CN102786951B - Crude gas guiding device for coal pyrolyzing furnace - Google Patents

Crude gas guiding device for coal pyrolyzing furnace Download PDF

Info

Publication number
CN102786951B
CN102786951B CN201210279196.3A CN201210279196A CN102786951B CN 102786951 B CN102786951 B CN 102786951B CN 201210279196 A CN201210279196 A CN 201210279196A CN 102786951 B CN102786951 B CN 102786951B
Authority
CN
China
Prior art keywords
raw gas
derivation
chamber
coal
feeder connection
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN201210279196.3A
Other languages
Chinese (zh)
Other versions
CN102786951A (en
Inventor
王新民
赵荣
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Shanxi Xinli Energy Technology Co Ltd
Original Assignee
Shanxi Xinli Energy Technology Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Shanxi Xinli Energy Technology Co Ltd filed Critical Shanxi Xinli Energy Technology Co Ltd
Priority to CN201210279196.3A priority Critical patent/CN102786951B/en
Publication of CN102786951A publication Critical patent/CN102786951A/en
Application granted granted Critical
Publication of CN102786951B publication Critical patent/CN102786951B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Abstract

The invention discloses a crude gas guiding device for a coal pyrolyzing furnace. The crude gas guiding device comprises a crude gas centralizing chamber, an inner guiding channel, an outer guiding channel, a main guiding channel and an annular guiding channel; the crude gas centralizing chamber is arranged on the top of a coking chamber of the coal pyrolyzing furnace, and the crude gas centralizing chamber and the coking chamber are integrally formed; the inner guiding channel is arranged in a flame path partition wall and penetrates through an inner ring wall of the coking chamber to lead to the coking chamber, and the outlet of the inner guiding channel penetrates through the inner ring wall to lead to the crude gas centralizing chamber; the outer guiding channel is arranged in an outer wall of the furnace body, a lower outer guiding channel inlet and an upper outer guiding channel inlet of the outer guiding channel penetrate through an outer ring wall of the coking chamber to lead to the coking chamber, and the outlet of the outer guiding channel penetrates the outer ring wall to lead to the crude gas centralizing chamber; and the main guiding channel is arranged in the outer wall of the furnace body to be communicated with the crude gas centralizing chamber, and extends upwards into the annular guiding channel arranged at the upper part of the outer wall of the furnace body, and the annular guiding channel is provided with a crude gas guiding port. The crude gas generated in the process of coal pyrolysis can be successfully guided by the crude gas guiding device.

Description

A kind of raw gas take-up gear of coal heat decomposition stove
Technical field
The present invention relates to a kind of gas eduction unit, particularly a kind of raw gas take-up gear of coal heat decomposition stove.
Background technology
Coal heat decomposition stove in the market (pit kiln) mostly adopts intermittent type coking, enter stove coal proportioning, dewater, enter coal, preheating, charing, burnt upgrading, dry each processing step such as put out is relatively independent, can not produce continuously, production efficiency is low; In addition, the raw gas producing in pyrolysis of coal process is containing a lot of useful compositions, as H 2s, HCH etc. sour gas, NH 3the organism such as alkaline gas, tar class, benzene class, naphthalene class, washing oil class, do not have the complete complete technique that raw gas derivation, reclaiming clean are used.
This impel the inventor to explore to create a set of complete Continuous coking and to raw gas derive, the reclaiming clean complete technique of recycle in addition.
Summary of the invention
The invention provides a kind of raw gas take-up gear of coal heat decomposition stove, this take-up gear can successfully be derived the raw gas producing in the pyrolysis of coal process of coking chamber.
Realizing the technical scheme that above-mentioned purpose takes is:
A raw gas take-up gear for coal heat decomposition stove, comprises raw gas concentration chamber, interior derivation passage, and outer derivation passage, derivation main channel, derive circuit; It is integrally formed that described raw gas concentration chamber is arranged on top and the coking chamber of coking chamber of coal heat decomposition stove; In described interior derivation channel setting quirk partition wall, interior derivation feeder connection leads to coking chamber through the interior ringwall of coking chamber, the raw gas concentration chamber that interior derivation channel outlet is led to coking chamber top through interior ringwall; In the exterior wall of described outer derivation channel setting body of heater, comprise lower outside derivation feeder connection, upper outside derivation feeder connection, described lower outside derivation feeder connection, upper outside derivation feeder connection lead to coking chamber through the outer ring wall of coking chamber, the raw gas concentration chamber that outer derivation channel outlet is led to coking chamber top through outer ring wall; Described derivation main channel is arranged in the exterior wall of body of heater of coal heat decomposition stove, derives main channel entrance and communicates with raw gas concentration chamber and extend up in the exterior wall top derivation circuit that body of heater is set again, and described derivation circuit arranges a raw gas export mouth.
Preferably, described interior derivation feeder connection and upper outside derivation feeder connection, lower outside derivation feeder connection arrange at least more than one respectively on the interior ringwall of coking chamber, outer ring wall.
Preferably, the setting of staggering up and down of described interior derivation feeder connection and lower outside derivation feeder connection, upper outside derivation feeder connection, described interior derivation feeder connection is higher than lower outside derivation feeder connection, but lower than upper outside derivation feeder connection place.
Preferably, the exterior wall of described body of heater is provided with the raw gas temperature monitoring holes that leads to raw gas concentration chamber, places raw gas temperature table in raw gas temperature monitoring holes.
Preferably, described raw gas temperature table is connected with industry control central electrical, and industry control center is by temperature in raw gas temperature table monitoring raw gas concentration chamber.
Constructional feature of the present invention be by the raw gas that different sections produce in coking chamber respectively from interior derivation feeder connection and lower outside derivation feeder connection, upper outside derivation feeder connection enter interior derivation passage and derivation passage collect again in raw gas concentration chamber in going out, certainly a large amount of raw gas in coking chamber are directly to rise up in raw gas concentration chamber, raw gas a large amount of in raw gas concentration chamber enter derivation circuit by deriving main channel, finally from raw gas export mouth, discharge.
Accompanying drawing explanation
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described in further detail.
Fig. 1 is F-F place enlarged view in Fig. 3;
Fig. 2 is w-w place schematic cross-section in Fig. 5;
Fig. 3 is the electrical connection schematic diagram at the present invention and industry control center;
Fig. 4 is general illustration in coal heat decomposition stove involved in the present invention;
Fig. 5 is the raw gas take-up gear assembling schematic diagram of coal heat decomposition stove of the present invention;
Fig. 6 is the raw gas condensing works schematic diagram of coal heat decomposition stove involved in the present invention;
Fig. 7 is afterburning air heating apparatus schematic diagram involved in the present invention;
Fig. 8 is d-d schematic cross-section in Fig. 7;
Fig. 9 is activated coke dry method withdrawer, activated coke bucket elevator, activated coke revivifier, cut tower, the oil gas air cooler assembling schematic diagram of raw gas reclaiming clean device involved in the present invention;
Figure 10 is cut tower, the oil gas air cooler assembling schematic diagram of raw gas reclaiming clean device involved in the present invention;
Figure 11 be raw gas reclaiming clean device involved in the present invention gas-liquid separator, air cooler,
Gas fan group assembling schematic diagram.
Embodiment
The specific embodiment of the raw gas take-up gear of a kind of coal heat decomposition stove of the present invention is mainly introduced in detail in following the 5th part chapter 1 first segment.
First is divided into stove coal proportioning and preparation
A kind of coal heat decomposition stove involved in the present invention, can enter stove coal proportioning according to different, obtains the coke that grade is different.
Following steps: 1) select 5 kinds of different coals, they are respectively bottle coal, rich coal, coking coal, 1/3rd coking coal, lean coal.2) bottle coal 20%~40% wherein; Rich coal 10%~20%; Coking coal 10%~20%; / 3rd coking coal 15%~30%; Lean coal 10%~15%, first mix the fragmentation of then sieving, until reaching 5mm, crushed particles is formed into below stove coal, certainly coal heat decomposition stove of the present invention to other proportioning and granular size to enter stove coal applicable equally, do not form the required restriction that enters stove coal dust of coal heat decomposition stove of the present invention, just by above, lifted enter stove coal proportioning and can reach more than 40% the weakly caking coal amount of allocating into, reduced the cost that enters stove coal and can obtain the coke of better quality again, on market, there is fine competitive power simultaneously.
Second section enters stove coal dewatering
Pit kiln in the market mostly adopts intermittent type coking, enters stove coal charge for wet coal, so power consumption has increased the cost of coking, enters dewatering of stove coal in advance by entering stove coal dewatering device to what enter this coal heat decomposition stove, plays energy-saving and cost-reducing effect.
Third part enters stove coal and enters coal, preheating, adjusting, cooling
Entering stove coal and generally can be down to normal temperature through temperature after carrying after dehydration, particularly winter temperature is lower, temperature may be lower, but but it is more suitable to wish that stove coal temperature remains between 200 ℃ to 300 ℃ during coking, so need to carry out preheating, adjusting, cooling before entering the coking chamber of coal heat decomposition stove to entering stove coal.
First segment enters stove coal and enters coal
Entering device for coal is used for entering stove coal after input dehydration
Second section enters the preheating of stove coal
Primary heater unit is arranged at into the below of device for coal and is positioned at the top of coal heat decomposition stove.Primary heater unit enters stove coal with preheating to what reduce through temperature after carrying.
The stove coal that enters after the 3rd joint preheating regulates
Enter stove coal surge bunker and be arranged on upper of furnace body and be positioned at primary heater unit bottom, enter stove coal surge bunker and be used for regulating in the coking chamber of coal heat decomposition stove and add the amount of injecting stove coal.
The 4th part enters stove pyrolysis of coal (charing heating, burnt upgrading, dry coke quenching)
First segment enters stove pyrolysis of coal charing heating
Enter in the coking chamber that stove coal enters coal heat decomposition stove and be heated and carry out pyrolysis charring, the purified gas that the raw gas producing in profit pyrolysis of coal process carries out after reclaiming clean carries out combustion heating, and utilizes the waste gas after burning to carry out the dry generation high-temperature combustible gas body combustion heating again that puts out.
The burnt upgrading of second section
Because coal carries out the coke forming after pyrolysis in coking chamber, the existence inequality of being heated, the situation that coke briquette grain size is irregular, preferably to coke, provide certain temperature and time, make fully to contact between coke, mutually carry out heat transmission, this just need to carry out burnt upgrading, utilize the waste heat of high temperature combustible exhaust gas itself that insulation institute's heat requirement and temperature are provided, the high temperature combustible exhaust gas temperature particularly just having entered is just applicable to burnt upgrading between 1000 ℃~1100 ℃, make coke retain certain hour in burnt upgrading chamber, fully contact between coke briquette grain, carry out each other heat transmission, reach evenly object of coke button size.
The 3rd joint quirk bow
The laying of various pipelines when providing support, is provided to internal combustion heating unit again in the effect of quirk bow.
The 4th joint dry coke quenching
Coke temperature after upgrading is higher, generally all at 1000 ℃~1100 ℃, need to carry out cooling could convenience to high temperature coke and carries and store, and need to carry out dry putting out.
The 5th joint continuous coking apapratus
Comprehensively above-mentioned, the feature of this routine Continuous coking is, by pyrolysis of coal charing, upgrading, the dry process integration that puts out in the hot body of heater of same coal, make charing, upgrading, dry putting out be able to continuous realization, overcome the discontinuous production efficiency of existing intermittent type coking technology technique low, how required the assorted plant area of equipment be large, the problem that human cost is high.
The comprehensive cyclic utilization of the 5th part, pyrolysis of coal gas
Chapter 1, the reclaiming clean utilization of raw gas (derivation, condensation, change are produced)
First segment raw gas take-up gear
The raw gas producing in pyrolysis of coal process is containing a lot of useful compositions, as H 2s, HCH etc. sour gas, NH 3the organism such as alkaline gas, tar class, benzene class, naphthalene class, washing oil class, need to derive to utilize raw gas.
As Fig. 5, raw gas take-up gear 8, comprises raw gas concentration chamber 81, interior derivation passage 82, and outer derivation passage 83, derivation main channel 84, derive circuit 85; It is integrally formed that raw gas concentration chamber 81 is arranged on top and the coking chamber 61 of coking chamber 61; As shown in Fig. 2, Fig. 5, interior derivation passage 82 arranges in quirk partition wall 635, and interior derivation feeder connection 821 leads to coking chamber 61 through interior ringwall 612 middle parts, the raw gas concentration chamber 81 that interior derivation channel outlet 822 is led to coking chamber top through interior ringwall 612; As shown in Fig. 2, Fig. 5, Fig. 1, outer derivation passage 83 arranges in the exterior wall of body of heater 91, lower outside derivation feeder connection 831, upper outside derivation feeder connection 834 lead to coking chamber 61 through outer ring wall 613 middle parts, the raw gas concentration chamber 81 that outer derivation channel outlet 832 is led to coking chamber top through outer ring wall 613.
As shown in Figure 5, deriving main channel 84 is arranged in the exterior wall of body of heater 91 of coal heat decomposition stove, derivation main channel entrance 841 communicates with raw gas concentration chamber 81 and extends up in the exterior wall top derivation circuit 85 that body of heater 91 is set again, and derives circuit 85 a raw gas export mouth 851 is set.
As Fig. 5, Fig. 2, shown in Fig. 1, in this example because coking chamber 61 annular chamber, so raw gas concentration chamber 81 is corresponding annular chamber also, article 6, in, deriving passage 82 is separately positioned in 6 road quirk partition walls 635, through interior ringwall 612, lead to coking chamber 61, article 6, outer derive passage 83 be separately positioned in the middle of body of heater 91 exterior walls through and outer quirk partition wall 625 and outer ring wall 613 lead to coking chamber 61, wherein, because the circumference of coking chamber 61, so interior ringwall 612 at coking chamber 61, on outer ring wall 613, be respectively arranged with a plurality of interior derivation feeder connections 821 and lower outside derivation feeder connection 831, upper outside derivation feeder connection 834, again because the height of coking chamber 61 is high, interior derivation feeder connection 821 and lower outside derivation feeder connection 831, the setting of staggering up and down of upper outside derivation feeder connection 834, as Fig. 5, in shown in Fig. 1, derive feeder connection 821 higher than lower outside derivation feeder connection 831, but lower than upper outside derivation feeder connection 834 places, this example adopts this structure better to derive the raw gas that in coking chamber 91, different sections produce, around raw gas concentration chamber 81, be also provided with 4 the larger raw gas of sectional area main channels 84 in addition and lead to derivation circuit 85, the object arranging like this can conveniently derive a large amount of raw gas in raw gas concentration chamber 81.
As shown in Figure 5, on the exterior wall of body of heater 91, be provided with the raw gas temperature monitoring holes 811 that leads to raw gas concentration chamber 81, in raw gas temperature monitoring holes 811, place raw gas temperature table 812.
As shown in Figure 3, raw gas temperature table 812 and 90 electrical connections of industry control center, industry control center 90 is by temperature in raw gas temperature table 812 monitoring raw gas concentration chamber 81.
This routine feature by the raw gas that different sections produce in coking chamber 61 respectively from interior derivation feeder connection 821 and lower outside derivation feeder connection 831, upper outside derivation feeder connection 834 enter interior derivation passage 82 and derivation passage collect again in raw gas concentration chamber 81 in going out 83, certainly a large amount of raw gas in coking chamber 61 are directly to rise up in raw gas concentration chamber 81, raw gas a large amount of in raw gas concentration chamber 81 enter derivation circuit 85 by deriving main channel 84, finally from raw gas export mouth 851, discharge.
Second section raw gas condensing works
As shown in Figure 5, higher from raw gas export mouth 851 discharge raw gas temperatures, for the ease of high temperature raw gas, changing antenatal conveying, need to use 86 pairs of high temperature raw gas of raw gas condensing works and carry out cooling.
As shown in Figure 6, raw gas condensing works 86 comprises, condensation housing 861, regulating wheel 862, sealing cover 860, threaded adjusting bar 863, water seal valve gap 864, water seal valve seat 865, effuser 867, ammoniacal liquor shower nozzle 868; Condensation housing 861 is long barrel shape, its side wall upper part offers raw gas admission port 869, ammoniacal liquor shower nozzle 868 is arranged on the top of condensation housing 861, stretch out and regulating wheel 862 thread connection from the top through hole 8611 of condensation housing 861 threaded adjusting bar 863 one end, sealing cover 860 is nested with on threaded adjusting bar 863 and is fixed on condensation housing 861, for shutoff top through hole 8611, prevent that raw gas from releasing from top through hole 8611; Threaded adjusting bar 863 the other ends and water seal valve gap 864 are connected to a fixed, water seal valve seat 865 is arranged on the interior middle and lower part of condensation housing 861 by upper and lower two of condensation housing 861 minutes, the water seal valve seat 865 middle parts one section of barrel-shaped opening bottleneck 8651 that raises up, water seal valve gap 864 tips upside down on opening bottleneck 8651; Effuser 867 is arranged on condensation housing 861 bottoms.
In addition, regulating wheel 862 can manual adjustment wheel, can also be the automatic regulating wheel with stepper-motor, and 90 pairs, industry control center regulating wheel 862 rotates and automatically controls as shown in Figure 3.
This routine feature is: when the raw gas of common 600 ℃~650 ℃ are discharged and entered condensation housing 861 by raw gas admission port 869 from raw gas export mouth 851, run into raw gas that the ammoniacal liquor of ammoniacal liquor shower nozzle 868 ejection lowered the temperature together with the mixed solution of coal tar and ammoniacal liquor, from flowing through between water seal valve gap 864 and barrel-shaped opening bottleneck 8651, enter condensation housing 861 bottoms, finally by effuser 867, carry and carry out follow-up purification recovery, this example drives threaded adjusting bar 863 to move up and down by the rotation of regulating wheel 862, thereby the degree of depth that drives water seal valve gap 864 to be buckled on opening bottleneck 8651 plays the raw gas pressure of controlling raw gas concentration chamber 81, booster action is played in pyrolysis of coal process control to coking chamber 61.
Described in comprehensive above first and second joint, a kind of raw gas of coal heat decomposition stove is derived condensation autocontrol method, and present method relates generally to and comprises raw gas take-up gear 8, raw gas condensing works 86, industry control center 90, and the step that present method realizes is:
(1) raw gas, by raw gas take-up gear 8, pyrolysis of coal in coking chamber 61 being produced is derived;
(2), the raw gas of derivation is passed into raw gas condensing works 8 and carry out ammoniacal liquor sprinkling cooling formation raw gas together with the mixed solution of coal tar and ammoniacal liquor;
(3), by industry control center 90, automatically regulate the regulating wheel of raw gas condensing works, thereby adjusting raw gas is realized the pressure-controlling to the raw gas in coking chamber 60 together with the circulation of the mixed solution of coal tar and ammoniacal liquor, plays the automatic control to pyrolysis of coal process.
The reclaiming clean of the 3rd joint raw gas
Raw gas after ammoniacal liquor sprays is transported to gas-liquid separation device together with the mixed solution of coal tar and ammoniacal liquor through effuser and carries out gas-liquid separation, in mixed solution after gas-liquid separation, contain multiple useful organic component and for industry, refine other auxiliary product as carbolic oil, naphtalene oil, washing oil, carbolineum etc., coal gas after gas-liquid separation is after air cooling cooling, after dry back receiving apparatus purifies recovery, become purified gas, purified gas can store for burning.
As shown in Figure 11, Fig. 9, Figure 10, raw gas reclaiming clean device 4 comprises gas-liquid separator 42, air cooler 43, gas fan group 44, activated coke dry method withdrawer 45, activated coke bucket elevator 46, activated coke revivifier 47, cut tower 48, oil gas air cooler 49.
As shown in Figure 11, Fig. 9, raw gas and coal tar and ammonia water mixture enter respectively in two branch roads through gas-liquid separation, raw gas Jing Yi road heating gas transfer lime 412 upwards leads to air cooler 43, coal tar and ammonia water mixture lead to coal tar ammonia precipitation process groove 42 downwards through another road mixed solution pipe 413, and coal tar ammonia precipitation process groove 42 is separated with ammonia precipitation process by coal tar; Air cooler 43 comprises air cooling housing 431, coal gas cooling pipe network (figure is not depending on going out), the inner air cooling chamber that forms of air cooling housing 431, coal gas cooling pipe network (figure is not depending on going out) forms independent loop and is placed in air cooling chamber, coal gas cooling pipe network entrance is connected with heating gas transfer lime 412 by the first air cooling gate valve 432, coal gas cooling pipe network outlet 433 is also provided with the second air cooling gate valve 434, gas fan group 44 is connected by the first air cooling gas conveying tube 414 and the second air cooling gate valve 434, and activated coke dry method withdrawer 45 communicates with gas fan group 44 by the second air cooling gas conveying tube 415.
As shown in Figure 9, activated coke dry method withdrawer 45 comprises that recycling shell collector 453, absorption storehouse 458, unsaturated activated coke enter storehouse 454, saturated active coke storage silo 456, recycling shell collector 453 is a cavity container, recycling shell collector 453 top purified gas output tubes 416, recycling shell collector 453 bottoms and the second gas conveying tube 415 are connected; Absorption storehouse 458 is arranged in sky recycling shell collector 453 between purified gas output tube 416 and the second gas conveying tube 415, top 4581, the bottom 4582 in absorption storehouse 458 are filtration net structure, absorption top, storehouse 4581 enters storehouse 454 with the unsaturated activated coke that is arranged on recycling shell collector 453 tops and is connected, and absorption top, storehouse 4581 and unsaturated activated coke enter the first recovery gate valve 455 is set between storehouse 454; Absorption storehouse bottom 4582 be arranged on recycling shell collector 453 bottoms with saturated active coke storage silo 456 is connected, bottom absorption storehouse 4582 and saturated active coke storage silo 456 between be provided with the second recovery gate valve 457.
As shown in Figure 9, activated coke revivifier 47 comprises revivifier housing 471, hot waste gas evaporation pipe network 472, unsaturated activated coke recovery bin 476, revivifier housing 471 is a cavity container, revivifier housing 471 tops are provided with saturated active coke and enter gate valve 475, bottom is provided with unsaturated activated coke discharge gate valve 474, unsaturated activated coke discharge gate valve 474 belows are provided with unsaturated activated coke recovery bin 476, are also provided with evaporation exhaust of oil pipe 473 on revivifier housing 471; 472 one-tenth independent loops of waste gas evaporation pipe network are arranged in revivifier housing 471 chambeies, the bottom of waste gas evaporation pipe network 472 is provided with hot waste gas and enters pipe 477, top is provided with hot waste gas delivery pipe 479, in order to increase hot waste gas at the flow velocity of waste gas evaporation pipe network 472, at waste gas evaporation pipe network 472 middle parts, be provided with waste gas circulation pipeline 478, waste gas circulation pipeline 478 stretch out revivifier housing 471 outer and hot waste gas blower fan (figure is not depending on going out) be connected.
As shown in Figure 9, activated coke bucket elevator 46 comprises saturated active coke bucket elevator 461, unsaturated activated coke bucket elevator 462, saturated active coke bucket elevator 461 one end are arranged in the saturated active coke storage silo 456 of activated coke dry method withdrawer 45 belows, and the saturated active coke that the other end leads to activated coke revivifier 47 tops enters gate valve 475; Unsaturated activated coke bucket elevator 462 one end are arranged in unsaturated activated coke recovery bin 476, and the unsaturated activated coke that the other end leads to activated coke dry method withdrawer 45 enters in storehouse 454.
As shown in figure 10, cut tower 48 comprises cut tower shell 481, crude benzol return channel 482, cut net 483, mixed triolein oil trap 484, carbolineum medial launder 485, cut tower shell 481 is a cavity container, the top of cut tower shell 481 is provided with light oil crude benzene vapor vent pipe 417, and cut tower shell 481 bottoms are carbolineum medial launder 485, cut net 483 is arranged in cut tower shell 481 and is positioned at the top of carbolineum medial launder 485, cut net 483 comprises lower cut net 4831, middle cut net 4832, upper cut net 4833, wherein descend cut net 4831, middle cut net 4832, upper cut net 4833 is disposed in cut tower shell 481 successively from top to bottom, lower cut net 4831, between middle cut net 4832, the evaporation exhaust of oil pipe 473 of cavity and activated coke revivifier 47 is connected, middle cut net 4832, upper cut net 4833 is provided with mixed triolein oil trap 484, between upper cut net 4833 and the top of cut tower shell 481, crude benzol return channel 482 is set.
As shown in figure 10, carbolineum medial launder 485 is mainly used to deposit carbolineum, and it is the common cooling structure of an industry (referring to the structrual description of following mixed triolein water cooler 487) that carbolineum medial launder 485 connects a carbolineum water cooler 486 with circulation pipe network.
As shown in figure 10, mixed triolein oil trap 484 comprises oil trap dividing plate 4841, oil trap is every cap 4842, in the middle of oil trap dividing plate 4841, raise up a split ring along 4843, oil trap every cap 4842 cover put split ring along 4843 on, split ring along 4843 and cut tower shell 481 between form oil-collecting tank 4844, oil-collecting tank 4844 slot parts are provided with the mixed triolein transfer lime 418 that passes cut tower shell 481, mixed triolein transfer lime 418 communicates with mixed triolein water cooler 487, mixed triolein water cooler 487 is common cooling structure, comprise and in cooler casing 4871, form waterway 4872, contaminated product cooling pipe network 4873 forms independent loop and is placed in waterway 4872, the entrance of contaminated product cooling pipe network 4873 communicates with mixed triolein transfer lime 418, the outlet of contaminated product cooling pipe network 4873 communicates with mixed triolein medial launder 488, mixed triolein medial launder 488 is mainly used to deposit mixed triolein.
As shown in figure 10, oil gas air cooler 49 comprises air cooler support body 491, air cooler pipe network 492, air cooling blower fan 493, air cooler support body 491 upper and lower parts form respectively airtight upper chamber 497, lower chamber 498, between upper chamber 497 and lower chamber 498, by air cooler pipe network 492, communicate, upper chamber 497 communicates with light oil crude benzene vapor vent pipe 417, lower chamber 498 is led in water-and-oil separator 495 and crude benzol backflash 496,495 industry common structures of water-and-oil separator, repeat no more.
This routine raw gas reclaiming clean technique is,
1, raw gas and coal tar ammonia water mixture are through gas-liquid separation, raw gas Jing Yi road heating gas transfer lime 412 upwards leads to air cooler 43 and carries out coolingly, and coal tar ammonia water mixture flows to tar ammonia settling bath 42 downwards through another road mixed solution pipe 413 and carries out precipitate and separate;
2, cooling raw gas is delivered in activated coke dry method withdrawer 45 and is carried out charcoal absorption through gas fan group 44, saturated gac falls into saturated active coke storage silo 456, through saturated activity charcoal bucket elevator 462, send into activated coke revivifier 47 and evaporate regeneration, unsaturated activated coke after evaporation falls into unsaturated activated coke recovery bin 476, through unsaturated activated coke bucket elevator 46, again send in activated coke dry method withdrawer 45 and enter absorption, so repeatedly carry out, purified gas after absorption is transported to combustion heater by purified gas output tube 416 and burns,
3, through activated coke revivifier 47, evaporate the light oil that contains of regeneration, crude benzol, mixed triolein, the compositions such as carbolineum enter cut tower 48 at oil gas by evaporation exhaust of oil pipe 473 and carry out cut, the carbolineum that proportion is larger flows in carbolineum medial launder by lower cut net 4833, the slightly heavy mixed triolein of proportion flows in the oil-collecting tank 4844 of mixed triolein oil trap 484, by mixed triolein transfer lime 418, enter in mixed triolein water cooler 487 cooling, finally store in mixed triolein medial launder 488, the light oil that proportion is lighter and crude benzol steam enter and oil gas air cooler 49, carry out condensation from light oil crude benzene vapor vent pipe 417, phlegma enters water-and-oil separator 495 and carries out oily water separation, light oil and crude benzol solution enter in crude benzol backflash 496, wherein a part is used for returning stream, part overflow is to light oil crude benzol medial launder.
Chapter 2, the recycle after raw gas reclaiming clean (burning, dryly put out, burnt upgrading, again burn, enter the preheating of stove coal, enter stove coal dewatering, tonifying Qi air heating)
First segment raw gas purifies the purified gas burning after reclaiming
Raw gas is through purifying after recovery, part purified gas be transported to this example above introduce enter combustion heater in the outer gas-operated thermal bath facility described in stove pyrolysis of coal charing part and the combustion heater in internal combustion heating unit burns, to pyrolysis of coal, provide thermal source.
Dry the putting out of waste gas after the burning of second section purified gas
Purified gas burning cmpletely in the combustion heater in gas-operated thermal bath facility and the combustion heater in internal combustion heating unit outside, utilize not combustion exhaust cmpletely to carry out the dry cooling of putting out to high temperature coke, generation water-gas can react when the moisture content in combustion exhaust does not contact with high temperature coke cmpletely, take away again remaining volatile combustible gases after high temperature coke upgrading simultaneously, the final high-temp waste gas that contains inflammable gas composition that forms, specifically see the introduction of above dry coke quenching chapters and sections, repeat no more here.
The burnt upgrading of high temperature combustible exhaust gas after dry the putting out of the 3rd joint
High temperature combustible exhaust gas temperature after dry putting out can reach 1000 ℃~1100 ℃, and burnt upgrading just in time need to be incubated upgrading at this temperature section, specifically how to be incubated upgrading, specifically sees and the introduction of above dry coke quenching chapters and sections repeats no more here.
High temperature combustible exhaust gas tonifying Qi burning again after dry the putting out of the 4th joint.
High temperature combustible exhaust gas is externally acting in STRENGTH ON COKE upgrading process, temperature can reduce, can drop to 900 ℃~1000 ℃, and pyrolysis of coal charing is temperature required higher in coking chamber, on average all at 1400 ℃~1500 ℃, so fill into air for the first time to high temperature combustible exhaust gas, carry out combustion heating, because coking chamber height is higher, and combustiblecomponents exists a certain amount of in high temperature combustible exhaust gas, so need to increase and have the 3rd combustion heater at internal combustion heating unit middle part, the 4th combustion heater is to supplement the required heat of pyrolysis of coal, finally on internal combustion heating unit top, fill into for the second time again air and carry out again abundant combustion heating by high temperature combustible exhaust gas, both reached to pyrolysis of coal and provided outside thermal source acting, can allow again high temperature combustible exhaust gas fully burn, the pollution of minimizing to atmospheric environment, specifically see the above narration entering in stove pyrolysis of coal charing, here repeat no more.
Hot waste gas after the 5th joint tonifying Qi burning enters the preheating of stove coal
Waste gas after the quenching waste gas heater burning of internal combustion heating unit, is discharged in exhaust air chamber, then to entering stove coal, carries out preheating by coal primary heater unit.
The 6th joint afterburning air heating
Waste gas after the preheating of coal preheater is transported to tubular heat exchanger and heats entering air in quenching waste gas heater, do not need extra thermal source to air heating, do not need to increase additional cost, both played the waste heat of the hot waste gas after the preheating of coal preheater had further been utilized, can give in quenching waste gas heater and fill into warm air again, high temperature combustible exhaust gas in quenching waste gas heater is fully burnt.
As Fig. 7, shown in Fig. 8, described tubular heat exchanger 40, comprise heat exchange housing 401, metal heat-exchange pipe network 403, hot waste gas admission passage 407, heat exchange waste gas exhaust channel 404, the interior formation waste gas heat radiation of heat exchange housing 401 chamber 402, hot waste gas admission passage 407 and heat exchange waste gas exhaust channel 404 are separately positioned on heat exchange housing 401 and with waste gas heat radiation chamber 402 and communicate, metal heat-exchange pipe network 403 is placed in waste gas heat radiation chamber 402, metal heat-exchange pipe network 403 comprises that air enters pipe 409 and Bas Discharged pipe 408, air enters pipe 409 and Bas Discharged pipe 408 stretches out respectively heat exchange housing 401 outsides.
As shown in Fig. 5, Fig. 7, Fig. 8, Fig. 4, exhaust air chamber 391 is assembled circuit 395 by heating by the exhaust gases passage 392 and waste gas and is communicated, the hot waste gas outlet 3951 that waste gas is assembled circuit 395 is connected to hot waste gas admission passage 407 by pipeline, the air airduct 6641 that air enters pipe 409 air blower 664 by pipeline and gas reversing system 66 is connected, Bas Discharged pipe 408 is mended pipe 632 with air and is connected, and heat exchange waste gas exhaust channel 404 is discharged main channel 405 with heat exchange waste gas and is connected.
This routine afterburning air heating Method And Principle is: the master of internal combustion heating unit, waste gas after secondary internal-quirk burning enters exhaust air chamber 391 from the bottom admission passage 3911 of exhaust air chamber 391 successively, after entering the preheating of stove coal by 392 pairs, heating by the exhaust gases passage, enter waste gas gathering circuit 395, from waste gas, assembling the waste gas primary outlet 3951 of circuit 395 discharges, temperature is now generally all 1000 ℃ of left and right, by hot waste gas admission passage 407, enter into waste gas heat radiation chamber 402 again and carry out heat exchange with metal heat-exchange pipe network 403, both played the waste heat of hot waste gas had further been utilized, can heat afterburning air again, promote the master of internal combustion heating unit, the high temperature combustible exhaust gas of secondary internal-quirk fully burns.
The 7th saves into stove coal dewatering
Hot waste gas is through to after afterburning air heating, and temperature decreases, and generally can drop to below 800 ℃, and for the relatively high hot waste gas of such temperature, a part can be used for to entering stove coal dewatering.
The 8th joint saturated active coke regeneration heating
Hot waste gas is through to after afterburning air heating, and temperature decreases, and generally can drop to below 800 ℃, and for the relatively high hot waste gas of such temperature, another part can be used for to saturated active coke regeneration heating.
The 6th part: pyrolysis of coal automatic control device
Comprehensively above-mentioned, as shown in Figure 3, pyrolysis of coal automatic control device comprises that industry control center 90 and above introduction connect thermometer and motor with industry control center 90.
Pyrolysis of coal automation control method comprises entering stove coal dewatering, enter the preheating of stove coal, entering the controls such as the adjusting of stove coal coal, the burning of outer gas-operated thermal bath facility, the commutation of gas reversing system, the adjusting of raw gas pressure of above introduction.
The 7th part: thermal cycling continuous and automatic coal heat decomposition stove
Comprehensively above-mentioned, thermal cycling continuous and automatic coal heat decomposition stove comprise above concrete introduction enter that stove coal enters coal, preheating, coal, cooling, charing, burnt upgrading, dryly puts out, raw gas derivation etc.

Claims (5)

1. a raw gas take-up gear for coal heat decomposition stove, is characterized in that: comprise raw gas concentration chamber, interior derivation passage, outer derivation passage, derivation main channel, derive circuit; It is integrally formed that described raw gas concentration chamber is arranged on top and the coking chamber of coking chamber of coal heat decomposition stove; In described interior derivation channel setting quirk partition wall, interior derivation feeder connection leads to coking chamber through the interior ringwall of coking chamber, the raw gas concentration chamber that interior derivation channel outlet is led to coking chamber top through interior ringwall; In the exterior wall of described outer derivation channel setting body of heater, comprise lower outside derivation feeder connection, upper outside derivation feeder connection, described lower outside derivation feeder connection, upper outside derivation feeder connection lead to coking chamber through the outer ring wall of coking chamber, the raw gas concentration chamber that outer derivation channel outlet is led to coking chamber top through outer ring wall; Described derivation main channel is arranged in the exterior wall of body of heater of coal heat decomposition stove, derives main channel entrance and communicates with raw gas concentration chamber and extend up in the exterior wall top derivation circuit that body of heater is set again, and described derivation circuit arranges a raw gas export mouth.
2. the raw gas take-up gear of a kind of coal heat decomposition stove according to claim 1, is characterized in that: described interior derivation feeder connection and upper outside derivation feeder connection, lower outside derivation feeder connection arrange at least one respectively on the interior ringwall of coking chamber, outer ring wall.
3. the raw gas take-up gear of a kind of coal heat decomposition stove according to claim 2, it is characterized in that: the setting of staggering up and down of described interior derivation feeder connection and lower outside derivation feeder connection, upper outside derivation feeder connection, described interior derivation feeder connection is higher than lower outside derivation feeder connection, but lower than upper outside derivation feeder connection place.
4. the raw gas take-up gear of a kind of coal heat decomposition stove according to claim 1, is characterized in that: the exterior wall of described body of heater is provided with the raw gas temperature monitoring holes that leads to raw gas concentration chamber, places raw gas temperature table in raw gas temperature monitoring holes.
5. the raw gas take-up gear of a kind of coal heat decomposition stove according to claim 4, is characterized in that: described raw gas temperature table is connected with industry control central electrical, and industry control center is by temperature in raw gas temperature table monitoring raw gas concentration chamber.
CN201210279196.3A 2012-08-06 2012-08-06 Crude gas guiding device for coal pyrolyzing furnace Active CN102786951B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201210279196.3A CN102786951B (en) 2012-08-06 2012-08-06 Crude gas guiding device for coal pyrolyzing furnace

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201210279196.3A CN102786951B (en) 2012-08-06 2012-08-06 Crude gas guiding device for coal pyrolyzing furnace

Publications (2)

Publication Number Publication Date
CN102786951A CN102786951A (en) 2012-11-21
CN102786951B true CN102786951B (en) 2014-03-12

Family

ID=47152544

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201210279196.3A Active CN102786951B (en) 2012-08-06 2012-08-06 Crude gas guiding device for coal pyrolyzing furnace

Country Status (1)

Country Link
CN (1) CN102786951B (en)

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103194272B (en) * 2013-04-10 2014-06-11 山西鑫立能源科技有限公司 Coal gangue pyrolysis gasification crude gas purified combustion recycling device
CN103215084B (en) * 2013-04-10 2014-07-02 山西鑫立能源科技有限公司 Coal gangue pyrolysis device
CN103224819B (en) * 2013-04-10 2014-07-02 山西鑫立能源科技有限公司 Guide, condensation, recovery and purification device of raw gas of coal gangue pyrolysis and gasification
CN103224814B (en) * 2013-04-10 2014-10-08 山西鑫立能源科技有限公司 Method for active coke regeneration through hot exhaust gas obtained by purification and combustion of coke oven raw gas in coal gangue pyrolysis gasification
CN103224818B (en) * 2013-04-10 2015-04-22 山西鑫立能源科技有限公司 Export condensation and recovery purification method for coke oven raw gas of coal gangue pyrolysis gasification

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1377649B1 (en) * 2001-04-12 2006-06-21 Fenner, Hans Rudolf Installation and method for producing energy using pyrolysis
CN202072660U (en) * 2011-06-13 2011-12-14 山西利华新科技开发有限公司 Coking furnace capable of circularly using heat energy
CN102250629B (en) * 2011-06-13 2013-09-04 山西利华新科技开发有限公司 Coking furnace capable of recycling heat energy and coking method
CN202116495U (en) * 2011-07-06 2012-01-18 中冶焦耐(大连)工程技术有限公司 Guiding device for crude gas of coke oven
CN102424757B (en) * 2011-12-16 2014-03-19 北京德天御投资管理有限责任公司 Gas heat carrier low-temperature retort furnace and dry quenching method
CN202898323U (en) * 2012-08-06 2013-04-24 山西鑫立能源科技有限公司 Raw gas exporting device of coal pyrolyzing furnace

Also Published As

Publication number Publication date
CN102786951A (en) 2012-11-21

Similar Documents

Publication Publication Date Title
CN102786951B (en) Crude gas guiding device for coal pyrolyzing furnace
CN103194265B (en) Thermal cycle continuous comprehensive method employing pyrolysis gasification of coal gangue
CN103194272B (en) Coal gangue pyrolysis gasification crude gas purified combustion recycling device
CN102786941A (en) Heat cycle continuous automatic coal pyrolyzing furnace
CN202786158U (en) Comprehensive coal pyrolysis gas recycling device
CN102816611B (en) Comprehensive and recycling utilization method of coal pyrolysis gases
CN103205278B (en) Thermal-cycle continuous pyrolysis-gasification comprehensive device for coal gangues
CN202953980U (en) Wild coal gas condensing device of coal pyrolysis furnace
CN102786952B (en) Crude gas condensing device for coal pyrolyzing furnace
CN103087783B (en) Device for exporting, condensing, recycling and purifying raw gas in coal pyrolysis furnace
CN202898323U (en) Raw gas exporting device of coal pyrolyzing furnace
CN102786974A (en) Automatic control method for crude gas lead-out and condensation of coal pyrolyzing furnace
CN202881216U (en) Delivery, condensation, recovery and purification device of raw gas in coal pyrolysis furnace
CN103224814B (en) Method for active coke regeneration through hot exhaust gas obtained by purification and combustion of coke oven raw gas in coal gangue pyrolysis gasification
CN103087782B (en) Method for exporting, condensing, recycling and purifying raw gas in coal pyrolysis furnace
CN203346360U (en) Raw gas exporting, condensation, recycling and purification device for pyrolysis gasification of coal gangue
CN102816580B (en) Method for preheating coal as fired by hot exhaust gas and regenerating active coke by hot exhaust gas
CN202936394U (en) Raw gas lead-out, condensation, recovery purification and combustion apparatus of coal pyrolyzing furnace
CN103113929B (en) Comprehensive recycling device for coal pyrolysis gas
CN203319950U (en) Regeneration device for active coke of hot waste gas generated by purifying and combusting raw coke oven gas during pyrolysis and gasification of coal gangue
CN203346355U (en) Raw gas purification, burning and recycling device for pyrolysis gasification of coal gangue
CN103275765B (en) Gangue pyrolysis gasification raw gas purification combustion recycle method
CN103242910B (en) Hot waste gas active coke regeneration device combining pyrolysis and gasification of coal gangue and purification and combustion of raw gas
CN102719258A (en) System and method for continuous pyrolysis and recycling application of biomass
CN103146438B (en) Raw coke oven gas conducting condensing and recovery and purification and combustion device for coal pyrolyzing furnace

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
COR Change of bibliographic data

Free format text: CORRECT: INVENTOR; FROM: WANG XINMIN TO: WANG XINMIN ZHAO RONG

CB03 Change of inventor or designer information
CB03 Change of inventor or designer information

Inventor after: Wang Xinmin

Inventor after: Zhao Rong

Inventor before: Wang Xinmin

GR01 Patent grant
GR01 Patent grant