CN103131432A - Method for recovering waste heat from coke oven raw gas - Google Patents
Method for recovering waste heat from coke oven raw gas Download PDFInfo
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- CN103131432A CN103131432A CN2013100624886A CN201310062488A CN103131432A CN 103131432 A CN103131432 A CN 103131432A CN 2013100624886 A CN2013100624886 A CN 2013100624886A CN 201310062488 A CN201310062488 A CN 201310062488A CN 103131432 A CN103131432 A CN 103131432A
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Abstract
The invention relates to a method for recovering waste heat from a coke oven raw gas. The method utilizes water as a heat exchange medium, water exchanges heat with the raw gas having a temperature of about 650-750DEG C in a riser heat exchanger, the temperature of the raw gas subjected to the heat exchange decreases to 480-550DEG C, the heat exchange medium forms a vapor-water mixture after heating, and enters a vapor bag, and the vapor-water mixture is separated to form high temperature water and saturated vapor by a vapor-water separator in the vapor bag; the raw gas discharged from the riser heat exchanger undergoes heat exchange in a bridge tube heat exchanger, the temperature of the raw gas subjected to the heat exchange decreases to 280-350DEG C, and the high temperature water obtained after the separation of the vapor-water separator undergoes heat exchange by the bridge tube heat exchanger, enters the vapor bag and generates saturated vapor, wherein the outer wall of the heat exchanger is cleaned through high-pressure ammonia water intermittent spray or water vapor intermittent blow in the bridge tube; and finally the temperature of the raw gas is reduced to 80-85DEG C by adopting ammonia water, and then the raw gas enters a gas collection tube. The method furthest recovers the waste heat of the raw gas and guarantees the continuous normal work of the heat exchangers under a complex condition.
Description
Technical field
The invention belongs to the high efficiente callback of process of coking residual heat resources and utilize technical field, particularly a kind of from coal oven dithio-gas the method for recovery waste heat.
Background technology
State Council points out in " energy-saving and emission-reduction " 12 " planning ", and it is one of ten large energy-saving and emission-reduction priority projects during " 12 " that the waste heat overbottom pressure is utilized engineering.The waste heat amount that produces in coking production process is large, can value high, have very large recycling value, be the energy-conservation importance of taping the latent power of coking industry.
650 ℃～750 ℃ high temperature raw gas that produce in the coke furnace carbonization chamber are overflowed through upcast.For the cooling down high-temperature raw gas, the traditional method of coking industry is to spray the cyclic ammonia water of a large amount of 70 ℃～75 ℃ at present, ammoniacal liquor absorbs heat and a large amount of evaporation, raw gas temperature is minimized to 80～85 ℃, after primary cooler further is cooled to normal temperature with coal gas, enters the recovery of postorder Coal Chemical Industry product and process workshop section again.The result of doing like this is: the heat that raw gas is taken out of is wasted, and the raw gas heat energy that both run off has increased again the consumption of water resources and the energy.
Calorific loss from process of coking distributes, the waste heat that raw gas contains has accounted for 36% left and right of total heat, the sensible heat amount of taking out of with red Jiao who releases from coking chamber is suitable, from the present economic benefit that produces of the waste heat that reclaims of ripe Dry Quenching Technology, the raw gas waste heat recovery also will produce considerable economic benefit, therefore, the recovery of coking high temperature raw gas waste heat becomes the heat subject of China's coking enterprise research and development in recent years.Coal chemical enterprise and research institutions associating in recent years, sum up experience and lessons, explore the UTILIZATION OF VESIDUAL HEAT IN approach, some achievements have been obtained, accumulated the experience of a lot of preciousnesses, mainly concentrated on upcast heat recovery technologies such as adopting thermal oil jacket pipe, heat pipe, boiler and semiconductor temperature differential generating and utilize the raw gas waste heat.
Yet, the upcast heat recovery technology is very limited its degree of utilizing to the raw gas waste heat because of the singularity of its heat exchange position, be mainly reflected in following three aspects: 1, the heat-obtaining temperature range is limited, in order to guarantee not a large amount of condensations in upcast of tar, raw gas temperature after heat-obtaining need remain on more than 480 ℃, and therefore the heat-obtaining of the reality front and back temperature difference is lower than 200 ℃; 2, only utilized the part sensible heat of raw gas, the condensation coking in order to prevent tar from undergoing phase transition can only obtain the sensible heat of a small amount of raw gas, and a large amount of latent heat and residue sensible heat are not recycled, therefore, the heat of its recovery only has less than 1/4th of heat that raw gas contains; 3, heat-obtaining efficient is low, is subjected to the restriction of upcast heat-exchanger rig heat exchange mode, and in the heat that migrates out, radiant heat occupies higher ratio, and only the raw gas of the heat-exchanger rig inwall of flowing through has been carried out effective heat exchange, and heat recovery efficiency is lower.Solution gradually along with aspect problems such as material, structures, the upcast heat recovery technology experienced development, stagnation, again after research and development, progressively moving towards industrial application, but be limited to the existence of above problem, the degree of depth of raw gas waste heat, efficient utilization still need the integrated use of more heat exchange modes to be achieved, and can not place hope on separately the upcast heat recovery technology.
In prior art, application number is to disclose the system and method that a kind of built-up type waste heat of coke oven crude gas reclaims superheated vapour in the Chinese patent application of 201210317957.X, this system and method adopts the mode that superheater is set and vaporizer is set in bridge tube in coke oven coke oven uprising tube, the steam water interface that produces in the bridge tube vaporizer enters the upcast superheater and produces superheated vapour after drum is isolated saturation steam.On the one hand, there is potential safety hazards such as doing the pot explosion in the upcast superheater that this method adopts, this is also to use unsuccessfully the 1970s and 1980s in last century " coke oven coke oven uprising tube gasification refrigerating mechanism ", the major cause that causes ascending tube crude-gas heat recovery technology development stagnation, on the other hand, the method does not provide rational solution for the tar condensing coking problem that produces after the bridge tube heat exchange.Application number is to disclose a kind of residual heat utilizing technology of coke oven crude gas in 200910230821.3 Chinese patent application, this technology is taked the raw gas with each carbonizing chamber to import boiler after collecting and is concentrated heat exchange, efficient is higher, but this technology has all restricted applying of this technology to raw gas delivery system strict insulation and seal request.
In a word, waste heat of coke oven crude gas reclaims must follow following principle: the one, reclaim on the spot, and avoid carrying the cooling coking and the sealingly secure problem that cause; The 2nd, rational deployment rationally utilizes limited space to reclaim to greatest extent the raw gas waste heat according to upcast and bridge tube practical situation separately; The 3rd, safety first, especially upcast heat-exchanger rig because of the singularity of its position, must be stopped various potential safety hazards.
Summary of the invention
Goal of the invention:
deficiency for the prior art existence, the present invention proposes a kind of method of recycling the raw gas waste heat from coal oven dithio-gas, the purpose of the method is to solve the high-quality heat waste that the cooling raw gas method of ammoniacal liquor in the past exists and consumption of cooling-water is large and the low problem of upcast waste-heat recovery device heat recovery efficiency, the mode that adopts simultaneously high pressure aqua ammonia intermittent shower or water vapor intermittently to purge solves the reduction of heat exchange efficiency problem that on bridge tube interchanger outer wall of inner tube, tar condenses and causes, can farthest reclaim sensible heat and the latent heat of raw gas, can guarantee again the continuous normal operation of heat-exchanger rig under complex working condition like this, with the waste heat that reclaims for generation of steam for Chemical Manufacture as thermal source or be used for generating, thereby realize the purpose of raw gas heat recovery.
Technical scheme:
The invention provides a kind of from coal oven dithio-gas the method for recovery waste heat, the method comprises the following steps:
A) the waste heat of coke oven crude gas retrieving arrangement is set, this device comprises upcast, bridge tube, upcast interchanger, bridge tube interchanger, drum, steam separator, service pump, deoxygenator; Wherein, described steam separator is arranged in described drum, and described upcast one end is connected to coke oven, and the other end is connected with an end of described bridge tube, and the other end of described bridge tube is connected to effuser; Raw gas is discharged through coke oven, arrives effuser through described upcast and described bridge tube successively; Wherein said deoxygenator receives the steam condensate from steam pipe system (or other sources), described service pump is connected to the entrance of described upcast interchanger, thereby the water after deoxygenation is sent into the entrance of described upcast interchanger, the outlet of described upcast interchanger is connected to described drum and enters described steam separator, the high-temperature water outlet of described steam separator is connected to the entrance of described bridge tube interchanger, the saturation steam outlet is connected to steam pipe system
B) utilize water as heat transferring medium, in the upcast interchanger with the approximately raw gas heat exchange of 650～750 ℃, the temperature of raw gas after heat exchange is reduced to 480～550 ℃, form steam water interface after heat transferring medium heats up and enter drum, be separated into high-temperature water and saturation steam by steam separator in drum;
The raw gas of c) discharging from the upcast interchanger is through the heat exchange of cross under interchanger, the temperature of raw gas after heat exchange is reduced to 280～350 ℃, high-temperature water described in a) enters drum and produces saturation steam after the heat exchange of bridge tube interchanger in step, and exchange heat pipe outer wall in the mode of bridge tube inner employing high pressure aqua ammonia intermittent shower or water vapor intermittently blowing and clean, and
E) adopt ammoniacal liquor that raw gas temperature is reduced to 80～85 ℃, enter effuser.
Wherein, all adopt pipeline to be connected between upcast interchanger and drum, between bridge tube interchanger and drum, and exchanging heat pipe outer wall in the mode of bridge tube inner employing high pressure aqua ammonia intermittent shower or water vapor intermittently blowing cleans, in order in time remove condensation and adhere to the tar of heat transfer tube outside wall surface, guarantee the patency that good heat transfer efficiency and raw gas flow.
In the method according to the application, at first the water after deoxygenation enter in the upcast interchanger as heat transferring medium, and then enter after treatment in the bridge tube interchanger as heat transferring medium.At first entering the bridge tube interchanger with water in prior art enters the upcast interchanger again and compares, the application with the water of lesser temps as the high temperature raw gas heat exchange in heat transferring medium and upcast, can effectively prevent from producing dry steam in upcast, thus the phenomenon that reduces and eliminate the explosion of dried pot.
In the method according to the application, exchange heat pipe outer wall in the mode of bridge tube inner employing high pressure aqua ammonia intermittent shower or water vapor intermittently blowing and clean.Compare with the technical scheme of the direct spraying cooling of ammoniacal liquor in prior art, the application's intermittent shower mode both can in time have been removed condensation and adhere to the tar of heat transfer tube outside wall surface, thereby guarantee the continuous normal operation of heat-exchanger rig under complex working condition like this, a large amount of wastes of heat in spray be can prevent again continuously, thereby sensible heat and the latent heat of raw gas farthest reclaimed.
The water vapor that above adopts can also can come from the drum of waste-heat recovery device from steam pipe system, and the small part steam that is about to the waste heat recovery generation is used for the cleaning of heat transfer tube outer wall.
The cleaning that the steam that employing steam pipe system or waste heat recovery produce is used for the heat transfer tube outer wall can reduce the calorific loss that cleans at heat transfer tube effectively.
One preferred embodiment in, described waste heat of coke oven crude gas retrieving arrangement can further comprise economizer, wherein, described economizer is connected between bridge tube and effuser, and heat transferring medium wherein is connected with the entrance of service pump and upcast interchanger, and, at described step e) further comprise before: d) utilize economizer further to reclaim the waste heat of raw gas, make raw gas temperature be reduced to 180～250 ℃.
One preferred embodiment in, described upcast interchanger adopts the jacketed pipe heat exchanger mode, walks raw gas in inner tube, leakes water in outer tube.Carry out and flow heat exchange from the water of circulating water main and raw gas, both all flow from bottom to top, the upcast inboard is heat insulating refractory material, and the outside is jacket heat-exchanger, can reclaim the high temperature sensible heat of raw gas more than 500 ℃ to avoid tar condensation coking on inwall.
The application's and the mode that flows heat exchange compare with the mode of cross-flow heat exchange in prior art, at first water at low temperature contacts the high temperature raw gas, the temperature of the high temperature raw gas that upcast bottom discharges from coke oven is fully reduced, prevented that further the phenomenon of dried pot explosion from occuring.
After having adopted the above-mentioned method according to the application, effectively prevented the phenomenon of the dried pot explosion in the upcast interchanger, and the heat that obtains in the upcast interchanger (steam quality) correspondingly decreases, in order to improve steam quality, the contriver is with upcast interchanger and the combination of bridge tube interchanger, the heat that provides by the bridge tube interchanger promotes steam quality, satisfies the downstream to the requirement of thermal source.
Another preferred embodiment in, described bridge tube interchanger adopts the tube and shell heat exchanger mode, tube side is water, shell side is raw gas.
Another preferred embodiment in, described bridge tube interchanger adopts the hot tube heat exchanger mode, namely adopts the method for inserting heat pipe in bridge tube that the heat of raw gas is conducted in the interchanger that is arranged in the bridge tube outside, the water that heating wherein contacts with heat pipe.
Another preferred embodiment in, the water after heat exchange enters drum, carries out carbonated drink and separate in drum, obtains the saturation steam that pressure is 0.4～1.0MPa.
Another preferred embodiment in, make the hot tube heat exchanger wing of described bridge tube outside.Hot tube heat exchanger after wing has increased heat interchanging area, reduces the convective heat exchange thermal resistance, improves total heat transfer property.
Thereby can incorporating steam pipe system into, the saturation steam that the method for recovery waste heat from coal oven dithio-gas obtains by coke oven coke oven uprising tube of the present invention and bridge tube combination provides thermal source for Chemical Manufacture, also can be used for steam-electric power, the steam condensate that obtains after use is through after desalination, enter and carry out thermal de-aeration in deoxygenator, deliver to the upcast interchanger by service pump again, so far complete water circuit.
Method according to the application, can be under the prerequisite of the total heat that the quality that guarantees to reclaim heat, raising are reclaimed, effectively prevent from doing the pot Decrepitation Phenomena, and can guarantee heat-exchanger rig normal operation continuously under complex working condition, greatly reduced the waste of Energy resources, improve equipment dependability, thereby improved production efficiency.
Description of drawings
Fig. 1 and Fig. 2 are the method flow schematic diagram that the raw gas waste heat is recycled in a kind of coke oven coke oven uprising tube provided by the invention and bridge tube combination.
In figure: 1, coke oven; 2, upcast 3, upcast interchanger; 4, bridge tube; 5, bridge tube interchanger; 6, drum; 7, deoxygenator; 8, service pump; 9, economizer; 21, ascending tube crude-gas outlet; 31, upcast heat exchanger entrance; 32, upcast heat exchanger exit; 41, bridge tube raw gas outlet; 42, high pressure aqua ammonia or steam entry; 43, a small amount of ammonia inlet; 51, bridge tube heat exchanger entrance; 52, bridge tube heat exchanger exit; 61, saturation steam; 71, de-mineralized water; 72, desalination deaerated water; 91, economizer entrance; 92, economizer exit.
Embodiment
By the following example, embodiment of the present invention are described.Yet, should be appreciated that embodiment of the present invention are not subject to the specific detail in the following example, because in view of disclosure of the present invention, other variations are known and apparent to those of ordinary skills.
Embodiment one:
Coke oven coke oven uprising tube and bridge tube combination waste-heat recovery device comprise upcast interchanger, bridge tube interchanger, drum and water feeding system.The concrete technology flow process that adopts is as follows: utilize service pump 8 to be transported in upcast interchanger 3 entrances 31 through the desalination deaerated water 72 that deoxygenator 7 carried out deoxidation treatment, heat exchange enters drum 6 by outlet 32 and carries out carbonated drink separation, the gained high-temperature water is after entrance 51 enters bridge tube interchanger 5 and carries out heat exchange, enter drum 6 and carry out carbonated drink and separate through exporting 52, producing pressure in drum is the saturation steam 61 of 0.4～1.0MPa.After raw gas passes through upcast interchanger and the heat exchange of bridge tube interchanger two-stage successively, temperature is down to 280～350 ℃, a small amount of ammoniacal liquor enters bridge tube heat exchanger exit place through entrance 43 and it is sprayed can make it be cooled to 80～85 ℃, then enters effuser through exporting 41.Wherein, high pressure aqua ammonia or water vapor enter the bridge tube top through entrance 42 the bridge tube exchanger tube wall are cleaned.
the tube side outer wall of bridge tube interchanger directly contacts with the raw gas cross-flow, when having improved heat exchange efficiency, also inevitably have above tar condenses in, thereby cause the working efficiency of interchanger to decrease, and might cause the obstruction of raw gas flow passage to a certain degree and cause safety problem, therefore the present invention has increased sprinkling system on this interchanger top, its spray medium can be high pressure aqua ammonia or water vapor, spray consumption and the frequency of medium by control, can in time remove the tar that condenses attached thereto, cleaning and the lubrication of realization to the tube side outer wall, guarantee good heat transfer efficiency, simultaneously, this spray also will be certain to the mobile generation of raw gas pushing effect, help to reduce the raw gas pressure reduction of interchanger front and back, guarantee the smoothness that raw gas flows in passage.And, for being cooled to the raw gas of 480～550 ℃ through the upcast interchanger, tar wherein in the situation that in the bridge tube interchanger process of heat exchanging pipe wall condensation and charing will greatly delay compared to 650～750 ℃, this just is conducive to adhere to the removal of tar more.
The advantage of this embodiment is to take full advantage of the high-quality waste heat of raw gas, the temperature of raw gas is reduced to 280～350 ℃, only reclaim high temperature sensible heat more than 480～500 ℃ compared to the upcast waste heat reclaiming process of applying, sensible heat and the latent heat of raw gas have been reclaimed more, and proposed to reclaim the solution of the tar condensing coking problem that raw gas latent heat causes, fundamentally guaranteed a difficult problem stable, safe retrieving raw gas waste heat.
Embodiment two:
Coke oven coke oven uprising tube and bridge tube combination waste-heat recovery device comprise upcast interchanger, bridge tube interchanger, economizer, drum and water feeding system.The concrete technology flow process is as follows: utilize service pump 8 will through desalination deaerated water 72 that deoxygenator 7 carried out deoxidation treatment through entrance 91 be transported to heat up in economizer 9 after, entered in upcast interchanger 3 entrances 31 by outlet 92, enter after heat exchange in drum 6, carry out carbonated drink separation, the gained high-temperature water is after entrance 51 enters 5 heat exchange of bridge tube interchanger, enter drum 6 again and carry out carbonated drink and separate through exporting 52, producing pressure in drum is the saturation steam 61 of 0.4～1.0MPa.After raw gas passes through upcast interchanger 3, bridge tube interchanger 5 and 9 three grades of heat exchange of economizer, temperature is down to 180～250 ℃, a small amount of ammoniacal liquor enters the economizer exit place through entrance 43 and it is sprayed can make it be cooled to 80～85 ℃, then enters effuser through exporting 41.Wherein, high pressure aqua ammonia or water vapor enter the bridge tube top through entrance 42 the bridge tube exchanger tube wall are cleaned.
The advantage of this embodiment is to take full advantage of the waste heat of raw gas, and the economizer of increase has further reclaimed the waste heat of 280～350 ℃ of raw gas, the temperature that enters upcast interchanger feedwater in order to lifting.Simultaneously, because raw gas temperature has been reduced to 180～250 ℃, so the ammonia spray consumption after economizer will reduce greatly.
Above-mentioned example is as an illustration purpose only, and scope of the present invention is not so limited.It is apparent modifying to one skilled in the art, and the present invention only is subjected to the restriction of claims scope.
Claims (9)
1. the method for a recovery waste heat from coal oven dithio-gas, the method comprises the following steps:
A) the waste heat of coke oven crude gas retrieving arrangement is set, this device comprises upcast, bridge tube, upcast interchanger, bridge tube interchanger, drum, steam separator, service pump, deoxygenator; Wherein, described steam separator is arranged in described drum, and described upcast one end is connected to coke oven, and the other end is connected with an end of described bridge tube, and the other end of described bridge tube is connected to effuser; Raw gas is discharged through coke oven, arrives effuser through described upcast and described bridge tube successively; Wherein said deoxygenator receives the steam condensate from steam pipe system or other sources, described service pump is connected to the entrance of described upcast interchanger, thereby the water after deoxygenation is sent into the entrance of described upcast interchanger, the outlet of described upcast interchanger is connected to described drum and enters described steam separator, the high-temperature water outlet of described steam separator is connected to the entrance of described bridge tube interchanger, the saturation steam outlet is connected to steam pipe system
B) utilize water as heat transferring medium, in the upcast interchanger with the approximately raw gas heat exchange of 650～750 ℃, the temperature of raw gas after heat exchange is reduced to 480～550 ℃, form steam water interface after heat transferring medium heats up and enter drum, be separated into high-temperature water and saturation steam by steam separator in drum;
The raw gas of c) discharging from the upcast interchanger is through the heat exchange of cross under interchanger, the temperature of raw gas after heat exchange is reduced to 280～350 ℃, high-temperature water described in a) enters drum and produces saturation steam after the heat exchange of bridge tube interchanger in step, and exchange heat pipe outer wall in the mode of bridge tube inner employing high pressure aqua ammonia intermittent shower or water vapor intermittently blowing and clean, and
E) adopt ammoniacal liquor that raw gas temperature is reduced to 80～85 ℃, enter effuser.
2. method according to claim 1, wherein, described water vapor is from steam pipe system or come from the drum of waste-heat recovery device.
3. method according to claim 1, wherein, described waste heat of coke oven crude gas retrieving arrangement can further comprise economizer, wherein, described economizer is connected between bridge tube and effuser, and heat transferring medium wherein is connected with the entrance of service pump and upcast interchanger, and, at described step e) further comprise before: d) utilize economizer further to reclaim the waste heat of raw gas, make raw gas temperature be reduced to 180～250 ℃.
4. method according to claim 1, wherein, described upcast interchanger adopts the jacketed pipe heat exchanger mode, walk raw gas in inner tube, leak water in outer tube, carry out and flow heat exchange from the water of circulating water main and raw gas, both all flow from bottom to top, the upcast inboard is heat insulating refractory material, and the outside is jacket heat-exchanger.
5. method according to claim 1, wherein, described bridge tube interchanger adopts the tube and shell heat exchanger mode, and tube side is water, and shell side is raw gas.
6. method according to claim 1, wherein, described bridge tube interchanger adopts the hot tube heat exchanger mode, namely adopts the method for inserting heat pipe in bridge tube that the heat of raw gas is conducted in the interchanger that is arranged in the bridge tube outside, the water that heating wherein contacts with heat pipe.
7. method according to claim 1, wherein, between upcast interchanger and drum, all adopt pipeline to be connected between bridge tube interchanger and drum.
8. method according to claim 1, wherein, the water after heat exchange enters drum, carries out carbonated drink separation in drum, obtains the saturation steam that pressure is 0.4～1.0MPa.
9. method according to claim 1, wherein, make the hot tube heat exchanger wing of described bridge tube outside.
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| CN104498057A (en) * | 2014-12-16 | 2015-04-08 | 济南冶金化工设备有限公司 | Recycling device and method for waste heat of high-temperature raw coal gas of coke oven |
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| CN108036290A (en) * | 2017-12-22 | 2018-05-15 | 中冶焦耐(大连)工程技术有限公司 | A kind of coal oven dithio-gas heat recovery process free of discontinuities |
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| CN110499168A (en) * | 2019-09-26 | 2019-11-26 | 葛霖 | A kind of series connection double base protection raw coke oven gas heat recovery heat exchanger tedge |
| CN111578247A (en) * | 2020-05-06 | 2020-08-25 | 武汉方特工业设备技术有限公司 | Waste heat recovery system |
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