CN102559283A - Recycling process of coal gas waste heat - Google Patents
Recycling process of coal gas waste heat Download PDFInfo
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- CN102559283A CN102559283A CN2011100943882A CN201110094388A CN102559283A CN 102559283 A CN102559283 A CN 102559283A CN 2011100943882 A CN2011100943882 A CN 2011100943882A CN 201110094388 A CN201110094388 A CN 201110094388A CN 102559283 A CN102559283 A CN 102559283A
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- 239000003034 coal gas Substances 0.000 title claims abstract description 65
- 239000002918 waste heat Substances 0.000 title abstract description 31
- 238000000034 method Methods 0.000 title abstract description 18
- 230000008569 process Effects 0.000 title abstract description 18
- 238000004064 recycling Methods 0.000 title abstract 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 93
- 239000007789 gas Substances 0.000 claims description 64
- 238000011084 recovery Methods 0.000 claims description 43
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 40
- 239000001301 oxygen Substances 0.000 claims description 40
- 229910052760 oxygen Inorganic materials 0.000 claims description 40
- 239000003245 coal Substances 0.000 claims description 31
- 238000005516 engineering process Methods 0.000 claims description 30
- 238000005406 washing Methods 0.000 claims description 24
- 239000007921 spray Substances 0.000 claims description 19
- 238000001179 sorption measurement Methods 0.000 claims description 16
- 238000010276 construction Methods 0.000 claims description 10
- 239000007788 liquid Substances 0.000 claims description 9
- 239000000945 filler Substances 0.000 claims description 8
- 239000003595 mist Substances 0.000 claims description 8
- 238000002156 mixing Methods 0.000 claims description 8
- 150000002989 phenols Chemical class 0.000 claims description 8
- 238000005204 segregation Methods 0.000 claims description 7
- 239000000463 material Substances 0.000 claims description 6
- 230000008439 repair process Effects 0.000 claims description 4
- 238000001704 evaporation Methods 0.000 claims description 3
- 230000008020 evaporation Effects 0.000 claims description 3
- 238000005194 fractionation Methods 0.000 claims description 3
- 230000008676 import Effects 0.000 claims description 3
- 150000002894 organic compounds Chemical class 0.000 claims description 3
- 238000009792 diffusion process Methods 0.000 claims description 2
- 230000010412 perfusion Effects 0.000 claims description 2
- 238000002309 gasification Methods 0.000 abstract description 24
- 239000002994 raw material Substances 0.000 abstract description 13
- 239000010865 sewage Substances 0.000 abstract description 7
- 239000006227 byproduct Substances 0.000 abstract 1
- 230000003247 decreasing effect Effects 0.000 abstract 1
- 239000002912 waste gas Substances 0.000 abstract 1
- 239000002351 wastewater Substances 0.000 abstract 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 20
- 229910021529 ammonia Inorganic materials 0.000 description 10
- 239000003921 oil Substances 0.000 description 8
- 239000002956 ash Substances 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 7
- 230000004927 fusion Effects 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 238000001816 cooling Methods 0.000 description 6
- 239000003077 lignite Substances 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 5
- 235000009508 confectionery Nutrition 0.000 description 5
- 238000000354 decomposition reaction Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 239000003345 natural gas Substances 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 229920006395 saturated elastomer Polymers 0.000 description 4
- 239000008234 soft water Substances 0.000 description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 238000000197 pyrolysis Methods 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 238000003786 synthesis reaction Methods 0.000 description 3
- OAKJQQAXSVQMHS-UHFFFAOYSA-N Hydrazine Chemical compound NN OAKJQQAXSVQMHS-UHFFFAOYSA-N 0.000 description 2
- 239000010883 coal ash Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000002594 sorbent Substances 0.000 description 2
- 239000011269 tar Substances 0.000 description 2
- 241000282326 Felis catus Species 0.000 description 1
- 206010019332 Heat exhaustion Diseases 0.000 description 1
- 206010021143 Hypoxia Diseases 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- -1 anaerobic (18) flow Chemical compound 0.000 description 1
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 1
- 239000003830 anthracite Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 235000011089 carbon dioxide Nutrition 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 208000018875 hypoxemia Diseases 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 238000004900 laundering Methods 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 238000001465 metallisation Methods 0.000 description 1
- 230000036284 oxygen consumption Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000010729 system oil Substances 0.000 description 1
- 239000003643 water by type 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
-
- 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 provides a recycling process of coal gas waste gas, belonging to the field of heat exchange, and particularly relates to a recycling process of the coal gas waste heat gasified by a pressure moving bed. For an existing pressure moving bed, when being used for recycling the coal gas waste heat, the coal gas waste heat is recovered as low-pressure steam by a waste heat boiler and cannot be taken as raw material water steam, so that the gasification costs are increased. According tho the invention, the recycling process of coal gas waste heat consists of a high-pressure mass transfer and heat transfer device (34), a low-pressure mass transfer and heat transfer device (14), a heat exchanger (49), a power recycling device (31), a recycling hot water pressure pump (23), a pressure machine (16), pipelines and the like, the existing coal gas waste heat recycling process is optimized, the coal gas recycling process is adopted in a recycling process of the coal gas waste heat gasified by the pressure moving bed, so that external supply steam consumption steam can be reduced dramatically, the coal gas sewage amount and the coal gas waste water processing expenses can be decreased greatly, the output of high value-added byproducts such as tar and the like can be increased, and the gasification cost of the moving pressure bed are better lowered.
Description
Technical field
The invention belongs to the heat exchange field, the moving-bed gasification technology of particularly pressurizeing, the Technology device and the flow process of coal gas waste heat recovery.
Background technology
As everyone knows, coal inhibition and generation sintetics is like H
2, NH
3, CH
4, CH
3OH, wet goods etc. adopt the pressurization moving-bed to carry out gasification, not only have the minimum advantage of unit raw gas oxygen consumption, but also have the advantage of the various feed coals that can adopt relatively inexpensive high moisture content, ash-rich.
Yet, because the top temperature of pressurization when moving the gasification of coal in the pool furnace, must be less than or equal to the ash fusion point temperature of feed stock for blast furnace coal.The feed coal ash fusion point that has is at 1200 ℃, and the feed coal ash fusion point that has then can reach 1500 ℃.Because the principal reaction of gasification is C+H
2O=CO+H
2, strong endothermic reaction, its chemical reaction equilibrium constant is directly proportional with temperature of reaction, and promptly gasification temperature is high more, and the equilibrium constant is big more, and resultant is many more, and steam decomposition rate is high more, and steam utilization is high more, and the gasification cost is just low more.Design the broken coal moving-bed pressure gasification process of 3.0MPa pressure at present, steam decomposition rate is usually 20~40%.
When adopting moisture content up to 40%, ash fusion point is at 1200 ℃ coal, or ash fusion point is used for coal gasification reaction C+H when being lower than 1100 ℃ coal and being raw material
2O=CO+H
2With CO transformationreation CO+H
2O=CO
2+ H
2Steam resolution ratio, be merely furnace bottom and go into more than 30% of the total vapour quantity of stove, if add brown coal dryer section in vapourizing furnace water vapor that is evaporated, then total steam decomposition rate is merely about 20%.Cause steam in the discharged producer gas up to about 55% thus.
When coals such as adopting low moisture content, high ash melting point meager lean coal, clean fine coal is raw material, though be used for C+H
2O=CO+H
2And CO+H
2O=CO
2+ H
2The gasification steam decomposition rate can reach nearly 40%.Because when the gasification temperature is lower than 700 ℃; Not only chemical reaction receives kinetic control, and chemical reaction rate is low, and the equilibrium constant is low; Steam decomposition rate is low; With feed coal in stove inner drying layer water evaporation less, the destructive distillation product is few in the destructive distillation layer, heat exhaustion is few, thus the temperature that makes discharged producer gas is up to more than 600 ℃.For the equipment such as coal supply apparatus that prevent the furnace retaining top are damaged by high temperature, also often take in stove, to spray water and reduce the discharged producer gas temperature.
Moreover, be raw material even adopt anthracite, meager lean coal, because pressurized gasification pressure is much higher more than atmospheric gasification, the tar and the dust of some amount arranged still in the destructive distillation product.So before the waste heat recovery of coal gas or cooling, all must spray water to coal gas, carry out preliminary dedusting cooling, significantly to reduce tar and the dust in the coal gas, make coal gas have 100% humidity condition.Otherwise the tar in the coal gas will seriously reduce the heat exchange effect attached to heat-exchange equipments such as the useless pot surface in flow process downstream.Therefore; 3.0MPa broken coal moving-bed pressure gasification process coal gas come out of the stove after; No matter whether reclaim the coal gas waste heat, all at first water sprays cooling, washing to coal gas of high temperature, make gas temperature drop to behind the water spray about 200 ℃ of dew-point temperatures; Moisture content in its wet gas also reaches more than 50%, carries out the recovery of waste heat or directly cooling again.
The retrieving arrangement of existing pressurization moving-bed coal gas waste heat is to adopt waste heat boiler the waste heat in about 3.0 coal gas of pressure to be converted into the low-pressure saturated steam of 0.5MPa pressure shown in 139 pages of accompanying drawing 1 and Chemical Industry Press's " synthesis gas process technology and DM " first versions in 2002.The high pressure coal that is rich in 50~60%% left and right sides saturated vapors is made leave with rage in the pipe, and pipe is outer for being heated the boiler soft water that produces steam, and its steam is generally used for the need of other technology.Because this LP steam output is very big, almost reaches the quantity suitable with the steam in the boiler total amount, because pressure is too low, can not remake the raw water steam of using for gasification, utility value is low, thereby has increased coal gas and products thereof cost greatly.
As adopt pressurization moving-bed gasification technology, be raw material production synthetic ammonia raw gas with meager lean coal, clean fine coal.Ton ammonia also needs the extra 3.8MPa that provides, 400 ℃ of MP steam 1600kg, oxygen 520Nm except that consuming vapourizing furnace jacket steam 800kg
3, raw material mark coal 1300kg; Produce gas sewage 2700kg, the 0.5MPa of ton ammonia coal gas waste heat recovery simultaneously low-pressure saturated steam 2300kg, ton ammonia consumes the soft water total amount and reaches 5 tons.Supply steam cost just to reach 160 yuan so that MP steam 100 yuan, ton ammonia per ton are only outer, produce 300000 tons of synthesis ammonia plants per year, annual 4800 ten thousand yuan of the steam costs that increase.
As adopt pressurization moving-bed gasification technology, be the raw material production synthetic natural gas with the brown coal of water content about 40%.Per 1000 mark side's gas products consume except that the about 1000kg of jacket steam; Also need the outer 3.8MPa of confession, 400 ℃ of MP steams reach 2000kg, oxygen 480Nm3, calorific value 13.44MJ (3210 kilocalories) raw material brown coal 4000kg; Produce about gas sewage 3000kg; The coal gas waste heat of per 1000 mark side's Sweet natural gases reclaims 0.5MPa low-pressure saturated steam 2500kg simultaneously, consumes the soft water total amount and reaches 6 tons.Supply steam cost to reach 200 yuan outward with 100 yuan of MP steams per ton, per 1000 mark side's Sweet natural gases, produce the gas works of 10 billion cubic meters per year, annual 200000000 yuan of the steam costs that increase.
In view of the deficiency of existing coal gas waste heat reclaiming process, improved coal gas heat recovery technology was given perfect below this case proposed.
Summary of the invention
1. coal gas heat recovery technology; Constitute by mass-and heat-transfer equipment, separator and pipeline; It is characterized in that, by spray washing water cooler (2), adsorption tower (2A) and (2B), high pressure mass-and heat-transfer equipment (34), power recovery device (31), low pressure mass-and heat-transfer equipment (14), circulating hot water force (forcing) pump (23), press (16), mixing tank (2C), interchanger (49), oxygenous matter (13), the CO of recommending
2Recommend matter (18) and the pipeline mutual group becomes coal gas heat recovery technology etc. no oxygen.
2. coal gas heat recovery technology according to claim 1 is characterized in that, is provided with first in the low pressure mass-and heat-transfer equipment (14) and puies forward vapour section (14A) and second and carry vapour section (14B) and mist segregation section (14C); Low-voltage high-temperature recirculated water (32) is gone into tower by mist segregation section (14C) bottom, and the oxygenous matter (13) of recommending is carried vapour section (14A) bottom by first and gone into tower, CO
2Recommending matter (18) etc. no oxygen carries vapour section (14B) bottom by second and goes into tower; The gas-liquid counter current contact is through evaporation of water diffusion gas water lift steam; Oxygenous concentration expressed in percentage by volume a:0.5%>=a≤100% of recommending oxygen in the matter (13), CO
2Recommend volumetric concentration<0.5% of oxygen in the matter (18) etc. no oxygen; Oxygenous flow and the CO that recommends matter (13)
2Ratio etc. no oxygen such as anaerobic (18) flow is 0~10.
3. coal gas heat recovery technology according to claim 1; It is characterized in that; Adopt the water at low temperature recirculated water (24A) of circulating hot water force (forcing) pump (23) outlet; Behind the heat in the coal gas of high temperature water (40A) that contains pitch coal air water (40), regenerative process desorb water (58) that entering interchanger (49) recovery spray washing water cooler (2) is discharged, cold cycle hot water (24) is in high pressure mass-and heat-transfer equipment (34), with high temperature wet gas (3A) counter current contact; After absorbing the heat in the wet gas, become the high temperature circulation water (25) that tower.
4. coal gas heat recovery technology according to claim 1; It is characterized in that; High pressure mass-and heat-transfer equipment (34) internals, low pressure mass-and heat-transfer equipment (14) internals adopt vertical sieve tray structure or valve tray structure or eddy flow plate structure or filling-material structure or board-like internals last, filler under unitized construction or board-like internals down; Filler is in last unitized construction, or rotation filling-material structure or rotation plank frame or rotate board-like filled unitized construction.
5. coal gas heat recovery technology according to claim 1; It is characterized in that; Gas-liquid counter current washing section (47) employing vertical sieve tray structure or valve tray structure or eddy flow plate structure or filling-material structure or board-like internals are set last in the spray washing water cooler (2); Filler under unitized construction or board-like internals down, filler is in last unitized construction.
6. coal gas heat recovery technology according to claim 1 is characterized in that, adopts adsorption tower (2A) and (2B) fractionation by adsorption in turn, and spray washing water cooler (2) exports macromolecular organic compounds such as part tar in the wet gas, oil, crude phenols; Press regenerate in turn adsorption tower (2A) and (2B) of superheated vapour (57) in the employing; The water that regenerative process desorbs, tar, oil, crude phenols, water vapor (58) get into mixing tank (2C) dissolving, import among the coal gas of high temperature water (40); Oil-containing gas liquor (45) row of the coal gas of high temperature water (40A) of mixing tank (2C) outlet after interchanger (49) reduces temperature is to the tar recovery process.
7. coal gas heat recovery technology according to claim 1 is characterized in that, press (16) is spiral-lobe compressor or axial compressor or turbo-compressor or piston compressor or mixed flow compressor.
8. coal gas heat recovery technology according to claim 1 is characterized in that, power recovery device (31) be axial-flow type hydraulic turbine or perfusion type hydraulic turbine or mixed-flow hydraulic turbine or centrifugal hydraulic turbine,
Adopt the foregoing invention content; Pressurization moving-bed gasification technology; When high moisture content brown coal with moisture 40% or clean fine coal or other coal are products such as raw material production Sweet natural gas; Infeed the stove steam consumption outside not only can subtracting all, also can send jacket steam 100t/h outside, reduce the gas making sewage treatment capacity more than 60%.
Top in the spray washing water cooler (2); Gas-liquid counter current washing section (47) is set; And adopt spray washing cooling makeup water line (35) to send here; Tar, phenol content are than circulation cleaning water much less, and major cycle hot water not only reduces tar, phenol, ammonia, particle concentration in the wet gas that gets into high pressure mass-and heat-transfer equipment (34) as the bath water of countercurrent washing section; And then minimizing gets into tar, phenol, ammonia, particle concentration in the vaporized chemical, the tar, phenol, the hydrazine yield that also increase are had high added value.
Especially adsorption tower (2A), (2B) temperature swing adsorption process; Separate macromolecular organic compounds such as part tar, oil, crude phenols in the coal gas; Both reduced through circulating hot water finally getting into the combustiblematerials components such as tar in the low pressure gas water lift steam (15), reclaimed combustiblematerials components such as tar through steam regeneration again.
Adopt interchanger (49); Heat in the high-temperature wash gas liquor (40) that spray washing water cooler (2) is discharged, the regeneration desorb water (58) that adsorption tower is discharged; Transfer in the low-temperature water heating (24) through high-temperature wash gas liquor (40A); Not only increase gas water lift steam (15) yield, avoided employing CO again
2Directly gas improves the steam in the temperature laundering gas liquor (40), and comhustible components such as the tar that brings get into the possibility of recovered steam, have also reduced the loss of high added value products such as tar.
In low pressure mass-and heat-transfer equipment (14), be provided with first put forward vapour section (14A) and second and carry vapour section (14B) and mist segregation section (14C) after, have the following advantages:
The oxygenous matter (13) of recommending is carried vapour section (14A) bottom by first and is gone into tower, and carries the CO that contains that vapour section (14B) comes up from second
2Recommend the steam of matter (18) etc. no oxygen after, will reduce the dividing potential drop of oxygen-containing gas, especially oxygen greatly, dissolve in its quantity of oxygen in the recirculated water thereby reduce;
CO
2Recommend matter (18) and carry vapour section (14B) bottom by second and go into tower etc. no oxygen, not only annoying proposition is dissolved in the minor amounts of oxygen in the recirculated water, reduces the quantity that oxygen finally gets into coal gas, and no oxygen is recommended matter (18) and the oxygenous matter of recommending
(13) be present in first jointly and carry in the vapour section (14A), will help reducing the dividing potential drop of gas phase water vapor, and increase the output of gas water lift steam (15);
Owing to export tolerance greater than many times of import tolerance at low pressure mass-and heat-transfer equipment (14); Outlet steam mist entrainment can not ignore; Mist segregation section (14C) is set on tower top, both can makes full use of the cat head space, minimizing equipment and pipeline; Recyclable again liquid separated also can reduce investment and occupation of land.
The oxygenous adjusting of volumetric concentration between 0.5~100% of recommending oxygen in the matter (13), the feed coal that can satisfy different ash fusion points to steam oxygen ratio demand;
Oxygenous flow and the CO that recommends matter (13)
2Etc. the adjusting of ratio between 0~10 of no oxygen such as anaerobic (18) flow, can satisfy end product to the ratio of carbon-hydrogen CO in the coal gas: H
2Demand;
Adopting the present invention, is raw material with moisture nearly 40% brown coal, produces the production line of 400 ten thousand stere Sweet natural gases daily, and annual 3000000 tons of the outer confession steam of practicing thrift reduce 3,000,000 tons of gas making sewages, reduce by 1,500 ten thousand yuan of cost of sewage disposal.
Pressurization moving-bed gasification technology, clean fine coal is a raw material production synthetic ammonia.When adopting inventing type to reclaim the coal gas waste heat, can reduce by 80% outer confession steam consumption, reduce by 75% gas making sewage treatment capacity.Produce 300000 tons of synthesis ammonia plants per year, annual 750000 tons of 520,000 tons of minimizings of the outer confession steam gas making sewages of practicing thrift.
97 lurgi pressure gasifier stoves of the Sa Suoer company in South Africa, the lurgi pressure gasifier that promptly is commonly called as usually, year 4300 ten thousand tons of long-flame coals of consumption; Produce 7500000 tons of fuel oils per year,, per hour can reduce outer 2000 tons of the steam that supply if this technology is adopted in its coal gas waste heat recovery; Can practice thrift 2,500,000 tons in mark coal the whole year; 5,000,000 tons of reducing emission of carbon dioxide, annual 2400 ten thousand tons of the gas sewages that reduce reduce cost 200,000,000 dollars every year.
The present invention is adopted in the coal gas waste heat recovery of a lurgi pressure gasifier surplus the following whole world 1000, will have the energy-saving and environmental protection and the economic benefit of 10 times Sasol.
The present invention adds the broken coal moving-bed in utilization and calms the anger on the basis of hypoxemia consumption and available any feed coal of metallization processes; Successfully solved the difficult problem that steam utilization is low, the gas sewage amount is huge, the water resources consumption is big, for China and global a new generation is that raw material system oil and gas or the like gasification chemical industry provides crucial technical support with the coal.
The present invention also can be used for the waste heat recovery of grace producer gas, the coal gas waste heat recovery of the coal gas waste heat recovery of normal pressure moving-bed oxygen enrichment coal generating gas and fluidized bed coal gasification.
Description of drawings
Accompanying drawing 1, existing moving-bed pressure gasifying gas waste-heat recovery device synoptic diagram.
Accompanying drawing 2 adopts the wall-type heat exchange mode to improve circulation warm water's coal gas waste-heat recovery device synoptic diagram.
Accompanying drawing 3, the undecomposed vapor recovery of gasification of the present invention is utilized process schematic representation
Among the figure:
1 heating gas pipeline from gas furnace;
2 coal gas spray washing condensing surfaces;
2A adsorption tower and sorbent material;
2B adsorption tower and sorbent material
The 2C mixing tank
The cooled gas line of 3 washings;
The 3A fractionation by adsorption high temperature wet gas and the pipeline behind the organic macromolecules such as gaseous state tar, oil, crude phenols class partly;
The gas-liquid separation section of 4 waste heat boiler bottoms;
5 reclaim the waste heat boiler of heat;
5a reclaims the recuperator of heat;
6 are recovered heat, the gas line after temperature reduces;
7 add the soft water pipeline of waste heat boiler;
8 waste heat boilers reclaim the pipeline of heat output LP steam;
9 gas condensed waters and pipeline;
10 water circulating pumps;
High-temperature wash water and pipeline after 11 pressurizations;
High-temperature wash water and pipeline behind the 12 washing coal gas;
13 oxygen or oxygen-rich air or nitrogen or CO from oxygenerator
2Gas and pipeline;
The adverse current low pressure mass-and heat-transfer equipment that 14 employing gas-liquids directly contact, effect is that the heat in the hot water is converted into oxygen or oxygen-rich air or nitrogen or CO
2In steam;
14A low pressure mass-and heat-transfer equipment first is put forward the vapour section;
14B low pressure mass-and heat-transfer equipment second is put forward the vapour section;
14C mist segregation section;
15 low pressure gas water lift steam and pipelines;
16 press, effect are that the steam oxygen mixed gas is added to the pressure that can get into gas furnace;
17 high-pressure water vapor pipelines are that the steam gas after the pressurization is recommended the matter mixed gas in the pipe;
18 oxygenless gas, carbonic acid gas or nitrogen pipeline;
19 deoxidation towers, effect are that gas is carried the oxygen that separates dissolving in the hot water, carries secretly;
20 carry oxygen pipeline, are the gas that gas has been carried the oxygen in the hot water in the pipe, are no oxygen (N
2, CO
2Deng), water vapor, oxygen three's mixed gas;
21 cold cycle hot water line;
22 cold cycle hot water and pipelines;
23 circulating hot water force (forcing) pumps;
Cold cycle hot water and pipeline after 24 pressurizations;
24A circulating hot water force (forcing) pump (23) outlet low-temperature circulating water and pipeline;
After heat temperature in the 25 receipts heat coal gas raises, high pressure-temperature circulating hot water and pipeline;
26 power steam pipelines;
27 turbine, effect provides the tool ability for press, and small-sized power also can adopt motor;
28 exhaust steam in steam turbine pipelines, steam devaporation condensing works in the pipe;
31 power recovery devices;
32 low-voltage high-temperature recirculated water and pipelines;
33 power compensation motors (also can be other motive power machine equipment);
The high pressure mass-and heat-transfer equipment that 34 employing gas-liquids directly contact;
35 spray washings cooling makeup water line;
36 from chuck or boiler or the shared vapour line of the two mixing;
37 oxygen pipelines from oxygenerator;
38 vapourizing furnaces;
39 qualified vaporized chemical pipelines;
The 40 high-temperature wash gas liquor and the pipelines that efflux;
40A dissolving, the high-temperature wash gas liquor and the pipeline of desorb water, tar, oil, crude phenols, water vapor have been imported;
44 replenish and to contain phenol gas liquor pipeline after the oils such as removing tar;
45 contain the pipeline of pitch coal air water row to the tar recovery process;
The countercurrent washing section that 47 spray washing water cooler internal upper parts are set up;
49 interchanger;
53 vapourizing furnace chuck drums;
54 vapourizing furnace chuck self-produced steam and pipelines;
55 self-produced steams are mended steam and the pipeline into vaporized chemical house steward (17);
56 self-produced steams are sent steam and pipeline outside;
57 superheated vapours and pipeline;
58 desorb water, tar, oil, crude phenols, water vapor and pipeline;
59 non-condensable gases and pipeline.
Embodiment
Below with Lower heat value 13.44MJ/kg, moisture 40% high moisture content, the brown coal raw material 645t/h that ash fusion point is 1200 ℃ adopts broken coal moving-bed pressure gasification process, and steam oxygen ratio is 6, CO
2/ O
2=1, total steam oxygen ratio is 7, and the process capability of producing 4,000,000 side's Sweet natural gases daily is an example, explains and uses the significant parameter that the present invention reclaims the embodiment of coal gas waste heat:
Wet gas total amount: 1,420,000 Nm
3/ h; 230 ℃ of temperature; Vapour content 53%; Pressure 3.0MPa.
Amount of oxygen: 83000Nm
3/ h; Pressure 1.6MPa.
CO
2Total amount: 83000Nm
3/ h; Pressure 1.6MPa.
Static equipment: high pressure mass-and heat-transfer equipment 1 cover;
Low pressure mass-and heat-transfer equipment 1 cover.
Alternating temperature adsorption tower one cover.
Spray washing water cooler one cover that contains the countercurrent washing section.
Rotating machinery: power recovery turbo 1 cover;
Circulating hot-water pump 1 cover;
Steam turbine drives or electronic press 1 cover.
Power consumption: 3.82MPa, 435 ℃ of power steam 200t/h.
10KV electrical source of power 900kw.
3.82MPa, 435 ℃ of steam steam are used in adsorption tower regeneration:
10t/h
Recovered steam :~480t/h.
Send 3.0MPa chuck saturation steam outside:
80t/h。
Claims (8)
1. coal gas heat recovery technology; Constitute by mass-and heat-transfer equipment, pipeline etc.; It is characterized in that, by spray washing water cooler (2), adsorption tower (2A) and (2B), high pressure mass-and heat-transfer equipment (34), power recovery device (31), low pressure mass-and heat-transfer equipment (14), circulating hot water force (forcing) pump (23), press (16), mixing tank (2C), interchanger (49), oxygenous matter (13), the CO of recommending
2Recommend matter (18) and the pipeline mutual group becomes coal gas heat recovery technology etc. no oxygen.
2. coal gas heat recovery technology according to claim 1 is characterized in that, is provided with first in the low pressure mass-and heat-transfer equipment (14) and puies forward vapour section (14A) and second and carry vapour section (14B) and mist segregation section (14C); Low-voltage high-temperature recirculated water (32) is gone into tower by mist segregation section (14C) bottom, and the oxygenous matter (13) of recommending is carried vapour section (14A) bottom by first and gone into tower, CO
2Recommending matter (18) etc. no oxygen carries vapour section (14B) bottom by second and goes into tower; The gas-liquid counter current contact is through evaporation of water diffusion gas water lift steam; Oxygenous concentration expressed in percentage by volume a:0.5%>=a≤100% of recommending oxygen in the matter (13), CO
2Recommend volumetric concentration<0.5% of oxygen in the matter (18) etc. no oxygen; Oxygenous flow and the CO that recommends matter (13)
2Ratio etc. no oxygen such as anaerobic (18) flow is 0~10.
3. coal gas heat recovery technology according to claim 1; It is characterized in that; Adopt the water at low temperature recirculated water (24A) of circulating hot water force (forcing) pump (23) outlet; Behind the heat in the coal gas of high temperature water (40A) that contains pitch coal air water (40), regenerative process desorb water (58) that entering interchanger (49) recovery spray washing water cooler (2) is discharged, cold cycle hot water (24) is in high pressure mass-and heat-transfer equipment (34), with high temperature wet gas (3A) counter current contact; After absorbing the heat in the wet gas, become the high temperature circulation water (25) that tower.
4. coal gas heat recovery technology according to claim 1; It is characterized in that; High pressure mass-and heat-transfer equipment (34) internals, low pressure mass-and heat-transfer equipment (14) internals adopt vertical sieve tray structure or valve tray structure or eddy flow plate structure or filling-material structure or board-like internals last, filler under unitized construction or board-like internals down; Filler is in last unitized construction, or rotation filling-material structure or rotation plank frame or rotate board-like filled unitized construction.
5. coal gas heat recovery technology according to claim 1; It is characterized in that; Gas-liquid counter current washing section (47) employing vertical sieve tray structure or valve tray structure or eddy flow plate structure or filling-material structure or board-like internals are set last in the spray washing water cooler (2); Filler under unitized construction or board-like internals down, filler is in last unitized construction.
6. coal gas heat recovery technology according to claim 1 is characterized in that, adopts adsorption tower (2A) and (2B) fractionation by adsorption in turn, and spray washing water cooler (2) exports macromolecular organic compounds such as part tar in the wet gas, oil, crude phenols; Press regenerate in turn adsorption tower (2A) and (2B) of superheated vapour (57) in the employing; The water that regenerative process desorbs, tar, oil, crude phenols, water vapor (58) get into mixing tank (2C) dissolving, import among the coal gas of high temperature water (40); Oil-containing gas liquor (45) row of the coal gas of high temperature water (40A) of mixing tank (2C) outlet after interchanger (49) reduces temperature is to the tar recovery process.
7. coal gas heat recovery technology according to claim 1 is characterized in that, press (16) is spiral-lobe compressor or axial compressor or turbo-compressor or piston compressor or mixed flow compressor.
8. coal gas heat recovery technology according to claim 1 is characterized in that, power recovery device (31) is axial-flow type hydraulic turbine or perfusion type hydraulic turbine or mixed-flow hydraulic turbine or centrifugal hydraulic turbine.
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CN105462617A (en) * | 2015-12-01 | 2016-04-06 | 大唐国际化工技术研究院有限公司 | Equipment and method for preparing superheated steam required by moving bed gasification furnace |
CN110467943A (en) * | 2018-05-11 | 2019-11-19 | 成都聚实节能科技有限公司 | A kind of natural gas from coal, alkene and coal tar method |
CN110628477A (en) * | 2019-09-20 | 2019-12-31 | 成都聚实节能科技有限公司 | Pressurized moving bed multi-layer hydrogenation coal-to-natural gas co-production method of fuel oil and aromatics |
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