CN1834210A - Process of producing synthetic gas of carbinol and dimethyl ether by all oxygen gasifying of poor goal - Google Patents
Process of producing synthetic gas of carbinol and dimethyl ether by all oxygen gasifying of poor goal Download PDFInfo
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Abstract
This invention relates to a method for manufacturing methanol and dimethyl ether by complete oxidation of inferior coal at normal pressure. Pure oxygen and water vapors are used as the gasifying agents. The method comprises the steps of: drying the raw material coal, pulverizing, and screening to coal powders with particle sizes less than 10mm, introducing into a furnace, mixing with pure oxygen and water vapors injected into the furnace by an injection nozzle, and gasifying to obtain feed gas for methanol synthesis. The method has such advantages as wide raw material resources, low cost, low investment, simple equipment structure, simple process, stable operation, high gasification strength, long operation period, low impairment rate, and simple waste treatment method.
Description
Technical field
The present invention relates to produce the methyl methanol syngas field, particularly relate to the method that methyl alcohol and dme synthetic gas are produced in a kind of low grade coal total oxygen gasification.
Technical background
At present, in Chemical Manufacture, the gasifying process of producing methyl alcohol with coal generating gas mainly contains shell dried coal powder gasifying process, Texaco's water coal slurry pressure gasification process, and strange fixed bed pressured gasification technology in Shandong and fixed bed be atmospheric gasification technology intermittently.More than these several gasification technologies obtained promotion and application in succession in the chemical enterprise at home.Because the gasification of shell dried coal powder, Texaco's water coal slurry pressure gasification, the strange fixed bed pressured gasification in Shandong etc. all are the large-scale Coal Gasification Technology from external introduction, the facility investment costliness, the operation expense height will be used high-quality anthracite.And intermittent type fixed bed atmospheric pressure gasification technology falls behind, and gas production rate is low, and raw material is confined to coke and high-quality anthracite block coal, costs an arm and a leg and supply falls short of demand, and methyl alcohol synthetic raw gas production cost height easily pollutes environment, flow process complexity, the H of synthetic gas
2O/CO≤1, its value is on the low side, weakens with the cheap advantage of coal price lattice.
Chinese patent CN2513997Y, 1418935, adopting lump coal and Sweet natural gas is raw material, and the furnace for preparing synthesis gas of ad hoc structure, add block Wingdale etc. in the gasification reaction, cause the flow process complexity to gas making and deslagging processing, difficulty increases, although adopt part lump coal instead of part Sweet natural gas, the technical process complexity, but cost is very high, Gas Prices costliness especially in recent years, and no Sweet natural gas area is difficult to realize.
Summary of the invention:
The objective of the invention is to overcome above-mentioned prior art and production technique and have weak point, through contriver's development research for many years and long-term industrialization production practice, develop a kind of total oxygen gasification of adopting low grade coal, invest little, technical process is simple, operate steadily, gasification intensity is big, and cost is low, equipment is long simple running period, the maintenance of equipment expense is low, and the three wastes are handled the novel method that methyl alcohol and dme synthetic gas are produced in simple, safe and reliable low grade coal total oxygen gasification.
The method that methyl alcohol and dme synthetic gas are produced in low grade coal total oxygen gasification provided by the invention comprises the following steps:
1. the pre-treatment of feed coal obtains the following fine coal of granularity 10mm with inferior raw material coal drying, fragmentation and screening and directly sends in the coal bin confession gasifier system gas raw material fine coal;
2. the conveying of raw material fine coal
Raw material fine coal in the coal bin of step in is 1. sent in the cone segments of vapourizing furnace bottom with screw-type coal distributor, and in defeated coal process, the nitrogen that feeds pressure in the coal bin and be 35KPa prevents that as safe gas gas is refunded in the coal bin in the stove;
3. gasification reaction
In vapourizing furnace, with concentration is that 99% pressure is that 45KPa oxygen and pressure are the vaporized chemical that the low-pressure steam of 0.3MPa is formed, in mixing tank behind the uniform mixing, by being arranged in vapourizing furnace, on the bottom, following vaporized chemical nozzle layer sprays in the vapourizing furnace and the fine coal generating gasification reaction that is in fluidized state with the stove internal combustion, stove bottom gasification reaction temperature is 950-1000 ℃, reaction pressure is 8-11Kpa, middle part gasification reaction temperature is 1000-1050 ℃, oxygen is 1 with the ratio of low-pressure steam: 0.8-0.9 (volume ratio), and fine coal is 3.4-3.8 with the ratio of steam: 1 (weight ratio) nozzle oxygen ratio up and down is 1: 3.0-4.5;
4. the cooling purifying and dedusting of synthetic gas
Synthetic gas by the top of gasification furnace output enters the dedusting of outlet of still cyclonic separator through last air flue, separate unreacted fine coal and return vapourizing furnace by return line, carry out the fluidized gasification reaction once more, the high temperature dust synthetic gas that leaves cyclonic separator removes waste heat boiler system recoveries heat, enter the preliminary scrubbing dust collection of empty spray tower after synthetic gas is cooled to 150-200 ℃, after entering the further scrubbing dust collection of synthesis gas washing tower again, again through venturi scrubber once more after the dedusting, the qualified synthetic gas of output;
5. lime-ash is controlled deslagging in good time
According to vapourizing furnace gasifier bed layer resistance, control deslagging by the terminal Eight characters comb of cone in good time.
Produce in the method for methyl alcohol and dme synthetic gas according to low grade coal total oxygen gasification provided by the invention, described low grade coal is the various inferior quality coals that the coal-mining industry field is known, for example, long bituminous coal, non-caking coal bituminous coal, weakly caking coal bituminous coal, the brown coal of ash-rich etc., because coal price is cheap, helps reducing production costs.The feed coal pre-treatment is simple, only needs through the one-level drying, and fragmentation, screening can meet produces the synthetic gas requirement.Because coal price is low, can realize low cost production, the raw materials cost of ton methyl alcohol is than low about 200 yuan of the Sweet natural gas system of employing methanol feedstock cost.
Drying, fragmentation, the screening pulverized coal particle size is below the 10mm, directly sends into coal bin, delivers to fragmentation if there is the raw material low grade coal that sifts out greater than the 10mm granularity to return, screening makes its granularity send into coal bin below 10mm, uses for vapourizing furnace gas making.Above-mentioned fine coal is delivered to gasification installation (general name) hopper by belt; deliver to the pressurization coal bin through screw-type coal distributor, the pressurize of coal bunker inflated with nitrogen is protected to 35KPa, prevents that gas is refunded in the coal bin in the stove; coal bunker for example volume is 270 cubic metres, is provided with level gauging and warning device.Fine coal in the pressurization coal bunker is delivered coal to cone position, vapourizing furnace bottom by the regulation and control of frequency by three screw-type coal distributors in bottom (power according to throughput and every feeder is decided), fine coal adds in the stove, stretches into external combustion gas by the fire hole in the middle part of the body of heater raw material fine coal in the stove is lighted.
Described vapourizing furnace is empty barrel structure, top is direct tube section, the bottom is a cone segments, the furnace lining refractory materials, two-layer dismountable nozzle is located at body of heater middle part direct tube section and bottom cone segments respectively, the nozzle layer of cone segments (claim down nozzle layer) is established 4-12 nozzle, and is excellent, elect 6-8 nozzle as, is evenly distributed on the cross section of stove cone with body of heater angled (presenting 20 ° of-30 ° of angles with the conical surface); The nozzle layer (deserving to be called nozzle layer) of middle part direct tube section is established 16-30 nozzle, is preferably 20-26 nozzle, is uniformly distributed on the cross section, cylindrical shell garden perpendicular to body of heater.For example but industrial production can reach 4.0 ten thousand Nm with vapourizing furnace separate unit stove production of synthetic gas
3/ h, 5 meters of diameters, 4 meters of internal diameters, high 41 meters, the bottom is high 4 meters cone segments, and top is direct tube section, and following nozzle layer is positioned at cone segments 3-3.8 rice, and the upper spray nozzle layer is positioned at apart from furnace roof 18-20 rice.This gasification furnace structure is simple, and maintenance capacity is little, owing to cancelled the grate of vapourizing furnace bottom, has avoided existing originally problems such as furnace bottom slagging scorification, and in fact the vapourizing furnace body is exactly an empty barrel structure.Vapourizing furnace only is made up of body of heater and dismountable nozzle of inner lining refractory, there are not driving part and easily worn part, and bed temperature relative wind bed gasification furnace is much lower, wearing and tearing and erosion intensity to refractory materials reduce greatly, therefore, less demanding to refractory materials, the vapourizing furnace operation factor is higher.
Fully few (having only three screw-type coal distributors and two the spiral residue extraction machines) running device of vapourizing furnace running is simple in structure, and running period is long, and failure rate is low, and the maintenance of equipment amount is few, and maintenance cost is low.In vapourizing furnace, carry out gasification reaction, will be in the vaporized chemical mixing tank thorough mixing vaporized chemical-concentration be 99% the pressure vaporized chemical (volume ratio 1 of oxygen and steam: 0.8-0.9) that to be 45Kpa oxygen (the empty oxygen that divides) form for the 0.3Mpa low-pressure steam with pressure, spray into by following nozzle layer, by the pressure of vaporized chemical self fine coal of stove internal combustion is blown afloat the boiling fluidisation, make the interior raw material fine coal of stove be in the boiling fluidized state, raw material fine coal and oxygen, steam fully contacts, react in vapourizing furnace direct tube section generating gasification, control stove bottom temperature of reaction is at 950-1000 ℃, vapourizing furnace internal reaction pressure is 8-11Kpa, control suitable gas flow rate, the i.e. control down nozzle layer amount that the sprays into vaporized chemical amount that makes nozzle layer up and down spray into vaporized chemical is in a suitable proportion, and for example the oxygen ratio is 1: 3.0-4.5 is beneficial to temperature controlling in the whole stove.The interior gas-solid of fluidized-bed is contacted better, strengthened thermal conduction and heat exchange, strengthened heat and mass transfer process, make gas be tending towards perfect.
Spraying into vaporized chemical by the upper spray nozzle layer goes in the vapourizing furnace, with carry tiny fine coal carbon granules from the bed bottom and rise to the further reaction of body of heater middle part, middle part gasification reaction temperature is 1000-1050 ℃, reduce fine coal concentration in the stove thus and reduce the amount of carry-over, improve gasification reaction conditions in the stove, gasification intensity is increased.Gasification intensity is higher, bed temperature can reach about 1050 ℃, and uniformity of temperature profile in the stove, all more than 900-950 ℃, fugitive constituent is heated and decomposes rapidly in the raw material, and cracking such as the high hydrocarbon polymer of tar are more complete, thereby synthetic gas is substantially free of tar phenols etc., alleviate purification burden and pollution, improve environment.Leave gasifier temperature and be 930-980 ℃ synthetic gas, after last gas leaves vapourizing furnace, enter outlet of still cyclonic separator (universal), separate unreacted coarse particles flying dust and return vapourizing furnace charging position by return line (internal diameter is 200mm), in stove, participate in the fluidized gasification reaction once more, not only improve the whole efficiency of carbon conversion of gasification, and unburned carbon in flue dust is reduced to below 20%, thereby improved the efficient and the coal rate of energy of gasification.Make separate unit stove production of synthetic gas can reach 4.0 ten thousand Nm
3/ h. carbon utilisation rate can reach 92%, and effective ingredient is higher in the synthetic gas, H
2+ CO can reach about 75%, H
2/ CO ratio is greater than 1.
The temperature of gasification bed is mainly by the amount that adds fine coal inferior in the vapourizing furnace, amount of oxygen and vapor volume, the three regulates, when amount of oxygen and vapor volume be vaporized chemical stable before topic down, the gasification bed temperature is mainly by adding the coal amount adjusting.The volume ratio of oxygen and steam general 1 in the vaporized chemical: 0.8-0.9.Low grade coal and steam weight ratio are 3.4-3.8: 1, wherein oxygen divides oxygen from sky, purity is crossed 99%, pressure is 45Kpa, steam is the low-pressure steam of 0.3Mpa, spray in the vapourizing furnace by nozzle layer about the stove by mixing the back before entering vapourizing furnace, the fine coal generating gasification reaction that is in fluidized state, output methyl methanol syngas with the stove internal combustion.
Leave the high-temperature gas of cyclonic separator, enter waste heat boiler top, the synthetic gas feeding water heater that comes out in the bottom through Y-tube.The synthetic gas temperature that well heater comes out is reduced to 150-200 ℃.
Waste heat boiler produces the 3.9MPa saturation steam, incorporates factory's middle pressure steam pipe network into, and hour gas production rate is 22 tons, useless pot inlet Y-tube, and the ash that waste heat boiler and feedwater heating apparatus separate enters the bottom water sealed tank, adds water with water seal and drains.
Synthetic gas behind the recovery waste heat, enter scrubbing dust collection system (general-purpose equipment technology), at first enter the dedusting of empty spray tower Quench, advance the stuffing washing tower dedusting then, after the Venturi scrubbing fly-ash separator dedusting of two-stage series connection makes the 65g/Nm of gas dustiness by useless pot inlet
3Reduce to 60mg/Nm
3, gas temperature is reduced to below 40 ℃, delivers to gas holder and stores.
Described deslagging is to control deslagging according to the gasifier bed layer resistance in good time, be the gasification reaction ash bed below the nozzle under the vapourizing furnace, the lime-ash that remains in herein in service passes through " eight " word comb of cone end, can divide two-way to be interrupted and drain into the slag storehouse, the slag storehouse is provided with level gauging, store a certain amount of after, be discharged to slag car outward transport, the vapourizing furnace deslagging temperature is 700-800 ℃, can add water in the slag storehouse before slag effluxes or add steam cooling.
Synthetic gas main technologic parameters provided by the invention:
Synthetic gas is formed:
| Synthetic gas is formed (%) (V) | |||||||
| CO | H 2 | CO 2 | CH 4 | O 2 | N 2 | CO+H 2 | |
| 35.2 | 38.8 | 22.2 | 2.5 | 0.4 | 1.1 | 74 | |
Vaporized chemical and coal consumption index
| Oxygen consumption tolerance (m 3/h) | Consumption quantity of steam t/h | Consumption of coal t/h | Producing coal tolerance Nm 3/h | |
| 9532 | 8.45 | 29.7 | 44533 |
Lime-ash remaining carbon: 11.45%
The transformation efficiency of carbon: 91.89%
Gasification efficiency: 72.62%
The invention provides the method characteristics that methyl alcohol and dme synthetic raw gas are produced in the gasification of low grade coal total oxygen:
1, the gasified raw material coal adopts low grade coal, and cost of material is low, and it is low to produce the synthetic gas cost, and the feed coal pre-treatment is simple.
2, gasification intensity is big, and separate unit vapourizing furnace methyl methanol syngas output can reach 4.0Nm
3/ h, carbon utilisation rate can reach 92%, and the synthetic gas effective ingredient is higher, H
2+ CO can reach about 74%.
3, gasification temperature height, bed temperature can reach about 1050 ℃, and uniformity of temperature profile in the stove does not contain materials such as tar, phenols in the synthetic gas, alleviate to purify burden and pollution.
4, the circulation of synthetic gas carry-over is melted down, spray into vaporized chemical by the upper spray nozzle layer that is located at the vapourizing furnace middle part, the particulate fine coal of carrying secretly from the bed bottom is further gasified, and the volatile matter that feed coal is produced in the vapourizing furnace bottom further divide synthesis gas componentses such as being cracked into methane; Take that in addition the isolated coarse particles flying dust of tornado dust collector is returned vapourizing furnace and participate in reaction, not only improved the whole efficiency of carbon conversion of gasification, and unburned carbon in flue dust is reduced to below 20%, thereby improved coal rate of energy in the gasification.
5, the stable cycle long, turndown ratio is big, produces load and can regulate arbitrarily in the 60-105% scope.
6, easy to operate, interfering factors is few, observes intuitively, and the start-stop appearance of vehicle is easy, realizes the DCS centralized Control.
7,4 meters high 41 meters bottoms of 5 meters internal diameters of vapourizing furnace diameter are high 4 meters cone segments, and top is direct tube section, for gas reaction provides sufficient reaction compartment.
8, gasification furnace structure is simple, and maintenance capacity is little, owing to cancelled the grate of vapourizing furnace bottom, has avoided problems such as unborn furnace bottom slagging scorification, and in fact the vapourizing furnace body is exactly an empty barrel structure.Vapourizing furnace only is made up of body of heater and dismountable nozzle of inner lining refractory, there are not driving part and easily worn part, and bed temperature relative wind bed gasification furnace is much lower, wearing and tearing and erosion intensity to refractory materials reduce greatly, therefore, less demanding to refractory materials, the vapourizing furnace operation factor is higher.
9, vapourizing furnace running device few (having only three spiral coal feeders and two spiral residue extraction machines), running transfer device structure simple, and running period is long, and failure rate is low, and the maintenance of equipment amount is few, and maintenance cost is low.
10, reduced investment, the construction period is short, and can go into operation half a year.
Specific embodiments:
The present invention further specifies the present invention with the following example, but protection scope of the present invention is not limited to embodiment.
Embodiment 1
Adopt the Inner Mongol long coal (genus low grade coal) of exempting to cross a river, carry out pure oxygen gasification, produce methyl methanol syngas, raw material is gone into stove and is regulated vapourizing furnace middle part temperature, bottom temp by oxygen and water vapor proportioning and furnace coal weight in the adjusting vaporized chemical, and then control gasification bed temperature, regulate feed gas composition by nozzle layer vaporized chemical ratio about regulating.Stove middle part temperature is controlled between 970-990 ℃, 960-980 ℃ of stove temperature of lower, control nozzle up and down sprayed into oxygen proportion 1: 4, had reached more satisfactory gasification result.
Main technologic parameters:
Furnace coal weight: 25t/h
Go into stove amount of oxygen: 9500m
3/ h
Go into stove oxygen pressure: 45KPa
Oxygen concentration: 99%
Steam in the boiler amount: 7.6t/h
Stove upper temp: 900-950 ℃
Temperature: 970-990 ℃ at stove middle part
Stove temperature of lower: 960-980 ℃
Lime-ash carbon residue: 11.46%
Flying dust carbon residue: 20.4%
Synthetic gas is formed and gas production rate
| Component | CO | H 2 | CO 2 | CH 4 | N 2 | CO+H 2 |
| Form V (%) | 35.8 | 37.5 | 21.2 | 2.8 | 2.3 | 73.3 |
Synthesis gas yield: 41340Nm
3/ h
Embodiment 2
Adopt Inner Mongol wild goose brown coal, pure oxygen gasification is produced methyl methanol syngas, according to feed stock for blast furnace coal character and add-on, regulates the cooperation ratio of stove oxygen and water vapor, controls, regulates vapourizing furnace middle part temperature, and bottom temp is regulated the gasification bed temperature.By regulating nozzle layer vaporized chemical ratio up and down, finely tune the unstripped gas component.Make stove middle part temperature be controlled at 950-980 ℃, the stove temperature of lower is controlled at 940-960 ℃, and the nozzle oxygen proportion was controlled at 1: 3.5 up and down, made producer be in the ideal vaporized state.
Main technologic parameters:
Furnace coal weight: 28.8t/h
Go into stove amount of oxygen: 9460m
3/ h
Go into stove oxygen pressure: 45KPa
Oxygen concentration: 99%
Steam in the boiler amount: 7.4t/h
Stove upper temp: 900-920 ℃
Temperature: 950-980 ℃ at stove middle part
Stove temperature of lower: 940-960 ℃
Lime-ash carbon residue: 6.28%
Flying dust carbon residue: 21.06%
Synthetic gas is formed and gas production rate
| Component | CO | H 2 | CO 2 | CH 4 | N 2 | CO+H 2 |
| Form V (%) | 35.6 | 38.3 | 21.9 | 2.4 | 1.8 | 73.9 |
Synthesis gas yield: 43530Nm
3/ h.
Claims (4)
1, the method for a kind of low grade coal total oxygen gasification production methyl alcohol and dme synthetic gas comprises the following steps:
1. the pre-treatment of feed coal
Inferior raw material coal drying, fragmentation and screening are obtained the following fine coal of granularity 10mm directly send in the coal bin, for gasifier system gas raw material fine coal;
2. the conveying of raw material fine coal
Raw material fine coal in the coal bin of step in is 1. sent in the cone segments of vapourizing furnace bottom with screw-type coal distributor, and in course of conveying, the nitrogen that feeds pressure in the coal bin and be 35KPa prevents that as safe gas gas is refunded in the coal bin in the stove;
3. gasification reaction
In vapourizing furnace, with concentration is that 99% pressure is that 45KPa oxygen and pressure are the vaporized chemical that the low-pressure steam of 0.3MPa is formed, in mixing tank behind the uniform mixing, by being arranged in vapourizing furnace, on the bottom, following vaporized chemical nozzle layer sprays in the vapourizing furnace and the fine coal generating gasification reaction that is in fluidized state with the stove internal combustion, stove bottom gasification reaction temperature is 950-1000 ℃, reaction pressure is 8-11Kpa, middle part gasification reaction temperature is 1000-1050 ℃, oxygen and low-pressure steam volume ratio are 1: 0.8-0.9, fine coal and steam weight ratio are 3.4-3.8: 1, and nozzle oxygen ratio is 1 up and down: 3.0-4.5;
4. the cooling purifying and dedusting of synthetic gas
Synthetic gas by the top of gasification furnace output enters the dedusting of outlet of still cyclonic separator through last air flue, separate unreacted fine coal and return vapourizing furnace by return line, carry out the fluidized gasification reaction once more, the high temperature dust synthetic gas that leaves cyclonic separator removes waste heat boiler system recoveries heat, enter the preliminary scrubbing dust collection of empty spray tower after synthetic gas is cooled to 150-200 ℃, after entering the further scrubbing dust collection of synthesis gas washing tower again, again through the venturi scrubber qualified synthetic gas of output after the dedusting once more;
5. lime-ash is controlled deslagging in good time
According to vapourizing furnace gasifier bed layer resistance, control deslagging by the terminal Eight characters comb of cone in good time.
2, the method that methyl alcohol and dme synthetic gas are produced in gasification according to the low grade coal total oxygen of claim 1 is characterized in that: described inferior raw material coal is the brown coal of long-flame coal, sticking or weak viscosity bituminous coal or ash-rich.
3, the method for producing methyl alcohol and dme synthetic gas according to the low grade coal total oxygen gasification of claim 1, it is characterized in that: described screw-type coal distributor is three.
4, the method for producing methyl alcohol and dme synthetic gas according to the low grade coal total oxygen gasification of claim 1, it is characterized in that: described vapourizing furnace is empty barrel structure, top is direct tube section, the bottom is a cone segments, furnace lining refractory materials, two-layer dismountable nozzle are located at body of heater middle part direct tube section and bottom cone segments respectively, and the nozzle layer of cone segments is established 4-12 nozzle, be 20 °-30 ° with the body of heater conical surface, be evenly distributed on the cross section of stove cone segments; The nozzle layer of middle part direct tube section is established 16-30 nozzle, is uniformly distributed on the cross section, cylindrical shell garden perpendicular to body of heater.
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|---|---|---|---|
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|---|---|---|---|
| CNB2006100765348A CN100419049C (en) | 2006-05-09 | 2006-05-09 | Process of producing synthetic gas of carbinol and dimethyl ether by all oxygen gasifying of poor goal |
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|---|---|
| CN1834210A true CN1834210A (en) | 2006-09-20 |
| CN100419049C CN100419049C (en) | 2008-09-17 |
Family
ID=37002107
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|---|---|---|---|
| CNB2006100765348A Expired - Fee Related CN100419049C (en) | 2006-05-09 | 2006-05-09 | Process of producing synthetic gas of carbinol and dimethyl ether by all oxygen gasifying of poor goal |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101654630B (en) * | 2009-09-01 | 2012-11-14 | 水煤浆气化及煤化工国家工程研究中心 | Safe logic control method of pulverized coal gasifier |
| CN103131477A (en) * | 2013-03-07 | 2013-06-05 | 中国天辰工程有限公司 | Novel brown coal gasification process |
| CN103773507A (en) * | 2014-01-23 | 2014-05-07 | 上海锅炉厂有限公司 | Dual-bed burning and gasification poly-generation device and method |
| CN105132036A (en) * | 2015-10-14 | 2015-12-09 | 江西荣恩能源科技有限公司 | Entrained flow bed dried coal dust gasification device for normal-pressure air gasification and gasification method of entrained flow bed dried coal dust gasification device |
| CN106635178A (en) * | 2016-12-20 | 2017-05-10 | 北京神雾环境能源科技集团股份有限公司 | Fluidized bed oxygen-rich gasification method |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1121561A (en) * | 1994-10-25 | 1996-05-01 | 刘家信 | Four-stroke non-supercharger diesel engine |
| CN1057322C (en) * | 1996-12-30 | 2000-10-11 | 金群英 | Method for continuously gasifying coal (coke) and purifying synthesized gas |
-
2006
- 2006-05-09 CN CNB2006100765348A patent/CN100419049C/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101654630B (en) * | 2009-09-01 | 2012-11-14 | 水煤浆气化及煤化工国家工程研究中心 | Safe logic control method of pulverized coal gasifier |
| CN103131477A (en) * | 2013-03-07 | 2013-06-05 | 中国天辰工程有限公司 | Novel brown coal gasification process |
| CN103773507A (en) * | 2014-01-23 | 2014-05-07 | 上海锅炉厂有限公司 | Dual-bed burning and gasification poly-generation device and method |
| CN103773507B (en) * | 2014-01-23 | 2015-08-19 | 上海锅炉厂有限公司 | Double bed burning and Gasification Polygeneration System device and method |
| CN105132036A (en) * | 2015-10-14 | 2015-12-09 | 江西荣恩能源科技有限公司 | Entrained flow bed dried coal dust gasification device for normal-pressure air gasification and gasification method of entrained flow bed dried coal dust gasification device |
| CN106635178A (en) * | 2016-12-20 | 2017-05-10 | 北京神雾环境能源科技集团股份有限公司 | Fluidized bed oxygen-rich gasification method |
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| Publication number | Publication date |
|---|---|
| CN100419049C (en) | 2008-09-17 |
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