CN104673394A - Dry powder solid fuel gasifying technology and system with waste heat recovery - Google Patents
Dry powder solid fuel gasifying technology and system with waste heat recovery Download PDFInfo
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- CN104673394A CN104673394A CN201510057797.3A CN201510057797A CN104673394A CN 104673394 A CN104673394 A CN 104673394A CN 201510057797 A CN201510057797 A CN 201510057797A CN 104673394 A CN104673394 A CN 104673394A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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Abstract
The invention relates to a dry powder solid fuel gasifying technology and a system with waste heat recovery and aims at solving the problems of the existing equipment such as complicated structure, high equipment investment and operation cost, easy dust deposition of system, low stability and environmental pollution. The technical scheme is as follows: pulverized coal is fed into a reaction chamber of a gasifier and conducts a gasifying reaction under the effect of a gasifying agent at 1200-1650 DEG C to generate a crude synthesis gas; the crude synthesis gas is cooled by water mist sprayed out by an atomizing nozzle when rising above the reaction chamber; then, the crude synthesis gas rises, is fed into a fire tube boiler through a gas pipe with a membrane water wall and further cooled through heat exchange with water between a tube pass and a shell pass, and then is fed into a multi-tube cyclone dust collector and a fly-ash filter for further dust removal until the dust content is less than 1mg/m<3>; and after the dust removal, the crude synthesis gas enters an economizer again and is further cooled to 220-260 DEG C before entering the next process. The technology and system provided by the invention have the advantages of simple technology, wide coal adaptability, low equipment investment cost and operation cost and environmental friendliness.
Description
Technical field
The present invention relates to a kind of coal gasifying process and system thereof, specifically a kind of band waste heat recovery dry-powder solid fuel gasifying process and system thereof.
Background technology
Powdered coal pressuring gasified technology and water coal slurry pressurized gasification technology are the powdered coal pressuring gasified technology of s-generation air flow bed.Compared with static bed coal gasification technology, there is in energy-saving and environmental protection and coal adaptability etc. very outstanding advantage.In s-generation gasifying process technology more advanced at present, most is representational is the water coal slurry pressurized gasification technology of GE company of the U.S. and Cophi Co., Ltd, the SCGP of Dutch Shell Co. Ltd and siemens GSP dried coal powder pressurized gasification work.
SHELL dry coal powder gasification technique principal feature is the charging of vapourizing furnace dry pulverized coal, multi-nozzle gasification, water wall liner, the coal gas of gasification is advanced into waste heat boiler cool, cooled coal gas is through dedusting, and wherein a part melts down Quench heating gas, and other synthetic gas enter lower procedure.There is following shortcoming in this technique: 1, device structure is complicated, and manufacture difficulty is large, and production cycle is long, and cost is high.Principal element is that waste heat boiler complex structure, Quench recycle gas compressor are valuable, and running cost is high; 2, have a definite limitation to coal, in coal, the alkali metal content such as potassium sodium is high, and easily dust stratification in useless pot, affects heat transfer efficiency, increases systemic resistance and falls.3。Synthetic gas solids content after ash disposal system ash disposal is generally 5 ~ 10mg/Nm3, can not be directly used in lower procedure, and need through washing the further ash disposal of workshop section and clarification workshop section, the ash washed is wet ash, can not recycle.
GSP bed pulverized coal gasification technology generally adopts water chilling process, and water consumption is large, and grey carbon content is high, efficiency of carbon conversion is low, and energy consumption is high, and the burner life-span is short, can not meet the requirement that large-scale plant long period uses, the wet ash that carbon content is large can not effectively utilize, and has a negative impact to environment.
The synthetic gas that Coal Gasification Technology produces all needs to carry out washing and gas-liquid separation, need Venturi scrubber, water wash column, multiple flash chamber, saturated hot-water tower, large-scale clarifying tank etc., technical process is long, and plant investment is large, take water resources, sewage discharge will produce serious harm to environment.
As can be seen here, although fine coal gasification process has certain advance, but how the flow process for synthetic gas production chemical product reduces facility investment further, reduces the device fabrication cycle technique, shortened process, realize coal high-efficiency to transform, clean utilization, energy-saving and water-saving is the direction that current those skilled in the art are devoted to study always.
Summary of the invention
The object of the invention is to solve the problems of the technologies described above, providing that a kind of technique is simple, coal adaptability is wide, good dedusting effect, facility investment become running cost low, environment amenable band waste heat recovery dry-powder solid fuel gasifying process.
The present invention also provides a kind of system for above-mentioned technique, has that system is simple, facility investment and running cost low, an effective control dust stratification problem, improves the advantage of synthetic gas Quench efficiency.
Present invention process comprises and passes in the reaction chamber of vapourizing furnace by coal dust, at the crude synthesis gas of the effect gasified reaction generation 1200 ~ 1650 DEG C of vaporized chemical, described crude synthesis gas is atomized nozzle ejection water smoke when rising to above reaction chamber is cooled to less than 850 DEG C, then the pneumatic tube risen through having membrane wall is sent in fire tube boiler the water heat exchange walking tube side and shell side and is cooled to less than 350 DEG C further, then send into Multi-tube cyclone duster, the further dedusting of fly-ash filter is less than 1mg/m to dustiness
3, the crude synthesis gas after dedusting enters after economizer is cooled to 220 ~ 260 DEG C further again and enters subsequent processing.
The water smoke particle diameter of described atomizing nozzle ejection is 80 ~ 250 μm.
Described atomizing nozzle and horizontal direction angle are 5 ~ 15 DEG C, and downward inclination angle is 5 ~ 15 degree, nozzle ejection cone angle 75 ~ 150 degree.
Present system comprises vapourizing furnace, described top of gasification furnace is connected with economizer with fire tube boiler, Multi-tube cyclone duster, fly-ash filter successively through pneumatic tube, described pneumatic tube has membrane wall, and the reaction chamber upper annular of described vapourizing furnace is provided with at least one deck atomizing nozzle.
Vapourizing furnace wall between described atomizing nozzle and reaction chamber is also provided with sootblower.
Described atomizing nozzle and horizontal direction angle are 5 ~ 15 DEG C, and downward inclination angle is 5 ~ 15 degree, nozzle ejection cone angle 75 ~ 150 degree.
Described fire tube boiler comprises tube side and shell side, heat transfer tube upper end in described tube side is communicated with upper tube box through upper tubesheet through tube head insert, wherein, described tube head insert is made up of the inserting paragraph with the grafting of heat transfer tube upper end and the open section that is communicated with upper tube box, described open section is the hydraucone with ramped shaped inwall, described bell-mouthed two ends are respectively big opening end and osculum end, and described osculum end is connected with the front end of inserting paragraph and inner wall surface seamlessly transits.
The cross section of described big opening end is Polygons, and the cross section of osculum end is circular.
The gradient of described bell-mouthed ramped shaped inwall is 5 °-20 °.
The cross section of described big opening end is pentagon or hexagon.
The water smoke that the present invention utilizes vapourizing furnace epimere atomizing nozzle to spray carries out the method for preliminary cooling to high-temperature crude synthesis gas, instead of the method that cooled crude synthesis gas melts down chilling high-temperature synthesis gas, solve and adopt part low temperature crude synthesis gas to melt down Quench must to configure the high cost problem and the large problem of crude synthesis gas recycle system power loss that large-scale recycle compressor causes, thus considerably reduce investment and running cost, realize the object at cost efficiency.Adopt multiclone to coordinate fly-ash filter can realize dry method ash disposal completely, and due to synthetic gas up, the carbon content of ash is low, can as the raw material of high-performance cement, solves environmental issue, does not need to carry out wet scrubbing, reduces the consumption of water.Adopt economizer to reclaim heat further simultaneously, reduce temperature, make synthetic gas directly can enter down-stream system.
Because crude synthesis gas temperature in vapourizing furnace can up to 1400 ~ 1700 DEG C, the inlet air temperature requirement that less than 850 DEG C meet sub sequent fire tubular boiler is fully cooled to for making crude synthesis gas, need the size droplet diameter of the spray film controlling atomizing nozzle ejection, chilled water is made to need fully atomization, with fully contacting of fortified water and synthetic gas, make High Temperature High Pressure crude synthesis gas fast cooling, atomizing particle size is preferably 80 ~ 250 μm, more preferably 150-180 μm.
Described vaporized chemical is oxygen and/or steam etc., and its add-on requires to operate with reference to existing gasification reaction.
Further, for the problem of dust stratification easy in system, contriver finds, dust stratification is mainly present in two places, one be easily be attached to vapourizing furnace atomizing nozzle below: due to crude synthesis gas rise to atomizing nozzle place time, the water smoke Quench cooling be ejected, the dust in gas is attached in water smoke and declines by gravity, very easily drop on wall below vapourizing furnace atomizing nozzle and plate face, cause local dust stratification.Two is easily be deposited on the upper tubesheet of fire tube boiler at dust: this is mainly because tube head insert is because of when arranging, open section protrudes from upper plate pipe, outside filling by mould material is fixed or suit porcelain bushing, this just causes mould material or porcelain bushing end face easily to form dust accretions region, when mould material occurs crackle or comes off, dust then can directly be deposited on upper tubesheet, make upper tubesheet heat exchange uneven, even cause the problem discovers such as upper tubesheet distortion.For the problems referred to above, inventors performed two places and improve, one is that the vapourizing furnace wall between atomizing nozzle and reaction chamber arranges sootblower, promotes that the dust after humidifying cooling falls in vapourizing furnace reaction chamber; Two is improve the tube head insert configuration in fire tube boiler, avoids dust to fall on upper tubesheet, overcomes the various problems brought of dust accretions.
In the present invention, the open section of tube head insert is designed to hydraucone, make its inwall form ramped shaped, avoid dust to pile up at big opening end, the gradient of preferred ramped shaped inwall is 5 °-20 ° and is beneficial to ash discharge, and more preferred slope is 7 °-15 °.The inner wall surface of described bell-mouthed osculum end and inserting paragraph front end seamlessly transits, and is conducive to the flowing of dusty gas like this.
The cross section of described big opening end is Polygons, be preferably pentagon or hexagon, like this, after tube head insert is installed, adjacent two bell-mouthed big opening ends of tube head insert can splice mutually, cover the air inlet face of upper tubesheet, without the need to mould material or porcelain bushing comprehensively, do not stay gap or platform between hydraucone and hydraucone, avoid the various problems that dust deposit brings at mould material end face or tube sheet surface.
Beneficial effect:
(1), the present invention adopts and carries out preliminary Quench at vapourizing furnace atomization nozzle ejection water smoke to crude synthesis gas, then fire tube boiler is utilized to lower the temperature further and reclaim heat energy, ensure that effective chill effect simultaneously, it also avoid the problems such as the energy consumption that partial synthesis gas backflow Quench brings is high, mounting structure is complicated; And adopt atomization Quench crude synthesis gas, humidifying and the separation of macrobead dust in crude synthesis gas can be promoted, significantly reduce the consumption of chilled water.
(2), owing to not adopting water-bath Quench in the cooling step of crude synthesis gas, dry method dust therefore in follow-up dust removal step, can be adopted to utilize Multi-tube cyclone duster to coordinate fly-ash filter further crude synthesis gas dedusting to be less than 1mg/m to dustiness
3, can directly with entering down-stream system.Isolated grey carbon content carbon content is less than mass percent 5%, as the raw material of high-performance cement, can improve the economic worth of byproduct.
(3), by add sootblower and the flowing of dust is conducive to the texture improvement of tube head insert, anti-Soot Performance is good, substantially increases the work-ing life of system, improves the adaptability of coal.
(4) stable, the facility investment of present system and production cost is low, technical process simple, running cost is lower, energy-saving and water-saving, environmentally friendly.
Accompanying drawing explanation
Fig. 1 is present invention process schema and system diagram;
Fig. 2 is the scheme of installation of tube head insert in tubular boiler.
Fig. 3 is tube head insert configuration schematic diagram;
Fig. 4 is many tube head insert aggregate erection schematic diagram.
Fig. 5 is the scheme of installation of atomizing nozzle 10 in vapourizing furnace 9.
Fig. 6 is the A-A sectional view in Fig. 5.
Wherein, 1-hydraucone, 1.1-big opening end, 1.2-osculum end, 1.3-slope, 2-inserting paragraph, 2.1-front end, 2.2-rear end, 3-fire tube boiler, 4-upper tubesheet, 5-heat transfer tube, 6-tube head insert, 7-refractory liner, 8-upper tube box, 9-vapourizing furnace, 9.1-reaction chamber, 10-atomizing nozzle, 11-sootblower, 12-Multi-tube cyclone duster, 13-fly-ash filter, 14-economizer, 15-pneumatic tube.
Embodiment
Below in conjunction with accompanying drawing, explanation is further explained to present system:
Vapourizing furnace 9 top through pneumatic tube 15 successively with fire tube boiler 3, Multi-tube cyclone duster 12, fly-ash filter 13 is connected with economizer 14, described pneumatic tube 15 has membrane wall, reaction chamber 9.1 upper annular of described vapourizing furnace 9 is provided with at least one deck atomizing nozzle 10, the water smoke that described atomizing nozzle 10 (if the employing patent No. is the two phase flow atomized injection cooling device of 200820067507.9) can spray liquids and gases mixing carries out Quench cooling to reacted crude synthesis gas, preferred described atomizing nozzle 10 is 5 ~ 15 DEG C with horizontal direction angle b, downward inclination angle c is 5 ~ 15 degree, nozzle ejection cone angle d is 75 ~ 150 degree, by controlling the angle of atomizing nozzle, the object of high-efficient atomizing can be realized, improve quick cold true effect.Vapourizing furnace 9 wall between described atomizing nozzle 10 and reaction chamber 9.1 is also provided with sootblower 11.In addition, be also provided with coal nozzle, vapor-nozzle etc. in described vapourizing furnace 9, this is prior art, is not described further at this.
Described fire tube boiler 3 has conventional tube side and shell side, heat transfer tube 5 upper end in described tube side is communicated with upper tube box 8 through upper tubesheet 4 through tube head insert 6, wherein, described tube head insert 6 is made up of the inserting paragraph 2 with heat transfer tube 5 upper end grafting and the open section that is communicated with upper tube box 8, described open section is the hydraucone 1 with ramped shaped inwall, the gradient a of ramped shaped inwall is 5 °-20 °, preferably 7 °-15 °, utilize the distinctive ramped shaped interior wall construction of hydraucone, the sectional area expanding air inlet avoids local dust to pile up simultaneously.The two ends of described hydraucone 1 are respectively big opening end 1.1 and osculum end 1.2, and described osculum end 1.2 is connected with the front end 2.1 of inserting paragraph 2 and inner wall surface seamlessly transits, and ash-laden gas is passed in heat transfer tube 5 by inserting paragraph 2 of passing through under the pleasant body of hydraucone 1 smoothly.The cross section of described big opening end 1.1 is Polygons, be preferably pentagon or hexagon, it is hexagon in the present embodiment, the cross section of osculum end 1.2 is circular, when arranging on upper tubesheet 4 like this, respective numbers, onesize tube head insert 6 are spliced according to the quantity correspondence on Polygons limit in the surrounding of each tube head insert 6, the upper tubesheet 4 of air inlet face all can be covered after hydraucone 1 splicing of final multiple tube head insert 6, drop space between hydraucone 1 and upper tubesheet 4 can be filled with refractory liner 7 easily, and without the need to mould material or be set with pipe box in addition.Wall thickness≤the 2mm of described inserting paragraph 2 and hydraucone 1.During installation, first the rear end 2.2 of the inserting paragraph 2 from tube head insert 6 is passed down through upper tubesheet 4 and inserts heat transfer tube 5, inserting paragraph 2 is made to be positioned at heat transfer tube, hydraucone 1 is positioned at above upper tubesheet 4, insert second Polygons tube head insert 6 (tubular stinger 2 and the hydraucone 1 be attached thereto) in the same way, adjustment orientation, makes hydraucone 1 big opening end 1.1 of adjacent two tube head inserts 6 contact, and its Polygons limit is cooperatively interacted splicing, clearance control is at≤0.5mm.Repeat above method, insert many tube head inserts 6 accordingly, the effect after grafting refers to Fig. 3.Space refractory liner 7 between the hydraucone 1 of Polygons tube head insert 6 and upper tubesheet 4 is filled.After dusty gas enters tubular boiler 3, enter heat transfer tube 5 indirect heat exchange through the hydraucone 1 of tube head insert 6 and tubular stinger 2, go out heat transfer tube 5 after heat exchange and discharge tubular boiler 3.
Technological process:
Dry pulverized coal enters in the reaction chamber 9.1 of vapourizing furnace 9 with being mixed together as the oxygen of vaporized chemical and some vapor, high-temperature crude synthesis gas is generated in reaction in furnace, temperature is 1200 ~ 1650 DEG C, in stove, vapor pressure is 1.0 ~ 6.5MPa, crude synthesis gas forms the bottom-up flowing of eddy flow in vapourizing furnace 9, less than 850 DEG C are cooled to by 80 ~ 250 μm of water smoke parts cold shock that the water/gas that the atomizing nozzle 10 that multi-layer annular is arranged sprays mixes above vapourizing furnace reaction chamber 9.1, sootblower 11 selective sootblowing, prevents dust in local deposits simultaneously; The pneumatic tube 15 of crude synthesis gas after cooling through having membrane wall enters fire tube boiler 3 and saturation water indirect heat exchange and to lower the temperature the crude synthesis gas byproduct water steam that obtain less than 350 DEG C, through multicyclone 12, the solid 100% that particle diameter contained in synthetic gas is greater than 5 μm is removed again, then the dry ash in fly-ash filter 13 further removing crude synthesis gas, the synthetic gas dustiness after ash disposal is less than 1mg/m
3, then enter after synthetic gas is cooled to 220 ~ 260 DEG C by economizer 14 further and enter subsequent processing, for lower procedure, multicyclone 12 is separated with fly-ash filter 13 raw material that the dry ash obtained can be used as high-performance cement.
Claims (10)
1. a band waste heat recovery dry-powder solid fuel gasifying process, it is characterized in that, coal dust is passed in the reaction chamber of vapourizing furnace, at the crude synthesis gas of the effect gasified reaction generation 1200 ~ 1650 DEG C of vaporized chemical, described crude synthesis gas is atomized nozzle ejection water smoke when rising to above reaction chamber is cooled to less than 850 DEG C, then the pneumatic tube risen through having membrane wall is sent in fire tube boiler the water heat exchange walking tube side and shell side and is cooled to less than 350 DEG C further, then send into Multi-tube cyclone duster, the further dedusting of fly-ash filter is less than 1mg/m to dustiness
3, the crude synthesis gas after dedusting enters after economizer is cooled to 220 ~ 260 DEG C further again and enters subsequent processing.
2. band waste heat recovery dry-powder solid fuel gasifying process as claimed in claim 1, it is characterized in that, the water smoke particle diameter of described atomizing nozzle ejection is 80 ~ 250 μm.
3. band waste heat recovery dry-powder solid fuel gasifying process as claimed in claim 1 or 2, it is characterized in that, described atomizing nozzle and horizontal direction angle are 5 ~ 15 DEG C, and downward inclination angle is 5 ~ 15 degree, nozzle ejection cone angle 75 ~ 150 degree.
4. a band waste heat recovery dry-powder solid fuel gasification system, comprise vapourizing furnace, it is characterized in that, described top of gasification furnace is connected with economizer with fire tube boiler, Multi-tube cyclone duster, fly-ash filter successively through pneumatic tube, described pneumatic tube has membrane wall, and the reaction chamber upper annular of described vapourizing furnace is provided with at least one deck atomizing nozzle.
5. band waste heat recovery dry-powder solid fuel gasification system as claimed in claim 4, is characterized in that, the vapourizing furnace wall between described atomizing nozzle and reaction chamber is also provided with sootblower.
6. band waste heat recovery dry-powder solid fuel gasification system as claimed in claim 4, it is characterized in that, described atomizing nozzle and horizontal direction angle are 5 ~ 15 DEG C, and downward inclination angle is 5 ~ 15 degree, nozzle ejection cone angle 75 ~ 150 degree.
7. the band waste heat recovery dry-powder solid fuel gasification system as described in any one of claim 4-6, it is characterized in that, described fire tube boiler comprises tube side and shell side, heat transfer tube upper end in described tube side is communicated with upper tube box through upper tubesheet through tube head insert, wherein, described tube head insert is made up of the inserting paragraph with the grafting of heat transfer tube upper end and the open section that is communicated with upper tube box, described open section is the hydraucone with ramped shaped inwall, described bell-mouthed two ends are respectively big opening end and osculum end, described osculum end is connected with the front end of inserting paragraph and inner wall surface seamlessly transits.
8. band waste heat recovery dry-powder solid fuel gasification system as claimed in claim 7, it is characterized in that, the cross section of described big opening end is Polygons, and the cross section of osculum end is circular.
9. band waste heat recovery dry-powder solid fuel gasification system as claimed in claim 7, it is characterized in that, the gradient of described bell-mouthed ramped shaped inwall is 5 °-20 °.
10. band waste heat recovery dry-powder solid fuel gasification system as claimed in claim 8, it is characterized in that, the cross section of described big opening end is pentagon or hexagon.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104987894A (en) * | 2015-07-08 | 2015-10-21 | 陕西延长石油（集团）有限责任公司 | Discharging device and method for solid particles in tar-containing coal gas |
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| CN104987894B (en) * | 2015-07-08 | 2019-01-18 | 陕西延长石油（集团）有限责任公司 | The tapping equipment and method of solid particle in a kind of coal gas containing tar |
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| CN104673394B (en) | 2017-07-25 |
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