CN102585905B - Bituminous coal fixed bed continuous gasification method - Google Patents
Bituminous coal fixed bed continuous gasification method Download PDFInfo
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- CN102585905B CN102585905B CN201210047994.3A CN201210047994A CN102585905B CN 102585905 B CN102585905 B CN 102585905B CN 201210047994 A CN201210047994 A CN 201210047994A CN 102585905 B CN102585905 B CN 102585905B
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- 238000002309 gasification Methods 0.000 title claims abstract description 66
- 239000002802 bituminous coal Substances 0.000 title claims abstract description 24
- 238000000034 method Methods 0.000 title claims abstract description 15
- 239000007789 gas Substances 0.000 claims abstract description 48
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 48
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 47
- 239000001301 oxygen Substances 0.000 claims abstract description 47
- 239000003034 coal gas Substances 0.000 claims abstract description 26
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims abstract description 20
- 239000002994 raw material Substances 0.000 claims abstract description 7
- 238000002156 mixing Methods 0.000 claims description 10
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 8
- 229910052799 carbon Inorganic materials 0.000 claims description 8
- 238000010926 purge Methods 0.000 claims description 6
- 239000000126 substance Substances 0.000 claims description 4
- 239000003245 coal Substances 0.000 abstract description 32
- 238000000354 decomposition reaction Methods 0.000 abstract description 6
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 239000003795 chemical substances by application Substances 0.000 abstract description 2
- 230000015572 biosynthetic process Effects 0.000 abstract 1
- 238000003786 synthesis reaction Methods 0.000 abstract 1
- 238000007664 blowing Methods 0.000 description 46
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 12
- 229910021529 ammonia Inorganic materials 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 238000000197 pyrolysis Methods 0.000 description 3
- 238000001035 drying Methods 0.000 description 2
- 239000000618 nitrogen fertilizer Substances 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
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Abstract
The invention discloses a bituminous coal fixed bed continuous gasification method, which adopts bituminous coal (lump coal or pulverized coal) as raw materials, and adopts enriched oxygen (or pure oxygen) and steam as gasification agent; and a first gasification furnace and a second gasification furnace of a fixed-bed gasification furnace are used for continuous gasification alternately in a forward direction and a reverse direction. According to the bituminous coal fixed bed continuous gasification method, the contents of tar and organic components in synthesis gas are effectively reduced, the steam decomposition rate and effective gas components in coal gas are improved, the production cost is reduced, the environment pollution is reduced, and the long-time stable operation is realized.
Description
Technical field
The present invention relates to a kind of production method of industrial gas, particularly relating to a kind of take bituminous coal as the continuous producing gas method of immovable bed of raw material, specifically refers to a kind of bituminous coal fixed bed continuous gasification method.
Background technology
At present, China's synthetic ammonia, nitrogen fertilizer production mainly adopt fixed-bed intermittent gasification technology, are raw material mainly with hard coal or coke.Traditional immovable bed gasification bituminous coal technology is due to the existence of drying layer, destructive distillation layer, make the tar content in coal gas too high, huge harm is all caused to pipeline, equipment and catalyst, adds the purifying treatment difficulty of water coolant simultaneously, become the bottleneck of restriction bituminous coal fixed bed gasification technology.Along with the rise of energy prices, the cost pressure of synthetic ammonia, nitrogenous fertilizer enterprises is also more and more serious.Therefore, adjust the raw material route of gas processed, with young bituminous coal inferior, cheap for raw material just becomes the important research topic of coal chemical industry one.In recent years, domesticly advanced air flow bed (coal gasification, coal water slurry gasification), fluidized-bed gasification technology are there is, these technology are by controlling gasification temperature at 1000 ~ 1600 DEG C, make the volatile matter cracking in feed coal, thus the tar content reduced in coal gas, improve the quality of coal gas, but these technological investments are high, the poor stability of long-term operation, working cost are high, are therefore also difficult at home carry out large-scale promotion.
Summary of the invention
Present approach provides a kind of bituminous coal fixed bed continuous gasification method, the tar in reduction synthetic gas and the content of organic constituent, improve effective gas composition in steam decomposition rate and coal gas, reduce production cost, minimizing environmental pollution, long-period stable operation.
For achieving the above object, the invention provides a kind of bituminous coal fixed bed continuous gasification method, take bituminous coal as raw material, and oxygen enrichment and steam are vaporized chemical, and it comprises the steps:
A: forward gas: oxygen enrichment and vapor mixing enter from the first vapourizing furnace (1) bottom, react in the first vapourizing furnace (1) generating gasification with bituminous coal, the coal gas produced from the first vapourizing furnace (1) top out, through uphill line (3) and vapor mixing, enter from the second vapourizing furnace (2) top, react in the second vapourizing furnace (2) generating gasification with bituminous coal, produce coal gas from the second vapourizing furnace (2) bottom out, enter gas main (5);
B: steam purge: steam enters from the second vapourizing furnace (2) bottom, with unnecessary coal gas in the second vapourizing furnace (2) from the second vapourizing furnace (2) top out, through uphill line (3) and vapor mixing, enter from the first vapourizing furnace (1) top, first vapourizing furnace (1) bottom out, enters gas main (5);
C: oppositely gas processed: oxygen enrichment and vapor mixing enter from the second vapourizing furnace (2) bottom, react in the second vapourizing furnace (2) generating gasification with bituminous coal, the coal gas produced from the second vapourizing furnace (2) top out, through uphill line (3) and vapor mixing, enter from the first vapourizing furnace (1) top, react in the first vapourizing furnace (1) generating gasification with bituminous coal, produce coal gas from the first vapourizing furnace (1) bottom out, enter gas main (5);
The vapourizing furnace of fixed-bed gasification furnace first described in above-mentioned steps (1) and the second vapourizing furnace (2) hocket forward and reverse gas processed continuously.
As a kind of preferred version, described oxygen-rich concentration is 35-45%; Described vapor pressure is 55-65kPa, and temperature is 155-165 DEG C; After described steam mixes with oxygen enrichment, pressure is 10-12kPa, and inlet air temperature is 110-130 DEG C; Described steam in the boiler is 3.8-4.1kg/Nm with the ratio entering stove pure oxygen amount
3, described in enter stove fixed carbon with the ratio entering stove pure oxygen amount be 0.93-0.94kg/Nm
3.
As another preferred version, described oxygen-rich concentration is 38-45%; Described vapor pressure is 60-65kPa, and temperature is 160-165 DEG C; After described steam mixes with oxygen enrichment, pressure is 10-11kPa, and inlet air temperature is 110-120 DEG C; Described steam in the boiler is 4.0-4.1kg/Nm with the ratio entering stove pure oxygen amount
3, described in enter stove fixed carbon with the ratio entering stove pure oxygen amount be 0.93-0.94kg/Nm
3.
As another preferred version, described oxygen-rich concentration is 38%; Described vapor pressure is 60kPa, and temperature is 160 DEG C; After described steam mixes with oxygen enrichment, pressure is 10kPa, and inlet air temperature is 110 DEG C; Described steam in the boiler is 4.0kg/Nm with the ratio entering stove pure oxygen amount
3, described in enter stove fixed carbon with the ratio entering stove pure oxygen amount be 0.94kg/Nm
3.
As another preferred version again, described vaporized chemical is pure oxygen and steam.
In forward gas-making process, upper steam blowing and oxygen-rich gasifying agent enter the semi-water gas that the first vapourizing furnace produces from bottom to top and enter the second vapourizing furnace from top to bottom with lower steam blowing, and the tar that contains in water-gas and undecomposed water vapour are decomposed in the second vapourizing furnace gasification layer; In reverse gas-making process, upper steam blowing and oxygen enter the semi-water gas that the second vapourizing furnace produces from bottom to top and enter the first vapourizing furnace from top to bottom with lower steam blowing, and the tar that contains in water-gas and undecomposed water vapour are decomposed at the first vapourizing furnace gasification layer; Simultaneously for ensureing process safety, between forward and reverse gas-making process, add the steam purge stage.
Technical scheme provided by the present invention prepares the qualified synthetic gas of tar content with hocket blowing up and blowing down of the mode that twin furnace is connected, tar content in descending coal gas is very low, major cause is that the organic components taken out of from drying layer, destructive distillation layer is when passing through gasification layer, obtain further gasification, and combustion, thus reduce the tar content in coal gas.
The present invention has the following advantages: 1, improve steam decomposition rate, reduces steam consumption; 2, high-temperature gas sensible heat is reclaimed, energy-conservation; 3, reduce high temperature to the impact of the equipment such as follow-up tornado dust collector, increase the service life; 4, the volatile matter that after coal can being made to enter stove, destructive distillation goes out and tar react through high temperature layer of charcoal generating gasification, eliminate these materials take the generation harm of rear workshop section to and reduce costs, can coal beyond gasifying smokeless coal and hard coal, expand the use range of resource; 5, reduce coal consumption, ammonia consumption, reduce CO
2discharge.
Accompanying drawing explanation
Fig. 1 is twin furnace of the present invention series connection oxygen enrichment (or pure oxygen) continuous gasification process schematic diagram.
In figure: 1, the first vapourizing furnace 2, second vapourizing furnace
3, uphill line 4, steam manifold
5, gas main 6, oxygen enrichment or pure oxygen house steward
7, up gas valve 8, steam main valve
9, the first vapourizing furnace blowing down steam valve 10, second vapourizing furnace blowing down steam valve
11, the first vapourizing furnace blowing up steam valve 12, second vapourizing furnace blowing up steam valve
13, the first vapourizing furnace oxygen enrichment valve 14, second vapourizing furnace oxygen enrichment valve
15, the first gasification furnace coal air valve 16, second gasification furnace coal air valve
Embodiment
Below tie the drawings and specific embodiments to be further described the present invention.
Embodiment one: as shown in Figure 1, first vapourizing furnace (1) and the second vapourizing furnace (2) are fixed-bed gasification furnace, be interconnected through uphill line (3), oxygen-rich concentration is 35%, vapor pressure is 55kPa, and temperature is 155 DEG C, and after steam mixes with oxygen enrichment, pressure is 11kPa, inlet air temperature is 120 DEG C, and steam in the boiler is 3.8kg/Nm with the ratio entering stove pure oxygen amount
3, entering stove fixed carbon with the ratio entering stove pure oxygen amount is 0.93kg/Nm
3, steam decomposition rate is 47%, and the valve event situation in each stage is as follows:
Forward gas stage valve switch conditions:
First vapourizing furnace oxygen enrichment valve (13) is opened; Second vapourizing furnace oxygen enrichment valve (14) closes; Steam main valve (8) is opened; First vapourizing furnace blowing down steam valve (9) closes; Second vapourizing furnace blowing down steam valve (10) is opened; First vapourizing furnace blowing up steam valve (11) is opened; Second vapourizing furnace blowing up steam valve (12) closes; Up gas valve (7) is opened; First gasification furnace coal air valve (15) closes; Second gasification furnace coal air valve (16) is opened.
The switch conditions of steam purge stage valve:
First vapourizing furnace oxygen enrichment valve (13) closes; Second vapourizing furnace oxygen enrichment valve (14) closes; Steam main valve (8) is opened; First vapourizing furnace blowing down steam valve (9) is opened; Second vapourizing furnace blowing down steam valve (10) closes; First vapourizing furnace blowing up steam valve (11) closes; Second vapourizing furnace blowing up steam valve (12) is opened; Up gas valve (7) is opened; First gasification furnace coal air valve (15) is opened; Second gasification furnace coal air valve (16) closes.
Reverse gas stage valve switch conditions processed:
First vapourizing furnace oxygen enrichment valve (13) closes; Second vapourizing furnace oxygen enrichment valve (14) is opened; Steam main valve (8) is opened; First vapourizing furnace blowing down steam valve (9) is opened; Second vapourizing furnace blowing down steam valve (10) closes; First vapourizing furnace blowing up steam valve (11) closes; Second vapourizing furnace blowing up steam valve (12) is opened; Up gas valve (7) is opened; First gasification furnace coal air valve (15) is opened; Second gasification furnace coal air valve (16) closes.
Forward or backwards during gas processed, the coal gas of first fixed-bed gasification furnace generation goes out from top, and temperature is 500-600 DEG C, and the coal gas of generation goes out from second fixed bed gasification furnace bottom, temperature≤300 DEG C, and ton ammonia produces tar 22.5kg/t, the maximum gas forming amount 9600Nm of single stove
3/ h, coal gas consists of: H
2: 36.5%, CO:22%, N
2: 18.5%, CO
2: 20.1%, O
2: 0.4%, CH
4: 2.1%, H
2s:437.2mg/Nm
3.
Embodiment two: as shown in Figure 1, first vapourizing furnace (1) and the second vapourizing furnace (2) are fixed-bed gasification furnace, be interconnected through uphill line (3), oxygen-rich concentration is 45%, vapor pressure is 65kPa, and temperature is 165 DEG C, and after steam mixes with oxygen enrichment, pressure is 12kPa, inlet air temperature is 130 DEG C, and steam in the boiler is 4.1kg/Nm with the ratio entering stove pure oxygen amount
3, entering stove fixed carbon with the ratio entering stove pure oxygen amount is 0.93kg/Nm
3, steam decomposition rate is 48%, and the valve event situation in each stage is as follows:
Forward gas stage valve switch conditions:
First vapourizing furnace oxygen enrichment valve (13) is opened; Second vapourizing furnace oxygen enrichment valve (14) closes; Steam main valve (8) is opened; First vapourizing furnace blowing down steam valve (9) closes; Second vapourizing furnace blowing down steam valve (10) is opened; First vapourizing furnace blowing up steam valve (11) is opened; Second vapourizing furnace blowing up steam valve (12) closes; Up gas valve (7) is opened; First gasification furnace coal air valve (15) closes; Second gasification furnace coal air valve (16) is opened.
The switch conditions of steam purge stage valve:
First vapourizing furnace oxygen enrichment valve (13) closes; Second vapourizing furnace oxygen enrichment valve (14) closes; Steam main valve (8) is opened; First vapourizing furnace blowing down steam valve (9) is opened; Second vapourizing furnace blowing down steam valve (10) closes; First vapourizing furnace blowing up steam valve (11) closes; Second vapourizing furnace blowing up steam valve (12) is opened; Up gas valve (7) is opened; First gasification furnace coal air valve (15) is opened; Second gasification furnace coal air valve (16) closes.
Reverse gas stage valve switch conditions processed:
First vapourizing furnace oxygen enrichment valve (13) closes; Second vapourizing furnace oxygen enrichment valve (14) is opened; Steam main valve (8) is opened; First vapourizing furnace blowing down steam valve (9) is opened; Second vapourizing furnace blowing down steam valve (10) closes; First vapourizing furnace blowing up steam valve (11) closes; Second vapourizing furnace blowing up steam valve (12) is opened; Up gas valve (7) is opened; First gasification furnace coal air valve (15) is opened; Second gasification furnace coal air valve (16) closes.
Forward or backwards during gas processed, the coal gas of first fixed-bed gasification furnace generation goes out from top, and temperature is 550-600 DEG C, the coal gas produced goes out from second fixed bed gasification furnace bottom, temperature≤300 DEG C, and ton ammonia produces tar 22.3kg/t, the maximum gas forming amount 9650Nm3/h of single stove, coal gas consists of: H2:38.5%, CO:20%, N2:19.5%, CO2:19.1%, O2:0.3%, CH4:2.2%, H2S:440.2mg/Nm3.
Embodiment three: as shown in Figure 1, first vapourizing furnace (1) and the second vapourizing furnace (2) are fixed-bed gasification furnace, be interconnected through uphill line (3), oxygen-rich concentration is 38%, vapor pressure is 60kPa, and temperature is 160 DEG C, and after steam mixes with oxygen enrichment, pressure is 10kPa, inlet air temperature is 110 DEG C, and steam in the boiler is 4.0kg/Nm with the ratio entering stove pure oxygen amount
3, entering stove fixed carbon with the ratio entering stove pure oxygen amount is 0.94kg/Nm
3, steam decomposition rate is 50%, and the valve event situation in each stage is as follows:
Forward gas stage valve switch conditions:
First vapourizing furnace oxygen enrichment valve (13) is opened; Second vapourizing furnace oxygen enrichment valve (14) closes; Steam main valve (8) is opened; First vapourizing furnace blowing down steam valve (9) closes; Second vapourizing furnace blowing down steam valve (10) is opened; First vapourizing furnace blowing up steam valve (11) is opened; Second vapourizing furnace blowing up steam valve (12) closes; Up gas valve (7) is opened; First gasification furnace coal air valve (15) closes; Second gasification furnace coal air valve (16) is opened.
The switch conditions of steam purge stage valve:
First vapourizing furnace oxygen enrichment valve (13) closes; Second vapourizing furnace oxygen enrichment valve (14) closes; Steam main valve (8) is opened; First vapourizing furnace blowing down steam valve (9) is opened; Second vapourizing furnace blowing down steam valve (10) closes; First vapourizing furnace blowing up steam valve (11) closes; Second vapourizing furnace blowing up steam valve (12) is opened; Up gas valve (7) is opened; First gasification furnace coal air valve (15) is opened; Second gasification furnace coal air valve (16) closes.
Reverse gas stage valve switch conditions processed:
First vapourizing furnace oxygen enrichment valve (13) closes; Second vapourizing furnace oxygen enrichment valve (14) is opened; Steam main valve (8) is opened; First vapourizing furnace blowing down steam valve (9) is opened; Second vapourizing furnace blowing down steam valve (10) closes; First vapourizing furnace blowing up steam valve (11) closes; Second vapourizing furnace blowing up steam valve (12) is opened; Up gas valve (7) is opened; First gasification furnace coal air valve (15) is opened; Second gasification furnace coal air valve (16) closes.
Forward or backwards during gas processed, the coal gas of first fixed-bed gasification furnace generation goes out from top, and temperature is 520-580 DEG C, the coal gas produced goes out from second fixed bed gasification furnace bottom, temperature≤300 DEG C, and ton ammonia produces tar 22.1kg/t, the maximum gas forming amount 9590Nm3/h of single stove, coal gas consists of: H2:37.5%, CO:20%, N2:19.5%, CO2:19.1%, O2:0.4%, CH4:3.1%, H2S:438.6mg/Nm3.
Claims (2)
1. a bituminous coal fixed bed continuous gasification method, take bituminous coal as raw material, oxygen enrichment and steam are vaporized chemical, and it comprises the steps:
A: forward gas: oxygen enrichment and vapor mixing enter from the first vapourizing furnace (1) bottom, react in the first vapourizing furnace (1) generating gasification with bituminous coal, the coal gas produced from the first vapourizing furnace (1) top out, through uphill line (3) and vapor mixing, enter from the second vapourizing furnace (2) top, react in the second vapourizing furnace (2) generating gasification with bituminous coal, produce coal gas from the second vapourizing furnace (2) bottom out, enter gas main (5);
B: steam purge: steam enters from the second vapourizing furnace (2) bottom, with unnecessary coal gas in the second vapourizing furnace (2) from the second vapourizing furnace (2) top out, through uphill line (3) and vapor mixing, enter from the first vapourizing furnace (1) top, first vapourizing furnace (1) bottom out, enters gas main (5);
C: oppositely gas processed: oxygen enrichment and vapor mixing enter from the second vapourizing furnace (2) bottom, react in the second vapourizing furnace (2) generating gasification with bituminous coal, the coal gas produced from the second vapourizing furnace (2) top out, through uphill line (3) and vapor mixing, enter from the first vapourizing furnace (1) top, react in the first vapourizing furnace (1) generating gasification with bituminous coal, produce coal gas from the first vapourizing furnace (1) bottom out, enter gas main (5);
The vapourizing furnace of fixed-bed gasification furnace first described in above-mentioned steps (1) and the second vapourizing furnace (2) hocket forward and reverse gas processed continuously;
Described oxygen-rich concentration is 38-45%; Described vapor pressure is 60-65kPa, and temperature is 160-165 DEG C; After described steam mixes with oxygen enrichment, pressure is 10-11kPa, and inlet air temperature is 110-120 DEG C; Described steam in the boiler is 4.0-4.1kg/Nm with the ratio entering stove pure oxygen amount
3, described in enter stove fixed carbon with the ratio entering stove pure oxygen amount be 0.93-0.94kg/Nm
3.
2. bituminous coal fixed bed continuous gasification method according to claim 1, is characterized in that: described oxygen-rich concentration is 38%; Described vapor pressure is 60kPa, and temperature is 160 DEG C; After described steam mixes with oxygen enrichment, pressure is 10kPa, and inlet air temperature is 110 DEG C; Described steam in the boiler is 4.0kg/Nm with the ratio entering stove pure oxygen amount
3, described in enter stove fixed carbon with the ratio entering stove pure oxygen amount be 0.94kg/Nm
3.
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| GB2510642B (en) * | 2013-02-12 | 2016-02-03 | Chinook End Stage Recycling Ltd | Waste processing |
| CN103756730B (en) * | 2014-01-22 | 2015-02-04 | 杭州全合科技有限公司 | Heat accumulating type powdered coal entrained bed gasification method |
| CN114106888A (en) * | 2021-11-22 | 2022-03-01 | 安徽晋煤中能化工股份有限公司 | Automatic optimization device for steam entering gas furnace |
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|---|---|---|---|---|
| CN1587354A (en) * | 2004-07-06 | 2005-03-02 | 杜三民 | Intermittent gas making method and device with bituminous coal fixing layer |
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| CN2711169Y (en) * | 2004-07-09 | 2005-07-20 | 杜三民 | Double fixed-bed intermittent gas prodn. furnace using soft coal as raw material |
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| CN1587354A (en) * | 2004-07-06 | 2005-03-02 | 杜三民 | Intermittent gas making method and device with bituminous coal fixing layer |
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