CN102199453A - Improved Lurgi gasification furnace waste heat recovering method and device - Google Patents
Improved Lurgi gasification furnace waste heat recovering method and device Download PDFInfo
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- CN102199453A CN102199453A CN2011100926482A CN201110092648A CN102199453A CN 102199453 A CN102199453 A CN 102199453A CN 2011100926482 A CN2011100926482 A CN 2011100926482A CN 201110092648 A CN201110092648 A CN 201110092648A CN 102199453 A CN102199453 A CN 102199453A
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- waste heat
- heat boiler
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- 239000002918 waste heat Substances 0.000 title claims abstract description 84
- 238000002309 gasification Methods 0.000 title claims abstract description 20
- 238000000034 method Methods 0.000 title claims abstract description 20
- 239000007921 spray Substances 0.000 claims abstract description 78
- 239000007789 gas Substances 0.000 claims abstract description 53
- 238000010438 heat treatment Methods 0.000 claims abstract description 14
- 238000011084 recovery Methods 0.000 claims abstract description 14
- 239000003245 coal Substances 0.000 claims abstract description 13
- 238000001816 cooling Methods 0.000 claims abstract description 9
- KSSNXJHPEFVKHY-UHFFFAOYSA-N phenol;hydrate Chemical compound O.OC1=CC=CC=C1 KSSNXJHPEFVKHY-UHFFFAOYSA-N 0.000 claims abstract description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 33
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims description 6
- 238000005406 washing Methods 0.000 claims description 6
- 238000012545 processing Methods 0.000 claims description 3
- 239000006227 byproduct Substances 0.000 abstract description 6
- 238000004519 manufacturing process Methods 0.000 abstract description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 230000002045 lasting effect Effects 0.000 description 1
- 230000021715 photosynthesis, light harvesting Effects 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000010079 rubber tapping Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000001131 transforming effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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Abstract
The invention belongs to the technical field of energy recovery and relates to a method for secondary recovery of waste heat of a Lurgi gasification furnace and a device for realizing the method. The waste heat recovery is realized by adopting two stages of waste heat boilers. The method comprises the following steps: raw gas discharged from the gasification process of coal is firstly subjected to spray cooling by utilizing diluted phenol water from a diluted phenol water tank in a primary spray cooler, the cooled raw gas enters to a primary waste heat boiler, and in the primary waste heat boiler, steam is generated by boiler feedwater in the heating shell pass of the raw gas; raw gas discharged from the primary waste heat boiler is subjected to spray cooling by utilizing diluted phenol water in a secondary spray cooler, the cooled raw gas enters into a secondary waste heat boiler, and in the secondary waste heat boiler, steam is generated by boiler feedwater in the heating shell pass of the raw gas. The device disclosed by the invention has the advantages of novel structure, simpleness in equipment manufacturing, low cost, optimized energy layout, energy resource saving, remarkable economic benefits and capabilities of generating partial 0.8-1.5MPa steam as a byproduct by utilizing the waste heat of the gasification furnace, meeting the requirement on a factory for the steam in the pressure range and effectively reducing the consumption of the steam with high pressure level.
Description
Technical field:
The invention belongs to technical field of energy recovery, relate to the method for Lurgi gasifier waste heat secondary recovery and realize the device of this method, the waste heat that causes in can the stove burning to various coal gas reclaims effectively, realizes the effect of energy-saving and emission-reduction.
Background technology:
Lasting high along with oil price, coal more and more comes into one's own in the application of the energy and chemical field, and gasification is cleaning, efficiently utilizes the effective means of coal, is widely used in the industry such as gas maked coal, synthetic ammonia, coal power generation; When raw gas leaves vapourizing furnace, temperature is generally all more than 400 ℃, in order to reclaim this part heat, present way is through the suitably cooling of spraying water with raw gas, send in the waste heat boiler, being used for the gasification boiler feedwater and producing pressure is the low-pressure steam of 0.5-0.7MPa, so the waste-heat recovery device of current Lurgi gasifier can only reclaim the low-pressure steam of 0.5-0.7MPa, thereby in general gasification plant, 0.5-0.7MPa steam more than needed in a large number, unnecessary low-pressure steam can only be as the power steam of low value, and the value of steam per ton only is equivalent to 20-30 unit; On the other hand, along with implementation of processes such as new phenol recovery, low-temperature rectisols, the steam supply wretched insufficiency of the 0.8-1.5MPa that device such as phenol recovery, low-temperature rectisol is required, be forced to replace from the steam that power-section extracts more than the pressure 2.0MPa, waste one's talent on a petty job, reduced the value of this part high pressure steam; Therefore, seek a kind of steam by vapourizing furnace waste heat by-product part 0.8-1.5MPa, satisfy the demand of plant area to this pressure range steam, reduce the consumption of high pressure grade steam, thereby optimize current energy layout, the technological method of increasing economic efficiency is the development research target of energy dissipation during current solution coal gasification is utilized.
Summary of the invention:
The objective of the invention is to overcome the defective of prior art, seek to design the device that provides a kind of improvement type coal to utilize the method for vapourizing furnace waste heat recovery in the process and realize this method.
To achieve these goals, the present invention adopts the two-stage waste heat boiler to realize waste heat recovery, after earlier the raw gas of coming out of the stove in the coal gasification process being used rare phenol water spray from rare phenol tank to be cooled to 200-270 ℃ in the one-level spray cooler, enter first step waste heat boiler, again in first step waste heat boiler, the oiler feed of raw gas heating shell side, the steam of generation pressure 0.8-1.5MPa; The raw gas that goes out first step waste heat boiler is cooled to 160-210 ℃ with rare phenol water spray in the secondary spray cooler after, enter second stage waste heat boiler, in the waste heat boiler of the second stage, the oiler feed of raw gas heating shell side, producing pressure is the steam of 0.3-0.8MPa; The raw gas that comes out from the coal gasification stove enters the one-level spray cooler through the raw gas pipeline, the spray water washing cooling that is come from tank, and the condensed water in the one-level spray cooler is discharged system handles from the bottom; Cooled raw gas enters the one-level waste heat boiler, the feedwater heating and gasifying that will enter by the feedwater pipeline, the raw gas of output one-level waste heat boiler enters the secondary spray cooler through the raw gas pipeline, the spray water washing cooling that is come from tank, the cooled raw gas of secondary enters the secondary waste heat boiler, the feedwater heating and gasifying that will enter by the feedwater pipeline; The raw gas of output secondary waste heat boiler enters subsequent handling processing through the raw gas pipeline; The steam that gasification produces in steam that gasification produces in the one-level waste heat boiler and the secondary waste heat boiler enters the steam pipe system of corresponding pressure respectively through steam-pipe; Condensed water in secondary spray cooler and the I and II waste heat boiler is drained in the tank by lower part outlet duct type separately and recycles.
The agent structure of the inventive method device for carrying out said comprises one-level waste heat boiler, secondary waste heat boiler, one-level spray cooler, secondary spray cooler, tank, raw gas intake ducting, feedwater pipeline, steam-pipe, replenishes the spray water pipeline, effluxes spray water pipeline and water circulating pump; The raw gas intake ducting connects one-level spray cooler opening for feed, the corresponding connection of tube side opening for feed of the centre exit place duct type of one-level spray cooler and one-level waste heat boiler, and the bottom of one-level spray cooler is shaped on and exports and efflux the spray water pipeline and be communicated with; The tube side outlet of one-level waste heat boiler is communicated with secondary spray cooler pipeline; The top inlet of one-level spray cooler and secondary spray cooler is connected with tank by the water circulating pump duct type; Secondary spray cooler, I and II waste heat boiler lower part outlet duct type respectively connect tank; The centre exit place of secondary spray cooler is communicated with the tube side opening for feed place duct type of secondary waste heat boiler; The shell side ingress of I and II waste heat boiler is connected with the feedwater pipeline respectively by pipeline, and the shell side outlet is connected with the steam-pipe that has pressure respectively by pipeline; The water inlet of tank is shaped on and replenishes the spray water pipeline.
The present invention compared with prior art, its structure design novelty, equipment preparation technology is simple, cost is low, can satisfy the demand of plant area to this pressure range steam by the steam of vapourizing furnace waste heat by-product part 0.8-1.5MPa, effectively reduce the consumption of high pressure grade steam, optimize the energy layout, save the energy, remarkable in economical benefits.
Description of drawings:
Fig. 1 is the structural principle synoptic diagram of waste-heat recovery device of the present invention.
Embodiment
Below in conjunction with accompanying drawing and by embodiment the present invention is further described.
Embodiment:
Present embodiment adopts the two-stage waste heat boiler to realize waste heat recovery, after earlier the raw gas of coming out of the stove in the coal gasification process being used rare phenol water spray from rare phenol tank to be cooled to 200-270 ℃ in the one-level spray cooler, enter first step waste heat boiler, again in first step waste heat boiler, the oiler feed of raw gas heating shell side, the steam of generation pressure 0.8-1.5MPa; The raw gas that goes out first step waste heat boiler is cooled to 160-210 ℃ with rare phenol water spray in the secondary spray cooler after, enter second stage waste heat boiler, in the waste heat boiler of the second stage, the oiler feed of raw gas heating shell side, producing pressure is the steam of 0.3-0.8MPa.
The agent structure that present embodiment is implemented comprises one-level waste heat boiler 3, secondary waste heat boiler 5, one-level spray cooler 1, secondary spray cooler 4, tank 2, raw gas intake ducting 6,7 and 8, feedwater pipeline 9, steam-pipe 10 and 11, replenishes spray water pipeline 12, effluxes spray water pipeline 13 and water circulating pump 14; Raw gas intake ducting 6 connects one-level spray cooler 1 opening for feed, the corresponding connection of tube side opening for feed of the centre exit place duct type of one-level spray cooler 1 and one-level waste heat boiler 3, the bottom of one-level spray cooler 1 are shaped on outlet and efflux spray water pipeline 13 and be communicated with; The tube side outlet of one-level waste heat boiler 3 is communicated with secondary spray cooler 4 pipelines; The top inlet of one-level spray cooler 1 and secondary spray cooler 4 is connected with tank 2 by recycle pump 14 duct types; Secondary spray cooler 4, I and II waste heat boiler 3,5 lower part outlets duct type respectively connect tank 2; The centre exit place of secondary spray cooler 4 is communicated with the tube side opening for feed place duct type of secondary waste heat boiler 5; I and II waste heat boiler 3 and 5 shell side ingress are connected with feedwater pipeline 9 respectively by pipeline, and the shell side outlet is connected with the steam-pipe 10 that has pressure respectively by pipeline; The water inlet of tank 2 is shaped on and replenishes spray water pipeline 12.
In the present embodiment implementation process, the raw gas that comes out from the coal gasification stove enters one-level spray cooler 1 through raw gas pipeline 6, and by the spray water washing cooling from tank 2, the condensed water in the one-level spray cooler 1 is discharged system handles from the bottom; Cooled raw gas enters one-level waste heat boiler 3, the feedwater heating and gasifying that will enter by feedwater pipeline 8, the raw gas of output one-level waste heat boiler 3 enters secondary spray cooler 4 through raw gas pipeline 7, by spray water washing cooling from tank 2, the cooled raw gas of secondary enters secondary waste heat boiler 5, the feedwater heating and gasifying that will enter by feedwater pipeline 9; The raw gas of output secondary waste heat boiler 5 enters subsequent handling processing through raw gas pipeline 8; The steam that gasification produces in steam that gasification produces in the one-level waste heat boiler 3 and the secondary waste heat boiler 5 enters the steam pipe system of corresponding pressure respectively through steam-pipe 10 and 11; Condensed water in secondary spray cooler 4 and I and II waste heat boiler 3 and 5 is drained in the tank 2 by lower part outlet duct type separately and recycles.
A practical application example of present embodiment: production capacity be 35000 marks upright/hour Lurgi gasifier, residual neat recovering system originally can by-product goes out 22 tons/hour of the steam of 0.5MPa; After its residual neat recovering system being pressed the workflow reengineering of accompanying drawing 1, tapping temperature be 570 ℃ raw gas after the one-level spray cooler is cooled to 250 ℃, enter the one-level waste heat boiler, by-product goes out 8 tons/hour of the steam of 1.5MPa; The raw gas that goes out the one-level waste heat boiler enters the secondary spray cooler, be cooled to 190 ℃ after, enter the secondary waste heat boiler, by-product goes out 12.5 tons/hour of the steam of 0.5MPa; The steam of transforming the 1.5MPa of back residual neat recovering system recovery is used for the phenol retrieving arrangement, and each hour can be saved 7.8 tons of 4.0MPa steam.
Claims (2)
1. improved Lurgi gasifier exhaust heat recovering method, it is characterized in that adopting the two-stage waste heat boiler to realize waste heat recovery, after earlier the raw gas of coming out of the stove in the coal gasification process being used rare phenol water spray from rare phenol tank to be cooled to 200-270 ℃ in the one-level spray cooler, enter first step waste heat boiler, the oiler feed of raw gas heating shell side in first step waste heat boiler again, the steam of generation pressure 0.8-1.5MPa; The raw gas that goes out first step waste heat boiler is cooled to 160-210 ℃ with rare phenol water spray in the secondary spray cooler after, enter second stage waste heat boiler, the oiler feed of raw gas heating shell side in the waste heat boiler of the second stage, producing pressure is the steam of 0.3-0.8MPa; The raw gas that comes out from the coal gasification stove enters the one-level spray cooler through the raw gas pipeline, the spray water washing cooling that is come from tank, and the condensed water in the one-level spray cooler is discharged system handles from the bottom; Cooled raw gas enters the one-level waste heat boiler, the feedwater heating and gasifying that will enter by the feedwater pipeline, the raw gas of output one-level waste heat boiler enters the secondary spray cooler through the raw gas pipeline, the spray water washing cooling that is come from tank, the cooled raw gas of secondary enters the secondary waste heat boiler, the feedwater heating and gasifying that will enter by the feedwater pipeline; The raw gas of output secondary waste heat boiler enters subsequent handling processing through the raw gas pipeline; The steam that gasification produces in steam that gasification produces in the one-level waste heat boiler and the secondary waste heat boiler enters the steam pipe system of corresponding pressure respectively through steam-pipe; Condensed water in secondary spray cooler and the I and II waste heat boiler is drained in the tank by lower part outlet duct type separately and recycles.
2. the device that improved Lurgi gasifier exhaust heat recovering method as claimed in claim 1 relates to is characterized in that the device main body structure comprises one-level waste heat boiler, secondary waste heat boiler, one-level spray cooler, secondary spray cooler, tank, raw gas intake ducting, feedwater pipeline, steam-pipe, replenishes the spray water pipeline, effluxes spray water pipeline and water circulating pump; The raw gas intake ducting connects one-level spray cooler opening for feed, the corresponding connection of tube side opening for feed of the centre exit place duct type of one-level spray cooler and one-level waste heat boiler, and the bottom of one-level spray cooler is shaped on and exports and efflux the spray water pipeline and be communicated with; The tube side outlet of one-level waste heat boiler is communicated with secondary spray cooler pipeline; The top inlet of one-level spray cooler and secondary spray cooler is connected with tank by the water circulating pump duct type; Secondary spray cooler, I and II waste heat boiler lower part outlet duct type respectively connect tank; The centre exit place of secondary spray cooler is communicated with the tube side opening for feed place duct type of secondary waste heat boiler; The shell side ingress of I and II waste heat boiler is connected with the feedwater pipeline respectively by pipeline, and the shell side outlet is connected with the steam-pipe that has pressure respectively by pipeline; The water inlet of tank is shaped on and replenishes the spray water pipeline.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2011100926482A CN102199453B (en) | 2011-04-01 | 2011-04-01 | Improved Lurgi gasification furnace waste heat recovering method and device |
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| CN2011100926482A CN102199453B (en) | 2011-04-01 | 2011-04-01 | Improved Lurgi gasification furnace waste heat recovering method and device |
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| CN102199453B CN102199453B (en) | 2013-05-08 |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102585916A (en) * | 2011-12-29 | 2012-07-18 | 武汉凯迪工程技术研究总院有限公司 | Biomass synthesized gas negative pressure purifying process method and system configuration for producing oil |
| CN102604685A (en) * | 2011-12-29 | 2012-07-25 | 武汉凯迪工程技术研究总院有限公司 | Biomass synthesis gas positive pressure purification process and system configuration for oil production |
| CN103265979A (en) * | 2013-06-03 | 2013-08-28 | 武汉凯迪工程技术研究总院有限公司 | Technology and device for cooling and purifying high-temperature and high-pressure biomass synthesis gas |
| CN104893762A (en) * | 2015-06-15 | 2015-09-09 | 林兆晟 | Raw gas ash handling system |
| CN106753589A (en) * | 2016-12-07 | 2017-05-31 | 广西北海浩邦新能源科技有限公司 | Charing fuel gas handling process |
| CN113865365A (en) * | 2021-10-26 | 2021-12-31 | 四川恩特普环保科技有限公司 | Waste heat recovery system of titanium factory |
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| CN101614498A (en) * | 2008-06-26 | 2009-12-30 | 上海梅山钢铁股份有限公司 | Raw coke over gas riser residual heat recovery device |
| CN101768474A (en) * | 2010-02-05 | 2010-07-07 | 刘金成 | Waste heat recovery process for high-temperature rough gas of entrained flow bed |
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2011
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN201242165Y (en) * | 2008-06-11 | 2009-05-20 | 周士友 | Two-stage vertical gas making blowing heat recovery device |
| CN101614498A (en) * | 2008-06-26 | 2009-12-30 | 上海梅山钢铁股份有限公司 | Raw coke over gas riser residual heat recovery device |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102585916A (en) * | 2011-12-29 | 2012-07-18 | 武汉凯迪工程技术研究总院有限公司 | Biomass synthesized gas negative pressure purifying process method and system configuration for producing oil |
| CN102604685A (en) * | 2011-12-29 | 2012-07-25 | 武汉凯迪工程技术研究总院有限公司 | Biomass synthesis gas positive pressure purification process and system configuration for oil production |
| CN102604685B (en) * | 2011-12-29 | 2014-11-26 | 武汉凯迪工程技术研究总院有限公司 | Biomass synthesis gas positive pressure purification process and system configuration for oil production |
| CN103265979A (en) * | 2013-06-03 | 2013-08-28 | 武汉凯迪工程技术研究总院有限公司 | Technology and device for cooling and purifying high-temperature and high-pressure biomass synthesis gas |
| CN103265979B (en) * | 2013-06-03 | 2015-04-08 | 武汉凯迪工程技术研究总院有限公司 | Technology and device for cooling and purifying high-temperature and high-pressure biomass synthesis gas |
| CN104893762A (en) * | 2015-06-15 | 2015-09-09 | 林兆晟 | Raw gas ash handling system |
| CN104893762B (en) * | 2015-06-15 | 2017-07-14 | 林兆晟 | Raw gas ash disposal system |
| CN106753589A (en) * | 2016-12-07 | 2017-05-31 | 广西北海浩邦新能源科技有限公司 | Charing fuel gas handling process |
| CN113865365A (en) * | 2021-10-26 | 2021-12-31 | 四川恩特普环保科技有限公司 | Waste heat recovery system of titanium factory |
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