CN1966612B - Low-temperature coal carbonization manufacturing technique - Google Patents
Low-temperature coal carbonization manufacturing technique Download PDFInfo
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- CN1966612B CN1966612B CN200610137759XA CN200610137759A CN1966612B CN 1966612 B CN1966612 B CN 1966612B CN 200610137759X A CN200610137759X A CN 200610137759XA CN 200610137759 A CN200610137759 A CN 200610137759A CN 1966612 B CN1966612 B CN 1966612B
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Abstract
The invention disclosed a low temperature coal dry distillating process which includes the following steps: choosing the material coal; the coal goes through coal cup, roller, and assistant coalbox to get into collecting umbrella and being separated; pre-heating the coal in the drying stage; dry-distillating at 100-550DEG C for about 4h, the temperature of heating region is 700-800DEG C to decrease the content of semi-coal to less than 6%; cooling the semi-coal through the water-cooling jacket box. The heat in the stove is all absorbed by the coal in the invention. It needs less time to dry distillate the coal and it's quite direct and simple. The invention adopts big containing space, the heating gas is provided uniformly to the bottom of the stove so the stove throughput is 3 times more than the traditional stove; it can heat the material more uniformly and it need less temperature control; the tar yield has been increased and the recovery rate has been increased from less than 50% to 80% or more.
Description
Technical field
The present invention relates to a kind of dry distillation of coal technology, relate in particular to a kind of low-temperature coal carbonization manufacturing technique.
Background technology
Existing dry distillation of coal technology adopts the internal combustion external-heat, and such distillation process temperature control is higher relatively, and the gas retort treatment capacity is relatively low, and heats inhomogeneously, makes tar yield lower.
Summary of the invention
In order to solve the problem of above-mentioned existence, goal of the invention of the present invention provides a kind of in dry distillation of coal process, the low-temperature coal carbonization manufacturing technique of maximized recovery coal tar.
Technical scheme of the present invention is achieved in that low-temperature coal carbonization manufacturing technique, comprises the steps:
1, choose feed coal: coal is bituminous coal and long-flame coal, non-caking coal or weakly caking coal, and granularity is 20mm-120mm;
2, feed coal adds from the furnace roof coal bunker, enters 4 auxiliary coal bins by 2 blowing cylinders, enters furnace roof portion by auxiliary coal bin sub-material, again the gas-collecting arrayed umbrella of installing by furnace roof portion sub-material once more; The feed coal that to go into stove is evenly distributed on the big cavity cross section of gas retort;
3, feed coal at first enters dryer section, be furnace roof gas-collecting arrayed umbrella section, utilize retort section from the hot gas flow that rises between coal cinder to advancing the feed coal preheating of stove, the gas after the preheating is by the collection of gas-collecting arrayed umbrella, derive furnace roof by 2 upcasts of furnace roof portion, the gas of being derived by upcast is raw gas;
4, feed coal drying section preheats under the back and moves up into retort section, temperature improves gradually, operating temperature is controlled at 100 ℃-550 ℃, about 4 hours of working time, coal is finished the low-temperature pyrolysis of coal before 550 ℃, coal tar is separated out fully at 550 ℃, and the fugitive constituent of semicoke is below 6%, furnace charge enters the heating zone in folding process relaying temperature of continuing rising, and the Heating Zone Temperature regulation and control make the semicoke fugitive constituent drop to below 6% between 700-800 ℃;
5, feed coal moves up into cooling section gradually down, furnace bottom is installed the water-cooling jacket coke discharge box, the high temperature semicoke is by the water-cooling jacket coke discharge box, part of waste heat is taken away by water-cooling jacket recirculated water, the high temperature semicoke descends and enters coke guide, the coke guide bottom is immersed in the water sealed tank water, the high temperature semicoke immerses and to extinguish in the water and produce a large amount of water vapour, the water vapour rising combines with the high temperature semicoke and produces a large amount of water-gas, water-gas is to the heat exchange of high temperature semicoke, semicoke cools, and rises and enter the retort section heating zone and mix with heated air furnace charge is heated in water-gas heating back;
6, the Heating temperature that adds the method regulation and control heating zone of quantity of hot air and coal gas amount by regulation and control, the temperature of heating zone is controlled at 700-800 ℃, the dilution of air and coal gas is made a gesture of measuring between 1: 1.5 to 1: 2.0, method by the regulation and control thinning ratio is adjusted Heating temperature, total tolerance of coal gas and air and the speed of pushing machine decision gas retort furnace top gas temperature, make furnace charge that the residence time more than 4 hours is arranged before 550 ℃ simultaneously, furnace temperature is by thermocouple assay.
The semicoke ratio that the low-temperature pyrolysis stove is gone into stove coal and production is 1.65: 1 to 1.75: 1, and the tar rate of recovery is more than 80%, and caloric power of gas is not less than 1970 kilocalories/Nm
3
The temperature out of the raw gas in the described production operation process is controlled in the 80-120 ℃ of scope.
Compared with prior art the invention has the beneficial effects as follows:
1, low-temperature coal carbonization manufacturing technique of the present invention adopts hot type of heating in the internal combustion, be designed to big cavity in the stove, prolong the low-temperature pyrolysis time, and adopt gas-collecting arrayed umbrella, branch duct mixer to cooperate grid wall and coke pushing mechanism, realized cloth evenly, homogeneous heating and discharging be even, give full play to the maximum production capacity of gas retort, improved single furnace output and quality product, emphasis is to improve tar yield, in dry distillation of coal process, reclaiming coal tar substantially, is that coal changes a kind of important channel on the oily direction.
2, the heat that joins in the stove is fully absorbed by coal, the destructive distillation time is short, directly rapidly, adopt big cavity design simultaneously, the even supply heated air of furnace bottom grid wall makes the gas retort treatment capacity improve more than 3 times and homogeneous heating than internal combustion external-heat stove, and temperature control is lower, tar yield is improved, bring up to present more than 80% by the former rate of recovery below 50%.
3, adopt big cavity design, increase furnace volume and prolong the destructive distillation time, reduce Heating temperature, improve tar yield.
4, the method that adds warm air and coal gas thinning ratio and regulation and control heated air total amount by adjustment realizes the temperature control of retort process, the simple and easy handling of regulation and control.
5, because pyrolysis temperature is low, and the gas retort furnace pressure is low, thus when building the low-temperature pyrolysis stove by laying bricks or stones less demanding to refractory materials, material price is low, investment obviously reduces.
Description of drawings
Fig. 1 is the used low-temperature pyrolysis side of a low-temperature coal carbonization manufacturing technique of the present invention stove one-piece construction synoptic diagram.
Embodiment
Below in conjunction with the drawings and specific embodiments the present invention is described in further detail, but not as a limitation of the invention.
Low temperature coal dry distillating square stove one-piece construction synoptic diagram as shown in Figure 1, the low-temperature coal carbonization manufacturing technique flow process is as follows:
1, to require into the stove coal be bituminous coal and long-flame coal, non-caking coal or weakly caking coal to the low-temperature pyrolysis stove, and granularity is 20 to 120 millimeters;
2, feed coal adds from furnace roof coal bunker 1, enter 4 auxiliary coal bins 3 by 2 blowing cylinders 2, enter furnace roof portion by auxiliary coal bin 3 sub-materials, gas-collecting arrayed umbrella 4 is installed by furnace roof portion, by gas-collecting arrayed umbrella 4 sub-material once more, the coal cinder that will go into stove is evenly distributed on the gas retort 5 big cavity cross section;
3, gas retort 5 adopts cavity uprightly to design, feed coal at first enters dryer section, be 4 sections of furnace roof gas-collecting arrayed umbrellas, utilize retort section from the hot gas flow that rises between coal cinder to advancing the feed coal preheating of stove, gas after the preheating is by the collection of gas-collecting arrayed umbrella 4, derive furnace roof by 2 upcasts of furnace roof portion 6, the gas of being derived by upcast 6 is raw gas; Hot waste gas after the coal gas that raw gas is mainly produced by destructive distillation in the stove, the heating, the water-gas that rises from cooling section and dryly go into the steam that the stove coal produces and form, the temperature out with raw gas in the production operation process is controlled in the 80-120 ℃ of scope.
4, furnace charge preheats under the back in dryer section and moves up into retort section, and temperature improves gradually, owing to be big cavity in the stove, the big travelling speed of capacity is slower, 100-550 ℃ of about 4 hours of working time, coal is finished the low-temperature pyrolysis of coal before 550 ℃, and coal tar is separated out fully at 550 ℃.Because the service requirements of semicoke, the fugitive constituent of semicoke is below 6%, and furnace charge enters the heating zone in folding process relaying temperature of continuing rising, and Heating Zone Temperature is regulated and control between 700-800 ℃, and the semicoke fugitive constituent is dropped to below 6%;
5, furnace charge moves down gradually by entering cooling section behind the heating zone, furnace bottom is installed water-cooling jacket coke discharge box 7, the high temperature semicoke is by water-cooling jacket coke discharge box 7, part of waste heat is taken away by water-cooling jacket recirculated water, the high temperature semicoke descends and enters coke guide 8, coke guide 8 bottoms are immersed in water sealed tank 9 water, the high temperature semicoke immerses and to extinguish in the water and produce a large amount of water vapour, the water vapour rising combines with the high temperature semicoke and produces a large amount of water-gas, water-gas is to the heat exchange of high temperature semicoke, semicoke cools, and rises and enter the retort section heating zone and mix with heated air furnace charge is heated in water-gas heating back;
6, the Heating temperature that adds the method regulation and control heating zone of quantity of hot air and coal gas amount by regulation and control, the temperature of heating zone is controlled at 700-800 ℃, the dilution of air and coal gas is made a gesture of measuring between 1: 1.5 to 1: 2.0 and is adjusted, method by the regulation and control thinning ratio is adjusted Heating temperature, total tolerance of coal gas and air and the speed of pushing machine 10 decision gas retort 5 furnace top gas temperatures.Dilution by regulation and control coal gas and air is the total amount of mixed gas and the speed of pushing machine 10 when, the temperature of gas retort heating zone is controlled between 700-800 ℃, make furnace charge that the residence time more than 4 hours is arranged before 550 ℃ simultaneously, make the furnace roof temperature of exit gas be controlled at 80-120 ℃ of scope, furnace temperature is by thermocouple assay.
The semicoke ratio that the low-temperature pyrolysis stove is gone into stove coal and production is 1.65: 1 to 1.75: 1.
The tar rate of recovery is more than 80%.
Caloric power of gas is not less than 1970 kilocalories/Nm
3
As shown in Figure 1, the gas flow process of low-temperature coal carbonization manufacturing technique is:
The coal gas that supply is melted down in the retort section utilization cooperates air that the raw material coal cinder that enters in the stove is heated destructive distillation, and coal gas that retort process produces and heat exhaust gases are mixed the formation raw gas and risen from the furnace charge layer, is collected and is derived through upcast 6 by furnace roof portion gas-collecting arrayed umbrella 4; Again through bridge tube 11 to gas liquor joint sealing 12, and discharge from gas liquor joint sealing 12 bottoms; Under the draft effect of gas fan 13, coal gas enters Venturi meter cold tower 14 just, Venturi meter just cold tower 14 cats head spray into heat ring water by shower nozzle, coal gas and spray water are mixed by the just cold tower 14 of Venturi meter after, parallel in the same way from top to down, reach preliminary refrigerative effect; Gas just enters rotating stream tray scrubber 15 bottoms in cold tower 14 bottoms from Venturi meter, gas from the eddy flow plate of rotating stream tray scrubber 15 by producing reverse contact of cool circulation water that swirling eddy and top from rotating stream tray scrubber 15 spray into, uniform mixing cools to coal gas, after coal gas cools, phlegma flows into the tower kerve, gas fan 13 is derived and entered to coal gas by gas fan 13 drafts from cat head, after gas fan 13 extractions and the pressurization, part coal gas is sent into the thermal source of gas retort 5 as heating after by firing tunnel in coking furnace pipeline and air mixed, part coal gas is supplied with dryer burning heating, remainder coal gas diffuses by diffusing a mouthful burning, or gives power station or other industrial user use.
Liquid flow is as follows:
Liquid flow divides heat recirculated water, cool circulation water, clear water recirculated water three cover circulating waters unify three circulating water pools and a tar pool.
By heat ring pump 16 with the first shower nozzle of cold tower 14 cats head of the water supply bridge tube 11 in thermal cycling pond 17 and Venturi meter, realization is to the preliminary spray cooling of coal gas, phlegma of collecting and spray after heat recirculated water flow into Venturi meter cold tower 14 kerves just, staticly settle getting back to thermal cycling pond 17 naturally through water return pipeline, coal tar and water sepn, coal tar is from being retracted to tar pool 18 under water.Heat recirculated water recycles.
By the water supply rotating stream tray scrubber 15 spray cooling coal gas of cold ring pump 19 with cool circulation water pond 20, phlegma and cool circulation water are collected by the tower kerve, getting back to cool circulation water pond 20 through the water return pipeline spontaneous current staticly settles, after coal tar and the water sepn, coal tar is from being retracted to tar pool 18 through tar pump 21 under water.Cool circulation water recycles.
By fresh water pump 22 clear water of clean water basin 23 is supplied with 7 pairs of semicokes of water-cooling jacket coke discharge box and tentatively cool, guarantee furnace bottom coke discharging system safety operation.Heat up after the clear water recirculated water heat exchange by coke discharge box 7, the recirculated water after the intensification is sent to tar pool 18 by pipeline, heats to tar pool by tar pool 18 heating calancrias, gets back to clean water basin 23 through the circulating water flow of tar pool 18 heating calancrias heat radiation and recycles.
Thermal cycling pond 17 and cool circulation water pond 20 staticly settle back coal tar tar pump 21 suction tar pools 18, give the heating of tar heating calancria by clear water recirculated water, coal tar further leaves standstill dehydration at tar pool 18, the water of deviating from is extracted out, and the coal tar after the dehydration is stored and extracted outer selling out with tar pump 18.
Claims (2)
1. low-temperature coal carbonization manufacturing technique comprises the steps:
1., choose feed coal: coal is a bituminous coal, and granularity is 20-120mm;
2., feed coal adds from the furnace roof coal bunker, enters 4 auxiliary coal bins by 2 blowing cylinders, enters furnace roof portion by auxiliary coal bin sub-material, the gas-collecting arrayed umbrella of installing by furnace roof portion sub-material once more again; The even cloth of feed coal that to go into stove is on the big cavity cross section of gas retort;
3., feed coal at first enters dryer section, be furnace roof gas-collecting arrayed umbrella section, utilize retort section from the hot gas flow that rises between coal cinder to advancing the feed coal preheating of stove, the gas after the preheating is by the collection of gas-collecting arrayed umbrella, derive furnace roof by 2 upcasts of furnace roof portion, the gas of being derived by upcast is raw gas;
4., feed coal drying section preheats under the back and moves up into retort section, temperature improves gradually, operating temperature is controlled at 100-550 ℃, be 4 hours working time, coal is finished the low-temperature pyrolysis of coal before 550 ℃, coal tar is separated out fully at 550 ℃, and the fugitive constituent of semicoke is below 6%, furnace charge enters the heating zone in folding process relaying temperature of continuing rising, and the Heating Zone Temperature regulation and control drop to below 6% at 700-800 ℃ of chien shih semicoke fugitive constituent;
5., feed coal moves up into cooling section gradually down, furnace bottom is installed the water-cooling jacket coke discharge box, the high temperature semicoke is by the water-cooling jacket coke discharge box, part of waste heat is taken away by water-cooling jacket recirculated water, the high temperature semicoke descends and enters coke guide, the coke guide bottom is immersed in the water sealed tank water, the high temperature semicoke immerses and to extinguish in the water and produce a large amount of water vapour, the water vapour rising combines with the high temperature semicoke and produces a large amount of water-gas, water-gas is to the heat exchange of high temperature semicoke, semicoke cools, and rises and enter the retort section heating zone and mix with heated air furnace charge is heated in water-gas heating back;
6., the Heating temperature that adds the method regulation and control heating zone of quantity of hot air and coal gas amount by regulation and control, the temperature of heating zone is controlled at 700-800 ℃, the dilution of air and coal gas is made a gesture of measuring between 1: 1.5 to 1: 2.0, method by the regulation and control thinning ratio is adjusted Heating temperature, total tolerance of coal gas and air and the speed of pushing machine decision gas retort furnace top gas temperature make furnace charge that the residence time more than 4 hours is arranged before 550 ℃ simultaneously.
2. low-temperature coal carbonization manufacturing technique according to claim 1, the temperature out that it is characterized by the raw gas in the production operation process is 80-120 ℃.
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|---|---|---|---|---|
| CN101463259A (en) * | 2007-12-19 | 2009-06-24 | 神木县三江煤化工有限责任公司 | Low temperature dry distillation coke oven hot-water circulation utilizing system |
| BRPI0822577A2 (en) * | 2008-04-15 | 2015-06-23 | Larry Hunt | Coal Enhancement Process |
| CN101514291B (en) * | 2009-02-27 | 2012-10-10 | 西安建筑科技大学 | Method for dry quenching by internal heat and low temperature carbonization of coal |
| CN101497801B (en) * | 2009-02-27 | 2012-02-01 | 西安建筑科技大学 | Oxygen-enriched low temperature dry distillation blow-in method for coal |
| CN101775321B (en) * | 2009-05-11 | 2013-02-27 | 神华集团有限责任公司 | Formed coke and production method of formed coke, coal gas and tar |
| CN101580728B (en) * | 2009-06-10 | 2012-10-03 | 中煤能源黑龙江煤化工有限公司 | Process technology for non-caking coal or weak caking coal |
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| CN103602344B (en) * | 2013-11-14 | 2015-06-24 | 宁夏科豪陶瓷有限公司 | Low energy consumption production method and device for firing building ceramic product by semi coke tail gas |
| CN104226064B (en) * | 2014-09-24 | 2016-06-22 | 神木县三江煤化工有限责任公司 | A kind of dust-laden carbonization gas dust arrester |
| CN104560070A (en) * | 2015-01-30 | 2015-04-29 | 锡林郭勒盟兴富能源开发有限责任公司 | Lignite low-temperature carbonization device |
| CN106047386A (en) * | 2016-05-20 | 2016-10-26 | 江苏盈丰智能工程科技有限公司 | Energy-saving type coal carbonization production method |
| CN106010600A (en) * | 2016-05-25 | 2016-10-12 | 武汉天颖环境工程股份有限公司 | Biomass continuous-feed pyrolyzing furnace |
| CN106190204A (en) * | 2016-07-11 | 2016-12-07 | 神木县三江煤化工有限责任公司 | A kind of waste heat recycling system for coal low temperature distillation stove and waste heat recycle method |
| CN108949207A (en) * | 2018-08-08 | 2018-12-07 | 陈伟 | A kind of internal-combustion and-heating type biomass continuously carbonizing system and its production technology |
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| US4230528A (en) * | 1977-08-30 | 1980-10-28 | Bergwerksverband Gmbh | Method for starting up plant for producing fine coke |
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Address after: 719300, building, Xingcheng street, Shenmu Dongxing street, Shaanxi Province Patentee after: Shenmu Sanjiang Coal Chemical LLC Address before: 719300, building, Xingcheng street, Shenmu Dongxing street, Shaanxi Province Patentee before: Sanjiang Coal Chemical Industry Co., Ltd., Shannxi Province Shenmu County |