CN104073267B - A kind of method reclaiming crude-gas sensible heat - Google Patents
A kind of method reclaiming crude-gas sensible heat Download PDFInfo
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- CN104073267B CN104073267B CN201310101105.1A CN201310101105A CN104073267B CN 104073267 B CN104073267 B CN 104073267B CN 201310101105 A CN201310101105 A CN 201310101105A CN 104073267 B CN104073267 B CN 104073267B
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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
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Abstract
The invention discloses a kind of method reclaiming crude-gas sensible heat, the upcast being included in coke oven installs heat-exchanger rig, and after three/two cycles of described coke oven coking cycles, the heat transferring medium in heat-exchanger rig starts flowing, starts the sensible heat reclaimed in raw gas.Processing method of the present invention is simply easy to realize, and by starting the recovery of crude-gas sensible heat at specific coking cycles, reclaims heat without misgivings, can avoid completely tar affects waste heat recovery problem in heat-transfer surface coking occurs.
Description
Technical field
The present invention relates to coal-blending coking technical field, be specifically related to raw gas and reclaim field.
Background technology
The raw gas temperature produced in modern coking by coke oven process is about 700-750 DEG C, derived by the upcast of coking chamber pusher side, spray with the thermal cycling ammoniacal liquor of temperature 80 DEG C when flowing through bridge tube, because partial ammonia water evaporates rapidly a large amount of heat absorption, make raw gas temperature be down to 80-100 DEG C, in coal gas, the tar condensing of about 60% is separated out simultaneously.Heat contained by raw gas accounts for the 32-35% of whole coking heat consumption, and this partial heat does not carry out efficient recovery, has wasted the energy.The high temperature raw gas oxygenation partial combustion that upcast is discharged by part coking technology produces the products such as synthetic gas, thus this partial heat energy of Appropriate application, this technology is not in this patent limit of consideration, this technology only considers traditional coking and recovery of chemical products technique, namely tar is extracted, the products such as crude benzol, ammonia, coal gas after the cooling of high temperature raw gas.As follows about the technology of raw gas waste heat recovery at present:
Volume 3 phase in " energy supply for metallurgy " May 4 in 1985 " the high efficiente callback novel method of coke oven coke oven uprising tube gas heat " describes the sprinkling heavy tar recovery crude-gas sensible heat method that Japan proposes.
Volume 5 phase in " combustion gas and heating power " September 15 nineteen ninety-five " Ascension Pipe Gasification water cooler Energy Saving Benefit Analysis " describes upcast and to gasify cooling system, is called for short SQ.Main existing problems: safety problem, coking problem, water jacket seepy question.
Patent publication No.: the CN101619848A such as Mei Gangqizhi hilllock, adopt high-end heat energy and low side absorption installation of heat energy and water charging system to form, can efficient recovery ascending tube crude-gas waste heat, make raw gas temperature decline 300 DEG C.The patent publication No. such as Chen little Yun: CN101614498A, comprise the upper and lower header be looped around outside raw coke over gas riser inwall, the separate heat pipe heat absorbing end that upper and lower header is communicated with through raw coke over gas riser inwall respectively to interior extraction one group by described upper and lower header, upwards be communicated with the two ends of separate heat pipe release end of heat respectively by connecting pipeline, described separate heat pipe release end of heat is positioned at heat exchange drum simultaneously.
" Shanghai Energy Conservation " 12 phases in 2009, Chen little Yun etc. " waste heat of coke oven crude gas reclaim investigation with experiment " carry out industrial on probation to above Patent equipment, but occur that heat exchange surface coking affects heat transfer problem.
The residual heat utilizing technology of coke oven crude gas of the patent application of publication number CN101701703A, high temperature raw gas in each coking chamber of coke oven is directly derived by the Y-tube on upcast top, spray without ammoniacal liquor, be connected with gathering tube by adapter, raw gas in each coking chamber is imported gathering tube, then enters waste heat boiler and carry out heat exchange; Raw gas after heat exchange, after the cooling of ammonia spray device, send recovery of chemical products system.
The patent CN201811187U such as Wuhan Iron and Steel Plant Yi Xiaodong, Novel residual heat utilization device for ascension pipe of coke oven, raw gas enters in upcast from upcast bottom, the heat-conducting medium between upcast inner/outer tube is transferred heat to by radiation heat transfer, heat-conducting medium transfers heat to the spiral pipe water pipe be coiled in wherein again, after recirculated water enters the coke oven ascending pipe afterheat utilization device of series connection successively by water-in topmost, part or all of vaporization, enter drum from last outlet, realize heat recovery.
Current upcast waste heat recovery mainly faces two problems, one be heat exchange material in use break leak enter coking chamber damage furnace wall brick, this can be avoided by selecting the method such as suitable steel material or reasonable arrangement heat transfer space, but after how controlling raw gas heat exchange in heat transfer process temperature make its not on heat-transfer surface condensation coking be a difficult problem, above technology all mentions a subject matter, and namely the easy coking of the heat-transfer surface of interchanger affects heat exchange and carries out.
Summary of the invention
Therefore, the technical problem to be solved in the present invention is to provide a kind of method avoiding the recovery crude-gas sensible heat of interchanger coking.
Technical scheme of the present invention is:
Reclaim a method for crude-gas sensible heat, the upcast being included in coke oven installs heat-exchanger rig, and after three/two cycles of described coke oven coking cycles, the heat transferring medium in heat-exchanger rig starts flowing, starts the sensible heat reclaimed in raw gas." heat transferring medium in heat-exchanger rig start flowing " comprises the two-layer meaning, one refer to and arrive the fixed time after, just in heat-exchanger rig, load heat transferring medium, heat transferring medium starts flowing; Two is in heat-exchanger rig, install heat transferring medium at the very start, and after the arrival fixed time, open necessary by-pass valve control, heat transferring medium starts flowing.Heat-exchanger rig can be coil arrangement around upcast internal diameter or other structure.
According to the method for recovery crude-gas sensible heat of the present invention, further, reach 450-550 DEG C at the charge of coke center of described coke oven, the heat transferring medium in heat-exchanger rig starts flowing, starts the sensible heat reclaimed in raw gas.After above-mentioned coking cycles, in coke oven, Center Temperature of Coke Cake generally reaches 450 DEG C-550 DEG C.
Wherein preferably, the coking cycles of described coke oven is 17-25 hour.
According to the method for recovery crude-gas sensible heat of the present invention, preferably, heat transferring medium is selected from the one in deep fat, deaerated water, gas.
Preferably, the magnetic valve controlling the flowing of described heat transferring medium is provided with in described heat-exchanger rig.
In the process of raw gas waste heat recovery, tar mainly in raw gas of the generation of upcast inner tubal wall place's coking and tube wall heat exchange are met cold condensing to and tube wall are brought, in the coking process of a coking chamber, the composition of raw gas and temperature are unstable, dynamic change, so want to reclaim raw gas waste heat and the condensation coking controlling tar is very difficult.We find, pushing up traditional coking process of coalingging at present, at 2/3 section of a coking cycles, after this without any tar ingredients in raw gas, now the raw gas composition hydrogen that mainly secondary pyrolysis produces is the coal gas of main composition, the heat of this part can be free from all inhibitions recovery, coal gas amount accounts for the 20-25% of whole coking cycles gas production rate, in table 1,2.
Table 1, raw gas temperature and gas production rate
Table 2, dry distillation of coal change in process
Before each coking chamber coking cycles, in 2/3 time, ensure do not have heat transferring medium to flow into heat-exchanger rig, within rear 1/3 time of each coking chamber coking cycles, ensure heat transferring medium flow into heat exchange, can to ensure like this in heat transfer process in raw gas composition almost without any tar ingredients, heat exchange can control outlet raw gas temperature extremely low (less than 200 DEG C), the situation that all there will not be heat-transfer surface coking to affect heat exchange to carry out.Heat transferring medium accurate flow control in coking cycles is controlled by the magnetic valve of each upcast internal heat system, control the opening and closing of heat-exchange system magnetic valve in an all upcast of coke oven to realize the efficient recovery of raw gas waste heat by computer, the UTILIZATION OF VESIDUAL HEAT IN waste heat boiler production low-pressure steam of recovery is incorporated to pipe network.The advantage of present method is completely need not by the impact of tar coking problem.
All upcasts all install heat-exchange equipment, such as water jacket heat exchange, deep fat heat exchange, gas converting heat etc.According to the different coking times in one group of coke oven residing for coking chamber, by magnetic valve reasonable arrangement heat transferring medium coking chamber reach be in coking cycles rear 1/3 time in the abundant heat exchange of rising Bottomhole pressure, and by waste heat boiler recovery waste heat.A waste heat boiler is joined in every 100 hole coking chamber suggestions.Although 2/3 time raw gas waste heat cannot reclaim before the method coking, advantage is that processing method is simply easy to realize, and reclaims heat without misgivings, can avoid completely tar affects waste heat recovery problem in heat-transfer surface coking occurs.Present method can reclaim the 10-20% of raw gas waste heat, and heat-exchange system heat-transfer surface material adopts boiler heat exchange material to realize.
Accompanying drawing explanation
Fig. 1 is upcast and boiler heat exchange system diagrammatic top view.
Fig. 2 is heat-exchange system structure iron in upcast.
In figure, 1-rising tube wall, 2-heat exchange coil, 3-steel inner sleeve, 4-heat transfer space, direction shown in arrow A is gas flue.
Embodiment
Embodiment 1
Reclaim a method for crude-gas sensible heat, install heat-exchanger rig at the upcast of coke oven, after three/two cycles of coke oven coking cycles, open the valve of magnetic valve, the heat transferring medium in heat-exchanger rig starts flowing, starts the sensible heat reclaimed in raw gas.Described heat transferring medium is deep fat.
As shown in Figure 1, be the vertical view of upcast and boiler heat exchange system.
Fig. 2 is upcast heat-exchange system structure iron.Raw gas rises, through rising tube wall 1, by heat exchange coil 2, and heat exchange in the heat transfer space 4 between steel inner sleeve 3 and rising tube wall 1, thus reclaim the sensible heat in raw gas.
6 meters of high coke ovens, 100 holes, adopt 5-2 coke pushing string sequential mode (numeral is coking chamber numbering)
05101520253035404550556065707580859095
27121722273237424752576267727782879297
49141924293439444954596469747984899499
16111621263136414651566166717681869196
38131823283338434853586368737883889398
After 0 coking chamber coking time reaches 15 hours, if be now 00:00 point, open electromagnetic valve to pass into heat transferring medium and carry out heat exchange, (coking chamber treatment time+repair time) 00:12 after 12 minutes, 5 coking chambers are opened electromagnetic valve and are passed into heat transferring medium and carry out heat exchange, after 12 minutes (operating time+repair time) 00:24, 10 coking chambers are opened electromagnetic valve and are passed into heat transferring medium and carry out heat exchange, after 12 minutes (operating time+repair time) 00:36, 15 coking chambers are opened electromagnetic valve and are passed into heat transferring medium and carry out heat exchange, by that analogy, 25 coking chambers are 01:00, ..., 95 coking chambers are 03:48, 2 coking chambers are 04:00, 7 coking chambers are 04:12, 12 coking chambers are 04:24, 17 coking chambers are 04:36, 22 coking chambers are 04:48, 27 coking chambers are that 05:00 opens magnetic valve, close 0 coking chamber magnetic valve simultaneously, 32 coking chambers are that 05:12 opens magnetic valve, close 5 coking chamber magnetic valves simultaneously, by that analogy.This process is dynamic process, relevant for interval time with coke pushing with coking time, always has the upcast of 25 coking chambers passing into heat transferring medium and reclaim raw gas waste heat in process of coking.
Waste heat recovery volume calculates:
Calculate with 6 meters of coke ovens of 100 hole coking chambers, after raw gas heat exchange, temperature is 150 DEG C, and result is as follows:
Recovery waste heat amount: Q=CTV=1.69* (750-150) * 330*25%=83655kj/t dry coal
Annual heat-recoverable is equivalent to 1200000*83655/7000kcal*1000=3415 ton mark coal
Purified gas is 1.69kj/kg. DEG C 0-750 DEG C of mean specific heat;
Medial temperature 750 DEG C in purified gas upcast;
Ton dry coal gas production rate is 330m
3;
1kg standard coal heat is 7000kcal;
Embodiment 2
Install heat-exchanger rig at the upcast of coke oven, after three/two cycles of coke oven coking cycles, open the valve of magnetic valve, the heat transferring medium in heat-exchanger rig starts flowing, starts the sensible heat reclaimed in raw gas.Described heat transferring medium is nitrogen.
Other are with embodiment 1.
Embodiment 3
Or, also can select when the charge of coke center of coke oven reaches 450-550 DEG C, start magnetic valve, make heat transferring medium start flowing, start the sensible heat reclaimed in raw gas.But temperature measuring is inconvenient, during operation, adopt coking cycles method more convenient.
Other are with embodiment 1.
Advantage of the present invention does not worry the generation of coking completely, the deaerated water of low temperature or thermal oil can be used to carry out heat exchange as heat transferring medium and reclaim raw gas waste heat.
Claims (5)
1. one kind is reclaimed the method for crude-gas sensible heat, the upcast being included in coke oven installs heat-exchanger rig, it is characterized in that: after three/two cycles of described coke oven coking cycles, the heat transferring medium in heat-exchanger rig starts flowing, starts the sensible heat reclaimed in raw gas.
2. the method for recovery crude-gas sensible heat according to claim 1, is characterized in that: reach 450-550 DEG C at the charge of coke center of described coke oven, and the heat transferring medium in heat-exchanger rig starts flowing, starts the sensible heat reclaimed in raw gas.
3. the method for recovery crude-gas sensible heat according to claim 1, is characterized in that: the coking cycles of described coke oven is 17-25 hour.
4. the method for recovery crude-gas sensible heat according to claim 1, is characterized in that: described heat transferring medium is selected from the one in deep fat, deaerated water, gas.
5. the method for recovery crude-gas sensible heat according to claim 1, is characterized in that: be provided with the magnetic valve controlling the flowing of described heat transferring medium in described heat-exchanger rig.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4270980A (en) * | 1978-05-26 | 1981-06-02 | Nippon Kokan Kabushiki Kaisha | Method for recovering and utilizing heat of coke-oven gas |
| CN101619894A (en) * | 2008-06-30 | 2010-01-06 | 上海梅山钢铁股份有限公司 | Two-time condensation recovery device for waste heat of coke-oven crude gas |
| CN102786953A (en) * | 2012-08-31 | 2012-11-21 | 上海宝钢节能技术有限公司 | Coke oven grouped novel bridge pipe crude gas waste heat recovery device |
| CN102977901A (en) * | 2012-12-21 | 2013-03-20 | 刘庸 | Coke furnace rising pipe waste heat recovery device |
-
2013
- 2013-03-26 CN CN201310101105.1A patent/CN104073267B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4270980A (en) * | 1978-05-26 | 1981-06-02 | Nippon Kokan Kabushiki Kaisha | Method for recovering and utilizing heat of coke-oven gas |
| CN101619894A (en) * | 2008-06-30 | 2010-01-06 | 上海梅山钢铁股份有限公司 | Two-time condensation recovery device for waste heat of coke-oven crude gas |
| CN102786953A (en) * | 2012-08-31 | 2012-11-21 | 上海宝钢节能技术有限公司 | Coke oven grouped novel bridge pipe crude gas waste heat recovery device |
| CN102977901A (en) * | 2012-12-21 | 2013-03-20 | 刘庸 | Coke furnace rising pipe waste heat recovery device |
Non-Patent Citations (2)
| Title |
|---|
| 《宝钢大容积焦炉的操作与热工管理》;程乐意等;《炼铁》;20051230;第24卷(第S1期);第138-141页 * |
| 《焦炉上升管中荒煤气余热回收的结焦问题研究》;张政等;《洁净煤技术》;20120228(第1期);第79-81页 * |
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