CN102492476A - Coal gas production method - Google Patents
Coal gas production method Download PDFInfo
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- CN102492476A CN102492476A CN2011104125924A CN201110412592A CN102492476A CN 102492476 A CN102492476 A CN 102492476A CN 2011104125924 A CN2011104125924 A CN 2011104125924A CN 201110412592 A CN201110412592 A CN 201110412592A CN 102492476 A CN102492476 A CN 102492476A
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- production method
- coal gas
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- 239000003034 coal gas Substances 0.000 title claims abstract description 31
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 25
- 239000000571 coke Substances 0.000 claims abstract description 24
- 239000002994 raw material Substances 0.000 claims abstract description 21
- 238000002309 gasification Methods 0.000 claims abstract description 13
- 239000000463 material Substances 0.000 claims abstract description 12
- 238000001816 cooling Methods 0.000 claims abstract description 11
- 239000013543 active substance Substances 0.000 claims abstract description 4
- 239000007789 gas Substances 0.000 claims description 39
- 238000006243 chemical reaction Methods 0.000 claims description 21
- 239000003795 chemical substances by application Substances 0.000 claims description 21
- 230000001737 promoting effect Effects 0.000 claims description 21
- 239000010881 fly ash Substances 0.000 claims description 14
- 238000000034 method Methods 0.000 claims description 12
- 238000001035 drying Methods 0.000 claims description 9
- 229910052760 oxygen Inorganic materials 0.000 claims description 9
- 239000000428 dust Substances 0.000 claims description 8
- 230000008569 process Effects 0.000 claims description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- 238000003801 milling Methods 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
- 238000000746 purification Methods 0.000 claims description 2
- 238000000227 grinding Methods 0.000 abstract description 4
- 238000002156 mixing Methods 0.000 abstract description 4
- 238000003756 stirring Methods 0.000 abstract description 3
- 230000015572 biosynthetic process Effects 0.000 abstract 1
- 238000003786 synthesis reaction Methods 0.000 abstract 1
- 230000008901 benefit Effects 0.000 description 7
- 239000003245 coal Substances 0.000 description 7
- 239000000203 mixture Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000010419 fine particle Substances 0.000 description 3
- 230000009466 transformation Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- 230000004044 response Effects 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 208000012826 adjustment disease Diseases 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- 239000002802 bituminous coal Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
- 230000000007 visual effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Abstract
The invention provides a coal gas production method, which comprises the following steps: grinding, stirring and mixing coke raw materials and a basic oxide active agent completely; conveying the materials evenly grinded and mixed to a storage bunker to be dried and preheated; conveying processed materials to a gasification furnace through conveying gas to be gasified; conveying the gasified gas to a cooling device to be cooled; conveying the cooled gas to a dedusting device to be dedusted; and conveying the dedusted gas to a purifying device to be purified. The coal gas production method can reduce production cost of synthesis gas or coal gas, recycles heat and active agents and the like, and is suitable for scale production of the coal gas.
Description
Technical field
The present invention relates to a kind of coal gas production method.
Background technology
Along with the minimizing day by day of traditional fossil energy (coal, oil, Sweet natural gas) reserves, and because the problem of environmental pollution that uses fossil energy to bring, the human existence development receives very big influence.Attention efficiently utilizes the reasonable utilization of the existing energy, but development utilization, and tap/dip deep into has the chemical industry of value energy, improves the efficiency of conversion of the energy, reduces the pollution waste, has become next step developing goal.
Industrial production coal gas forms as material gasification with bituminous coal, hard coal mostly, but hard coal is underproduce, and price goes up year by year, and economic benefit is greatly affected.And coke is compared with coal under the same conditions, and reactive behavior is lower.If directly adopt coke producing coal in next life gas, its transformation efficiency is lower, has directly influenced economic benefit.But its cheap price advantage becomes another outlet that improves the industrial production economic benefit.
Show Fe after deliberation
2O
3, CaO, MgO, K
2O, Na
2Basic oxide such as O, the gasification reaction of STRENGTH ON COKE has positive catalysis, in coke, adds basic oxide as promoting agent, the reactive behavior in the time of can significantly improving coke gasification.
Therefore, a kind of method of producing coal gas efficiently, cheaply need be developed in this area.
Summary of the invention
The objective of the invention is to provide a method of passing through to improve active scale prodn synthetic gas of coke gasification reaction or coal gas efficiently, cheaply.
In order to realize the object of the invention, adopt following technical scheme:
A kind of coal gas production method comprises the steps:
1) raw material and basic oxide promoting agent are fully ground, stirs, mix;
2) the uniform material of ground and mixed is delivered to warehouse drying, preheating;
3) utilize the mass transport of carrying gas that warehouse is processed to arrive the vapourizing furnace gasification;
4) gas after will gasifying is sent into the water cooler cooling;
5) cooled gas is sent into the fly-ash separator dedusting;
6) gas after the dedusting is sent into purification utensil.
Wherein, preferably, the heat that process of cooling absorbed is used for the material in the warehouse is carried out drying preheating.
The temperature of reaction of above-mentioned vapourizing furnace is 1100 ℃～1400 ℃, and working pressure is between 0.8～1.67MPa.
Above-mentioned basic oxide are Fe
2O
3, CaO, MgO, K
2O or Na
2O.Said raw material and basic oxide promoting agent are milled to granularity and are the 100-300 order, and be preferable, and it is the 120-150 order that said raw material and basic oxide promoting agent are milled to granularity.
Wherein, preferably, the isolated gas of fly-ash separator, part raw gas are sent back to as recycle stock and are continued to participate in reaction in the vapourizing furnace, with control gasifier temperature and pressure.
Wherein, preferably, above-mentioned conveying gas is oxygen and superheated vapour.
Wherein, preferably above-mentioned vapourizing furnace is a fluidized-bed.
Wherein, preferably, above-mentioned fly-ash separator is equipped with cyclone separator.
Wherein, preferably, step 1) is accomplished in shredder, and said shredder is equipped with whipping appts below milling apparatus.
Wherein, preferably, the isolated flying dust of fly-ash separator is recycled from the bottom, arrives shredder as the active agent delivery that reclaims.
Wherein, preferably, the heat that is absorbed in the step 4) process of cooling is transferred to warehouse, the material in the warehouse is carried out drying, preheating.
Advantage of the present invention:
The first, the raw material that the present invention selects for use is coke (comprising coke powder, nut coke).The cost of general feed coal accounts for 40%～50% of gas prodn cost.Because what this process method adopted is coke, the purchase price of raw material is lower by 60%～70% than lump coal, and is cheap, so that the cost of coal gas significantly descend.
The second, the present invention through grinding, fully is crushed to fine particle with raw material with used raw coke, has increased its specific surface area.Make that in vapourizing furnace raw material can fully contact with the gas of participating in reaction, can effectively reduce the reaction times, improves gasification efficiency.
The 3rd, the present invention adopts basic oxide (Fe
2O
3, CaO, MgO etc.) as promoting agent, before reaction, grind with raw material, make basic oxide and raw material thorough mixing, and adopt oxygen, superheated vapour as carrying gas to send in the vapourizing furnace in the lump.Make raw material uniform distribution in the stove, catalytic alkali metal performs to the best, helps to reduce temperature of reaction, shortens the reaction times, reduces reaction pressure.
The 4th, the present invention utilizes the part raw gas behind the elementary cooling and dedusting to send back in the vapourizing furnace as recycle stock.First, participate in reaction, make that reaction is more abundant, regulate the furnace gas composition, promote gas quality and transformation efficiency as recycle stock; Secondly,, can cooperate and carry gas control reaction temperature together, remain in the scope of optimal reaction temperature as cold gas.In addition, the heat that cooling is absorbed can be used for former abrasive lapping, mixed drying and preheating.
The 5th, use improved shredder to be used to improve the reactive behavior of coke among the present invention.At first, the grinding system of upper part that can be through wherein grinds to form fine particle with coke (coke powder, nut coke) and promoting agent, 100 orders-300 order, and under the effect of lower part stirring system further thorough mixing; Secondly, it can recycle the promoting agent in the flying dust, grinds, mixes with raw material, recycles promoting agent, reduces the use cost of promoting agent.
Description of drawings
Fig. 1 is the coke gasification process flow diagram.
Fig. 2 is a coke gasification device simplified schematic diagram.
Fig. 3 is the grinding machine structure synoptic diagram.
1, coke; 2, promoting agent (basic oxide); 3, carry gas; 4, shredder; 5, warehouse; 6, vapourizing furnace; 7, water cooler; 8, fly-ash separator; 9, the isolated gas of fly-ash separator, i.e. part raw gas; 10, slag; 11, the heat that is absorbed in the process of cooling; 12 cleaners; 13, coal gas; 14, flying dust;
41, material inlet; 42, promoting agent opening for feed; 43, flying dust (promoting agent) reclaims mouth; 44, discharge port.
Embodiment
The employed vapourizing furnace that gasifies is broadly divided into three types: fixed bed, fluidized-bed and air flow bed.Fixed-bed structure is simple, and operation reduces by half, but the residence time of raw material in bed is longer, and it is also inhomogeneous to be heated in the fixed bed, and the heat exchange effect is unsatisfactory; Fluidized-bed, also very convenient to the vapourizing furnace charging time, the reaction environment in the bed is also relatively more even, but raw material properties is required relatively strictness, and when using different raw materials, operating just shows slightly inconvenience; Air flow bed, the raw material residence time in bed is short, and reaction is fast, and also relatively evenly, operating temperature is higher for temperature in the stove, and equipment is had strict requirement.
Present method adopts fluidized-bed, through adjustment coke attribute, adds promoting agent; Improve the interior condition of stove etc., the adjustment reaction is temperature required, has reduced the pressure to equipment requirements; Improve the gasification transformation efficiency of coke, thereby embody the price advantage and the economic benefit of coke production synthetic gas or coal gas.
As shown in Figure 2, the gasification system that the present invention adopts comprises shredder 4, warehouse 5, vapourizing furnace 6, water cooler 7, fly-ash separator 8, cleaner 12.
The structure of shredder 4 is as shown in Figure 3; The similar normally used whisking appliance of main body profile; It is one jar of shape; Upper part is a milling apparatus, and lower part is a whipping appts, and milling apparatus top is provided with 3 imports: raw material (coke, coke powder, nut coke) opening for feed 41, promoting agent opening for feed 42, flying dust (promoting agent) reclaim mouth 43.The whipping appts bottom is provided with discharge port 44.
Warehouse 5, vapourizing furnace 6, water cooler 7, fly-ash separator 8, cleaner 12 are multipurpose plant basically.Raw coke 1 is sent into from opening for feed 41, and promoting agent 2 (is generally Fe
2O
3, CaO, basic oxide such as MgO) send into from opening for feed 42; Raw material and promoting agent in shredder 4 thorough mixing, grind to form fine particle (general 90% above raw material is ground to 100 orders-300 order and gets final product, preferred 120-150 order), discharge from discharge port 44 and send into warehouse 5 and carry out drying; Preheating utilizes oxygen and superheated vapour as carrying gas 3, evenly sends into material in the vapourizing furnace 6 in the lump; Carry the gas feed rate through adjustment, the recycle stock feed rate is controlled at reaction environment in the reasonable range; The working pressure of vapourizing furnace is generally between 0.8～1.67MPa; Optimum response pressure is between 1.3MPa-1.5MPa, and generally between 1100 ℃～1400 ℃, optimal reaction temperature is between 1200 ℃～1300 ℃ for the temperature of reaction of vapourizing furnace.In the raw gas composition of gasification back, CO
2, CO, H
2Account for 4%, 58% and 24% (being volume percent) of total raw gas composition here, all the other are O
2, CH
4And other rare gas elementes etc.
The slag 10 that vapourizing furnace 6 is produced is discharged from vapourizing furnace 6 bottoms, and synthetic gas is discharged from the top and got into water cooler 7, and the heat 11 that is absorbed in the process of cooling is used for the material in the warehouse 5 is carried out drying; Preheating utilizes cyclone separator in the gas entering fly-ash separator 8 of supercooler 7, isolated flying dust 14 is recycled from the bottom; As the promoting agent that reclaims, reclaim mouth 43 through flying dust and be transported in the shredder 4 fly-ash separator 8 isolated gases; Be part raw gas 9 as recycle stock, recycle stock flow visual response situation is regulated through the electrical control valve, sends back in the vapourizing furnace 6 and to continue to participate in molecular balance; The working pressure of vapourizing furnace is controlled between 0.8～1.67MPa; Temperature is controlled between 1100 ℃～1400 ℃, and remaining gas gets into cleaner 12 and does further to purify, last output coal gas 13.Native system also can be used to produce other synthetic gas.
All documents in that the present invention mentions are all quoted as a reference in this application, are just quoted such as a reference separately as each piece document.Should be understood that in addition after having read above-mentioned teachings of the present invention, those skilled in the art can do various changes or modification to the present invention, these equivalent form of values fall within the application's appended claims institute restricted portion equally.
Claims (16)
1. a coal gas production method is characterized in that, comprises the steps:
1) raw coke and basic oxide promoting agent are fully ground, stirred, mix;
2) the uniform material of ground and mixed is delivered to warehouse drying, preheating;
3) utilize the mass transport of carrying gas that warehouse is processed to arrive the vapourizing furnace gasification;
4) gas after will gasifying is sent into the water cooler cooling;
5) cooled gas is sent into the fly-ash separator dedusting;
6) gas after the dedusting is sent into purification utensil.
2. coal gas production method according to claim 1 is characterized in that, wherein, said step 1) is accomplished in shredder, and said shredder is equipped with whipping appts below milling apparatus.
3. coal gas production method according to claim 1 is characterized in that, the temperature of reaction of said vapourizing furnace is 1100 ℃～1400 ℃, and working pressure is between 0.8～1.67MPa.
4. coal gas production method according to claim 1 is characterized in that, said conveying gas is oxygen and superheated vapour.
5. coal gas production method according to claim 1 is characterized in that, said vapourizing furnace is a fluidized-bed.
6. coal gas production method according to claim 1 is characterized in that said fly-ash separator is equipped with cyclone separator.
7. according to the described coal gas production method of the arbitrary claim of claim 1-6, it is characterized in that said basic oxide are Fe
2O
3, CaO, MgO, K
2O or Na
2O.
8. according to the described coal gas production method of the arbitrary claim of claim 1-6, it is characterized in that it is the 100-300 order that said raw material and basic oxide promoting agent are milled to granularity.
9. according to the described coal gas production method of the arbitrary claim of claim 1-6, it is characterized in that, the heat that is absorbed in the step 4) process of cooling is transferred to warehouse, the material in the warehouse is carried out drying, preheating.
10. according to Claim 8 or 9 described coal gas production methods, it is characterized in that, the isolated portion gas of said fly-ash separator, promptly the part raw gas is sent back to as recycle stock and is continued to participate in reaction in the vapourizing furnace, with control gasifier temperature and pressure.
11. coal gas production method according to claim 10 is characterized in that, said basic oxide are Fe
2O
3, CaO, MgO, K
2O or Na
2O.
12. coal gas production method according to claim 2 is characterized in that, the isolated flying dust of said fly-ash separator is recycled from the bottom, arrives shredder as the active agent delivery that reclaims.
13. coal gas production method according to claim 12 is characterized in that, the heat that is absorbed in the step 4) process of cooling is transferred to warehouse, and the material in the warehouse is carried out drying, preheating.
14. coal gas production method according to claim 13 is characterized in that, the temperature of reaction of said vapourizing furnace is 1100 ℃～1400 ℃, and working pressure is between 0.8～1.67MPa.
15. coal gas production method according to claim 14 is characterized in that, it is the 100-300 order that said raw material and basic oxide promoting agent are milled to granularity.
16. coal gas production method according to claim 15 is characterized in that, said basic oxide are Fe
2O
3, CaO, MgO, K
2O or Na
2O.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011104125924A CN102492476A (en) | 2011-12-13 | 2011-12-13 | Coal gas production method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011104125924A CN102492476A (en) | 2011-12-13 | 2011-12-13 | Coal gas production method |
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|---|---|
| CN102492476A true CN102492476A (en) | 2012-06-13 |
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|---|---|---|---|
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111978992A (en) * | 2012-12-26 | 2020-11-24 | Sk新技术株式会社 | Integrated gasification unit for carbonaceous fuels |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102226111A (en) * | 2011-05-27 | 2011-10-26 | 吴道洪 | Method for gasifying cyclone bed powder coal |
| CN102245747A (en) * | 2008-12-08 | 2011-11-16 | 通用电气公司 | Gasifier additives for improving refractory life |
-
2011
- 2011-12-13 CN CN2011104125924A patent/CN102492476A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102245747A (en) * | 2008-12-08 | 2011-11-16 | 通用电气公司 | Gasifier additives for improving refractory life |
| CN102226111A (en) * | 2011-05-27 | 2011-10-26 | 吴道洪 | Method for gasifying cyclone bed powder coal |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111978992A (en) * | 2012-12-26 | 2020-11-24 | Sk新技术株式会社 | Integrated gasification unit for carbonaceous fuels |
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Application publication date: 20120613 |
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