CN103087782B - Method for exporting, condensing, recycling and purifying raw gas in coal pyrolysis furnace - Google Patents
Method for exporting, condensing, recycling and purifying raw gas in coal pyrolysis furnace Download PDFInfo
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- CN103087782B CN103087782B CN201210279068.9A CN201210279068A CN103087782B CN 103087782 B CN103087782 B CN 103087782B CN 201210279068 A CN201210279068 A CN 201210279068A CN 103087782 B CN103087782 B CN 103087782B
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Abstract
The invention discloses a method for exporting, condensing, recycling and purifying raw gas in a coal pyrolysis furnace. The method comprises the following steps of: (1) exporting raw gas out of a carbonization chamber; (2) spraying ammonia water onto the exported raw gas to cool the exported raw gas to form mixed liquor of raw gas together with coal tar and ammonia water; (3) adjusting the flow quantity of the mixed liquor of raw gas together with coal tar and ammonia water, thus controlling the pressure of the raw gas in the carbonization chamber; (4) carrying out gas-liquor separation on the mixed liquor of raw gas together with coal tar and ammonia water, cooling the raw gas and carrying out precipitation separation on the mixed liquor of coal tar and ammonia water; (5) adsorbing the cooled raw gas with active coke, carrying out evaporative regeneration on the saturated active coke, utilizing the evaporated unsaturated active coke to carry out adsorption again, repeating the processes and using the purified gas obtained after adsorption for combustion; and (6) carrying out evaporative regeneration and distillation on the saturated active coke. By the method, various organic matters of the raw gas are recycled so as to purify the raw gas into purified gas.
Description
Technical field
The present invention relates to a kind of gas and derive condensation and recovery and purification method, particularly a kind of raw gas of coal heat decomposition stove derives condensation and recovery and purification method.
Background technology
Coal heat decomposition stove (pit kiln) in the market mostly adopts intermittent type coking, the proportioning of as-fired coal, dewater, enter coal, preheating, charing, burnt upgrading, it is dry that each processing step such as to put out relatively independent, can not carry out continuous seepage, production efficiency is low; In addition, the raw gas produced in pyrolysis of coal process contains much useful composition, 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 be used to raw gas derivation, reclaiming clean.
This impel the present inventor to explore to create the Continuous coking of complete set and raw gas is derived, the complete technique of reclaiming clean in addition recycle.
Summary of the invention
The raw gas that the invention provides a kind of coal heat decomposition stove derives condensation and recovery and purification method, the method is by the technique being concatenated into complete set after the raw gas derivation produced in the pyrolysis of coal process of coking chamber, condensation, Recovery Purifying, realize in raw gas containing various useful composition as organic recovery such as tar class, benzene class, naphthalene class, washing oil classes, simultaneously again raw gas is cleaned into flammable purified gas.
Realizing the technical scheme that above-mentioned purpose takes is:
The raw gas of coal heat decomposition stove derives condensation and a recovery and purification method, and the equipment involved by present method comprises raw gas take-up gear, raw gas condensing works, raw gas reclaiming clean device, and the step that present method realizes is:
(1) raw gas, pyrolysis of coal in coking chamber produced by raw gas take-up gear is derived;
(2), the raw gas of derivation is passed into raw gas condensing works to carry out ammoniacal liquor and spray cooling and form the mixed solution of raw gas together with coal tar and ammoniacal liquor;
(3), by the regulating wheel of raw gas condensing works, regulate raw gas together with the circulation of the mixed solution of coal tar and ammoniacal liquor thus the pressure-controlling realized the raw gas in coking chamber;
(4), raw gas together with coal tar and ammonia water mixture through gas-liquid separation, raw gas upwards leads to air cooling through a road heating gas transfer lime of raw gas reclaiming clean device and cools, and coal tar ammonia water mixture flows to tar ammonia settling bath downwards through a road mixed solution pipe of another raw gas reclaiming clean device and carries out precipitate and separate;
(5), cooling raw gas is delivered to through gas fan group in the activated coke Dry recovery device of raw gas reclaiming clean device and is carried out activated coke absorption, saturated activated coke falls into saturated active coke storage silo, send into active coke through saturated active coke bucket elevator and carry out evaporation regeneration, unsaturated activated coke after evaporation falls into unsaturated activated coke recovery bin, again send in activated coke Dry recovery device through unsaturated activated coke bucket elevator and enter absorption, so repeatedly carry out, the purified gas after absorption is used for burning;
(6), active coke through raw gas reclaiming clean device carry out evaporating regeneration containing light oil, crude benzol, mixed triolein, the compositions such as carbolineum enter cut tower by evaporation exhaust of oil pipe and carry out cut, the carbolineum that proportion is larger flows in carbolineum medial launder by lower cut net, the slightly heavy mixed triolein of proportion flows in the oil-collecting tank of mixed triolein oil trap, entered in mixed triolein water cooler by mixed triolein transfer lime and cool, finally store in mixed triolein medial launder, the light oil that proportion is lighter and crude benzol steam enter oil gas air cooler from light oil crude benzene vapor vent pipe and carry out condensation, phlegma enters water-and-oil separator and carries out oily water separation, light oil and crude benzol solution enter in crude benzol backflash, wherein a part is used for returning stream, part overflow is to light oil crude benzol medial launder.
Feature of the present invention each the relatively independent technique such as raw gas derivation, condensation, Recovery Purifying produced in the pyrolysis of coal process of coking chamber will be conspired to create to a complete technique, realize in raw gas containing various useful composition as organic recovery such as tar class, benzene class, naphthalene class, washing oil classes, again raw gas is cleaned into flammable purified gas simultaneously, is convenient to raw gas recycle further again.
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 general illustration in coal heat decomposition stove involved in the present invention;
Fig. 4 is the electrical connection schematic diagram at industry control center involved in the present invention;
Fig. 5 is the raw gas take-up gear assembling schematic diagram of coal heat decomposition stove involved in 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 supplemental combustion air heating unit schematic diagram involved in the present invention;
Fig. 8 is d-d schematic cross-section in Fig. 7;
Fig. 9 is activated coke Dry recovery device, activated coke bucket elevator, active coke, 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 is gas-liquid separator, air cooler, the gas fan group assembling schematic diagram of raw gas reclaiming clean device involved in the present invention;
Embodiment
The raw gas derivation condensation of a kind of coal heat decomposition stove of the present invention and the specific embodiment of recovery and purification method are mainly introduced in detail in first, second and third joint of following Part V chapter 1.
First part's as-fired coal proportioning and preparation
A kind of coal heat decomposition stove involved in the present invention, according to different as-fired coal proportionings, can obtain the coke that grade is different.
Following steps: 1) select the coal that 5 kinds different, they are bottle coal, rich coal, coking coal, 1/3rd coking coal, lean coal respectively.2) wherein bottle coal 20% ~ 40%; Rich coal 10% ~ 20%; Coking coal 10% ~ 20%; / 3rd coking coal 15% ~ 30%; Lean coal 10% ~ 15%, first mix fragmentation of then sieving, until crushed particles reaches below 5mm form as-fired coal, the as-fired coal of certain coal heat decomposition stove of the present invention to other proportioning and granular size is applicable equally, do not form the restriction to as-fired coal powder needed for coal heat decomposition stove of the present invention, just can reach more than 40% to the weakly caking coal amount of allocating into by above lifted as-fired coal proportioning, the cost reducing as-fired coal can obtain again the coke of better quality simultaneously, commercially has fine competitive power.
Second section as-fired coal dewaters
Pit kiln in the market mostly adopts intermittent type coking, and as-fired coal material is wet coal, so power consumption, increases the cost of coking, is dewatered in advance by the carrying out of as-fired coal dewatering unit to the as-fired coal entering this coal heat decomposition stove, play energy-saving and cost-reducing effect.
Part III as-fired coal enters coal, preheating, adjustment, cooling
As-fired coal after dehydration temperature after conveying generally can be down to normal temperature, particularly winter temperature is lower, temperature may be lower, but but it is more suitable to wish during coking that as-fired coal temperature remains between 200 DEG C to 300 DEG C, so need before entering the coking chamber of coal heat decomposition stove, to carry out preheating, adjustment, cooling to as-fired coal.
First segment as-fired coal enters coal
Enter device for coal be used for input dehydration after as-fired coal
The preheating of second section as-fired coal
Primary heater unit is arranged at the below into device for coal and is positioned at the top of coal heat decomposition stove.The as-fired coal that primary heater unit preheating reduces temperature after conveying.
Section three, the as-fired coal after preheating regulates
As-fired coal surge bunker is arranged on upper of furnace body and is positioned at primary heater unit bottom, and as-fired coal surge bunker is used for regulating the amount of as-fired coal of annotating in the coking chamber of coal heat decomposition stove.
Part IV as-fired coal pyrolysis (charing heating, burnt upgrading, dry coke quenching)
First segment as-fired coal pyrolysis charring heats
As-fired coal enters in the coking chamber of coal heat decomposition stove and is carried out pyrolysis charring by heating, the purified gas that the raw gas produced 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 dry putting out to produce high-temperature combustible gas body combustion heating again.
The burnt upgrading of second section
Due to coal in coking chamber, carry out pyrolysis after the coke that formed, there is inequality of being heated, the situation that coke briquette grain size is irregular, preferably provide certain temperature and time to coke, make fully to contact between coke, mutually carry out heat trnasfer, this just needs to carry out burnt upgrading, the waste heat of high temperature combustible exhaust gas itself is utilized to provide insulation institute's heat requirement and temperature, the high temperature combustible exhaust gas temperature particularly just entered just is applicable to burnt upgrading between 1000 DEG C ~ 1100 DEG C, coke is made to retain certain hour in burnt upgrading room, fully contact between coke briquette grain, carry out heat trnasfer each other, reach the even object of coke button size.
Section three, Flame path arch
There is provided the laying of various pipeline to again while the effect of Flame path arch provides support combustion heating unit.
Section four, dry coke quenching
Coke temperature after upgrading is higher, generally all at 1000 DEG C ~ 1100 DEG C, needs to carry out cooling to high temperature coke and could facilitate conveying and store, need to carry out dry putting out.
Section five, 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, charing, upgrading, dry putting out is made to be able to continuous realization, overcome the discontinuous production efficiency of existing intermittent type coking technology technique low, the assorted many required plant areas of equipment are large, the problem that human cost is high.
The comprehensive cyclic utilization of Part V, pyrolysis of coal gas
Chapter 1, the reclaiming clean of raw gas utilizes (derivation, condensation, change are produced)
First segment raw gas take-up gear
The raw gas produced in pyrolysis of coal process contains much useful composition, 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; Raw gas concentration chamber 81 be arranged on the top of coking chamber 61 and coking chamber 61 integrally formed; 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 in the middle part of interior ringwall 612, and interior derivation channel outlet 822 leads to the raw gas concentration chamber 81 at 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 in the middle part of outer ring wall 613, and outer derivation channel outlet 832 leads to the raw gas concentration chamber 81 at 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, derive main channel inlets 841 to communicate with raw gas concentration chamber 81 and extend up to the exterior wall top arranging body of heater 91 again and derive in circuit 85, derivation circuit 85 arranges a raw gas export mouth 851.
As Fig. 5, Fig. 2, shown in Fig. 1, because coking chamber 61 annular chamber in this example, so raw gas concentration chamber 81 also corresponding annular chamber, article 6, deriving passage 82 in is separately positioned in 6 road quirk partition walls 635, coking chamber 61 is led to through interior ringwall 612, article 6, outer derivation passage 83 is separately positioned in the middle of body of heater 91 exterior wall and leads to coking chamber 61 through with outer quirk partition wall 625 and outer ring wall 613, wherein, because the circumference of coking chamber 61, so in coking chamber 61 ringwall 612, outer ring wall 613 is respectively arranged with multiple interior derivation feeder connection 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, upper outside derivation feeder connection about 834 staggers setting, as Fig. 5, feeder connection 821 is derived higher than lower outside derivation feeder connection 831 in shown in Fig. 1, but lower than upper outside derivation feeder connection 834 place, this example adopts this structure better can to derive the raw gas that section different in coking chamber 91 produces, also be provided with 4 larger raw gas main channels 84 of sectional area around raw gas concentration chamber 81 in addition and lead to derivation circuit 85, the object of such setting conveniently can derive a large amount of raw gas in raw gas concentration chamber 81.
As shown in Figure 5, the exterior wall of body of heater 91 is provided with the raw gas temperature monitoring holes 811 leading to raw gas concentration chamber 81, in raw gas temperature monitoring holes 811, places raw gas temperature table 812.
As shown in Figure 3, raw gas temperature table 812 and industry control center 90 are electrically connected, and temperature in raw gas concentration chamber 81 is monitored by raw gas temperature table 812 in industry control center 90.
The raw gas that section different in coking chamber 61 produces is entered interior derivation passage 82 from interior derivation feeder connection 821 and lower outside derivation feeder connection 831, upper outside derivation feeder connection 834 to this routine feature respectively and outer derivation passage goes out 83 to collect in raw gas concentration chamber 81 again, a large amount of raw gas in certain coking chamber 61 directly rise up in raw gas concentration chamber 81, raw gas a large amount of in raw gas concentration chamber 81 enters derivation circuit 85 by deriving main channel 84, finally discharges from raw gas export mouth 851.
Second section raw gas condensing works
As shown in Figure 5, discharge raw gas temperature from raw gas export mouth 851 higher, carry change is antenatal for the ease of high temperature raw gas, need to use raw gas condensing works 86 pairs of high temperature raw gas and cool.
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 in 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, threaded adjusting bar 863 one end is stretched out and regulating wheel 862 thread connection from the top through hole 8611 of condensation housing 861, 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 raw gas from releasing from top through hole 8611; Threaded adjusting bar 863 the other end and water seal valve gap 864 are connected to a fixed, water seal valve seat 865 to be arranged in condensation housing 861 middle and lower part by condensation housing about 861 points two, raise up in the middle part of water seal valve seat 865 one section of barrel-shaped opening bottleneck 8651, and water seal valve gap 864 tips upside down on opening bottleneck 8651; Effuser 867 is arranged on bottom condensation housing 861.
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: enter condensation housing 861 when the raw gas of usual 600 DEG C ~ 650 DEG C are discharged from raw gas export mouth 851 by raw gas admission port 869, run into the ammoniacal liquor raw gas of being lowered the temperature that ammoniacal liquor shower nozzle 868 the sprays mixed solution together with coal tar and ammoniacal liquor, condensation housing 861 bottom is entered from flowing through between water seal valve gap 864 and barrel-shaped opening bottleneck 8651, subsequent purification recovery is carried out finally by effuser 867 conveying, this example drives threaded adjusting bar 863 to move up and down by the rotation of regulating wheel 862, thus drive water seal valve gap 864 degree of depth be buckled on opening bottleneck 8651 to play the raw gas pressure controlling raw gas concentration chamber 81, booster action is played to the pyrolysis of coal process control of coking chamber 61.
Described in comprehensive first and second joint above, condensation autocontrol method derived by a kind of raw gas of coal heat decomposition stove, 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, pyrolysis of coal in coking chamber 61 produced by raw gas take-up gear 8 is derived;
(2), the raw gas of derivation is passed into raw gas condensing works 8 to carry out ammoniacal liquor and spray cooling and form the mixed solution of raw gas together with coal tar and ammoniacal liquor;
(3) regulating wheel of raw gas condensing works, is automatically regulated by industry control center 90, regulate raw gas together with the circulation of the mixed solution of coal tar and ammoniacal liquor thus the pressure-controlling realized the raw gas in coking chamber 60, play the automatic control to pyrolysis of coal process.
Section three, the reclaiming clean of 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, other auxiliary product is refined containing multiple useful organic component such as carbolic oil, naphtalene oil, washing oil, carbolineum etc. for industry in mixed solution after gas-liquid separation, coal gas after gas-liquid separation is after air cooling cooling, after Dry recovery device Recovery Purifying, 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 recovery device 45, activated coke bucket elevator 46, active coke 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 in two branch roads through gas-liquid separation respectively, raw gas upwards leads to air cooler 43 through a road heating gas transfer lime 412, 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 is separated with ammonia precipitation process by coal tar ammonia precipitation process groove 42, air cooler 43 comprises air cooling housing 431, coal gas cooling pipe network (figure is not depending on going out), air cooling housing 431 inside forms air cooling chamber, 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, activated coke Dry recovery device 45 is communicated with gas fan group 44 by the second air cooling gas conveying tube 415.
As shown in Figure 9, activated coke Dry recovery device 45 comprises 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 tube 416, recycling shell collector 453 bottom and the second gas conveying tube 415 are connected; Absorption storehouse 458 to be 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 being arranged on recycling shell collector 453 top and is connected, and absorption top, storehouse 4581 and unsaturated activated coke enter between storehouse 454 and arrange the first recovery gate valve 455; Bottom absorption storehouse, 4582 are connected with saturated active coke storage silo 456 with being arranged on bottom recycling shell collector 453, and absorption is provided with the second recovery gate valve 457 bottom storehouse between 4582 and saturated active coke storage silo 456.
As shown in Figure 9, active coke 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 top is provided with saturated active coke and enters gate valve 475, bottom is provided with unsaturated activated coke discharge gate valve 474, be provided with unsaturated activated coke recovery bin 476 below unsaturated activated coke discharge gate valve 474, revivifier housing 471 be also provided with evaporation exhaust of oil pipe 473; Waste gas evaporation pipe network 472 one-tenth independent loop is arranged in revivifier housing 471 chamber, 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 the flow velocity of hot waste gas at waste gas evaporation pipe network 472, in the middle part of waste gas evaporation pipe network 472, 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 (scheming depending on not 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 is arranged in the saturated active coke storage silo 456 below activated coke Dry recovery device 45, and the saturated active coke that the other end leads to active coke 47 top enters gate valve 475; Unsaturated activated coke bucket elevator 462 one end is arranged in unsaturated activated coke recovery bin 476, and the unsaturated activated coke that the other end leads to activated coke Dry recovery device 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, is carbolineum medial launder 485 bottom cut tower shell 481, cut net 483 to be arranged in cut tower shell 481 and to be 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 active coke 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 (structrual description see following mixed triolein water cooler 487) of an industry 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, raise up a split ring along 4843 in the middle of oil trap dividing plate 4841, oil trap is put at split ring along on 4843 every cap 4842 cover, split ring forms oil-collecting tank 4844 along between 4843 and cut tower shell 481, oil-collecting tank 4844 groove portion is provided with the mixed triolein transfer lime 418 passing 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 in cooler casing 4871 and 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 part forms airtight upper chamber 497, lower chamber 498 respectively, communicated by air cooler pipe network 492 between upper chamber 497 and lower chamber 498, 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, water-and-oil separator 495 industry common structures, repeat no more.
Comprehensively go out a kind of raw gas by the content described in first, second and third joint of more than this chapter and derive condensation and reclaiming clean device and method, this device comprises raw gas take-up gear 8, raw gas condensing works 86, raw gas reclaiming clean device 4.
The step that present method realizes is:
(1) raw gas, pyrolysis of coal in coking chamber 61 produced by raw gas take-up gear 8 is derived;
(2), the raw gas of derivation is passed into raw gas condensing works 8 to carry out ammoniacal liquor and spray cooling and form the mixed solution of raw gas together with coal tar and ammoniacal liquor;
(3), by the regulating wheel 83 of raw gas condensing works 8, regulate raw gas together with the circulation of the mixed solution of coal tar and ammoniacal liquor thus the pressure-controlling realized the raw gas in coking chamber 61;
(4), raw gas together with coal tar and ammonia water mixture through gas-liquid separation, raw gas upwards leads to air cooler 43 through a road heating gas transfer lime 412 of raw gas reclaiming clean device 4 and cools, and coal tar ammonia water mixture flows to tar ammonia settling bath 42 downwards through a road mixed solution pipe 413 of another raw gas reclaiming clean device 4 and carries out precipitate and separate;
(5), cooling raw gas is delivered to through gas fan group 44 in the activated coke Dry recovery device 45 of raw gas reclaiming clean device 4 and is carried out activated coke absorption (also can be referred to as activated coke absorption in industry), saturated activated coke falls into saturated active coke storage silo 456, send into active coke 47 through saturated active coke bucket elevator 462 and carry out evaporation regeneration, unsaturated activated coke after evaporation falls into unsaturated activated coke recovery bin 476, again send in activated coke Dry recovery device 45 through unsaturated activated coke bucket elevator 46 and enter absorption, so repeatedly carry out, purified gas after absorption is transported to combustion heater by purified gas output tube 416 and burns,
(6), active coke 47 through raw gas reclaiming clean device 4 carry out evaporating regeneration containing light oil, crude benzol, mixed triolein, the compositions such as carbolineum enter cut tower 48 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, entered in mixed triolein water cooler 487 by mixed triolein transfer lime 418 and cool, finally store in mixed triolein medial launder 488, the light oil that proportion is lighter and crude benzol steam enter oil gas air cooler 49 from light oil crude benzene vapor vent pipe 417 and carry out condensation, 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, recycle after raw gas reclaiming clean (burning, dryly to put out, burnt upgrading, again burning, as-fired coal preheating, as-fired coal dewater, tonifying Qi air heating)
Purified gas burning after first segment raw gas Recovery Purifying
Raw gas is after Recovery Purifying, part purified gas is transported to the combustion heater in the above outer gas-operated thermal bath facility described in as-fired coal pyrolysis charring part introduced of this example and the combustion heater in combustion heating unit burns, and provides thermal source to pyrolysis of coal.
Waste gas after the burning of second section purified gas is dry to be put out
Do not burn cmpletely in the combustion heater of purified gas outside in gas-operated thermal bath facility and the combustion heater in combustion heating unit, utilize not cmpletely combustion exhaust carry out dryly putting out cooling to high temperature coke, moisture content not cmpletely in combustion exhaust can react when contacting with high temperature coke generation water-gas, volatile combustible gases remaining after simultaneously taking away again high temperature coke upgrading, final formation contains the high-temp waste gas of inflammable gas composition, specifically see the introduction of above dry coke quenching chapters and sections, repeat no more here.
Section three, dry put out after the burnt upgrading of high temperature combustible exhaust gas
Dry put out after high temperature combustible exhaust gas temperature can reach 1000 DEG C ~ 1100 DEG C, and burnt upgrading just in time needs to carry out insulation upgrading at this temperature section, specifically how to carry out insulation upgrading, specifically sees and the introduction of above dry coke quenching chapters and sections repeats no more here.
Section four, dry put out after the tonifying Qi burning again of high temperature combustible exhaust gas.
High temperature combustible exhaust gas externally does work in STRENGTH ON COKE upgrading processes, temperature can reduce, 900 DEG C ~ 1000 DEG C can be dropped to, and pyrolysis of coal charing is temperature required higher in coking chamber, average all at 1400 DEG C ~ 1500 DEG C, 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 in the middle part of combustion heating unit have the 3rd combustion heater, 4th combustion heater is with the heat needed for supplementary pyrolysis of coal, last second time of carrying out again on combustion heating unit top fills into air and carries out Thorough combustion heating again by high temperature combustible exhaust gas, both reached and provided outside thermal source acting to pyrolysis of coal, can allow again high temperature combustible exhaust gas Thorough combustion, reduce the pollution to atmospheric environment, specifically see describing in above as-fired coal pyrolysis charring, here repeat no more.
Section five, the hot waste gas as-fired coal preheating after tonifying Qi burning
Waste gas after the quenching waste gas heater burning of combustion heating unit, is discharged in exhaust air chamber, then carries out preheating by coal primary heater unit to as-fired coal.
Section six, supplemental combustion air heating
Waste gas after coal preheater preheats 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 and the waste heat of the hot waste gas after coal preheater preheats had been utilized further, can give in quenching waste gas heater again and fill into warm air, make high temperature combustible exhaust gas Thorough combustion in quenching waste gas heater.
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, waste gas heat dissipation cavity 402 is formed in heat exchange housing 401, hot waste gas admission passage 407 and heat exchange waste gas exhaust channel 404 to be separately positioned on heat exchange housing 401 and to communicate with waste gas heat dissipation cavity 402, metal heat-exchange pipe network 403 is placed in waste gas heat dissipation cavity 402, metal heat-exchange pipe network 403 comprises air and enters pipe 409 and air discharge duct 408, air enters pipe 409 and air discharge duct 408 stretches out heat exchange housing 401 outside respectively.
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 assembles circuit 395 is connected to hot waste gas admission passage 407 by pipeline, air is entered pipe 409 and is connected by the air duct 6641 of the air blower 664 of pipeline and gas reversing system 66, air discharge duct 408 and air are mended pipe 632 and are connected, and heat exchange waste gas exhaust channel 404 and heat exchange waste gas are discharged main channel 405 and is connected.
The supplemental combustion air heating means principle of this example is: the master of 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, circuit 395 is assembled by entering waste gas after the 392 pairs of as-fired coal preheatings of heating by the exhaust gases passage, the waste gas primary outlet 3951 assembling circuit 395 from waste gas is discharged, temperature is now general all at about 1000 DEG C, enter into waste gas heat dissipation cavity 402 by hot waste gas admission passage 407 again and carry out heat exchange with metal heat-exchange pipe network 403, both played and the waste heat of hot waste gas had been utilized further, supplemental combustion air can be heated again, promote the master of combustion heating unit, the high temperature combustible exhaust gas Thorough combustion of secondary internal-quirk.
Section seven, as-fired coal dehydration
Hot waste gas is after to supplemental combustion air heating, and temperature decreases, and generally can drop to less than 800 DEG C, and for the hot waste gas that such temperature is relatively high, a part can be used for dewatering to as-fired coal.
Section eight, saturated active coke regeneration heating
Hot waste gas is after to supplemental combustion air heating, and temperature decreases, and generally can drop to less than 800 DEG C, and for the hot waste gas that such temperature is relatively high, another part can be used for saturated active coke regeneration heating.
Part VI: pyrolysis of coal automatic control device
Comprehensively above-mentioned, as shown in Figure 3, pyrolysis of coal automatic control device comprises industry control center 90 and above introduction connects thermometer and motor with industry control center 90.
Pyrolysis of coal automation control method comprises the control such as as-fired coal dehydration, as-fired coal preheating, the adjustment of as-fired coal coal, the burning of outer gas-operated thermal bath facility, the commutation of gas reversing system, the adjustment of raw gas pressure of above introduction.
Part VII: thermal cycling continuous and automatic coal heat decomposition stove
Comprehensively above-mentioned, the as-fired coal that thermal cycling continuous and automatic coal heat decomposition stove comprises above concrete introduction enters coal, preheating, coal, cooling, charing, burnt upgrading, dryly to put out, raw gas derivation etc.
Claims (1)
1. the raw gas of coal heat decomposition stove derives condensation and a recovery and purification method, it is characterized in that: the equipment involved by present method comprises raw gas take-up gear, raw gas condensing works, raw gas reclaiming clean device, and the step that present method realizes is:
(1), by raw gas take-up gear the raw gas that different section in coking chamber produces entered from interior derivation feeder connection and lower outside derivation feeder connection, upper outside derivation feeder connection respectively and collect in raw gas concentration chamber again interior derivation passage and outer derivation passage, a large amount of raw gas in coking chamber directly rise up in raw gas concentration chamber, raw gas a large amount of in raw gas concentration chamber enters derivation circuit by deriving main channel, finally discharges from raw gas export mouth;
(2), the raw gas of derivation is passed into raw gas condensing works to carry out ammoniacal liquor and spray cooling and form the mixed solution of raw gas together with coal tar and ammoniacal liquor;
(3), threaded adjusting bar is driven to move up and down by the rotation of the regulating wheel of raw gas condensing works, thus drive the degree of depth of water-sealed valve cover buckle on opening bottleneck, regulate raw gas together with the circulation of the mixed solution of coal tar and ammoniacal liquor thus the pressure-controlling realized the raw gas in coking chamber;
(4), raw gas together with coal tar and ammonia water mixture through gas-liquid separation, raw gas upwards leads to air cooling through a road heating gas transfer lime of raw gas reclaiming clean device and cools, and coal tar ammonia water mixture flows to tar ammonia settling bath downwards through a road mixed solution pipe of another raw gas reclaiming clean device and carries out precipitate and separate;
(5), cooling raw gas is delivered to through gas fan group in the activated coke Dry recovery device of raw gas reclaiming clean device and is carried out activated coke absorption, saturated activated coke falls into saturated active coke storage silo, send into active coke through saturated active coke bucket elevator and carry out evaporation regeneration, unsaturated activated coke after evaporation falls into unsaturated activated coke recovery bin, again send in activated coke Dry recovery device through unsaturated activated coke bucket elevator and enter absorption, so repeatedly carry out, purified gas after absorption is used for burning, waste gas after purified gas burning is dry to be put out, dry put out after high temperature combustible exhaust gas again tonifying Qi burning, supplemental combustion air heating rear portion hot waste gas is used for saturated active coke regeneration heating,
(6), active coke through raw gas reclaiming clean device carry out evaporating regeneration containing light oil, crude benzol, mixed triolein, carbolineum composition enters cut tower by evaporation exhaust of oil pipe and carries out cut, the carbolineum that proportion is larger flows in carbolineum medial launder by lower cut net, the slightly heavy mixed triolein of proportion flows in the oil-collecting tank of mixed triolein oil trap, entered in mixed triolein water cooler by mixed triolein transfer lime and cool, finally store in mixed triolein medial launder, the light oil that proportion is lighter and crude benzol steam enter oil gas air cooler from light oil crude benzene vapor vent pipe and carry out condensation, phlegma enters water-and-oil separator and carries out oily water separation, light oil and crude benzol solution enter in crude benzol backflash, wherein a part is used for returning stream, part overflow is to light oil crude benzol medial launder.
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| CN102250629A (en) * | 2011-06-13 | 2011-11-23 | 山西利华新科技开发有限公司 | Coking furnace capable of recycling heat energy and coking method |
| CN102519285A (en) * | 2011-12-23 | 2012-06-27 | 东北大学 | Integrated technique and special equipment for raw gas waste heat recovery and steam replacement with heat transfer soil |
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| CN102250629A (en) * | 2011-06-13 | 2011-11-23 | 山西利华新科技开发有限公司 | Coking furnace capable of recycling heat energy and coking method |
| CN102519285A (en) * | 2011-12-23 | 2012-06-27 | 东北大学 | Integrated technique and special equipment for raw gas waste heat recovery and steam replacement with heat transfer soil |
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