxygen deprivation fluidized bed combustion downdraft gasification process and the device that prepare no tar products gas |
| CN1994865B (en) * | 2006-12-12 | 2011-05-18 | 华东理工大学 | Gasification device for two-stage gasification coupled with heat recovery and washing and its uses |
| CN101307258B (en) * | 2007-10-12 | 2011-06-29 | 李东田 | Gas generator device for recovering sensible beat of slag obtained from gas producer |
| CN101298569B (en) * | 2008-06-26 | 2011-05-11 | 华东理工大学 | Gasification method of shock chilling type pulp or powder carbonaceous material |
| CN102071069B (en) * | 2010-11-25 | 2013-12-25 | 中国科学院山西煤炭化学研究所 | Device and method for regulating temperature of coal gas at outlet of fluidized bed gasifier |
| CN103965981B (en) | 2013-01-31 | 2016-05-25 | 通用电气公司 | The apparatus and method of preparation water-coal-slurry |
| CN104694167A (en) * | 2014-12-12 | 2015-06-10 | 周士友 | Novel two-stage type gas-solid bed continuous gasification device |
| CN105925313A (en) * | 2016-07-17 | 2016-09-07 | 昆明新能源发展有限公司 | Carbon dioxide/coal coke gasification method and device thereof |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4872886A (en) * | 1985-11-29 | 1989-10-10 | The Dow Chemical Company | Two-stage coal gasification process |
-
2000
- 2000-01-13 CN CN00111437A patent/CN1118544C/en not_active Expired - Fee Related
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4872886A (en) * | 1985-11-29 | 1989-10-10 | The Dow Chemical Company | Two-stage coal gasification process |
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