CN102585905A - Bituminous coal fixed bed continuous gasification method - Google Patents
Bituminous coal fixed bed continuous gasification method Download PDFInfo
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- CN102585905A CN102585905A CN2012100479943A CN201210047994A CN102585905A CN 102585905 A CN102585905 A CN 102585905A CN 2012100479943 A CN2012100479943 A CN 2012100479943A CN 201210047994 A CN201210047994 A CN 201210047994A CN 102585905 A CN102585905 A CN 102585905A
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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 working method of industrial gas, relating in particular to a kind of is the continuous producing gas method of immovable bed of raw material with bituminous coal, specifically is meant the continuous producing gas method of a kind of bituminous coal immovable bed.
Background technology
At present, China's synthetic ammonia, nitrogen fertilizer production mainly adopt fixed bed intermittent gasification technology, are raw material with hard coal or coke how.Traditional immovable bed gasification bituminous coal technology is because the existence of drying layer, destructive distillation layer; Make that the tar content in the coal gas is too high; Pipeline, equipment and catalyst are all caused huge harm, increased 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, the raw material route of adjustment system gas is that raw material just becomes important research project of Coal Chemical Industry industry with inferior, cheap young bituminous coal.In recent years; Domestic advanced air flow bed (coal gasification, coal water slurry gasification), the fluidized-bed gasification technology of having occurred, these technology at 1000～1600 ℃, make the volatile matter cracking in the feed coal through the control gasification temperature; Thereby reduced the tar content in the coal gas; Improved the quality of coal gas, but these technological investments are high, the poor stability of long-term operation, working cost are high, therefore also are difficult to carry out large-scale promotion at home.
Summary of the invention
The inventive method provides a kind of bituminous coal immovable bed continuous producing gas method, and the tar in the reduction synthetic gas and the content of organic constituent improve effective gas composition in steam decomposition rate and the coal gas, reduce production costs, and reduce environmental pollution, long-period stable operation.
For realizing above-mentioned purpose, the present invention provides a kind of bituminous coal immovable bed continuous producing gas method, is raw material with bituminous coal, and oxygen enrichment and steam are vaporized chemical, and it comprises the steps:
A: forward system gas: oxygen enrichment and steam get into from first vapourizing furnace (1) bottom; React in first vapourizing furnace (1) generating gasification with bituminous coal, the coal gas of generation comes out from first vapourizing furnace (1) top, through uphill line (3) and steam; Get into from second vapourizing furnace (2) top; React in second vapourizing furnace (2) generating gasification with bituminous coal, produce coal gas and come out, get into gas main (5) from second vapourizing furnace (2) bottom;
B: steam purge: steam gets into from second vapourizing furnace (2) bottom; Come out from second vapourizing furnace (2) top with unnecessary coal gas in second vapourizing furnace (2),, get into from first vapourizing furnace (1) top through uphill line (3) and steam; Coming out in first vapourizing furnace (1) bottom, gets into gas main (5);
C: oppositely make gas: oxygen enrichment and steam get into from second vapourizing furnace (2) bottom; React in second vapourizing furnace (2) generating gasification with bituminous coal, the coal gas of generation comes out from second vapourizing furnace (2) top, through uphill line (3) and steam; Get into from first vapourizing furnace (1) top; React in first vapourizing furnace (1) generating gasification with bituminous coal, produce coal gas and come out, get into gas main (5) from first vapourizing furnace (1) bottom;
First vapourizing furnace of fixed-bed gasification furnace described in the above-mentioned steps (1) and second vapourizing furnace (2) hocket forward and the reverse gas of system continuously.
As a kind of preferred version, said oxygen-rich concentration is 35-45%; Said vapor pressure is 55-65kPa, and temperature is 155-165 ℃; Said steam mixes back pressure with oxygen enrichment be 10-12kPa, and inlet air temperature is 110-130 ℃; Said steam in the boiler is 3.8-4.1kg/Nm with the ratio of going into stove pure oxygen amount
3It is, said that to go into stove fixed carbon be 0.93-0.94kg/Nm with the ratio of going into stove pure oxygen amount
3
As another preferred version, said oxygen-rich concentration is 38-45%; Said vapor pressure is 60-65kPa, and temperature is 160-165 ℃; Said steam mixes back pressure with oxygen enrichment be 10-11kPa, and inlet air temperature is 110-120 ℃; Said steam in the boiler is 4.0-4.1kg/Nm with the ratio of going into stove pure oxygen amount
3It is, said that to go into stove fixed carbon be 0.93-0.94kg/Nm with the ratio of going into stove pure oxygen amount
3
As another preferred version, said oxygen-rich concentration is 38%; Said vapor pressure is 60kPa, and temperature is 160 ℃; Said steam mixes back pressure with oxygen enrichment be 10kPa, and inlet air temperature is 110 ℃; Said steam in the boiler is 4.0kg/Nm with the ratio of going into stove pure oxygen amount
3It is, said that to go into stove fixed carbon be 0.94kg/Nm with the ratio of going into stove pure oxygen amount
3
As another preferred version again, said vaporized chemical is pure oxygen and steam.
In the forward gas-making process; Last steam blowing and oxygen-rich gasifying agent get into semi-water gas that first vapourizing furnace produces from bottom to top and get into second vapourizing furnace from top to bottom with steam blowing down, and the tar and the undecomposed water vapour that contain in the water-gas are decomposed in second vapourizing furnace gasification layer; In reverse gas-making process; Last steam blowing and oxygen get into semi-water gas that second vapourizing furnace produces from bottom to top and get into first vapourizing furnace from top to bottom with steam blowing down, and the tar and the undecomposed water vapour that contain in the water-gas are decomposed at first vapourizing furnace gasification layer; Be assurance process safety simultaneously, between forward and reverse gas-making process, added the steam purge stage.
Blow on technical scheme provided by the present invention hockets with the placed in-line mode of twin furnace and descend blowing to be equipped with the qualified synthetic gas of tar content; Tar content in the descending coal gas is very low; Major cause is that organic component of taking out of from drying layer, destructive distillation layer is during from top to bottom through the gasification layer; Obtain further gasification, and combustion, thereby reduced the tar content in the coal gas.
The present invention has the following advantages: 1, improve steam decomposition rate, reduce steam consumption; 2, reclaim the high-temperature gas sensible heat, energy-conservation; 3, reduce the influence of high temperature, increase the service life equipment such as follow-up tornado dust collector; 4, can make coal go into behind the stove dried distilled volatile matter and tar through the reaction of pyrocarbon layer generating gasification; Eliminating these materials takes back workshop section to and produces harm and reduce cost; Can gasify coal beyond hard coal and the hard coal enlarges the use range of resource; 5, reduce coal consumption, ammonia consumption, reduce CO
2Discharging.
Description of drawings
Fig. 1 is twin furnace series connection oxygen enrichment (or pure oxygen) continuous gasification process synoptic diagram of the present invention.
Among the figure: 1, 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, steam blowing valve under steam blowing valve 10, second vapourizing furnace under first vapourizing furnace
11, steam blowing valve on steam blowing valve 12, second vapourizing furnace on first vapourizing furnace
13, the first vapourizing furnace oxygen enrichment valve 14, the second vapourizing furnace oxygen enrichment valve
15, the first gasification furnace coal air valve 16, the second gasification furnace coal air valve
Embodiment
Below knot accompanying drawing and specific embodiment are done to describe further to the present invention.
Embodiment one: shown in accompanying drawing 1, first vapourizing furnace (1) is fixed-bed gasification furnace with second vapourizing furnace (2), is interconnected through uphill line (3); Oxygen-rich concentration is 35%; Vapor pressure is 55kPa, and temperature is 155 ℃, and steam mixes back pressure with oxygen enrichment be 11kPa; Inlet air temperature is 120 ℃, and steam in the boiler is 3.8kg/Nm with the ratio of going into stove pure oxygen amount
3, going into stove fixed carbon is 0.93kg/Nm with the ratio of going into stove pure oxygen amount
3, steam decomposition rate is 47%, the valve event situation in each stage is as follows:
Forward system gas stage valve switch situation:
The first vapourizing furnace oxygen enrichment valve (13) is opened; The second vapourizing furnace oxygen enrichment valve (14) closes; Steam main valve (8) is opened; Steam blowing valve (9) closes under first vapourizing furnace; Steam blowing valve (10) is opened under second vapourizing furnace; Steam blowing valve (11) is opened on first vapourizing furnace; Steam blowing valve (12) closes on second vapourizing furnace; Up gas valve (7) is opened; The first gasification furnace coal air valve (15) closes; The second gasification furnace coal air valve (16) is opened.
The switch situation of steam purge stage valve:
The first vapourizing furnace oxygen enrichment valve (13) closes; The second vapourizing furnace oxygen enrichment valve (14) closes; Steam main valve (8) is opened; Steam blowing valve (9) is opened under first vapourizing furnace; Steam blowing valve (10) closes under second vapourizing furnace; Steam blowing valve (11) is opened on first vapourizing furnace; Steam blowing valve (12) closes on second vapourizing furnace; Up gas valve (7) is opened; The first gasification furnace coal air valve (15) is opened; The second gasification furnace coal air valve (16) closes.
Reverse system gas stage valve switch situation:
The first vapourizing furnace oxygen enrichment valve (13) closes; The second vapourizing furnace oxygen enrichment valve (14) is opened; Steam main valve (8) is opened; Steam blowing valve (9) is opened under first vapourizing furnace; Steam blowing valve (10) closes under second vapourizing furnace; Steam blowing valve (11) closes on first vapourizing furnace; Steam blowing valve (12) is opened on second vapourizing furnace; Up gas valve (7) is opened; The first gasification furnace coal air valve (15) closes; The second gasification furnace coal air valve (16) is opened.
When making gas forward or backwards, the coal gas that first fixed-bed gasification furnace produces goes out from the top, and temperature is 500-600 ℃, and the coal gas of generation goes out from second fixed bed gasification furnace bottom, temperature≤300 ℃, 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: shown in accompanying drawing 1, first vapourizing furnace (1) is fixed-bed gasification furnace with second vapourizing furnace (2), is interconnected through uphill line (3); Oxygen-rich concentration is 45%; Vapor pressure is 65kPa, and temperature is 165 ℃, and steam mixes back pressure with oxygen enrichment be 12kPa; Inlet air temperature is 130 ℃, and steam in the boiler is 4.1kg/Nm with the ratio of going into stove pure oxygen amount
3, going into stove fixed carbon is 0.93kg/Nm with the ratio of going into stove pure oxygen amount
3, steam decomposition rate is 48%, the valve event situation in each stage is as follows:
Forward system gas stage valve switch situation:
The first vapourizing furnace oxygen enrichment valve (13) is opened; The second vapourizing furnace oxygen enrichment valve (14) closes; Steam main valve (8) is opened; Steam blowing valve (9) closes under first vapourizing furnace; Steam blowing valve (10) is opened under second vapourizing furnace; Steam blowing valve (11) is opened on first vapourizing furnace; Steam blowing valve (12) closes on second vapourizing furnace; Up gas valve (7) is opened; The first gasification furnace coal air valve (15) closes; The second gasification furnace coal air valve (16) is opened.
The switch situation of steam purge stage valve:
The first vapourizing furnace oxygen enrichment valve (13) closes; The second vapourizing furnace oxygen enrichment valve (14) closes; Steam main valve (8) is opened; Steam blowing valve (9) is opened under first vapourizing furnace; Steam blowing valve (10) closes under second vapourizing furnace; Steam blowing valve (11) is opened on first vapourizing furnace; Steam blowing valve (12) closes on second vapourizing furnace; Up gas valve (7) is opened; The first gasification furnace coal air valve (15) is opened; The second gasification furnace coal air valve (16) closes.
Reverse system gas stage valve switch situation:
The first vapourizing furnace oxygen enrichment valve (13) closes; The second vapourizing furnace oxygen enrichment valve (14) is opened; Steam main valve (8) is opened; Steam blowing valve (9) is opened under first vapourizing furnace; Steam blowing valve (10) closes under second vapourizing furnace; Steam blowing valve (11) closes on first vapourizing furnace; Steam blowing valve (12) is opened on second vapourizing furnace; Up gas valve (7) is opened; The first gasification furnace coal air valve (15) closes; The second gasification furnace coal air valve (16) is opened.
When making gas forward or backwards, the coal gas that first fixed-bed gasification furnace produces goes out from the top, and temperature is 550-600 ℃, and the coal gas of generation goes out from second fixed bed gasification furnace bottom; Temperature≤300 ℃, 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: shown in accompanying drawing 1, first vapourizing furnace (1) is fixed-bed gasification furnace with second vapourizing furnace (2), is interconnected through uphill line (3); Oxygen-rich concentration is 38%; Vapor pressure is 60kPa, and temperature is 160 ℃, and steam mixes back pressure with oxygen enrichment be 10kPa; Inlet air temperature is 110 ℃, and steam in the boiler is 4.0kg/Nm with the ratio of going into stove pure oxygen amount
3, going into stove fixed carbon is 0.94kg/Nm with the ratio of going into stove pure oxygen amount
3, steam decomposition rate is 50%, the valve event situation in each stage is as follows:
Forward system gas stage valve switch situation:
The first vapourizing furnace oxygen enrichment valve (13) is opened; The second vapourizing furnace oxygen enrichment valve (14) closes; Steam main valve (8) is opened; Steam blowing valve (9) closes under first vapourizing furnace; Steam blowing valve (10) is opened under second vapourizing furnace; Steam blowing valve (11) is opened on first vapourizing furnace; Steam blowing valve (12) closes on second vapourizing furnace; Up gas valve (7) is opened; The first gasification furnace coal air valve (15) closes; The second gasification furnace coal air valve (16) is opened.
The switch situation of steam purge stage valve:
The first vapourizing furnace oxygen enrichment valve (13) closes; The second vapourizing furnace oxygen enrichment valve (14) closes; Steam main valve (8) is opened; Steam blowing valve (9) is opened under first vapourizing furnace; Steam blowing valve (10) closes under second vapourizing furnace; Steam blowing valve (11) is opened on first vapourizing furnace; Steam blowing valve (12) closes on second vapourizing furnace; Up gas valve (7) is opened; The first gasification furnace coal air valve (15) is opened; The second gasification furnace coal air valve (16) closes.
Reverse system gas stage valve switch situation:
The first vapourizing furnace oxygen enrichment valve (13) closes; The second vapourizing furnace oxygen enrichment valve (14) is opened; Steam main valve (8) is opened; Steam blowing valve (9) is opened under first vapourizing furnace; Steam blowing valve (10) closes under second vapourizing furnace; Steam blowing valve (11) closes on first vapourizing furnace; Steam blowing valve (12) is opened on second vapourizing furnace; Up gas valve (7) is opened; The first gasification furnace coal air valve (15) closes; The second gasification furnace coal air valve (16) is opened.
When making gas forward or backwards, the coal gas that first fixed-bed gasification furnace produces goes out from the top, and temperature is 520-580 ℃, and the coal gas of generation goes out from second fixed bed gasification furnace bottom; Temperature≤300 ℃, 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 (5)
1. the continuous producing gas method of bituminous coal immovable bed is a raw material with bituminous coal, and oxygen enrichment and steam are vaporized chemical, and it comprises the steps:
A: forward system gas: oxygen enrichment and steam get into from first vapourizing furnace (1) bottom; React in first vapourizing furnace (1) generating gasification with bituminous coal, the coal gas of generation comes out from first vapourizing furnace (1) top, through uphill line (3) and steam; Get into from second vapourizing furnace (2) top; React in second vapourizing furnace (2) generating gasification with bituminous coal, produce coal gas and come out, get into gas main (5) from second vapourizing furnace (2) bottom;
B: steam purge: steam gets into from second vapourizing furnace (2) bottom; Come out from second vapourizing furnace (2) top with unnecessary coal gas in second vapourizing furnace (2),, get into from first vapourizing furnace (1) top through uphill line (3) and steam; Coming out in first vapourizing furnace (1) bottom, gets into gas main (5);
C: oppositely make gas: oxygen enrichment and steam get into from second vapourizing furnace (2) bottom; React in second vapourizing furnace (2) generating gasification with bituminous coal, the coal gas of generation comes out from second vapourizing furnace (2) top, through uphill line (3) and steam; Get into from first vapourizing furnace (1) top; React in first vapourizing furnace (1) generating gasification with bituminous coal, produce coal gas and come out, get into gas main (5) from first vapourizing furnace (1) bottom;
First vapourizing furnace of fixed-bed gasification furnace described in the above-mentioned steps (1) and second vapourizing furnace (2) hocket forward and the reverse gas of system continuously.
2. the continuous producing gas method of bituminous coal immovable bed according to claim 1 is characterized in that: said oxygen-rich concentration is 35-45%; Said vapor pressure is 55-65kPa, and temperature is 155-165 ℃; Said steam mixes back pressure with oxygen enrichment be 10-12kPa, and inlet air temperature is 110-130 ℃; Said steam in the boiler is 3.8-4.1kg/Nm with the ratio of going into stove pure oxygen amount
3It is, said that to go into stove fixed carbon be 0.93-0.94kg/Nm with the ratio of going into stove pure oxygen amount
3
3. the continuous producing gas method of bituminous coal immovable bed according to claim 1 is characterized in that: said oxygen-rich concentration is 38-45%; Said vapor pressure is 60-65kPa, and temperature is 160-165 ℃; Said steam mixes back pressure with oxygen enrichment be 10-11kPa, and inlet air temperature is 110-120 ℃; Said steam in the boiler is 4.0-4.1kg/Nm with the ratio of going into stove pure oxygen amount
3It is, said that to go into stove fixed carbon be 0.93-0.94kg/Nm with the ratio of going into stove pure oxygen amount
3
4. the continuous producing gas method of bituminous coal immovable bed according to claim 1 is characterized in that: said oxygen-rich concentration is 38%; Said vapor pressure is 60kPa, and temperature is 160 ℃; Said steam mixes back pressure with oxygen enrichment be 10kPa, and inlet air temperature is 110 ℃; Said steam in the boiler is 4.0kg/Nm with the ratio of going into stove pure oxygen amount
3It is, said that to go into stove fixed carbon be 0.94kg/Nm with the ratio of going into stove pure oxygen amount
3
5. the continuous producing gas method of bituminous coal immovable bed according to claim 1 is characterized in that: said vaporized chemical is pure oxygen and steam.
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| CN201210047994.3A CN102585905B (en) | 2012-02-29 | 2012-02-29 | Bituminous coal fixed bed continuous gasification method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210047994.3A CN102585905B (en) | 2012-02-29 | 2012-02-29 | Bituminous coal fixed bed continuous gasification method |
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| CN102585905A true CN102585905A (en) | 2012-07-18 |
| CN102585905B CN102585905B (en) | 2014-12-17 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103756730A (en) * | 2014-01-22 | 2014-04-30 | 杭州全合科技有限公司 | Heat accumulating type powdered coal entrained bed gasification method |
| GB2510642A (en) * | 2013-02-12 | 2014-08-13 | Chinook End Stage Recycling Ltd | Waste gasification to produce energy |
| 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 |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1587354A (en) * | 2004-07-06 | 2005-03-02 | 杜三民 | Intermittent gas making method and device with bituminous coal fixing layer |
| CN2711169Y (en) * | 2004-07-09 | 2005-07-20 | 杜三民 | Double fixed-bed intermittent gas prodn. furnace using soft coal as raw material |
-
2012
- 2012-02-29 CN CN201210047994.3A patent/CN102585905B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1587354A (en) * | 2004-07-06 | 2005-03-02 | 杜三民 | Intermittent gas making method and device with bituminous coal fixing layer |
| CN2711169Y (en) * | 2004-07-09 | 2005-07-20 | 杜三民 | Double fixed-bed intermittent gas prodn. furnace using soft coal as raw material |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2510642A (en) * | 2013-02-12 | 2014-08-13 | Chinook End Stage Recycling Ltd | Waste gasification to produce energy |
| GB2510642B (en) * | 2013-02-12 | 2016-02-03 | Chinook End Stage Recycling Ltd | Waste processing |
| US9920928B2 (en) | 2013-02-12 | 2018-03-20 | Chinook End-Stage Recycling Limited | Waste processing |
| CN103756730A (en) * | 2014-01-22 | 2014-04-30 | 杭州全合科技有限公司 | Heat accumulating type powdered coal entrained bed gasification method |
| 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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