CN104046392A - Pre-combustion method used for coal gasifier - Google Patents
Pre-combustion method used for coal gasifier Download PDFInfo
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- CN104046392A CN104046392A CN201310139151.0A CN201310139151A CN104046392A CN 104046392 A CN104046392 A CN 104046392A CN 201310139151 A CN201310139151 A CN 201310139151A CN 104046392 A CN104046392 A CN 104046392A
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- gas
- gasifier
- combustion chamber
- burner
- pyrolysis
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Abstract
A vaporization method uses pyrolysis and/or purging airflow generated by a coal gasifier as a raw material of a combustor and a combustion chamber. The above pyrolysis and/or purging gas is combusted in the combustor and the combustion chamber together with oxygen-containing airflow when flow coal dust and/or crushed coke exist(s), so the obtained hot fuel gas is supplied to the gasifier, and provides heat and reaction components in the gasifier to help coal gasification. The gasifier generates the pyrolysis and purging gas, and the gas can be recovered and is supplied to the combustor and the combustion chamber.
Description
Technical field
The present invention relates to a kind of pre-burning method for coal gasifier.
Background technology
It is quite extensive that intermittent coal gas device that can gasifying smokeless coal is applied in small chemical industry.Especially in China, thousands of intermittent coal gas devices are used to the industry of coal conversion ammonification.But because its efficiency is low, output is low and discharge a large amount of pollutents, traditional batch formula gasifier has started to lose its advantage as raw material producer in chemical industry.And the coal gasifier thermo-efficiency of these patterns is low, this just makes its working cost more expensive.
Intermittently coal gasifier also can be used to synthetic gas or the gas mixture of production application in liquid fuel, hydrogen, geseous fuel and metallurgical operations.
These lower efficiency have caused higher running cost and lower efficiency of carbon conversion.This just causes in the material mixed gas producing by conversion process the gas concentration of required hydrogen and carbon monoxide low.These lower efficiency mean that a large amount of pollutents with higher carbon discharge are by discharged to atmosphere.
In gasification, in gasifier, coal bed contacts in succession with air and water vapor.At oxidation stage, coal bed temperature raises and produces the gaseous mixture including carbonic acid gas, carbon monoxide, water vapor, hydrogen, methane and other hydrocarbon polymers, and this gaseous mixture is called as sweeping gas.After this, to injection water steam in gasifier and generate the material synthesis gas that mainly comprises carbon monoxide and hydrogen.
The gas that required final product is still produced for representative with gas mixture also can further react to generate the hydrogen of additional quantity.By making synthetic gas carry out fischer-tropsch reaction to carry out the production of other alkane.Or, coal gas is carried out to the transformationreation of water-gas to produce more hydrogen.
The present invention provides some to improve to these poor efficiency parts, and to be coal dust by making sweeping gas and being attached with Powdered bottom coke realized with the fuel gas that produces steam and spray high temperature in oxidation stage forward direction gasifier to oxygenated fuel burner/combustion chamber recirculation by gasifier in this improvement.The fuel gas of combustion chamber is used for the dehumidifying of coal bed and removes volatilization.Thus by make coal dust recirculation and again burning improve efficiency of carbon conversion and reduce discharged to the powder particle of atmosphere.Further can make gas ingredients carbon monoxide and hydrogen increase required and useful in material mixed gas.
Summary of the invention
In first embodiment of the present invention, disclose a kind of gasification process comprising the following steps:
A) feed to burner the pyrolysis gas that contains the coal dust bottom coke of the pulverizing of gasifier (and/or from);
B) in burner, feed oxygen-containing gas and low heating value fuel gas;
C) from combustion chamber to gasifier, feed hot fuel gas to produce pyrolysis gas; And
D) reclaim pyrolysis gas.
This gasification process is the gasification of coal but also can be applicable to use other gasifications of other reaction materials.The preferred batch operation of this gasification process, wherein pyrolysis gas burned and by feed gasifier, so gasifier will carry out the production of synthetic gas.But this whole process should be carried out continuously, the pyrolysis gas reclaiming from gasifier in the time that gasifier produces synthetic gas is by this fed burner and combustion chamber assembly.
The pyrolysis gas that reclaims and fed burner and combustion chamber assembly from gasifier is typically made up of hydrogen, carbon monoxide, carbonic acid gas, nitrogen, methane and other hydrocarbon polymers.
Combustion chamber is communicated with burner and gasification unit fluid.
Oxygen-containing gas is selected from the combination that comprises oxygen or oxygen-rich air.
Term " low calorie fuels " refers to the relatively low fuel of flammable content, for example hydrogen, carbon monoxide, methane or other hydrocarbon polymers.
By being installed around combustion chamber, moisture film wall can produce water vapor.
Flow out the hot fuel gas temperature of combustion chamber between 800-900 DEG C and typically contain flying dust, this flying dust is entering before gasification installation by prior device from wherein removing.This hot fuel gas flows out combustion chamber and with 10000-20000Nm
3the speed of/h is fed gasifier.Typicalness, this hot fuel gas is fed the top of gasifier.
Gasifier is produced and is mainly comprised the pyrolysis gas of hydrogen, carbon monoxide, carbonic acid gas, nitrogen and methane and the synthetic gas as its plan product.Synthetic gas is recovered and is fed storage or other unit operations so as to application hydrogen and carbon monoxide.Pyrolysis gas is exhaust flow substantially, that this exhaust flow reclaims in the methods of the invention and feed burner so as to burning and by burning fuel gas feed gasification unit.Pyrolysis gas is the gas producing in the time that the high-temperature fuel gas producing from combustion chamber reacts with coal bed in the high temperature pyrolysis stage of gasifier.Hot fuel gas is typically made up of carbonic acid gas, nitrogen and flying dust.
Except the synthetic gas of the gasification the finished product that obtain as hope and pyrolysis gas, also can produce sweeping gas.This sweeping gas produces from gasifier purge stages, in the air combustion of purge stages coal bed and gasifier inside with raising coal bed temperature.The present invention is intended to, and this sweeping gas can form a part for the pyrolysis gas that feeds burner and also can from gasifier, be recovered thus.
Like this, whole gasification can be regarded as three steps.The first step is pyrolysis, and the fuel gas that wherein comes from combustion chamber reacts with coal bed and Heat of Formation is vented one's spleen.Second step is to purge, and wherein air reacts with coal bed and generates sweeping gas.The 3rd step is gasification, and wherein steam reacts with coal bed and produces synthetic gas.
Method of the present invention can be applied to the intermittent type gasifier of the multiple fixed bed of processing hard coal or coal briquette.These coals are typically present in gasifier with the form (size: 25-75mm) of large aggregate or piece.
In gasifier operation, bottom coke is collected, pulverizes and along with gasifier pyrolysis gas and/or sweeping gas are transported to burner, provides thus the fuel of combustion chamber.The coke of this kind of pulverizing stems from bottom coke and in particle size, is conventionally greater than coal dust and in the magnitude of about ten millimeters.Be pointed out that, bottom coke is pulverized before entering burner with coal dust.Therefore in practice of the present invention, the coke of pulverizing can be used as the additional of coal dust and feeds burner.The hot fuel gas being produced by combustion chamber contacts with the coal bed in gasifier after entering gasifier.Dehumidified and except volatilization coal can react generation pyrolysis gas, then carry out traditional intermittent type fixed bed gasifiers operational process, comprise oxidation stage (generation sweeping gas) and gasifying stage (generation syngas mixture).Synthetic gas can be stored or directly deliver in the chemical operation that needs hydrogen and/or carbon monoxide, and pyrolysis gas/sweeping gas can directly feed in burner and combustion chamber assembly.
Brief description of the drawings
Accompanying drawing is the schematic diagram of the attached intermittent coal gas device that has precombustion assembly.
Embodiment
The invention provides the use of the precombustion chamber of the intermittent coal gas device upstream that is arranged on fixed bed.
Referring to accompanying drawing, accompanying drawing has been described the intermittent type gasifier unit A of the fixed bed being made up of reactor, and its medium-sized coal coal bed is positioned at the distribution of fire grate D top to allow bottom to enter gas or steam.The temperature of the fuel gas outlet of combustion chamber C is typically about 800-900 DEG C.Oxygen-containing gas feeds burner B by circuit 1.Burner B is set to come from by circuit 2 acceptance the discharge air-flow of gasifier A.Pyrolysis gas and sweeping gas that this air-flow is hydrogen, carbon monoxide, carbonic acid gas, nitrogen and methane by major ingredient form.This pyrolysis and gaseous purge stream also can comprise and come from the coal dust of gasification unit A or the coke of pulverizing.Fuel, oxygen-containing gas and pyrolysis gas mixture feed combustion chamber C from burner.Water vapor produces from being arranged on combustion chamber C moisture film wall around.
The mixture reaction that feeds combustion chamber C forms the fuel gas stream that chief component is carbonic acid gas, nitrogen, flying dust and some water vapors.This kind of fuel gas temperature that is about to flow out combustion chamber C is at 800-900 DEG C.This fuel gas stream feeds gasifier A by circuit 3.
The fuel gas stream that comes from combustion chamber C will enter gasifier A and provide heat for occurring in the dehumidifying in gasifier A and removing volatilization process by circuit 3.In the C of combustion chamber, the coke of oxygen and pyrolysis/sweeping gas and pulverizing (and/or coal dust) reacts.The relative percentage composition of all compositions of reactant is the oxygen of 10-15% hydrogen, 15-20% carbon monoxide, 3-8% carbonic acid gas, 35-40% nitrogen, 3-8% methane and 25-30%, with 300-500 kg/hr (Kg/hour), the gasifier bottom coke that contains about 20% weight percent carbon.These reactants are conventionally with 10000-20000Nm
3the speed of/h feeds.
From gasifier A, dehumidify and remove the pyrolysis gas producing in volatilization process and collect and be recycled to burner B by circuit 2.After this, the operation of gasifier proceeds to traditional mode to generate sweeping gas (coming from oxidising process) and synthetic gas (coming from gasification).Sweeping gas leaves gasifier A by circuit 2, returns to burner B.Synthetic gas is admitted to downstream unit by circuit 6.
When the present invention describes with reference to relevant exemplary embodiments, obviously the present invention has other forms and the amendment that much it will be apparent to those skilled in the art.The appended claim of the present invention is constructed to cover all this obvious form and modification in the application's true spirit and scope conventionally.
Claims (17)
1. a gasification process, comprises the following steps:
A) feed the pyrolysis gas that contains coal dust from gasifier to burner;
B) in described burner, feed oxygen-containing gas and low heating value fuel gas;
C) from combustion chamber to described gasifier, feed hot fuel gas to produce pyrolysis gas; And
D) reclaim described pyrolysis gas.
2. method according to claim 1, is characterized in that, described gasification process is carried out in batches.
3. method according to claim 1, is characterized in that, the gasification that described gasification process is coal.
4. method according to claim 1, is characterized in that, described pyrolysis gas comprises hydrogen, carbon monoxide, carbonic acid gas, nitrogen, methane and other hydrocarbon polymers.
5. method according to claim 1, is characterized in that, described combustion chamber is communicated with described gasifier fluid.
6. method according to claim 1, is characterized in that, described oxygen-containing gas is selected from the combination that comprises oxygen and oxygen-rich air.
7. method according to claim 1, is characterized in that, produces water vapor by being arranged on described combustion chamber moisture film wall around.
8. method according to claim 1, is characterized in that, the temperature of leaving the hot fuel gas of described combustion chamber is 800-900 DEG C.
9. method according to claim 1, is characterized in that, the pyrolysis gas of step in c) is fed to described burner.
10. method according to claim 1, is characterized in that, the fuel gas of described heat is with 10000-20000Nm
3the speed of/h feeds described gasifier from described combustion chamber.
11. methods according to claim 1, is characterized in that, the fuel gas of described heat is fed to the top of described gasifier.
12. methods according to claim 1, is characterized in that, the hot fuel gas of step in c) comprises carbonic acid gas, nitrogen, flying dust and water vapor.
13. methods according to claim 1, is characterized in that, described burner and described combustion chamber fluid are communicated with.
14. methods according to claim 1, is characterized in that, also comprise the step that feeds the coke of pulverizing from described gasifier to described burner.
15. methods according to claim 1, is characterized in that, described low calorie fuels is selected from comprise the combination of hydrogen, carbon monoxide and methane.
16. methods according to claim 1, is characterized in that, also comprise the step that reclaims sweeping gas from described gasifier.
17. methods according to claim 1, is characterized in that, also comprise the step that reclaims synthetic gas from described gasifier.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310139151.0A CN104046392A (en) | 2013-03-15 | 2013-03-15 | Pre-combustion method used for coal gasifier |
| GB201311221A GB201311221D0 (en) | 2013-03-15 | 2013-06-25 | Pre-combustion method for use in coal gasifiers |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310139151.0A CN104046392A (en) | 2013-03-15 | 2013-03-15 | Pre-combustion method used for coal gasifier |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN104046392A true CN104046392A (en) | 2014-09-17 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201310139151.0A Pending CN104046392A (en) | 2013-03-15 | 2013-03-15 | Pre-combustion method used for coal gasifier |
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| CN (1) | CN104046392A (en) |
| GB (1) | GB201311221D0 (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3951615A (en) * | 1973-05-18 | 1976-04-20 | Dr. C. Otto & Comp. G.M.B.H. | Cylindrical pressure reactor for producing a combustible gas |
| CN1074699A (en) * | 1992-01-23 | 1993-07-28 | 浙江大学 | Circulation fluidized-bed gas-steam combine producing process and device |
| CN1515654A (en) * | 1997-12-18 | 2004-07-28 | 株式会社荏原制作所 | Fuel gasification system |
| CN1754945A (en) * | 2004-09-30 | 2006-04-05 | 中国科学院工程热物理研究所 | Double-circulating fluid bed coal gas-steam combined production method and device |
-
2013
- 2013-03-15 CN CN201310139151.0A patent/CN104046392A/en active Pending
- 2013-06-25 GB GB201311221A patent/GB201311221D0/en not_active Ceased
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3951615A (en) * | 1973-05-18 | 1976-04-20 | Dr. C. Otto & Comp. G.M.B.H. | Cylindrical pressure reactor for producing a combustible gas |
| CN1074699A (en) * | 1992-01-23 | 1993-07-28 | 浙江大学 | Circulation fluidized-bed gas-steam combine producing process and device |
| CN1515654A (en) * | 1997-12-18 | 2004-07-28 | 株式会社荏原制作所 | Fuel gasification system |
| CN1754945A (en) * | 2004-09-30 | 2006-04-05 | 中国科学院工程热物理研究所 | Double-circulating fluid bed coal gas-steam combined production method and device |
Also Published As
| Publication number | Publication date |
|---|---|
| GB201311221D0 (en) | 2013-08-14 |
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Address after: Munich, Germany Applicant after: Linde AG Address before: Munich, Germany Applicant before: Linde AG |
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Application publication date: 20140917 |