CN103980946A - No-emission anthracite segmented pyrolysis and upgrading utilization method and no-emission anthracite segmented pyrolysis and upgrading utilization device - Google Patents
No-emission anthracite segmented pyrolysis and upgrading utilization method and no-emission anthracite segmented pyrolysis and upgrading utilization device Download PDFInfo
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- CN103980946A CN103980946A CN201410212243.1A CN201410212243A CN103980946A CN 103980946 A CN103980946 A CN 103980946A CN 201410212243 A CN201410212243 A CN 201410212243A CN 103980946 A CN103980946 A CN 103980946A
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- light oil
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 115
- 238000000034 method Methods 0.000 title claims abstract description 44
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 title claims abstract description 10
- 239000003830 anthracite Substances 0.000 title claims abstract description 10
- 239000007789 gas Substances 0.000 claims abstract description 152
- 238000002309 gasification Methods 0.000 claims abstract description 108
- 239000003921 oil Substances 0.000 claims abstract description 73
- 239000003245 coal Substances 0.000 claims abstract description 60
- 239000000295 fuel oil Substances 0.000 claims abstract description 44
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 18
- 239000000428 dust Substances 0.000 claims abstract description 17
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims abstract description 16
- 239000000571 coke Substances 0.000 claims abstract description 16
- 239000000126 substance Substances 0.000 claims abstract description 15
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N phenol group Chemical group C1(=CC=CC=C1)O ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims abstract description 7
- 239000000470 constituent Substances 0.000 claims description 44
- KSSNXJHPEFVKHY-UHFFFAOYSA-N phenol;hydrate Chemical compound O.OC1=CC=CC=C1 KSSNXJHPEFVKHY-UHFFFAOYSA-N 0.000 claims description 27
- 238000005406 washing Methods 0.000 claims description 24
- 230000011218 segmentation Effects 0.000 claims description 17
- 229910052799 carbon Inorganic materials 0.000 claims description 10
- 239000000203 mixture Substances 0.000 claims description 9
- 230000008676 import Effects 0.000 claims description 8
- 239000002918 waste heat Substances 0.000 claims description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 6
- 239000003034 coal gas Substances 0.000 claims description 6
- 230000003247 decreasing effect Effects 0.000 claims description 6
- 229910052760 oxygen Inorganic materials 0.000 claims description 6
- 239000001301 oxygen Substances 0.000 claims description 6
- 239000007921 spray Substances 0.000 claims description 6
- 238000002156 mixing Methods 0.000 claims description 5
- 239000002826 coolant Substances 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 3
- 239000004484 Briquette Substances 0.000 claims description 2
- 238000011084 recovery Methods 0.000 claims description 2
- 238000005516 engineering process Methods 0.000 abstract description 9
- 239000003795 chemical substances by application Substances 0.000 abstract 2
- 239000003949 liquefied natural gas Substances 0.000 abstract 2
- 239000000498 cooling water Substances 0.000 abstract 1
- 230000008569 process Effects 0.000 description 17
- 239000002994 raw material Substances 0.000 description 10
- 238000012545 processing Methods 0.000 description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 7
- 239000007787 solid Substances 0.000 description 5
- 238000000746 purification Methods 0.000 description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 235000011089 carbon dioxide Nutrition 0.000 description 3
- 238000009826 distribution Methods 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 238000009413 insulation Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 238000006722 reduction reaction Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000003912 environmental pollution Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 210000000003 hoof Anatomy 0.000 description 2
- 238000005984 hydrogenation reaction Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 238000011001 backwashing Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000002817 coal dust Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- 230000021715 photosynthesis, light harvesting Effects 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000009290 primary effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000006479 redox reaction Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000008234 soft water Substances 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Classifications
-
- 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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- Industrial Gases (AREA)
Abstract
The invention relates to a no-emission segmented pyrolysis and upgrading utilization method and a no-emission segmented pyrolysis and upgrading utilization device. According to the method, CO2, pure oxygen and superheated steam are taken as gasifying agents, and the gasifying agents and coke generated by the anthracite are gasified in a coal gasification pyrolyzing furnace so as to produce gasified gas; the gasified gas is mixed with a light oil component generated by a low-temperature pyrolysis section and a heavy oil component generated by a high-temperature pyrolysis section so as to form raw gas; the raw gas sequentially enters a cyclone dust collector and a sensible heat recoverer so that the dust is removed through centrifuging and the heat is recycled; then the raw gas enters a tar recoverer to remove the heavy oil component and the light oil component; the raw gas enters an intercooler so as to be cooled by circulating cooling water and washed to separate out phenolic water; finally, trace light oil component of the raw gas is removed again by an electric fishing light oil device, and high-quality synthetic gas is obtained. The content of CO and H2 in the synthetic gas reaches over 80%, the synthetic gas can be converted and purified to prepare chemical products such as oil and LNG (liquefied natural gas), and the separated heavy oil component, the light oil component and phenolic water can be recycled, so that the no-emission coal segmented pyrolysis and upgrading utilization method is a new energy technology.
Description
Technical field
The invention belongs to coal pyrolysis technology field, be specifically related to a kind of hard coal segmentation pyrolysis sub-prime without discharge and utilize method and device.
Background technology
At present, existing pure oxygen continuous gasification process is generally taking secondary metallurgical, carbonic acid gas, pure oxygen as gasified raw material, and at high temperature, red-hot carbon and carbonic acid gas generation redox reaction are produced raw gas (CO:68～70%, CO
2: 28～29%, H
2+ N
2: 1～1.2%), then through the synthetic relevant derived product of the synthetic gas purifying, conversion preparation is qualified.But, quite high (fugitive constituent 1% left and right of ingredient requirement that this technique is used, fixed carbon 82.5% left and right, the burnt standard of country's secondary), cost is high (the burnt market price 1800-2000 yuan/ton of secondary, and interior ground of low-rank coal 500-700 yuan/ton) also, and importantly existing producing in coal gas technological process cannot obtain heavy oil component, light oil constituents, make it can not be recovered utilization, thereby raw material can not be fully utilized.
Present stage, China's atmospheric gasification technique was all taking hard coal as main, due to technologic defect, cause the conversion efficiency of carbon content in coal low, after gasification, in lime-ash, the content of carbon residue is higher, generally, between 8-15%, carbon residue content when fluctuation appears in technique in lime-ash can be higher.At present atmospheric gasification mainly contains air+steam and two kinds of techniques of oxygen enrichment+steam, and in these two kinds of techniques, effective gas content of gasification gas is all lower, generally all below 75%, also has a small amount of pyrolysis product, but all do not recycle in gasification.These pyrolysis products are processed as waste gas in follow-up gas sweetening operation, and follow-up gas purification treatment process is brought to larger negative impact.
At present, any gasifying process all can be attended by CO
2the generation of gas, current technique be all through after after operation separating treatment or to another one device, recycle, or to airborne release, cause environmental pollution, energy dissipation.Outstanding along with environmental problem, CO
2emission reduction work is particularly important, how to optimize gasifying process, reduces CO
2generation, realize CO
2recycling will be one of important development direction of China's environmental technology.
Summary of the invention
Technical problem to be solved by this invention is to provide a kind of hard coal segmentation pyrolysis sub-prime without discharge and utilizes method and device, obtains CO and H
2content reaches more than 80% high-quality natural gas and synthetic gas, and reclaims heavy oil component, light oil constituents, phenol water in hard coal, realizes heavy oil component, light oil constituents, phenol water and separates with raw gas, the object of utilizing to reach hard coal pyrolysis sub-prime.
Mentality of designing of the present invention is: taking hard coal as feed coal, with CO
2, pure oxygen and superheated vapour be vaporized chemical, specifically utilizes CO
2, the pure oxygen novel pure oxygen continuous gasification process that enters continuously stove after mixing with superheated vapour from gasification pyrolysis oven bottom comes pyrolysis, gasifying smokeless coal, obtain raw gas, realize raw material coal grading utilization through dedusting, separation etc. again, not only widened raw material sources, and the present invention adopts CO
2for vaporized chemical, break through the high drawback of pure oxygen gasification process costs, also can from raw gas, separate and reclaim heavy oil component, light oil constituents, phenol water, make hard coal obtain utilizing more fully.
In order to solve the problems of the technologies described above, the technical solution used in the present invention is as follows:
Hard coal segmentation pyrolysis sub-prime without discharge is utilized a method, comprises the steps:
(1) hard coal is added to gasification pyrolysis oven, in stove, layer and section carries out pyrolysis, gasification; Gasification pyrolysis oven comprises low temperature pyrogenation section, high temperature pyrolysis section, gasification section; Hard coal by pyrolysis, generates light oil constituents and semicoke in low temperature pyrogenation section, and semicoke enters high temperature pyrolysis section, and is generated heavy oil component and coke by high temperature pyrolysis, and coke enters gasification section;
By CO
2, 99.6% purity oxygen and superheated vapour enter stove continuously from gasification pyrolysis oven bottom after mixing, and react generation gasification gas in stove in gasification section with the reverse coke generating gasification entering; On gasification gas, be advanced into high temperature pyrolysis section, directly the semicoke in high temperature pyrolysis section carried out to high temperature pyrolysis, generate heavy oil component and coke; Heavy oil component and gasification gas enter low temperature pyrogenation section, and the gas mixture of final heavy oil component, light oil constituents and gasification gas is that raw gas shifts out gasification pyrolysis oven;
(2) raw gas that step (1) obtains is centrifuged dedusting, temperature≤550 DEG C of raw gas after dedusting; Then entering waste-heat recovery device, reclaim sensible heat of raw gas, raw gas temperature is down to≤and 320 DEG C;
(3) utilize method de-oiling, the dedusting of recirculated water spray washing through the raw gas of step (2) dedusting, heat recuperation, remove heavy oil component, light oil constituents wherein, decreasing ratio >=99% of heavy oil component+light oil constituents, isolated heavy oil component, light oil constituents enter tar groove with recirculated water and recycle;
(4) raw gas that removes heavy oil component, light oil constituents that step (3) obtains is recycled water coolant and is indirectly cooled to≤and 40 DEG C; Meanwhile, utilize washing pump closed cycle washing to isolate the phenol water in raw gas, isolated phenol water enters phenol tank and recycles;
(5) by step (4) through cooling, remove coal gas that phenol water obtains through the de-oiling of electric fishing light oil device, dedusting, remove wherein micro-light oil constituents, make final heavy oil component+light oil constituents decreasing ratio >=99.9%, obtain the synthetic gas of high-quality, isolated light oil constituents enters tar light oil groove and recycles.
In addition, described step (1) Raw consumption is: hard coal 610～645kg/kNm
3(CO+H
2) (every generation 1000Nm
3(CO+H
2) available gas needs 610～645kg hard coal, lower same), superheated vapour 250～285kg/kNm
3(CO+H
2), purity oxygen 330～360Nm
3/ kNm
3(CO+H
2), CO
2135～145Nm
3/ kNm
3(CO+H
2).
Again, in described step (1), gasification pyrolysis oven furnace pressure is 10～20KPa, and in stove, layer and section carries out pyrolysis, gasification, and low temperature pyrogenation section temperature is 550～750 DEG C, high temperature pyrolysis section temperature is 750～1050 DEG C, and in stove, gasification section temperature is 1050～1300 DEG C.
Again, anthracitic thermal value >=5500Kcal/kg described in described step (1).
Preferably, described in step (1), hard coal is anthracite block coal or anthracite briquette.
Without a hard coal segmentation pyrolysis sub-prime use device for discharge, comprising:
Gasification pyrolysis oven, it is provided with and is positioned at the vaporized chemical import of bottom and the discharge outlet being communicated with stove low temperature pyrogenation section, and wherein, vaporized chemical import connects CO by pipeline
2, pure oxygen and superheated vapour mixture source of the gas;
Heat reclaim unit, comprises tornado dust collector and sensible heat recoverer; The inlet mouth of described tornado dust collector connects the discharge outlet of gasification pyrolysis oven by pipeline, described sensible heat recoverer is provided with gas inlet, gas exit, and the gas inlet of described sensible heat recoverer connects the air outlet of tornado dust collector by pipeline;
Tar withdrawer, the tar outlet that it is provided with gas entry, clean gas outlet and is positioned at bottom, the gas entry of tar withdrawer is connected with the gas exit of sensible heat recoverer by pipeline;
Inter cooler, its underpart is provided with phenol water out; The entrance of described inter cooler is connected with the clean gas outlet of tar withdrawer by pipeline, and the tower reactor of described inter cooler connects into circulation loop by pipeline and a washing pump;
Electric fishing light oil device, the light oil outlet that it is provided with gas entry, gas exit and is positioned at bottom, the gas entry of electric fishing light oil device is connected with the outlet of inter cooler, the gas exit connecting conveying pipe road of electric fishing light oil device.
Preferably, described gasification pyrolysis oven is layer and section formula gasification pyrolysis oven.
Further, described tar withdrawer is spray-type washing tower, by low-temperature circulating water, raw gas is carried out to spray washing, and primary effect is to reduce raw gas temperature, ensures more than 99% light oil constituents liquefaction; Next utilizes the mode of spray washing that the gas solid matter that goes out tornado dust collector is separated, to remove light oil constituents, heavy oil component and a small amount of solid dust in raw gas.
Described sensible heat recoverer is waste heat boiler.
Working process of the present invention is as follows: from raw materials pretreatment operation come stone coal through belt conveyor from gasification pyrolysis oven upper feeding storehouse, timing adds gasification pyrolysis oven by the control of hydraulic program valve by feed coal, at low temperature pyrogenation section feed coal by pyrolysis, generate light oil constituents and semicoke, semicoke enters high temperature pyrolysis section; By CO
2, 99.6% purity oxygen and superheated vapour enter stove continuously from gasification pyrolysis oven bottom after mixing, and react generation gasification gas in stove in gasification section with the reverse coke generating gasification entering; On gasification gas, be advanced into high temperature pyrolysis section, directly the semicoke in high temperature pyrolysis section carried out to high temperature pyrolysis, generate coke and heavy oil component, heavy oil component and gasification gas enter low temperature pyrogenation section in the lump; Final heavy oil component, light oil constituents and gasification gas shift out gasification pyrolysis oven in the lump.
The raw gas that gasification pyrolysis oven generates, from the discharge outlet of gasification pyrolysis oven is discharged, enters tornado dust collector and carries out dedusting, mainly isolates the solid particulate matters such as coal dust in the discharge raw gas of pyrolytic gasification stove; Entered sensible heat recoverer by the raw gas after dedusting and carry out heat recuperation, then entering tar withdrawer by the gas entry of tar withdrawer utilizes the method for recirculated water spray washing to carry out de-oiling, dedusting, then escape and enter inter cooler from the clean gas outlet of tar withdrawer, the isolated heavy oil component of tar withdrawer and light oil constituents enter tar groove by the tar outlet that is positioned at bottom and recycle; Raw gas enters and is recycled water coolant after inter cooler and is indirectly cooled to≤and 40 DEG C, meanwhile, wash phenol water is wherein isolated by closed cycle, and reclaim micro-light oil constituents through electric fishing light oil device, and then obtain the synthetic gas of high-quality of the present invention.
The synthetic gas composition of the high-quality that the present invention prepares is: CO>=35%, H
2>=45%, CO
2≤ 18%, CO and H
2content can reach more than 80%, further closes gas produce the Chemicals such as oil, LNG through techniques such as conversion, purifications.
The present invention is first with CO
2for vaporized chemical, enter in the lump gasification pyrolysis oven with pure oxygen, steam, in gasification section generation reduction reaction, generate available gas CO, reaction equation: CO
2+ C=2CO-165KJ, is greatly reducing CO
2when discharge, realize comprehensive utilization of resources, turned waste into wealth, protected environment.
The present invention rationally utilizes gasification sensible heat; realize the layer and section pyrolysis sub-prime in gasification pyrolysis oven; in sub-prime process, protect to greatest extent the molecular structure of light oil constituents and heavy oil component; the sub-prime utilization of light oil constituents that content is lower and heavy oil component is maximized, thereby reach the object of anthracitic comprehensive utilization, high added value.From raw gas, separating the heavy oil component and the light oil constituents that obtain just can meet the need of market through simple hydrogenation upgrading.The present invention is through closed cycle washing isolated phenol water from raw gas, and entering phenol tank can be recycled.Visible, no waste exhaust gas emission of the present invention, has avoided contaminate environment, has reduced unfavorable factors such as building separately exhaust gas processing device increase investment, is a kind of environmentally friendly coal comprehensive utilization, Gasification Polygeneration System technique.
Of the present invention compact to design without gasification pyrolysis oven and follow-up cleaning apparatus, sensible heat recoverer, tar withdrawer etc. in the hard coal segmentation pyrolysis sub-prime use device of discharge, all can adopt commercially available equipment, material is easily purchased, can realize and in raw gas, extract heavy oil component, light oil constituents, isolate the functions such as phenol water, gas solid separation, realize anthracitic sub-prime utilization, realize high additive value, reach efficient energy-saving, fully utilize the object of effective energy.
Beneficial effect of the present invention:
1. the present invention is with CO
2, pure oxygen and vapour mixture are vaporized chemical, adopt pure oxygen continuous gasification technology, steam decomposition rate is high, resultant quantity is greater than other atmospheric fixed bed gasifying process, form rational sensible heat amount vector, meet reasonable heat dispersing, rationally set up the effect in each responding layer district, make gasification pyrolysis oven Nei Geshu district heat distribution high in middle and lower part temperature, the rational deployment that two ends temperature is low, raw gas is produced in this strengthening gasification that is highly advantageous to, also formed that steam decomposes under hot conditions and the gasification condition of carbonic acid gas fast restore, improved the thermo-efficiency that gasification pyrolysis oven is produced simultaneously,
2. with respect to traditional coke gasification production line, the present invention is an innovation at the lower pure oxygen gasification hard coal of low pressure condition (10～20KPa), in reaction process, energy consumption is low, to have flow process short, non-environmental-pollution, raw material availability is high, high production, quality better, comprehensive utilization ratio advantages of higher, this is a kind of advanced technologies in the comprehensive utilization of coal;
3. the present invention adopts 99.6% pure oxygen, has greatly improved smokeless coal gasification rate, makes lime-ash remaining carbon≤2% of gasification pyrolysis oven discharge, has significantly reduced raw material consumption, has improved feedstock conversion utilization ratio;
4. effectively reduce latent heat losses and sensible heat loss, improve gasification pyrolysis oven heat trans-utilization rate, cold gas efficiency reaches 80～82%, protection of the environment;
5. the present invention has widened the raw material route of coal gasification, and adopting hard coal is gasified raw material coal, and feed coal is not had to very special quality requirement;
6. the present invention has realized anthracitic time processing comprehensive utilization, realize kerosene comprehensive utilization of separation, and the washing water of non-exhaust emission, washing phenol water adopt closed cycle in process of production, realize the zero release of the three wastes, it is a kind of environmentally friendly novel process, belong to clean coal gasification technology, meet national low-carbon environment-friendly industry policy and Strategy of Circular Economy thinking of development completely.
7. the present invention is by CO
2gasify as vaporized chemical, be converted into CO available gas, there is significant environmental benefit and economic benefit, belong to carbon emission reduction technology.
Brief description of the drawings
Fig. 1 is the structural representation of one embodiment of the invention.
Embodiment
Below in conjunction with specific embodiment, technical scheme of the present invention is described in further detail, but content of the present invention is not limited to this.In the following example, do not indicate the experimental technique of actual conditions, conventionally according to normal condition, or the condition of advising according to manufacturer.
Referring to Fig. 1, the hard coal segmentation pyrolysis sub-prime use device without discharge of the present invention, comprising:
Gasification pyrolysis oven 1, it is provided with and is positioned at the vaporized chemical import 11 of bottom and the discharge outlet 12 being communicated with stove pyrolysis section, and wherein, vaporized chemical import 11 connects CO by pipeline
2, pure oxygen and superheated vapour mixture source of the gas;
Heat reclaim unit, comprises tornado dust collector 2 and sensible heat recoverer 3; The inlet mouth 21 of described tornado dust collector 2 connects the discharge outlet 12 of gasification pyrolysis oven 1 by pipeline, described sensible heat recoverer 3 is provided with gas inlet 31, gas exit 32, and the gas inlet 31 of described sensible heat recoverer 3 connects the air outlet 22 of tornado dust collector 2 by pipeline;
Tar withdrawer 4, the tar outlet 43 that it is provided with gas entry 41, clean gas outlet 42 and is positioned at bottom, the gas entry 41 of tar withdrawer 4 is connected with the gas exit 32 of sensible heat recoverer 3 by pipeline;
Inter cooler 5, its underpart is provided with phenol water out 51; The entrance of described inter cooler 5 is connected with the clean gas outlet 42 of tar withdrawer 4 by pipeline; The tower reactor of described inter cooler 5 connects into a circulation loop by pipeline and valve and a washing pump 6;
Electric fishing light oil device 7, described electric fishing light oil device 7 is provided with gas entry 71, gas exit 72 and is positioned at the light oil outlet 73 of bottom, and the gas entry 71 of electric fishing light oil device 7 is connected with the outlet of inter cooler 5, the gas exit 72 connecting conveying pipe roads of electric fishing light oil device 7.
In the present embodiment, described gasification pyrolysis oven 1 is layer and section formula gasification pyrolysis oven.
Described tar withdrawer 4 is spray-type washing tower.Described sensible heat recoverer 3 is waste heat boiler.
The present embodiment appointed condition used is as follows:
1, gasification pyrolysis oven 1 is layer and section formula gasification pyrolysis oven:
Device parameter:
Diameter: Φ 2740mm
Equipment total height: 10750mm
Low temperature pyrogenation section height: 1000mm
The heat insulation mode of low temperature pyrogenation section: plastic pouring material
High temperature pyrolysis section height: 1500mm
The heat insulation mode of high temperature pyrolysis section: middle pressure water wall
Gasification section height: 5000mm
The heat insulation mode of gasification section: middle pressure water wall
Low temperature and high temperature pyrolysis section equipment connection mode: welded type
Structure formation: vertical barrel type
Support pattern: upper support
Deslagging mode: solid continuous discharging slag
Processing parameter:
Operating pressure: 20KPa
Gasification temperature: 1050-1300 DEG C
Feed coal treatment capacity: 3090Kg/h
Vapor temperature: 250 DEG C
Steam consumption: 1368Kg/h
CO
2temperature: 100 DEG C
CO
2consumption: 696m
3/ h
2, tornado dust collector 2:
Device parameter:
Diameter: Φ 1600mm
Highly: 9430mm
Separator cartridge diameter: Φ 1000mm
Separator cartridge height: 1200mm
Equipment importation diameter: Φ 1000mm
Equipment exit diameter: Φ 800mm
Processing parameter:
Import raw gas temperature: 550 DEG C
Outlet raw gas coal powder density: 80mg/Nm
3
3, sensible heat recoverer 3 is waste heat boiler:
Device parameter:
Diameter: Φ 2600mm
Highly: 19000mm
Superheat section diameter: Φ 2000mm
Superheat section heat interchanging area: 300m
2
Steam segment diameter: Φ 2000mm
Steam segment heat interchanging area: 1400m
2
Heat exchange mode: heat pipe-type
Processing parameter:
Process tolerance: 8000Nm
3/ h
Gas inlet temperature: 550 DEG C
Gas outlet temperature: 320 DEG C
Soft water temperature: 32 DEG C
By-product superheat steam temperature: 220 DEG C
By-product superheated vapour pressure: 0.5MPa
Tower body resistance drop: 300Pa
4, tar withdrawer 4 is spray-type washing tower:
Device parameter:
Diameter: Φ 3200mm
Highly: 12500mm
The shower nozzle distribution number of plies: 5 layers
Nozzle type: the shape of a hoof
Nozzle layout of sprinkler mode: crisscross formula
Demister pattern: rotary vane type
Processing parameter:
Process tolerance: 8000Nm
3/ h
Gas outlet temperature: 50 DEG C
Inflow temperature: 32 DEG C
Return water temperature: 40 DEG C
Tower body resistance drop: 5KPa
5, inter cooler 5:
Device parameter:
Diameter: Φ 3000mm
Highly: 12000mm
The shower nozzle distribution number of plies: 3 layers
Nozzle type: the shape of a hoof
Nozzle layout of sprinkler mode: crisscross formula
Heat transfer tube diameter: Φ 25mm
Processing parameter:
Process tolerance: 7000Nm
3/ h
Gas outlet temperature: 30 DEG C
Inflow temperature: 15 DEG C
Return water temperature: 25 DEG C
Tower body resistance drop: 2KPa
6, electric fishing light oil device 7:
Device parameter:
Diameter: Φ 3000mm
Highly: 13000mm
Pole plate length: 6000mm
Processing parameter:
Process tolerance: 7000Nm
3/ h
Gas outlet temperature: 30 DEG C
Backwashing time interval: 24h
Tower body resistance drop: 40Pa
Voltage: 380V
Coal segmentation pyrolysis sub-prime without discharge of the present invention is utilized method, comprises the steps:
The present embodiment gasification pyrolysis oven used is specially a layer and section formula gasification pyrolysis oven simultaneously with low temperature pyrogenation, high temperature pyrolysis and gasification function.Gasification pyrolysis oven comprises low temperature pyrogenation section, high temperature pyrolysis section and gasification section from top to down.Low temperature pyrogenation section temperature is 550～750 DEG C, and high temperature pyrolysis section temperature is 750～1050 DEG C, and in stove, gasification section temperature is 1050～1300 DEG C.
(1) the 3090Kg/h anthracite block coal coming from raw materials pretreatment operation is through belt conveyor from gasification pyrolysis oven 1 upper feeding storehouse, and timing enters furnace gas by hydraulic program valve control coal, and gasification pyrolysis oven furnace pressure is 20KPa.
Anthracite block coal typical case ature of coal: carbon content: 70%～85%, fugitive constituent :≤10%, calorific value is 5500～8000Kcal/kg approximately.
Anthracite block coal by pyrolysis, generates light oil constituents and semicoke in low temperature pyrogenation section, and semicoke enters high temperature pyrolysis section, and is generated heavy oil component and coke by high temperature pyrolysis, and coke enters gasification section; From the 1728Nm of empty operation break-down
3the 696Nm that/h99.6% pure oxygen, rear workshop section come
3/ h CO
2enter continuously stove with the vaporized chemical import 11 that from coal gas 1 bottom occurs after boiler overheating 1368Kg/h vapor mixing, the coke generating gasification generating with the reverse high temperature pyrolysis section entering in gasification section in stove is reacted and is generated gasification gas; On gasification gas, be advanced into high temperature pyrolysis section, directly the semicoke in high temperature pyrolysis section carried out to high temperature pyrolysis, generate heavy oil component and coke; Heavy oil component and gasification gas enter low temperature pyrogenation section, and the gas mixture of final heavy oil component, light oil constituents and gasification gas is that raw gas is discharged from the discharge outlet 12 of gasification pyrolysis oven 1.
(2) raw gas carries out gas purification processing: the raw gas of discharging from gasification pyrolysis oven 1 enters tornado dust collector 2 by the inlet mouth 21 of described tornado dust collector 2 and carries out centrifugal dust-removing, temperature≤550 DEG C of raw gas after dedusting; Then after dedusting, raw gas enters sensible heat recoverer 3 by the gas inlet 31 of sensible heat recoverer 3 and is recovered sensible heat wherein, and gas temperature is down to below 320 DEG C.
(3) entering tar withdrawer 4 through the gas entry 41 of tar withdrawer 4 again through the raw gas of dedusting, heat recuperation utilizes the method for recirculated water spray washing to carry out de-oiling, dedusting, remove heavy oil component, light oil constituents wherein, decreasing ratio >=99% of heavy oil component and light oil constituents, isolated heavy oil component, light oil constituents enter tar groove 401 from the tar outlet 43 of tar withdrawer 4 bottoms and recycle, and the raw gas that removes heavy oil component, light oil constituents enters inter cooler 5 from the clean gas outlet 42 of tar withdrawer 4.
(4) raw gas that enters inter cooler 5 is recycled water coolant and is indirectly cooled to below 40 DEG C; Meanwhile, utilize washing pump 6 closed cycles washings to isolate the phenol water in raw gas, isolated phenol water flows out from the phenol water out 51 of inter cooler 5, and enters phenol tank 501 and recycle.
(5) in the present embodiment, open control valve 100, closed control valve 200, to discharge by the gas entry 71 of electric fishing light oil device 7 and enter electric fishing light oil device 7 from inter cooler 5 with coal gas that remove after phenol water through indirectly cooling, remove again micro-light oil constituents, make final heavy oil component+light oil constituents decreasing ratio >=99.9%, obtain the synthetic gas of high-quality of the present invention, be delivered to user from gas exit 72 through pipeline and use.Isolated light oil constituents on the lenient side oil export 73 enters light oil groove 701 and recycles.
The high-quality synthetic gas composition of the present embodiment gained is: CO:35%, H
2: 45%, CO
2: 18%, single stove aerogenesis 6000Nm
3/ h.
The high-quality synthetic gas that the present invention obtains further closes gas through techniques such as conversion, purifications and produces the Chemicals such as oil, LNG.
In step (3), (5), from raw gas, separating the heavy oil component, the light oil constituents that obtain just can meet the need of market through simple hydrogenation upgrading.The raw gas that step (3) obtains enters inter cooler, under the effect of washing pump, through closed cycle washing isolated phenol water from raw gas, entering phenol tank can be recycled, specifically can adopt existing phenol water vapo(u)rization system, separate unit gasification pyrolysis oven configures a set of phenol water vapo(u)rization system, adopt phenol water evaporating heat exchanger evaporation phenol water to generate phenol water vapor, in the situation that realizing heat exchange function, can evaporate the phenol water that gasification pyrolysis oven produces, both utilize the waste heat of hypomere coal gas, avoided again contaminate environment.
Claims (9)
1. utilize a method without the hard coal segmentation pyrolysis sub-prime of discharge, comprise the steps:
1) hard coal is added to gasification pyrolysis oven, in stove, layer and section carries out pyrolysis, gasification; Gasification pyrolysis oven comprises low temperature pyrogenation section, high temperature pyrolysis section, gasification section; Hard coal by pyrolysis, generates light oil constituents and semicoke in low temperature pyrogenation section; Semicoke enters high temperature pyrolysis section, and is generated heavy oil component and coke by high temperature pyrolysis, and coke enters gasification section;
By CO
2, 99.6% purity oxygen and superheated vapour enter stove continuously from gasification pyrolysis oven bottom after mixing, and react generation gasification gas in gasification section with the reverse coke generating gasification entering; On gasification gas, be advanced into high temperature pyrolysis section, directly the semicoke in high temperature pyrolysis section carried out to high temperature pyrolysis, generate heavy oil component and coke; Heavy oil component and gasification gas enter low temperature pyrogenation section, and the gas mixture of final heavy oil component, light oil constituents and gasification gas is that raw gas shifts out gasification pyrolysis oven;
2) step 1) raw gas that obtains is centrifuged dedusting, temperature≤550 DEG C of raw gas after dedusting; Then entering waste-heat recovery device, reclaim sensible heat of raw gas, raw gas temperature is down to≤and 320 DEG C;
3) through step 2) raw gas of dedusting, heat recuperation utilizes method de-oiling, the dedusting of recirculated water spray washing, remove heavy oil component, light oil constituents wherein, decreasing ratio >=99% of heavy oil component+light oil constituents, isolated heavy oil component, light oil constituents enter tar groove with recirculated water and recycle;
4) step 3) raw gas that removes heavy oil component, light oil constituents that obtains is recycled water coolant and is indirectly cooled to≤and 40 DEG C; Meanwhile, utilize washing pump closed cycle washing to isolate the phenol water in raw gas, isolated phenol water enters phenol tank and recycles;
5) by step 4) through cooling, remove coal gas that phenol water obtains through the de-oiling of electric fishing light oil device, dedusting, remove wherein micro-light oil constituents, make final heavy oil component+light oil constituents decreasing ratio >=99.9%, thereby obtain the synthetic gas of high-quality, isolated light oil constituents enters tar light oil groove and recycles.
2. the hard coal segmentation pyrolysis sub-prime without discharge according to claim 1 is utilized method, it is characterized in that step 1) Raw consumption is: hard coal 610～645kg/kNm
3(CO+H
2), superheated vapour 250～285kg/kNm
3(CO+H
2), purity oxygen 330～360Nm
3/ kNm
3(CO+H
2), CO
2135～145Nm
3/ kNm
3(CO+H
2).
According to claim 1 without discharge hard coal segmentation pyrolysis sub-prime utilize method, it is characterized in that step 1) described in anthracitic thermal value >=5000Kcal/kg.
According to described in claim 1 or 2 or 3 without discharge hard coal segmentation pyrolysis sub-prime utilize method, it is characterized in that step 1) described in hard coal be anthracite block coal or anthracite briquette.
5. the hard coal segmentation pyrolysis sub-prime without discharge according to claim 1 is utilized method, it is characterized in that, step 1) in gasification pyrolysis oven furnace pressure be 10～20KPa, low temperature pyrogenation section temperature is 550～750 DEG C, high temperature pyrolysis section temperature is 750～1050 DEG C, and in stove, gasification section temperature is 1050～1300 DEG C.
6. without a hard coal segmentation pyrolysis sub-prime use device for discharge, it is characterized in that, comprise,
Gasification pyrolysis oven, it is provided with and is positioned at the vaporized chemical import of bottom and the discharge outlet being communicated with stove low temperature pyrogenation section, and wherein, vaporized chemical import connects CO by pipeline
2, pure oxygen and superheated vapour mixture source of the gas;
Heat reclaim unit, comprises tornado dust collector and sensible heat recoverer; The inlet mouth of described tornado dust collector connects the discharge outlet of gasification pyrolysis oven by pipeline, described sensible heat recoverer is provided with gas inlet, gas exit, and the gas inlet of described sensible heat recoverer connects the air outlet of tornado dust collector by pipeline;
Tar withdrawer, the tar outlet that it is provided with gas entry, clean gas outlet and is positioned at bottom, the gas entry of tar withdrawer is connected with the gas exit of sensible heat recoverer by pipeline;
Inter cooler, its underpart is provided with phenol water out; The entrance of described inter cooler is connected with the clean gas outlet of tar withdrawer by pipeline, and the tower reactor of described inter cooler connects into circulation loop by pipeline and a washing pump;
Electric fishing light oil device, the light oil outlet that it is provided with gas entry, gas exit and is positioned at bottom, the gas entry of electric fishing light oil device is connected with the outlet of inter cooler, the gas exit connecting conveying pipe road of electric fishing light oil device.
7. the hard coal segmentation pyrolysis sub-prime use device without discharge according to claim 6, is characterized in that, described gasification pyrolysis oven is layer and section formula gasification pyrolysis oven.
8. the hard coal segmentation pyrolysis sub-prime use device without discharge according to claim 6, is characterized in that, described tar withdrawer is spray-type washing tower.
9. the hard coal segmentation pyrolysis sub-prime use device without discharge according to claim 6, is characterized in that, described sensible heat recoverer is waste heat boiler.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104785016A (en) * | 2015-04-10 | 2015-07-22 | 陕西煤业化工集团神木天元化工有限公司 | Dedusting agent as well as process and device for coal pyrolysis gas dedusting with dedusting agent |
| CN105779023A (en) * | 2016-04-19 | 2016-07-20 | 华能国际电力股份有限公司 | Pyrolysis gas waste heat recovering system and method |
| CN107475798A (en) * | 2017-08-07 | 2017-12-15 | 海南大学 | A kind of nano-fiber material for the extraction of uranium from seawater and preparation method thereof |
| CN111718737A (en) * | 2020-06-29 | 2020-09-29 | 中国科学院过程工程研究所 | Process method and system device for preparing high-quality oil gas by pyrolyzing low-caking coal |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5064444A (en) * | 1986-10-16 | 1991-11-12 | Bergwerksverband Gmbh | Process for the allothermic gasification of coal |
| DK175601B1 (en) * | 1997-04-22 | 2004-12-20 | Kjeld Nicolajsen | Preparing a gasification gas for bio-fuel - comprises contacting flow of fuel with counter flow of gas generated by burning coal or hydrocarbon fuel in e.g. power station or boiler |
| CN102465043A (en) * | 2010-11-01 | 2012-05-23 | 中国科学院过程工程研究所 | Multi-section fractional pyrolysis gasification device and method for solid fuel |
| CN202482281U (en) * | 2011-12-31 | 2012-10-10 | 李叔锟 | Two-step method pulverized coal fluidized gasification device |
| CN203065417U (en) * | 2012-12-31 | 2013-07-17 | 焦作市汇力机械制造有限公司 | Three-section authigenic flow guide groove type continuous pyrolysis gasification furnace for bulk rubbish combustible material |
| CN204022766U (en) * | 2014-05-19 | 2014-12-17 | 昊华骏化集团有限公司 | A kind of hard coal segmentation pyrolysis sub-prime use device without discharge |
-
2014
- 2014-05-19 CN CN201410212243.1A patent/CN103980946B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5064444A (en) * | 1986-10-16 | 1991-11-12 | Bergwerksverband Gmbh | Process for the allothermic gasification of coal |
| DK175601B1 (en) * | 1997-04-22 | 2004-12-20 | Kjeld Nicolajsen | Preparing a gasification gas for bio-fuel - comprises contacting flow of fuel with counter flow of gas generated by burning coal or hydrocarbon fuel in e.g. power station or boiler |
| CN102465043A (en) * | 2010-11-01 | 2012-05-23 | 中国科学院过程工程研究所 | Multi-section fractional pyrolysis gasification device and method for solid fuel |
| CN202482281U (en) * | 2011-12-31 | 2012-10-10 | 李叔锟 | Two-step method pulverized coal fluidized gasification device |
| CN203065417U (en) * | 2012-12-31 | 2013-07-17 | 焦作市汇力机械制造有限公司 | Three-section authigenic flow guide groove type continuous pyrolysis gasification furnace for bulk rubbish combustible material |
| CN204022766U (en) * | 2014-05-19 | 2014-12-17 | 昊华骏化集团有限公司 | A kind of hard coal segmentation pyrolysis sub-prime use device without discharge |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104785016A (en) * | 2015-04-10 | 2015-07-22 | 陕西煤业化工集团神木天元化工有限公司 | Dedusting agent as well as process and device for coal pyrolysis gas dedusting with dedusting agent |
| CN105779023A (en) * | 2016-04-19 | 2016-07-20 | 华能国际电力股份有限公司 | Pyrolysis gas waste heat recovering system and method |
| CN107475798A (en) * | 2017-08-07 | 2017-12-15 | 海南大学 | A kind of nano-fiber material for the extraction of uranium from seawater and preparation method thereof |
| CN111718737A (en) * | 2020-06-29 | 2020-09-29 | 中国科学院过程工程研究所 | Process method and system device for preparing high-quality oil gas by pyrolyzing low-caking coal |
| CN111718737B (en) * | 2020-06-29 | 2021-07-09 | 中国科学院过程工程研究所 | Process method and system device for preparing high-quality oil gas by pyrolyzing low-caking coal |
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