CN86105803A - Technology for production of raw-material gas for synthetic ammonia by coal gasification in two stage oven - Google Patents
Technology for production of raw-material gas for synthetic ammonia by coal gasification in two stage oven Download PDFInfo
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- CN86105803A CN86105803A CN86105803.8A CN86105803A CN86105803A CN 86105803 A CN86105803 A CN 86105803A CN 86105803 A CN86105803 A CN 86105803A CN 86105803 A CN86105803 A CN 86105803A
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Abstract
The present invention is the improvement of two sections stove circulation method coal gasifying process.For overcome existing two sections stove circulation method gasifications can not the direct production syngas for synthetic ammonia and the fixed intermittent layer gasification stove to the demanding shortcoming of solid fuel, the present invention with two sections stove gas-making processes be divided into blowing, on blow gas, blow to blow on gas, the secondary and blow off five step cycle with air and carry out down, under blow and allocate an amount of air in the gas into, and last blowing gas process carried out sub-gas operation and control epimere gas temperature out direct production syngas for synthetic ammonia, simultaneously can coproduction town gas and power gas.Tolerance ratio, component and the calorific value of three kinds of coal gas can be regulated as required.
Description
The invention belongs to the improvement of fixed bed circulation method coal gasifying process.
The fixed bed circulation method coal gasifying process that uses mainly contains two kinds of forms at present, and a kind of is to be the intermittent gasification method of representative with the U.G.I. simple stationary gas producer, and another kind is to be two sections stove cycle gasification methods of representative with I.G.I..Traditional U.G.I. producer gas generator is gas-made technology intermittently, can only use coke and hard coal to be raw material, if use non-hard coal then exist the methane content height, destructive distillation product such as tar and the emulsifying water of oil-containing phenol seriously are difficult to problems such as processing, and should not make the synthetic ammonia unstripped gas.In order to make full use of bituminous coal, sub-bituminous coal and brown coal, Italian I.G.I. company has developed two-stage gasifier before the World War II.At [" two sections stove bituminous coal gasification systems of I.G.I. ammonia " " little nitrogenous fertilizer designing technique " No.6, P.20～27(1984)] in the document, this Wella (S.Villa), Ao Hansen (O.Hansen), Pi Bidesen (B.Pedersen) has introduced Italian I.G.I. company for selecting optimal fixation bed coal-gasification and coal gas treatment process, once did comparative study, pointed out that circulation method only just can take in when coke or smokeless coal gasification.Therefore, use the two sections non-hard coal circulation method of stove gasifying process also just to be used for production city coal gas at present.[" Town gas from coal(cyclic process), Section(c) " Coal, gasi-fication seminar, People ' s Republic of China(Beijing, Shenyang, Shanghai) May 1984] in the document, this Wella (S.Villa), Ao Hansen (O.Hansen), Pi Bidesen (B.Pedersen) has introduced the technological process of two sections stove circulation methods of I.G.I. gasification system town gas, its gas-making process is by blowing, steam purge, last blowing gas, under blow and blow five step cycle on gas and the secondary steam and carry out, control with hydraulic pressure (or air pressure) automatic controls, each circulation continues 3～5 minutes.The water-gas of producing through further handling, is made the town gas that closes in requiring as increase calorific value and CO conversion etc.
If want, then need the water-gas of producing is further handled, as air separation facility is set to join technology such as nitrogen with above-mentioned explained hereafter syngas for synthetic ammonia.But this just makes the investment of production and cost improve greatly, and makes process complications, thereby is uneconomic.
In order to overcome the deficiencies in the prior art, the present invention is improved two sections stove circulation method coal gasifying process, use coal, be that non-hard coal is a raw material especially, adopt two sections stove technique for circular gasifying can the direct production syngas for synthetic ammonia, start a non-hard coal raw material of gathering materials on the spot, make full use of this area cheapness for Ammonia Production, make the technological transformation approach that the Ammonia Production cost reduces significantly, remarkable in economical benefits improves.
A kind of is two sections stove circulation methods of raw material coal gasifying process with the coal, it is characterized in that each working cycle include blowing, on blow gas, under blow and blow on gas, the secondary and air blows off five stages, under blow the gas stage and allocate air into, and carried out sub-gas operation and control epimere gas temperature out, direct production syngas for synthetic ammonia in the last blowing gas stage.
In order to use coal, be that non-hard coal is a raw material especially, adopt two sections stove circulation method gasifying process direct production syngas for synthetic ammonia, this technology is allocated an amount of air (its air tolerance is determined by the material balance of ammonia production system) into blowing the gas stage down, and added sub-gas operation in the last blowing gas stage, the semi-water gas that blowing mixed gas (being epimere gas) that the gas stage produced and following blowing gas stage are produced separates fully, and the water-gas that the last blowing gas stage is produced separates at furnace interior with destructive distillation gas with dividing, will go up the blowing purified gas (being hypomere gas) of drawing from the retort section parichnos that the gas stage produced then and mix as syngas for synthetic ammonia (being semi-water gas) at the syngas for synthetic ammonia gas holder with many nitrogen coal gas that the following blowing gas stage is produced.Because this part coal gas is that so methane content is reduced to below 1.5% in the coal gas, tar content is reduced to 0.2 gram/standard rice by the middle temperature semicoke gasification generation of gasification section
3Below.Simultaneously,,, can adopt water of condensation and tar in the indirect refrigerated separation coal gas, avoid the emulsification of oil-containing phenol water, make phenol water be easy to handle so destructive distillation tolerance is few owing in gasification, have only the coal seam of part coal gas by retort section.So the present invention has overcome above-mentioned unborn problem, having realized adopting non-hard coal is the purpose of two sections stove circulation methods of raw material gasifying process direct production syngas for synthetic ammonia.
In order to carry out sub-gas operation, be provided with two electronic (or pneumatic) variable valve of thermoswitch control at the epimere gas of two sections stoves and the exit of hypomere gas, by last blowing gas is carried out sub-gas operation, the coal gas amount in retort section coal seam is directly passed through in control, realize control epimere gas temperature out at 100～150 ℃, its optimum temperature range is different different because of coal, generally at 115～125 ℃, to guarantee the complete destructive distillation of coal, produce qualified syngas for synthetic ammonia.
In technology of the present invention, allocate the air capacity of blowing down in the steam into blowing the gas stage down, the material balance that depends on the syngas for synthetic ammonia production system, in working cycle, blow off the nitrogen amount that two stages bring in the syngas for synthetic ammonia system and will satisfy (CO+H in the syngas for synthetic ammonia by blowing gas and air down
2)/N
2=3.1～3.2 requirement.
In the two sections non-hard coal circulation method of stove gasifying process processes, coal carbonization and gasification are carried out in stove simultaneously, gasification operation normally whether, key is whether the coal carbonization degree complete.In two sections stove circulation method gasifying process, coal carbonization mainly contains two kinds of forms: a kind of is direct destructive distillation (hot destructive distillation in also claiming), and a kind of is indirect destructive distillation (also claiming outer hot destructive distillation).As coal carbonization medium (also claim heat carry source), if with the direct destructive distillation of blowing air coal seam, then the dry distillation gas of drawing from two sections stove epimeres outlets is as power gas; If more than blow the direct destructive distillation of coal gas coal seam, then the dry distillation gas of drawing from epimere gas outlet is as town gas; Coal becomes semicoke through after the destructive distillation, enters gasification section and gasifies, and the coal gas that is produced is as syngas for synthetic ammonia.The ratio of these three kinds of coal gas tolerance can be regulated on demand, promptly can the full scale production syngas for synthetic ammonia; Also can produce syngas for synthetic ammonia coproduction power gas; Or the production syngas for synthetic ammonia, coproduction town gas and power gas (also can not coproduction power gas); Or full scale production town gas.If to produce syngas for synthetic ammonia, when coproduction power gas or full scale production syngas for synthetic ammonia, then blowing air is all carried the source as the interior hot destructive distillation heat of destructive distillation coal, its technical process is as follows:
Accompanying drawing is a process flow sheet of the present invention
Wherein:
1. automatic stoker 10. scrubber towers
2. retort section 11. vertical tube water coolers
3. gasification section 12. first electro detarrers
4. turn round fire grate 13. indirect coolers
5. ash bucket 14. second electro detarrers
6. tornado dust collector A
1, A
2Temperature control valve (TCV)
7. waste heat boiler B
1The steam coal air valve
8. chimney B
2The town gas valve
9. gas washing case C synthetic ammonia feedstock air valve
Lump coal (being non-smokeless lump coal especially) 20-40 millimeter, expansion index≤2, fixed carbon content 〉=30% is intermittently added the retort section (2) on two sections stoves (cold hearth or hot wall stove) top from furnace roof by automatic stoker (1). The coal blowing-out gas that the section of being vaporized (3) is come in retort section (2) slowly heats, and coal generates dry distillation gas, pyrolysis water, tar and middle temperature semicoke in heating process. The middle temperature semicoke of pyrolysis drops to gasification section (3) approximately through 6-8 hour from retort section (2), and temperature rises to 700-800 ℃ from normal temperature, and the water content of coal is more high, and required destructive distillation (heating) time is also more long.
In the technological operation of the present invention, each circulation divides blowing, upper blowing gas, lower blowing gas, secondary blowing up and air to blow off five stages, the time duration of each circulation 2.5～4 minutes.
(1) the blowing stage: the air from air blast enters in the gasification section (3) from furnace bottom, carries out Combustion reaction improves furnace temperature. Blowing-out gas is left the rear about 800 ℃ of coal seams that enter retort section (2) of gasification section (3), carries out coal carbonization. Dry distillation gas, pyrolysis water and tar steam export through valve A from epimere gas with blowing-out gas1Draw, calorific value is about 600 kilocalories/standard meter3, about 120 ℃ of temperature, through vertical tube cooler (11), the saturated cooling of weak aqua ammonia with tower cleans in carbonization workshop section is beneficial to the operation of electro detarrer. Go out about 80～100 ℃ of vertical tube cooler (11) gas temperature, enter first electro detarrer (12), heavy tar is removed lower, advance then indirect cooler (13), gas temperature is down to about 60 ℃, and most of pyrolysis water condensation enters cesspool, and gas enters second electro detarrer (14) moisture content in tar light oil and the small part coal gas is removed, the coal gas that goes out second electro detarrer (14) can be used as gas for motor fuel, through valve B1Remove the gas for motor fuel gas holder.
(2) the upper blowing gas stage: steam enters gasification layer from two sections furnace bottoms, carries out the steam decomposition reaction and generates CO, H2、CO
2Deng gas, leave gasification section (3), coal gas enters the airway of retort section (2), carries out the outer hot destructive distillation of coal, the valve A in the outlet of hypomere gas2Draw, about 600 ℃ of temperature after cyclone dust collectors (6) dedusting, at waste heat boiler (7) gas recovery sensible heat, produces 3 kilograms per centimeter2Low-pressure steam, go out waste heat boiler (7) after, about 180 ℃ of gas temperature, through gas washing case (9), aeration tower (10) further dedusting be cooled to about 40 ℃ and remove the syngas for synthetic ammonia gas holder through valve C. During outside hot destructive distillation of coal, the dry distillation gas of decomposition, pyrolysis water and tar steam export through valve A from two sections stove epimere gas1Draw, cool off, purify through valve B through vertical tube cooler (11), first electro detarrer (12), indirect cooler (13), second electro detarrer (14)4Remove the gas for motor fuel gas holder, the gas liquor of condensation enters cesspool, and tar enters the tar storage tank. In order to control the calorific value of gas for motor fuel, satisfy the requirement of internal combustion engine (generally at 1200 kilocalories/standard meter3About), blowing up coal gas can be told a part and carry out direct destructive distillation, remove the power gas holder with dry distillation gas.
(3) the lower blowing gas stage: steam enters gasification section (3) with an amount of air of allocating into (its tolerance is determined by the material balance of ammonia production system) from the airway of retort section (2), steam, air and red-hot carbon-coating burn and the steam decomposition reaction, generate CO, H2、N
2、
CO
2Etc. many nitrogen coal gas, to draw from furnace bottom, about 200 ℃ of temperature is removed the syngas for synthetic ammonia gas holder after gas washing case (9), aeration tower (10) dedusting cooling.
(4) the secondary blowing up stage: behind the depressed bundle of lower blowing, need the blowing down coal gas emptying with the furnace bottom space, for air blows off ready. Carry out the indirect steam blowing up, the same blowing gas of coal gas flow process.
(5) air blows off the stage: this part blowing air is reclaimed, and as one of the source of nitrogen in the syngas for synthetic ammonia, coal gas flows to also the same blowing gas.
Blowing, on blowing gas in the stage, the thermal equilibrium of retort section is depended in the distribution of epimere gas and hypomere gas two tunnel tolerance, big more by the tolerance of retort section, then epimere gas temperature out is high more.When epimere gas temperature out is lower than this technology because of the different optimum control temperature of coal, when for example being lower than 120 ℃, the coal carbonization shortage of heat, the thermoswitch auto-action leaves big epimere gas outlet regulating valve A
1, turn down hypomere gas outlet regulating valve A
2, strengthen direct pyrogenous coal gas tolerance, to improve destructive distillation layer temperature; When epimere gas temperature out is higher than the specified controlled temperature of this technology, when for example being higher than 120 ℃, the thermoswitch action turns down epimere gas outlet regulating valve A
1, open big hypomere gas outlet regulating valve A
2In the blowing stage, if epimere temperature degree is higher than this technology according to coal and different controlled temperature, for example 150 ℃, the then programme-controlled chimney valve of opening is automatically directly drawn a part of blowing air through chimney emptying through the parichnos and the outlet of hypomere gas of retort section (2).Can reach the operation of coal carbonization optimizing with this control mode.
If the present invention's full scale production syngas for synthetic ammonia, then operate the same, but its power gas part emptying.
The present invention also can be when producing syngas for synthetic ammonia coproduction town gas and power gas, promptly when more than blow coal gas as the interior hot destructive distillation thermal source of coal during with the complete destructive distillation of coal, the coal gas that goes out retort section is as town gas.It with compare with the technology of producing syngas for synthetic ammonia coproduction power gas, difference only is:
(1) the blowing stage: based on the technology of production of raw-material gas for synthetic ammonia, blowing air all by the coal seam of retort section (2), come out of the stove after cool off, purify and remove the power gas gas holder by blowing air; And when the coproduction town gas, blowing air through gasification layer back major part from the parichnos of retort section (2) through tornado dust collector (6), waste heat boiler (7), then through chimney (8) emptying, only there is a small amount of blowing air to draw from the outlet of epimere gas as interior hot destructive distillation thermal source, after cooling, purification, removes the power gas gas holder by the coal seam of retort section (2).The temperature that how much also depends on the outlet of epimere gas of this part blowing air tolerance.
In the blowing stage, if the gas in upper segment temperature is lower than this technology because of the different controlled temperature of coal, for example be lower than 100 ℃, the then programme-controlled chimney valve of closing automatically, blowing air directly enters the destructive distillation coal seam, improves the temperature of destructive distillation layer.
(2) go up the blowing gas stage: when producing syngas for synthetic ammonia coproduction power gas, water-gas goes out most of parichnos and the outlet of hypomere gas through retort section (2) of gasification layer and remove the syngas for synthetic ammonia gas holder behind dedusting, recovery sensible heat, the coal seam (temperature that how much also depend on gas in upper segment outlet of this part coal gas tolerance) of a small amount of coal gas by retort section (2) only arranged, mix with destructive distillation gas, draw from the outlet of epimere gas, after cooling off, removing tar, remove the power gas gas holder; And when the coproduction town gas since on to blow coal gas be to carry the source as hot destructive distillation heat in coal main, so bigger by the coal gas amount in retort section coal seam, destructive distillation gas is drawn through cooling, purification after valve B through the outlet of epimere gas
2Remove the town gas gas holder.
If the calorific value to the power gas of coproduction on the technology is had relatively high expectations, control section town gas (being epimere gas) enters the power gas gas holder on demand.
When production syngas for synthetic ammonia coproduction town gas, during not coproduction power gas, then power gas part emptying.
When the full scale production town gas, do not allocate air with different only being down of full scale production syngas for synthetic ammonia technical process in the blowing gas, air blows off the employing steam purge simultaneously.
More than various gas-made technologies, can select as required.In every kind of gas-made technology, tolerance ratio, component and the calorific value of three kinds of coal gas can be regulated by respectively making the methods such as time distribution in gas stage in sub-gas operation and the adjusting working cycle on demand, uses programme-controlled (or robot calculator) Control Circulation process.The town gas of this explained hereafter, wherein CO content is about 30%, and calorific value is at 3000～3200 kilocalories/standard rice
3About.If require lower CO content, can reach requirement by means such as CO conversion or CO methanations.The calorific value higher as needs also can be situated between certainly by the way of the gain of heat.
The various coal gas that produced in the technology of the present invention can use the automatic sampling analysis of chromatographic instrument, also can use other method to analyze.
Because the present invention can use various low grade coals, as meager coal, bottle coal, long bituminous coal and brown coal direct production syngas for synthetic ammonia, power gas and town gas, this technological operation simultaneously is simple, is easy to grasp, so have wide range of applications, can be used for synthesis ammonia plant and prepare syngas for synthetic ammonia; Or during attached product power gas generates electricity or produces in the preparation syngas for synthetic ammonia, low-pressure steam, for our factory and society provide the power needs; Also can be when producing syngas for synthetic ammonia coproduction town gas and power gas (or not coproduction power gas); Or only production city coal gas in, the civilian of small city need etc.
Technology of the present invention has overcome existing immovable bed technique for circular gasifying direct production syngas for synthetic ammonia to the demanding shortcoming of feed coal, Ammonia Production can be gathered materials on the spot, the non-hard coals such as meager coal, bottle coal, long bituminous coal and brown coal that comprehensive utilization is cheap, cost can will hang down 80-100 unit/ton ammonia, thereby economic benefit of enterprises can significantly improve.
Because the present invention can the coproduction town gas, so it is again an approach of building an economical rationality of town gas gas supply station.For the little synthesis ammonia plant of producing 1.5 ten thousand tons per year, the town gas of coproduction can be for the civilian needs of 140,000 populations, and its investment and working cost are low more about 50% than building gas station separately, the coal gas cost＜0.1 yuan/standard rice that dispatches from the factory
3, the calorific value of coal gas is at 3000-3200 kilocalorie/standard rice
3
But because of the present invention's coproduction power gas also,, the Lowlevel thermal energy of synthesis ammonia system is made full use of again, reduce the externally dependence of power supply of synthesis ammonia system, help self balance of steam if adopt reliable internal combustion turbine and waste heat boiler to combine.
In addition, existing little ammonia plant retrofit is a gas-made technology of the present invention, and except that town gas and power gas partly need new going up the device, Ammonia Production partly changes also smaller, implements the solution of the present invention transformation and carries out easily.
Embodiment 1
Two sections stove circulation method gasifications are produced syngas for synthetic ammonia coproduction power gas technology
Furnace structure: two sections stoves of cold wall type, 2260 millimeters of stove footpath φ, 12000 millimeters of height overalls, wherein retort section is high 6100 millimeters
Coal and granularity: coal in the first day of the lunar month (bituminous coal), 20-40 millimeter
Gas in upper segment temperature control: 120 ℃
Working cycle perdurability: 3 minutes
The working cycle time distributes: blowing: 25%
Last blowing gas: 30%
Under blow gas: 35%
Blow on the secondary: 6%
Air blows off: 4%
Use the programme-controlled Control Circulation process of hydraulic pressure, each stage respectively has the control situation of closing valve to see Table 1-1 in the working cycle
Various coal gas of this explained hereafter and component thereof, calorific value and tolerance ratio see Table 1-2
Table 1-1
Blow down on the secondary in the blowing and blow off parking
The blowing threshold switch closes switch
The steam main valve closes opens the switch pass
Last steam blowing valve closes the switch switch and closes
Following steam blowing valve closes switch and closes
Under blow pressure lock and close to close switch and close
The town gas valve closes Guan Guanguan
Steam coal air valve switch switch
The hypomere gas valve closes the switch switch
Under blow gas valve and close to close switch and close
The chimney valve closes Guan Guanguan to be opened
Table 1-2
Syngas for synthetic ammonia (%) power gas (%)
H
240.80 2.00
CO 27.20 8.00
CO
28.90 17.00
N
221.60 70.00
CH
41.10 2.00
CnHm 1.00
H
2S trace (about 1.5 gram/standard rices
3)
O
20.40
Calorific value (kilocalorie/standard rice
3) 546
Tolerance is than (standard rice
3/ time platform) 2,800 2200
Two sections stove circulation method gasifications are produced syngas for synthetic ammonia coproduction town gas technology
Furnace structure: two sections stoves of cold wall type, 2260 millimeters of stove footpath φ, 12000 millimeters of height overalls, wherein retort section is 6100 millimeters
Coal and granularity: coal in the first day of the lunar month (bituminous coal), 20～40 millimeters
Gas in upper segment temperature control: 120 ℃
Working cycle perdurability: 3.5 minutes
The working cycle time distributes: blowing: 22%
Last blowing gas: 30%
Under blow gas: 38%
Blow on the secondary: 6%
Air blows off: 4%
Use robot calculator Control Circulation process, each stage respectively has the control situation of closing valve to see Table 2-1 in the working cycle
Various coal gas of this explained hereafter and component thereof, calorific value and tolerance ratio see Table 2-2, power gas part emptying wherein.
Table 2-1
Blow down on the secondary in the blowing and blow off parking
The blowing threshold switch closes switch
The steam main valve closes opens the switch pass
Last steam blowing valve closes the switch switch and closes
Following steam blowing valve closes switch and closes
Under blow pressure lock and close to close switch and close
The town gas valve closes the switch switch
The power gas threshold switch closes Guan Guanguan
The hypomere gas valve closes the switch switch
Under blow gas valve and close to close switch and close
The chimney threshold switch closes Guan Guankai
Table 2-2
Syngas for synthetic ammonia (%) town gas (%) power gas (%)
H
240.80 49.62 2.00
CO 27.20 34.13 8.00
CO
28.90 8.68 17.00
N
221.60 72.00
CH
41.10 6.45 1.00
C
2H
60.61
C
3H
80.49
CnHm
H
2S trace (about 1.5 gram/standard rices
3) 0.30(gram/standard rice
3)
O
20.40
Calorific value (kilocalorie/standard rice
3) 3,057 320
Tolerance is than (standard rice
3/ time platform) 1,650 880 2000
Claims (4)
1, a kind of is two sections stove circulation methods of raw material coal gasifying process with the coal, it is characterized in that each working cycle include blowing, on blow gas, blow and blow on gas, the secondary and air blows off five stages down, under blow the gas stage and allocate air into, and carried out sub-gas operation and control epimere gas temperature out, direct production syngas for synthetic ammonia in the last blowing gas stage.
2, by the described technology of claim 1, it is characterized in that in its sub-gas operation be two variable valve that are arranged on by adjusting in two sections stove epimere gas and the outlet of hypomere gas, and control epimere gas temperature out is to carry out under 100-150 ℃, and optimum temperature range is 115-125 ℃.
3, by the described technology of claim 1, the air tolerance that the blowing gas stage is allocated under it is characterized in that is to determine according to the material balance of syngas for synthetic ammonia production system.
4, by claim 1,2,3 described technologies, it is characterized in that coproduction town gas and power gas simultaneously, tolerance ratio, component and the calorific value of three kinds of coal gas can be regulated as required.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 86105803 CN1006896B (en) | 1986-07-24 | 1986-07-24 | Technology for production of raw-material gas for synthetic ammonia by coal gasification in two stage oven |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 86105803 CN1006896B (en) | 1986-07-24 | 1986-07-24 | Technology for production of raw-material gas for synthetic ammonia by coal gasification in two stage oven |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN86105803A true CN86105803A (en) | 1988-06-01 |
| CN1006896B CN1006896B (en) | 1990-02-21 |
Family
ID=4802972
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 86105803 Expired CN1006896B (en) | 1986-07-24 | 1986-07-24 | Technology for production of raw-material gas for synthetic ammonia by coal gasification in two stage oven |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1006896B (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101825222A (en) * | 2009-03-03 | 2010-09-08 | 新奥科技发展有限公司 | Coal gasification gas provision method and system |
| CN102399592A (en) * | 2011-10-08 | 2012-04-04 | 湖北双环科技股份有限公司 | Segmenting and partitioning coal gasification process of fixed bed |
| CN103710050A (en) * | 2014-01-09 | 2014-04-09 | 杨皓 | Improved fixed bed coal gas-making furnace for producing gas |
| CN104232165A (en) * | 2014-09-26 | 2014-12-24 | 贵州开磷（集团）有限责任公司 | Gas making technology adopting 1.5-2.0cm small-grain coal |
| CN105647590A (en) * | 2015-12-04 | 2016-06-08 | 孔令增 | Method for synthesizing ammonia and urea by continuous pure oxygen gasification and power generation cogeneration in two-stage gas furnace |
-
1986
- 1986-07-24 CN CN 86105803 patent/CN1006896B/en not_active Expired
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101825222A (en) * | 2009-03-03 | 2010-09-08 | 新奥科技发展有限公司 | Coal gasification gas provision method and system |
| CN102399592A (en) * | 2011-10-08 | 2012-04-04 | 湖北双环科技股份有限公司 | Segmenting and partitioning coal gasification process of fixed bed |
| CN103710050A (en) * | 2014-01-09 | 2014-04-09 | 杨皓 | Improved fixed bed coal gas-making furnace for producing gas |
| CN104232165A (en) * | 2014-09-26 | 2014-12-24 | 贵州开磷（集团）有限责任公司 | Gas making technology adopting 1.5-2.0cm small-grain coal |
| CN105647590A (en) * | 2015-12-04 | 2016-06-08 | 孔令增 | Method for synthesizing ammonia and urea by continuous pure oxygen gasification and power generation cogeneration in two-stage gas furnace |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1006896B (en) | 1990-02-21 |
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