CN103980946B - A kind of anthracite segmentation pyrolysis sub-prime Application way without discharge and device - Google Patents
A kind of anthracite segmentation pyrolysis sub-prime Application way without discharge and device Download PDFInfo
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- CN103980946B CN103980946B CN201410212243.1A CN201410212243A CN103980946B CN 103980946 B CN103980946 B CN 103980946B CN 201410212243 A CN201410212243 A CN 201410212243A CN 103980946 B CN103980946 B CN 103980946B
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 91
- 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 34
- 239000003830 anthracite Substances 0.000 title claims abstract description 34
- 230000011218 segmentation Effects 0.000 title claims abstract description 14
- 239000007789 gas Substances 0.000 claims abstract description 133
- 238000002309 gasification Methods 0.000 claims abstract description 101
- 239000003921 oil Substances 0.000 claims abstract description 77
- 239000003245 coal Substances 0.000 claims abstract description 71
- 239000000470 constituent Substances 0.000 claims abstract description 46
- 239000000295 fuel oil Substances 0.000 claims abstract description 42
- 238000000034 method Methods 0.000 claims abstract description 31
- KSSNXJHPEFVKHY-UHFFFAOYSA-N phenol;hydrate Chemical compound O.OC1=CC=CC=C1 KSSNXJHPEFVKHY-UHFFFAOYSA-N 0.000 claims abstract description 27
- 239000000571 coke Substances 0.000 claims abstract description 16
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 11
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 11
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 7
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 7
- 239000001301 oxygen Substances 0.000 claims abstract description 7
- 238000011084 recovery Methods 0.000 claims abstract description 7
- 239000000498 cooling water Substances 0.000 claims abstract description 5
- 238000005406 washing Methods 0.000 claims description 18
- 239000002994 raw material Substances 0.000 claims description 12
- 239000003034 coal gas Substances 0.000 claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 10
- 229910052799 carbon Inorganic materials 0.000 claims description 9
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims description 6
- 239000007921 spray Substances 0.000 claims description 6
- 239000002918 waste heat Substances 0.000 claims description 6
- 239000004615 ingredient Substances 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 4
- 239000008246 gaseous mixture Substances 0.000 claims description 3
- 239000004484 Briquette Substances 0.000 claims description 2
- 239000000306 component Substances 0.000 claims 1
- 239000000428 dust Substances 0.000 abstract description 14
- 239000003795 chemical substances by application Substances 0.000 abstract description 11
- 238000006243 chemical reaction Methods 0.000 abstract description 9
- 238000005516 engineering process Methods 0.000 abstract description 9
- 239000000203 mixture Substances 0.000 abstract description 8
- 238000000746 purification Methods 0.000 abstract description 5
- 239000000126 substance Substances 0.000 abstract description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 24
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 15
- 230000008569 process Effects 0.000 description 15
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 14
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 7
- 241000628997 Flos Species 0.000 description 6
- 230000008676 import Effects 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- 239000007787 solid Substances 0.000 description 5
- 229960004424 carbon dioxide Drugs 0.000 description 4
- 230000007613 environmental effect Effects 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 238000009826 distribution Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000009413 insulation Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000006722 reduction reaction Methods 0.000 description 3
- 238000005201 scrubbing Methods 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
- 238000003912 environmental pollution Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 210000000003 hoof Anatomy 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
- 238000012545 processing Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000005979 thermal decomposition reaction Methods 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 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
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000002817 coal dust Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000007599 discharging 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
- 230000002349 favourable effect Effects 0.000 description 1
- 238000005984 hydrogenation reaction Methods 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
- 239000013618 particulate matter Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 239000000843 powder Substances 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
- 238000005493 welding type Methods 0.000 description 1
Classifications
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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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- Industrial Gases (AREA)
Abstract
A kind of anthracite segmentation pyrolysis sub-prime Application way without discharge and device, with CO2, purity oxygen and superheated steam be that the coke generating gasification that gasifying agent generates with anthracite in coal gasification pyrolysis oven react and generated gasification gas；Light oil constituents, the heavy oil component of high temperature pyrolysis section generation that gasification gas generates with low temperature pyrogenation section mix composition raw gas；Raw gas subsequently enters cyclone dust extractor, sensible heat recoverer by centrifugal dust-removing, heat recovery；Enter back into tar withdrawer removing heavy oil component and light oil constituents；It is circulated cooling water subsequently into inter cooler indirectly to cool down, wash and isolate phenol water, is finally removed trace light oil constituents again by electric fishing light oil device, finally give the synthesis gas of high-quality.CO and H in this synthesis gas2Content can reach more than 80%, can produce the chemical products such as oil, LNG through techniques such as conversion, purifications, and isolated heavy oil component, light oil constituents, phenol water all can be recycled, and is that a kind of coal segmentation pyrolysis sub-prime utilizes without discharge new energy technology.
Description
Technical field
The invention belongs to coal pyrolysis technology field, be specifically related to a kind of anthracite segmentation pyrolysis point without discharge
Matter Application way and device.
Background technology
At present, existing pure oxygen continuous gasification process is usually with secondary metallurgical, carbon dioxide, pure oxygen as gas
Change raw material, at high temperature, red-hot carbon and carbon dioxide generation redox reaction produce raw gas (CO:
68～70%, CO2: 28～29%, H2+N2: 1～1.2%), more purified, conversion prepare qualified conjunction
Become gas synthesis associated downstream product.But, this technique use ingredient requirement at a relatively high (fugitive constituent about 1%,
Fixed carbon about 82.5%, two grades of burnt standards of country), cost the highest (two grades of burnt market prices 1800-2000 unit/
Ton, and 500-700 yuan/ton of ground in low-order coal), it is important that existing producing in coal gas technical process cannot obtain
Heavy oil component, light oil constituents so that it is can not be recycled, so that raw material can not be fully utilized.
Present stage China's atmospheric gasification technique is all based on anthracite, due to technologic defect, causes coal
The conversion efficiency of middle carbon is low, and after gasification, in lime-ash, the content of carbon residue is higher, typically between 8-15%, and technique
The residual carbon content occurred during fluctuation in lime-ash can be higher.At present atmospheric gasification mainly have air+steam and oxygen-enriched+
Two kinds of techniques of steam, in both technique, effective Gas content all ratios of gasification gas are relatively low, the most all 75%
Hereinafter, gasification also has a small amount of thermal decomposition product, but does not the most recycle.These thermal decomposition products exist
Subsequent gases cleaning procedure processes as waste gas, and follow-up gas purification treatment process is brought bigger
Negative effect.
At present, any gasifying process all can be attended by CO2The generation of gas, current technique be all through
Recycle after rear operation separating treatment or to another one device, or to airborne release, cause
Environmental pollution, energy waste.Prominent along with environmental problem, CO2Emission reduction work is particularly important, how to optimize
Gasifying process, reduces CO2Generation, it is achieved CO2Recycling will be the important development side of China's Environmental Technology
One of to.
Summary of the invention
The technical problem to be solved is to provide a kind of anthracite segmentation pyrolysis sub-prime without discharge and utilizes
Method and device, obtains CO and H2Content reaches high-quality natural gas and the synthesis gas of more than 80%, and returns
Receive the heavy oil component in anthracite, light oil constituents, phenol water, it is achieved heavy oil component, light oil constituents, phenol water with
The separation of raw gas, to reach the purpose that anthracite pyrolysis sub-prime utilizes.
The mentality of designing of the present invention is: with anthracite as feed coal, with CO2, pure oxygen and superheated steam be gas
Agent, specifically utilizes CO2, pure oxygen bottom coal gasification pyrolysis oven, enter stove continuously after mixing with superheated steam
Novel pure oxygen continuous gasification process be pyrolyzed, gasifying smokeless coal, obtain raw gas, then removing dust, separation
Etc. realizing the classified utilization of feed coal, not only widen raw material sources, and the present invention has used CO2For gasification
Agent, breaches the drawback that pure oxygen gasification process costs is high, also can be separated and recovered from from raw gas heavy oil component,
Light oil constituents, phenol water so that anthracite has obtained utilizing more fully.
In order to solve above-mentioned technical problem, the technical solution used in the present invention is as follows:
A kind of anthracite segmentation pyrolysis sub-prime Application way without discharge, comprises the steps:
(1) anthracite adding coal gasification pyrolysis oven, in stove, layer and section carries out being pyrolyzed, gasifying；Coal
Gasification and pyrolysis stove includes low temperature pyrogenation section, high temperature pyrolysis section, gasification section；Anthracite is in low temperature pyrogenation section
Being pyrolyzed, generate light oil constituents and semicoke, semicoke enters high temperature pyrolysis section, and is generated weight by high temperature pyrolysis
Oil ingredient and coke, coke enters gasification section；
By CO2, 99.6% purity oxygen and superheated steam mixing after bottom coal gasification pyrolysis oven, enter stove continuously,
Generation gasification gas is reacted with the reverse coke generating gasification entered in gasification section in stove；On gasification gas
It is advanced into high temperature pyrolysis section, directly the semicoke in high temperature pyrolysis section is carried out high temperature pyrolysis, generate heavy oil group
Divide and coke；Heavy oil component enters low temperature pyrogenation section, final heavy oil component, light oil constituents with gasification gas
Coal gasification pyrolysis oven is removed with the i.e. raw gas of gaseous mixture of gasification gas；
(2) raw gas that step (1) obtains is by centrifugal dust-removing, temperature≤550 DEG C of raw gas after dedusting；
Subsequently into waste-heat recovery device, reclaiming sensible heat of raw gas, raw gas temperature is down to≤320 DEG C；
(3) method utilizing recirculated water spray washing through step (2) dedusting, the raw gas of heat recovery
Removing oil, dedusting, remove heavy oil component therein, light oil constituents, the removal efficiency of heavy oil component+light oil constituents
>=99%, isolated heavy oil component, light oil constituents enter tar groove with recirculated water and recycle；
(4) step (3) obtain removing heavy oil component, light oil constituents raw gas by recirculated cooling water
Indirectly it is cooled to≤40 DEG C；Meanwhile, washing pump closed cycle is utilized to wash the phenol water isolating in raw gas,
Isolated phenol water enters phenol tank and recycles；
(5) by cooled for step (4), the removing coal gas that obtains of phenol water through electric fishing light oil device removing oil,
Dedusting, removes wherein trace light oil constituents, makes final heavy oil component+light oil constituents removal efficiency >=99.9%,
Obtaining the synthesis gas of high-quality, isolated light oil constituents enters light tar groove and recycles.
It addition, raw material dosage is in described step (1): anthracite 610～645kg/kNm3(CO+H2) (every
Generate 1000Nm3(CO+H2) available gas needs 610～645kg anthracites, lower same), superheated steam
250～285kg/kNm3(CO+H2), purity oxygen 330～360Nm3/kNm3(CO+H2), CO2135～145
Nm3/kNm3(CO+H2)。
Also, coal gasification pyrolysis oven furnace pressure is 10～20KPa in described step (1), layer and section in stove
Carrying out being pyrolyzed, gasifying, low temperature pyrogenation section temperature is 550～750 DEG C, high temperature pyrolysis section temperature be 750～
1050 DEG C, in stove, gasification section temperature is 1050～1300 DEG C.
Again, anthracitic caloric value >=5500Kcal/kg described in described step (1).
Preferably, described in step (1), anthracite is anthracite block coal or anthracite briquette.
A kind of anthracite segmentation pyrolysis sub-prime without discharge utilizes device, including:
Coal gasification pyrolysis oven, it is provided with and is positioned at the gasifying agent import of bottom and connects with stove low temperature pyrogenation section
Floss hole, wherein, gasifying agent import connects CO by pipeline2, pure oxygen and superheated steam mixture
Source of the gas；
Heat reclaim unit, including cyclone dust extractor and sensible heat recoverer；The air inlet of described cyclone dust extractor
Mouth connects the floss hole of coal gasification pyrolysis oven by pipeline, and described sensible heat recoverer is provided with gas inlet, coal
Gas exports, and the gas inlet of described sensible heat recoverer connects the gas outlet of cyclone dust extractor by pipeline；
Tar withdrawer, it is provided with gas entry, clean gas outlet and is positioned at the tar outlet of bottom, burnt
The gas entry of oil saver 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 reclaimed with tar by pipeline
The clean gas outlet of device connects, and the tower reactor of described inter cooler is connected into looped back by pipeline and a washing pump
Road；
Electric fishing light oil device, it is provided with gas entry, gas exit and is positioned at the light oil outlet of bottom, electric fishing
The gas entry of light oil device is connected with the outlet of inter cooler, the gas exit connecting conveying pipe of electric fishing light oil device
Road.
Preferably, described coal gasification pyrolysis oven is layer and section formula coal gasification pyrolysis oven.
Further, described tar withdrawer is fountain scrubbing tower, sprays raw gas by low-temperature circulating water
Drip washing is washed, and primary effect is to reduce raw gas temperature, it is ensured that the light oil constituents liquefaction of more than 99%；Secondly profit
By the mode of spray washing, the gas solid matter going out cyclone dust extractor is separated, to remove in raw gas
Light oil constituents, heavy oil component and a small amount of solid dust.
Described sensible heat recoverer is waste heat boiler.
The work process of the present invention is as follows: the stone coal from pretreatment of raw material operation is through belt conveyor
From coal gasification pyrolysis oven upper feeding storehouse, timing controls to add feed coal coal gas heat-transformation by hydraulic program valve
Solving stove, be pyrolyzed at low temperature pyrogenation section feed coal, generate light oil constituents and semicoke, semicoke enters high temperature pyrolysis
Section；By CO2, 99.6% purity oxygen and superheated steam mixing after bottom coal gasification pyrolysis oven, enter stove continuously,
Generation gasification gas is reacted with the reverse coke generating gasification entered in gasification section in stove；Advance on gasification gas
Enter high temperature pyrolysis section, directly the semicoke in high temperature pyrolysis section is carried out high temperature pyrolysis, generate coke and heavy oil group
Point, heavy oil component and gasification gas enter low temperature pyrogenation section in the lump；Final heavy oil component, light oil constituents are gentle
Change coal gas and remove coal gasification pyrolysis oven in the lump.
The raw gas that coal gasification pyrolysis oven generates, after the floss hole of coal gasification pyrolysis oven is discharged, enters whirlwind and removes
Dirt device carries out dedusting, mainly isolates the solid particulate matter such as the coal dust discharged in raw gas of pyrolysis gasification furnace；
Entered sensible heat recoverer by the raw gas after dedusting and carry out heat recovery, then by the coal gas of tar withdrawer
Entrance enters tar withdrawer and utilizes the method for recirculated water spray washing to carry out removing oil, dedusting, then from tar
The clean gas outlet of withdrawer escapes and enter inter cooler, the isolated heavy oil component of tar withdrawer and light oil
Component is entered tar groove by the tar outlet being positioned at bottom and recycles；Raw gas is circulated after entering inter cooler
Cooling water is cooled to≤40 DEG C indirectly, is separated out by phenol moisture therein by closed cycle washing meanwhile, and
Reclaim trace light oil constituents through electric fishing light oil device, and then obtain the synthesis gas of the high-quality of the present invention.
The synthesis gas composition of the high-quality that the present invention prepares is: CO >=35%, H2>=45%, CO2≤ 18%,
CO and H2Content can reach more than 80%, closes gas further through techniques such as conversion, purifications and produces oil, LNG
Etc. chemical products.
The present invention is first with CO2For gasifying agent, enter coal gasification pyrolysis oven in the lump with pure oxygen, steam, at gas
Change section generation reduction reaction, generate available gas CO, reaction equation: CO2+ C=2CO-165KJ,
Greatly reduce CO2While discharge, it is achieved that comprehensive utilization of resources, turn waste into wealth, protect environment.
Appropriate application of the present invention gasification sensible heat, it is achieved that the layer and section pyrolysis sub-prime in coal gasification pyrolysis oven,
During sub-prime, protect the molecular structure of light oil constituents and heavy oil component to greatest extent, make content relatively low
Light oil constituents and the sub-prime of heavy oil component utilize and maximize, thus reach anthracitic comprehensive utilization, high attached
Value added purpose.From raw gas, heavy oil component and the light oil constituents of isolated just may be used through the upgrading of simple hydrogenation
Meet the market demand.The present invention, through closed cycle washing isolated phenol water from raw gas, enters phenol water
Groove can be recycled.Visible, no waste waste gas of the present invention discharges, it is to avoid pollution environment, decreases
Individually build exhaust gas processing device and increase the unfavorable factor such as investment, be the comprehensive utilization of a kind of environmentally friendly coal,
Gasification Polygeneration System technique.
Anthracite segmentation pyrolysis sub-prime without discharge of the present invention utilizes in device coal gasification pyrolysis oven and follow-up
Dust arrester, sensible heat recoverer, tar withdrawer etc. are compact to design, all can use commercial equipment, and material is easy
Purchase, can realize raw gas extracting heavy oil component, light oil constituents, isolating the merits such as phenol water, gas solid separation
Can, it is achieved anthracitic sub-prime utilizes, it is achieved high additive value, reach efficient energy-saving, comprehensive utilization effectively
The purpose of the energy.
Beneficial effects of the present invention:
1. the present invention is with CO2, pure oxygen and vapour mixture be gasifying agent, use pure oxygen continuous gasification technology,
Steam decomposition rate is high, and product quantity, more than other atmospheric fixed-bed gasification technique, forms rational sensible heat
Amount vector, meets the effect rationally disperseing heat, rationally setting up each conversion zone district, makes coal gas heat-transformation
Solving the heat distribution of Lu Neigeshu district and be in the rational deployment that middle and lower part temperature is high, two ends temperature is low, this is the most favourable
Produce raw gas in strengthening gasification, also form steam and decompose under the high temperature conditions and carbon dioxide fast restore
Gasification condition, improve simultaneously coal gasification pyrolysis oven produce the thermal efficiency；
2., relative to traditional coke gasification production line, the present invention is pure oxygen under lower pressure (10～20KPa)
Gasifying smokeless coal is an innovation, and in course of reaction, energy consumption is low, it is short to have flow process, non-environmental-pollution, raw material
Utilization rate is high, and high production, quality better, comprehensive utilization ratio advantages of higher, this is in the comprehensive utilization of coal
A kind of advanced technologies；
3. the present invention uses 99.6% pure oxygen, substantially increases smokeless coal gasification rate, makes coal gasification pyrolysis oven discharge
Lime-ash remaining carbon≤2%, significantly reduce consumption of raw materials, improve raw material trans-utilization rate；
4. effectively reduce latent heat losses and sensible heat loss, improve coal gasification pyrolysis oven converting heat utilization rate,
Cold gas efficiency reaches 80～82%, protects environment；
5. the present invention has widened the raw material route of coal gasification, and using anthracite is gasified raw material coal, right
Feed coal does not has very special quality requirement；
6. present invention achieves and anthracitic time processing comprehensively utilized, it is achieved that kerosene comprehensive utilization of separation,
And non-exhaust emission, the washings of washing phenol water use closed cycle in process of production, it is achieved that the three wastes
Zero-emission, is a kind of environmentally friendly new technology, belongs to clean coal gasification technology, complies fully with country's low-carbon (LC)
Environmental protection industry policy and Strategy of Circular Economy thinking of development.
7. the present invention is by CO2Gasify as gasifying agent, be converted into CO available gas, have significantly
Environmental benefit and economic benefit, belong to carbon emission reduction technology.
Accompanying drawing explanation
Fig. 1 is the structural representation of one embodiment of the invention.
Detailed description of the invention
Below in conjunction with specific embodiment technical scheme is described in further detail, but present disclosure
It is not limited to this.The following example is not indicated the experimental technique of actual conditions, generally according to normal condition,
Or according to the condition proposed by manufacturer.
Seeing Fig. 1, the anthracite segmentation pyrolysis sub-prime without discharge of the present invention utilizes device, including:
Coal gasification pyrolysis oven 1, it is provided with and is positioned at the gasifying agent import 11 of bottom and connects with stove pyrolysis section
Floss hole 12, wherein, gasifying agent import 11 connects CO by pipeline2, pure oxygen and superheated steam mixture
Source of the gas；
Heat reclaim unit, including cyclone dust extractor 2 and sensible heat recoverer 3；Described cyclone dust extractor 2
Air inlet 21 connected the floss hole 12 of coal gasification pyrolysis oven 1, described sensible heat recoverer 3 by pipeline
Being provided with gas inlet 31, gas exit 32, pipeline is passed through in the gas inlet 31 of described sensible heat recoverer 3
Connect the gas outlet 22 of cyclone dust extractor 2；
Tar withdrawer 4, its be provided with gas entry 41, clean gas outlet 42 and be positioned at bottom tar go out
Mouth 43, the gas entry 41 of tar withdrawer 4 gas exit 32 by pipeline with sensible heat recoverer 3
Connect；
Inter cooler 5, its underpart is provided with phenol water out 51；The entrance of described inter cooler 5 passes through pipeline and tar
The clean gas outlet 42 of withdrawer 4 connects；The tower reactor of described inter cooler 5 is by pipeline and valve and a washing
Pump 6 connects into a closed circuit；
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 end
The light oil outlet 73 in portion, the gas entry 71 of electric fishing light oil device 7 is connected with the outlet of inter cooler 5, and electric fishing is light
The gas exit 72 connecting conveying pipe road of oil device 7.
In the present embodiment, described coal gasification pyrolysis oven 1 is layer and section formula coal gasification pyrolysis oven.
Described tar withdrawer 4 is fountain scrubbing tower.Described sensible heat recoverer 3 is waste heat boiler.
Appointed condition used by the present embodiment is as follows:
1, coal gasification pyrolysis oven 1 is layer and section formula coal 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 setting-out cold wall
Gasification section height: 5000mm
The heat insulation mode of gasification section: middle setting-out cold wall
Low temperature and high temperature pyrolysis section equipment connection mode: welding type
Version: straight barrel type
Support pattern: upper support
Deslagging mode: solid continuous discharging slag
Technological parameter:
Operating pressure: 20KPa
Gasification temperature: 1050-1300 DEG C
Feed coal treating capacity: 3090Kg/h
Vapor (steam) temperature: 250 DEG C
Steam consumption: 1368Kg/h
CO2Temperature: 100 DEG C
CO2Consumption: 696m3/h
2, cyclone dust extractor 2:
Device parameter:
Diameter: Φ 1600mm
Highly: 9430mm
Cylinder diameter: Φ 1000mm
Cylinder height: 1200mm
Equipment importation diameter: Φ 1000mm
Equipment outlet diameter: Φ 800mm
Technological parameter:
Import raw gas temperature: 550 DEG C
Outlet raw gas coal powder density: 80mg/Nm3
3, sensible heat recoverer 3 is waste heat boiler:
Device parameter:
Diameter: Φ 2600mm
Highly: 19000mm
Superheat section diameter: Φ 2000mm
Superheat section heat exchange area: 300m2
Steam segment diameter: Φ 2000mm
Steam segment heat exchange area: 1400m2
Heat exchange mode: heat pipe-type
Technological parameter:
Process tolerance: 8000Nm3/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 steam pressure: 0.5MPa
Tower body resistance drop: 300Pa
4, tar withdrawer 4 is fountain scrubbing 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
Technological parameter:
Process tolerance: 8000Nm3/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 exchanger tube diameter: Φ 25mm
Technological parameter:
Process tolerance: 7000Nm3/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
Technological parameter:
Process tolerance: 7000Nm3/h
Gas outlet temperature: 30 DEG C
Backwashing time is spaced: 24h
Tower body resistance drop: 40Pa
Voltage: 380V
The coal segmentation pyrolysis sub-prime Application way without discharge of the present invention, comprises the steps:
Coal gasification pyrolysis oven used by the present embodiment specially one has low temperature pyrogenation, high temperature pyrolysis and coal simultaneously
The layer and section formula coal gasification pyrolysis oven of gasification function.Coal gasification pyrolysis oven include from top to down low temperature pyrogenation section,
High temperature pyrolysis section and gasification section.Low temperature pyrogenation section temperature is 550～750 DEG C, high temperature pyrolysis section temperature be 750～
1050 DEG C, in stove, gasification section temperature is 1050～1300 DEG C.
(1) the 3090Kg/h anthracite block coal come from pretreatment of raw material operation is pyrolyzed from coal gasification through belt conveyor
Stove 1 upper feeding storehouse, timing controls coal by hydraulic program valve and enters furnace gas, in coal gasification pyrolysis oven stove
Pressure is 20KPa.
Anthracite block coal typical case's ature of coal: phosphorus content: 70%～85%, fugitive constituent: 10%, calorific value about 5500～8000
Kcal/kg。
Anthracite block coal is pyrolyzed in low temperature pyrogenation section, generates light oil constituents and semicoke, and semicoke enters high temperature pyrolysis
Section, and generated heavy oil component and coke by high temperature pyrolysis, coke enters gasification section；From space division operation
1728Nm3The 696Nm that/h99.6% pure oxygen, rear workshop section come3/h CO2Mix with boiler overheating 1368Kg/h steam
Occur the gasifying agent import 11 bottom 1 to enter stove continuously from coal gas after conjunction, enter with reverse in gasification section in stove
High temperature pyrolysis section generated coke generating gasification reaction generate gasification gas；Height it is advanced on gasification gas
Temperature pyrolysis section, directly carries out high temperature pyrolysis to the semicoke in high temperature pyrolysis section, generates heavy oil component and coke；
Heavy oil component enters low temperature pyrogenation section with gasification gas, final heavy oil component, light oil constituents and gasification gas
Gaseous mixture i.e. raw gas is discharged from the floss hole 12 of coal gasification pyrolysis oven 1.
(2) raw gas carries out gas purification process: from the raw gas of coal gasification pyrolysis oven 1 discharge by described rotation
The air inlet 21 of wind cleaner unit 2 enters cyclone dust extractor 2 and is centrifuged dedusting, the temperature of raw gas after dedusting
≤550℃；Then after dedusting, raw gas enters sensible heat recoverer 3 by the gas inlet 31 of sensible heat recoverer 3
Being recovered sensible heat therein, gas temperature is down to less than 320 DEG C.
(3) removing dust, the raw gas gas entry 41 through tar withdrawer 4 again of heat recovery enter Jiao
Oil saver 4 utilizes the method for recirculated water spray washing to carry out removing oil, dedusting, remove heavy oil component therein,
Removal efficiency >=99% of light oil constituents, heavy oil component and light oil constituents, isolated heavy oil component, light oil constituents
Tar outlet 43 bottom tar withdrawer 4 enters tar groove 401 and recycles, removing heavy oil component,
The raw gas of light oil constituents enters inter cooler 5 from the clean gas outlet 42 of tar withdrawer 4.
(4) raw gas entering inter cooler 5 is cooled to less than 40 DEG C indirectly by recirculated cooling water；Meanwhile, profit
Isolating the phenol water in raw gas with washing pump 6 closed cycle washing, isolated phenol water is from inter cooler 5
Phenol water out 51 flows out, and enters phenol tank 501 and recycle.
(5), in the present embodiment, open control valve 100, closing control valve 200, through indirectly cooling down and will take off
Electric fishing light oil device is entered by the gas entry 71 of electric fishing light oil device 7 except the coal gas after phenol water is discharged from inter cooler 5
7, remove the light oil constituents of trace again, make final heavy oil component+light oil constituents removal efficiency >=99.9%,
To the synthesis gas of the high-quality of the present invention, it is delivered to user from gas exit 72 through pipeline and uses.Isolated
Light oil constituents enters light oil groove 701 from light oil outlet 73 and recycles.
The high-quality synthesis gas composition of the present embodiment gained is: CO:35%, H2: 45%, CO2: 18%,
Single stove aerogenesis 6000Nm3/h。
The high-quality synthesis gas that the present invention obtains closes gas further through techniques such as conversion, purifications and produces oil, LNG
Etc. chemical products.
In step (3), (5) from raw gas the heavy oil component of isolated, light oil constituents through being simply hydrogenated with upgrading
Just the market demand can be met.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, tool
Body can use existing phenol water vapo(u)rization system, and separate unit coal gasification pyrolysis oven configures a set of phenol water vapo(u)rization system, adopts
Generate phenol water vapour with phenol water evaporating heat exchanger evaporation phenol water, in the case of realizing heat exchange function, can evaporate
The phenol water that coal gasification pyrolysis oven produces, had both utilized the waste heat of hypomere coal gas, avoided again polluting environment.
Claims (3)
1., without an anthracite segmentation pyrolysis sub-prime Application way for discharge, comprise the steps:
1) anthracite adding coal gasification pyrolysis oven, in stove, layer and section carries out being pyrolyzed, gasifying；
Coal gasification pyrolysis oven includes low temperature pyrogenation section, high temperature pyrolysis section, gasification section；Anthracite is at low temperature pyrogenation
It is pyrolyzed in Duan, generates light oil constituents and semicoke；Semicoke enters high temperature pyrolysis section, and by high temperature pyrolysis
Generating heavy oil component and coke, coke enters gasification section；
By CO2, 99.6% purity oxygen and superheated steam mixing after enter continuously bottom coal gasification pyrolysis oven
Stove, reacts generation gasification gas with the reverse coke generating gasification entered in gasification section；Gasification gas
On be advanced into high temperature pyrolysis section, directly the semicoke in high temperature pyrolysis section is carried out high temperature pyrolysis, generates weight
Oil ingredient and coke；Heavy oil component and gasification gas enter low temperature pyrogenation section, final heavy oil component, light
The gaseous mixture of oil ingredient and gasification gas i.e. raw gas removal coal gasification pyrolysis oven；
Wherein, step 1) in coal gasification pyrolysis oven furnace pressure be 10～20KPa, 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；
Step 1) in raw material dosage be: anthracite 610～645kg/kNm3(CO+H2), superheated steam
250～285kg/kNm3(CO+H2), purity oxygen 330～360Nm3/kNm3(CO+H2), CO2
135～145Nm3/kNm3(CO+H2)；
2) step 1) raw gas that obtains by centrifugal dust-removing, temperature≤550 DEG C of raw gas after dedusting；
Subsequently into waste-heat recovery device, reclaiming sensible heat of raw gas, raw gas temperature is down to≤320 DEG C；
3) through step 2) dedusting, the raw gas of the heat recovery method that utilizes recirculated water spray washing
Removing oil, dedusting, remove heavy oil component therein, light oil constituents, taking off of heavy oil component+light oil constituents
Except rate >=99%, isolated heavy oil component, light oil constituents enter tar groove with recirculated water and reclaim
Utilize；
4) step 3) obtain removing heavy oil component, light oil constituents raw gas by recirculated cooling water
Indirectly it is cooled to≤40 DEG C；Meanwhile, washing pump closed cycle is utilized to wash the phenol isolating in raw gas
Water, isolated phenol water enters phenol tank and recycles；
5) by step 4) cooled, the removing coal gas that obtains of phenol water through electric fishing light oil device removing oil,
Dedusting, removes wherein trace light oil constituents, make final heavy oil component+light oil constituents removal efficiency >=
99.9%, thus obtain the synthesis gas of high-quality, isolated light oil constituents enters light tar groove and reclaims
Utilize.
Anthracite segmentation pyrolysis sub-prime Application way without discharge the most according to claim 1, its feature exists
In, step 1) described in anthracitic caloric value >=5000Kcal/kg.
Anthracite segmentation pyrolysis sub-prime Application way without discharge the most according to claim 1 and 2, it is special
Levy and be, step 1) described in anthracite be anthracite block coal or anthracite briquette.
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| 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 |
| CN107475798B (en) * | 2017-08-07 | 2020-01-03 | 海南大学 | Nanofiber material for extracting uranium from seawater and preparation method thereof |
| 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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| DE3635215A1 (en) * | 1986-10-16 | 1988-04-28 | Bergwerksverband Gmbh | METHOD FOR ALLOTHERMAL CARBON GASIFICATION AND FLUID BED GAS GENERATOR FOR CARRYING OUT THE METHOD |
| 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 |
| CN102465043B (en) * | 2010-11-01 | 2013-07-31 | 中国科学院过程工程研究所 | Multi-section fractional pyrolysis gasification device and method for solid fuel |
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Denomination of invention: No-emission anthracite segmented pyrolysis and upgrading utilization method and no-emission anthracite segmented pyrolysis and upgrading utilization device Effective date of registration: 20191012 Granted publication date: 20170104 Pledgee: Zhumadian Rural Commercial Bank Co., Ltd. Pledgor: Henan Shunda Amperex Technology Limited Registration number: Y2019980000246 |
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