CN104498107B - A kind of process the apparatus and method that coal oven dithio-gas is coal-tar middle oil - Google Patents

A kind of process the apparatus and method that coal oven dithio-gas is coal-tar middle oil Download PDF

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CN104498107B
CN104498107B CN201410807691.6A CN201410807691A CN104498107B CN 104498107 B CN104498107 B CN 104498107B CN 201410807691 A CN201410807691 A CN 201410807691A CN 104498107 B CN104498107 B CN 104498107B
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gas
catalyst
air
cracking reaction
catalytic cracking
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CN104498107A (en
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于庆波
谢华清
刘军祥
秦勤
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Northeastern University China
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/34—Purifying combustible gases containing carbon monoxide by catalytic conversion of impurities to more readily removable materials
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/002—Removal of contaminants
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/32—Purifying combustible gases containing carbon monoxide with selectively adsorptive solids, e.g. active carbon
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/584—Recycling of catalysts

Abstract

The invention belongs to catalytic cracking of tar and heat recovery technology field, be specifically related to a kind of process the apparatus and method that coal oven dithio-gas is coal-tar middle oil.Apparatus of the present invention include catalytic cracking reaction device, catalyst regenerator, gas-solid separator, air preheater, waste heat boiler and charging gear；In catalytic cracking reaction device, high temperature coke oven raw coke oven gas occurs cracking reaction to generate little molecule fuel gas under the effect of catalyst, the solid particle that catalyst and reaction produce carries lower entrance gas-solid separator at coal gas, coke-stove gas after gas solid separation enters waste heat boiler, waste heat is recovered further, solid particle enters catalyst regenerator, and under the effect of hot-air, catalyst realizes regeneration, the high-temperature flue gas preheated air of generation.The present invention takes full advantage of the tar in coal oven dithio-gas, macromolecule hydrocarbon, makes them be converted into little molecule fuel gas, improve coke-stove gas yield, the coke-stove gas high-temperature residual heat being simultaneously wasted in the original technique of efficient recovery.

Description

A kind of process the apparatus and method that coal oven dithio-gas is coal-tar middle oil
Technical field
The invention belongs to catalytic cracking of tar and heat recovery technology field, be specifically related to a kind of process the apparatus and method that coal oven dithio-gas is coal-tar middle oil.
Background technology
Tar is gaseous form when high temperature, but just exists with the thick form of liquid when temperature is below 500 DEG C, is easily deposited in the equipment such as pipeline, instrument, causes equipment to block.Coke-stove gas after purification is mainly composed of H2(53% ~ 59%), CH4(25% ~ 30%), CO(about 6%), CO2(about 2.5%) and a small amount of CnHm、N2Deng, it is the coal gas of a kind of high-quality, but the coal-tar middle oil content of raw coke oven gas before purifying can reach 80 ~ 120g/m3, so need before to coke oven gas purification containing tar processing fall.At present in terms of coal oven dithio-gas purified treatment, the most commonly used technological process is the high temperature raw coke oven gas (750 ~ 850 DEG C) produced by coke furnace carbonization chamber, discharge is introduced through tedge, bridge tube, being removed by the macromole carbonaceous materials such as the tar in raw coke oven gas by spray ammonia in bridge tube, coke-stove gas is cooled to about 85 DEG C simultaneously.This technique does not only utilize the physical thermal contained by tar and chemical energy, makes the high-temperature residual heat of coal oven dithio-gas be wasted simultaneously yet.
Summary of the invention
The problem existed for prior art and defect, the present invention provides a kind of and processes the apparatus and method that coal oven dithio-gas is coal-tar middle oil, it is therefore an objective to the waste heat of Appropriate application coal oven dithio-gas, and high efficiente callback utilizes tar and is effectively improved coke-stove gas yield.
The device realizing the object of the invention includes catalytic cracking reaction device, catalyst regenerator, gas-solid separator, air preheater, waste heat boiler and charging gear, described catalytic cracking reaction device lower end air inlet is connected with coke furnace carbonization chamber gas exit, side charging aperture is connected with charging gear, and upper end discharging opening is connected with gas-solid separator；The gas outlet, upper end of gas-solid separator is connected with waste heat boiler, and lower end discharging opening is connected with the upper end charging aperture of catalyst regenerator；The lower end discharging opening of catalyst regenerator is connected with charging gear, and the air intake of side is connected with the hot air outlet of air preheater, and the exhanst gas outlet of side is connected with the high-temperature flue gas import of air preheater.
Wherein, described catalytic cracking reaction device is fluidized-bed reactor, fluidizing agent is the tar cracking catalyst of particle diameter 20 ~ 500 microns, catalyst is entered catalytic cracking reaction device by charging gear by catalyst regenerator, coke furnace carbonization chamber high temperature raw coke oven gas out is entered by bottom catalytic cracking reaction device, makes catalyst granules form fluidization.
Described catalyst regenerator is lower denidation reactor or moving-burden bed reactor；When catalyst regenerator is lower denidation reactor, the upper end charging aperture of catalyst regenerator is connected with gas-solid separator by control valve, and catalyst leans on the effect of self gravitation and up hot-air to move from top to bottom in catalytic cracking reaction device；When catalyst regenerator is moving-burden bed reactor, it is made up of two moving beds, the upper end charging aperture of each moving bed material outlet by reversal valve, material inlet is connected with the lower end discharging opening of gas-solid separator, lower end discharging opening is connected with charging gear by control valve, the air intake of side is connected with the air outlet slit of reversal valve, the air intlet of reversal valve is connected with the hot air outlet of air preheater, the exhanst gas outlet of side is connected with the high-temperature flue gas import of air preheater by control valve, during work, two moving beds one provide catalyst for catalytic cracking reaction device, another introduces hot-air and is passed through beds, realize catalyst regeneration, the two alternately changes jobs mutually.
Use said apparatus to process the method that coal oven dithio-gas is coal-tar middle oil, follow the steps below:
(1) joining in catalyst regenerator by catalyst, fed rear enclosed charge door, and keeping temperature is 850 ~ 950 DEG C, is passed through the delivery rate in catalytic cracking reaction device by charging gear control and regulation catalyst；
(2) in catalytic cracking reaction device, it is passed through the high temperature coke oven raw coke oven gas of 750 ~ 900 DEG C, catalyst is made to form fluidization, the macromole carbon compounds such as the tar gas simultaneously contained in raw coke oven gas are fully contacted with catalyst, catalytic cracking reaction occurs, and then coke-stove gas carries the carbon granule entrance gas-solid separator of catalyst and cracking reaction generation；
(3) after gas solid separation, coke-stove gas enters the further recovery waste heat of waste heat boiler, the steam produced is incorporated in steam pipe system, solid particle enters in catalyst regenerator, air preheater introduces cold air, it is passed through in catalyst regenerator after being heated to more than 850 DEG C, solid particle and hot air, the carbon distribution of solid particles surface, coke-like thing and the charcoal particle burning that is mixed in catalyst granules are totally, realize the regeneration of catalyst, the high-temperature flue-gas produced is at least 900 DEG C, enter into the high-temperature flue gas import of air preheater from the exhanst gas outlet of catalyst regenerator, for heating cold air.
Wherein, when the catalyst regenerator used is lower denidation reactor, the solid particle returning catalyst regenerator is with the hot air being passed through, burning and CO to occur in dropping process2Desorption reaction；When the catalyst regenerator used is made up of two moving-burden bed reactors, catalyst is joined in a moving bed of catalyst regenerator, through charging gear, catalyst is sent in catalytic cracking reaction device by this moving bed, by adjusting control valve and reversal valve, the hot air outlet of air preheater is made to be connected with the air intake of another moving bed side, in the solid particle of gas solid separation passes through another moving bed of reversal valve return catalyst regenerator, hot-air is passed into the beds of moving bed and contacts generation burning and CO with solid particle2Desorption reaction, after the catalyst discharge in the moving bed of supply catalyst, adjusts control valve and reversal valve, two moving bed exchange work, another moving bed supplies catalyst by charging gear, it is achieved the continuous and steady operation of device.
Described catalyst is the catalyst of CaO base, is to be calcined, by calcium acetate or calcium hydroxide, the CaO that CaO or the calciferous ore calcination prepared prepares.
Described catalytic cracking reaction device be utilize coal oven dithio-gas and catalyst self heat of high temperature to maintain catalytic cracking reaction device in temperature at 750 DEG C ~ 850 DEG C.
Compared with prior art, the feature of the present invention and providing the benefit that:
The CaO base catalyst that the inventive method is selected is in addition to reacting as catalyst coke tar cracking, also by the CO of absorption cracking reaction generation2And original CO in coal oven dithio-gas2, promoting the process that coke tar cracking reacts further, improve coke-stove gas yield and calorific value, dominant response involved in catalytic cracking reaction device is:
Wherein, CnHmFor alkane, alkene or alkynes, m=2n+2,2n-2 or 2n, n is the integer of >=1.
The catalyst regenerator operating temperature of the present invention controls more than 900 DEG C, through hot-air and the carbon distribution of catalyst surface of air preheater preheating, coke-like thing and be mingled with the combustion reaction that carbon granule in the catalyst occurs and provide heat for catalyst regenerator, it is not necessary to be additionally provided thermal source.
In the catalyst regenerator of the present invention, in addition to there is the combustion reaction of the material such as carbon distribution, coke-like thing, higher operating temperature can make CO absorption in catalytic cracking reaction device2Catalyst generation desorption reaction, i.e. CaCO3Cracking reaction, it is achieved the regeneration of catalyst:
；
The present invention takes full advantage of tar, the macromolecule hydrocarbon etc. processed by original technique spray cleaning in coal oven dithio-gas, them are made to be converted into little molecule combustible component, improve coke-stove gas yield, decrease the input (such as the use etc. of a large amount of ammonia) of operating cost simultaneously；The present invention makes coke-stove gas successively provide heat for catalytic cracking reaction device and waste heat boiler, the coke-stove gas high-temperature residual heat being wasted in the former technique of efficient recovery；In addition the catalyst used in the present invention can realize recycling utilization, decreases cost of investment.
Accompanying drawing explanation
Fig. 1 is the process flow diagram of the present invention；
Fig. 2 be the catalyst regenerator in the coal-tar middle oil device of coal oven dithio-gas that processes of the present invention be intention during lower denidation reactor；
Fig. 3 be the catalyst regenerator in the coal-tar middle oil device of coal oven dithio-gas that processes of the present invention be that work during moving-burden bed reactor runs one of schematic diagram；
Fig. 4 be the catalyst regenerator in the coal-tar middle oil device of coal oven dithio-gas that processes of the present invention be that work during moving-burden bed reactor runs the two of schematic diagram；
Wherein: 1: catalytic cracking reaction device；2: gas-solid separator；3: control valve；3-1: the first control valve；3-2: the second control valve；3-3: the three control valve；3-4: the four control valve；4: catalyst regenerator；4-1: the first moving bed；4-2: the second moving bed；5: charging gear；6: waste heat boiler；7: air preheater；8-1: the first reversal valve；8-2 the second reversal valve；9: reversal valve material inlet；10-1: reversal valve the first material outlet；10-2: reversal valve the second material outlet；11: reversal valve air intlet；12-1: reversal valve the first air outlet slit；12-2: reversal valve the second air outlet slit；
Wherein:Represent the flow direction of coal oven dithio-gas；Represent the flow direction of catalyst；In catalyst regeneratorRepresent the flow direction of hot-air.
Detailed description of the invention
The device realizing the object of the invention includes catalytic cracking reaction device 1, catalyst regenerator 4, gas-solid separator 2, air preheater 7, waste heat boiler 6 and charging gear 5, described catalytic cracking reaction device 1 lower end air inlet is connected with coke furnace carbonization chamber gas exit, side charging aperture is connected with charging gear 5, and upper end discharging opening is connected with gas-solid separator 2；The gas outlet, upper end of gas-solid separator 2 is connected with waste heat boiler 6, and lower end discharging opening is connected with the upper end charging aperture of catalyst regenerator 4；The lower end discharging opening of catalyst regenerator 4 is connected with charging gear 5, and the air intake of side is connected with the hot air outlet of air preheater 7, and the exhanst gas outlet of side is connected with the high-temperature flue gas import of air preheater 7.
Wherein, described catalytic cracking reaction device 1 is fluidized-bed reactor, fluidizing agent is the tar cracking catalyst of particle diameter 20 ~ 500 microns, catalyst is entered catalytic cracking reaction device 1 by charging gear 5 by catalyst regenerator 4, coke furnace carbonization chamber high temperature raw coke oven gas out is entered by bottom catalytic cracking reaction device 1, makes catalyst granules form fluidization.
Described catalyst regenerator 4 is lower denidation reactor or moving-burden bed reactor；
As shown in Figure 2, when catalyst regenerator 4 is lower denidation reactor, the upper end discharging opening of catalyst regenerator 4 is connected with gas-solid separator 2 by control valve 3, and catalyst leans on the effect of self gravitation and up hot-air to move from top to bottom in catalytic cracking reaction device 1；
nullAs shown in Figure 3，When catalyst regenerator 4 is moving-burden bed reactor，It is made up of two moving bed 4-1 and 4-2，The upper end charging aperture of each moving bed reversal valve the first material outlet 10-1 and reversal valve the second material outlet 10-2 by the first reversal valve 8-1、Material inlet 9 is connected with the lower end discharging opening of gas-solid separator 2，Lower end discharging opening is connected with charging gear by the 3rd control valve 3-3 and the 4th control valve 3-4，The air intake of side and reversal valve the first air outlet slit 12-1 of the second reversal valve 8-2 and reversal valve the second air outlet slit 12-2 are connected，Reversal valve air intlet 11 is connected with the hot air outlet of air preheater 7，The exhanst gas outlet of side passes through the first control valve 3-1、Second control valve 3-2 is connected with the high-temperature flue gas import of air preheater 7，During work, two moving bed 4-1 and 4-2 mono-provide catalyst for catalytic cracking reaction device 1，Another introduces hot-air and realizes catalyst regeneration，The two alternately changes jobs mutually.
The present invention also provides for a kind of processing the method that coal oven dithio-gas is coal-tar middle oil, is described further the inventive method with specific embodiment below in conjunction with the accompanying drawings.
Table 1 coal oven dithio-gas forms
In the embodiment of the present invention, certain coke oven with coke output as 100t/h is as object, and its coal oven dithio-gas produced per hour is 42000Nm3, raw coke oven gas composition is shown in Table 1.
Tar cracking catalyst uses the catalyst of CaO base, by calcium acetate or calcium hydroxide or other calcium oxide presoma at the temperature calcination of >=900 DEG C, it is thus achieved that calcium oxide powder be broken to particle diameter 20 ~ 500 microns as catalyst for cracking.
Embodiment 1
When catalyst regenerator uses the form of lower denidation, seeing Fig. 1 and 2, being embodied as step is:
(1) being joined in catalyst regenerator 4 by catalyst, fed rear enclosed charge door, and keeping temperature is 850 ~ 950 DEG C, and control catalyst being passed through the delivery rate in catalytic cracking reaction device by charging gear 5 is 2 ~ 3kg/s；
(2) in catalytic cracking reaction device 1, it is passed through the high temperature coke oven raw coke oven gas of 750 ~ 900 DEG C, makes catalyst form fluidization, the tar gas that simultaneously contains in raw coke oven gas, crude benzol, C10H8It is fully contacted Deng with catalyst, the H that catalytic cracking reaction produces occurs2、CO、CH4、CnHmImport in coke-stove gas etc. little molecule combustible gas, improve gas yield, the CO that the cracking reaction of CaO absorption simultaneously produces2And original CO in coal oven dithio-gas2, improve combustible gas concentration in coal gas, and then improve calorific value of gas, then coke-stove gas carries the carbon granule entrance gas-solid separator 2 of catalyst and cracking reaction generation；
(3) after gas solid separation, coke-stove gas enters the further recovery waste heat of waste heat boiler 6, the steam produced is incorporated in steam pipe system, solid particle returns catalyst regenerator 4, air preheater 7 introduces cold air, being passed through in catalyst regenerator 4 after being heated to more than 850 DEG C, the solid particle returning catalyst regenerator 4 is with the hot air being passed through, burning and CO to occur in dropping process2Desorption reaction, the carbon distribution of solid particles surface, coke-like thing and the charcoal particle burning that is mixed in catalyst granules are totally, realize the regeneration of catalyst, the high-temperature flue-gas produced is at least 900 DEG C, enter into the high-temperature flue gas import of air preheater 7 from the exhanst gas outlet of catalyst regenerator 4, for heating cold air.
When catalyst regenerator uses the form of moving bed, seeing Fig. 1, Fig. 3 and Fig. 4, it concretely comprises the following steps:
(1) catalyst is joined in the first moving bed 4-1, fed rear enclosed charge door, keeping temperature is 850 ~ 950 DEG C, close the first control valve 3-1 and the 3rd control valve 3-3, open the second control valve 3-2 and the 4th control valve 3-4, adjust the first reversal valve 8-1, reversal valve material inlet 9 is made to connect with reversal valve the second material outlet 10-2, adjust the second reversal valve 8-2, reversal valve air intlet 11 is made to connect with reversal valve the second air outlet slit 12-2, it is 2 ~ 3kg/s that first moving bed 4-1 control catalyst to be passed through the delivery rate in catalytic cracking reaction device by charging gear 5；
(2) in catalytic cracking reaction device 1, it is passed through the high temperature coke oven raw coke oven gas of 750 ~ 900 DEG C, makes catalyst form fluidization, the tar gas that simultaneously contains in raw coke oven gas, crude benzol, C10H8It is fully contacted Deng with catalyst, the H that catalytic cracking reaction produces occurs2、CO、CH4、CnHmImport in coke-stove gas etc. little molecule combustible gas, improve gas yield, the CO that the cracking reaction of CaO absorption simultaneously produces2And original CO in coal oven dithio-gas2, improve combustible gas concentration in coal gas, and then improve calorific value of gas, then coke-stove gas carries the carbon granule entrance gas-solid separator 2 of catalyst and cracking reaction generation；
(3) after gas solid separation, coke-stove gas enters the further recovery waste heat of waste heat boiler 6, the steam produced is incorporated in steam pipe system, solid particle is in the first reversal valve 8-1 enters the second moving bed 4-2, air preheater 7 introduces cold air, it is passed through after being heated to more than 850 DEG C in the beds of the first moving bed 4-1, makes the carbon distribution of catalyst surface, coke-like thing and be mingled with charcoal particle burning in the catalyst totally, simultaneously CO absorption in catalytic cracking reaction device 12Catalyst occur CO2Desorption reaction, it is achieved the regeneration of catalyst, the high-temperature flue-gas of generation is at least 900 DEG C, enters into the high-temperature flue gas import of air preheater 7 from the exhanst gas outlet of the first moving bed 4-1 and the second control valve 3-2, for heating cold air；
nullWhen the catalyst discharge in the first moving bed 4-1 is complete，Adjust the first reversal valve 8-1、The circulating direction of the second reversal valve 8-2 and the first control valve 3-1、Second control valve 3-2、3rd control valve 3-3 and the on off state of the 4th control valve 3-4，The reversal valve material inlet 9 of the i.e. first reversal valve 8-1 is connected with reversal valve the first material outlet 10-1，The reversal valve air intlet 11 of the second reversal valve 8-2 is connected with reversal valve the first air outlet slit 12-1，Open the first control valve 3-1 and the 3rd control valve 3-3，Close the second control valve 3-2 and the 4th control valve 3-4，The second moving bed 4-2 is made to provide catalyst for catalytic cracking reaction device 1，And the first moving bed 4-1 introduces hot-air and realizes catalyst regeneration，First moving bed 4-1 and the second moving bed 4-2 alternately changes jobs mutually，Realize the continuous and steady operation of system.

Claims (4)

1. one kind processes the device that coal oven dithio-gas is coal-tar middle oil, it is characterised in that include catalytic cracking reaction device, catalyst regenerator, gas-solid separator, air preheater, waste heat boiler and charging gear；Described catalytic cracking reaction device lower end air inlet is connected with coke furnace carbonization chamber gas exit, and side charging aperture is connected with charging gear, and upper end discharging opening is connected with gas-solid separator；The gas outlet, upper end of gas-solid separator is connected with waste heat boiler, and lower end discharging opening is connected with the upper end charging aperture of catalyst regenerator；The lower end discharging opening of catalyst regenerator is connected with charging gear, and the air intake of side is connected with the hot air outlet of air preheater, and the exhanst gas outlet of side is connected with the gas approach of air preheater；Described catalytic cracking reaction device is fluidized-bed reactor, fluidizing agent is the tar cracking catalyst granule of particle diameter 20 ~ 500 microns, catalyst is entered catalytic cracking reaction device by charging gear by catalyst regenerator, coke furnace carbonization chamber out raw coke oven gas is entered by catalytic cracking reaction device lower end air inlet, makes catalyst granules form fluidization.
The most according to claim 1 a kind of process the device that coal oven dithio-gas is coal-tar middle oil, it is characterised in that described catalyst regenerator is lower denidation reactor or moving-burden bed reactor；
When catalyst regenerator is lower denidation reactor, the upper end charging aperture of catalyst regenerator is connected with gas-solid separator by control valve, and catalyst leans on the effect of self gravitation and up hot-air to move from top to bottom in catalytic cracking reaction device；
When catalyst regenerator is moving-burden bed reactor, it is made up of two moving beds, the upper end charging aperture of each moving bed material outlet by reversal valve, material inlet is connected with the lower end discharging opening of gas-solid separator, lower end discharging opening is connected with charging gear by control valve, the air intake of side is connected with the air outlet slit of reversal valve, the air intlet of reversal valve is connected with the hot air outlet of air preheater, the exhanst gas outlet of side is connected with the gas approach of air preheater by control valve, during work, two moving beds one provide catalyst for catalytic cracking reaction device, another introduces hot-air and is passed through beds, realize catalyst regeneration, the two alternately changes jobs mutually.
3. use the device described in claim 1 to process the method that coal oven dithio-gas is coal-tar middle oil, it is characterised in that to follow the steps below:
(1) joining in catalyst regenerator by catalyst, fed rear enclosed charge door, and keeping temperature is 850 ~ 950 DEG C, is passed through the delivery rate in catalytic cracking reaction device by charging gear control and regulation catalyst；Described catalyst is the CaO base catalyst of particle diameter 20 ~ 500 microns, is to be calcined, by calcium acetate or calcium hydroxide, the CaO that CaO or the calciferous ore calcination prepared prepares；
(2) in catalytic cracking reaction device, it is passed through the high temperature coke oven raw coke oven gas of 750 ~ 900 DEG C, catalyst is made to form fluidization, the tar gas macromole carbon compound simultaneously contained in raw coke oven gas is fully contacted with catalyst, catalytic cracking reaction occurs, and then coke-stove gas carries the carbon granule entrance gas-solid separator of catalyst and cracking reaction generation；Catalytic cracking reaction device be utilize coal oven dithio-gas and catalyst self heat of high temperature to maintain catalytic cracking reaction device in temperature at 750 ~ 850 DEG C；
(3) after gas solid separation, coke-stove gas enters the further recovery waste heat of waste heat boiler, the steam produced is incorporated in steam pipe system, solid particle enters in catalyst regenerator, air preheater introduces cold air, it is passed through in catalyst regenerator after being heated to more than 850 DEG C, solid particle and hot air, the carbon distribution of solid particles surface, coke-like thing and the charcoal particle burning that is mixed in catalyst granules are totally, realize the regeneration of catalyst, the high-temperature flue-gas produced is at least 900 DEG C, enter into the high-temperature flue gas import of air preheater from the exhanst gas outlet of catalyst regenerator, for heating cold air.
The most according to claim 3 a kind of process the method that coal oven dithio-gas is coal-tar middle oil, it is characterized in that when the catalyst regenerator used is lower denidation reactor, the solid particle returning catalyst regenerator is with the hot air being passed through, burning and CO to occur in dropping process2Desorption reaction；
When the catalyst regenerator used is made up of two moving-burden bed reactors, catalyst is joined in a moving bed of catalyst regenerator, through charging gear, catalyst is sent in catalytic cracking reaction device by this moving bed, by adjusting control valve and reversal valve, the hot air outlet of air preheater is made to be connected with the air intake of another moving bed side, in the solid particle of gas solid separation passes through another moving bed of reversal valve return catalyst regenerator, hot-air is passed into the beds of moving bed and contacts generation burning and CO with solid particle2Desorption reaction, after the catalyst discharge in the moving bed of supply catalyst, adjusts control valve and reversal valve, two moving bed exchange work, another moving bed supplies catalyst by charging gear, it is achieved the continuous and steady operation of device.
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