CN201578875U - Low-temperature condensation and adsorption recovery device containing high-concentration low-level aromatic hydrocarbon exhaust gas - Google Patents
Low-temperature condensation and adsorption recovery device containing high-concentration low-level aromatic hydrocarbon exhaust gas Download PDFInfo
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- CN201578875U CN201578875U CN 200920247547 CN200920247547U CN201578875U CN 201578875 U CN201578875 U CN 201578875U CN 200920247547 CN200920247547 CN 200920247547 CN 200920247547 U CN200920247547 U CN 200920247547U CN 201578875 U CN201578875 U CN 201578875U
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Abstract
The utility model relates to a low-temperature condensation and adsorption recovery device containing high-concentration low-level aromatic hydrocarbon exhaust gas, which is characterized in that the device comprises a first-order condensation zone, a second-order condensation zone and an absorption zone, wherein the absorption zone comprises at least two absorbers for the switchover operations of absorption and regeneration; a heating device is arranged in the absorption zone; the regenerative operation adopts vacuum regeneration, and gas discharged in vacuum regeneration is recycled to an inlet of the first-order condensation zone. The device recovers high-concentration low-level aromatic hydrocarbon exhaust gas in air by adopting the low temperature condensation technology, and absorbs, processes and gathers low-level aromatic hydrocarbon in low temperature air for the recovery by adopting the silicagel adsorbent absorbing technology, thereby controlling standard discharge of offgas and reducing equipment investment and operation cost.
Description
Technical field
The utility model relates to a kind of cryogenic temperature condensation reclaimer of volatile organic steam, relates in particular to the cryogenic temperature condensation-adsorption and enrichment reclaimer that contains the rudimentary aromatic hydrocarbon gas of high concentration in the air.
Background technology
Under the situation of not carrying out closed loading and high efficiente callback processing, the entrucking process of benzene,toluene,xylene with the extremely strong high concentration benzene,toluene,xylene steam of discharging toxicity, causes the serious pollution of operation field and ambient air.
GB16297-1996 " discharge standard of air pollutants " regulation, the emission limit of benzene is 12mg/m
3, toluene emission limit be 40mg/m
3, dimethylbenzene emission limit be 70mg/m
3With benzene is example, and in the gas of entrucking process discharging, the concentration of benzene can reach 100g/m
3More than, if be 100g/m to concentration in the gas
3Benzene vapour recycle, exhaust emissions concentration reaches 12mg/m
3The standard limited value requirement, the rate of recovery should be more than 99.99%.
CN99113874.0 " a kind of waste gas containing benzene burning purification method " discloses a kind of waste gas containing benzene and has burned purification method.Waste gas containing benzene is heated to 300 ℃-400 ℃ by heating furnace, and waste gas containing benzene after will heating again feeds incinerator, with after the combustion gas mixing in incinerator with 750 ℃ of-850 ℃ of burning points burning back dischargings.Benzene is inflammable and explosive chemical products, and high temperature heat source is used in the taboo of petrochemical industry product reservoir area, and burning method is handled benzene vapour, is a kind of waste of resource.
CN86106882 " the liquid one gas absorption process of purification containing benezene waste gas " discloses a kind of purification method of containing benezene waste gas, in the common fillers tower, adopt sulfolane, the N-methyl pyrrolidone, methyl-sulfoxide, carbonic allyl ester solution or its mixture are as the absorbent of benzene class toxic gas, heating desorption under the condition of negative pressure in revolving the film tower makes absorbent regeneration constitute the liquid one gas absorption process of closed cycle.The rate of recovery of absorption process is lower than 99%, and this method purifies back tail gas benzene concentration, can't reach 12mg/m
3The standard limited value requirement.
CN200610020410.8 " a kind of method for treating benzene storage tank tailed gas " discloses a kind of method for treating benzene storage tank tailed gas, mainly comprise: in storage tank, charge into nitrogen and make overwrite media, make storage tank keep sealing with water seal arrangement, keep certain pressure in the storage tank, the gaseous mixture that storage tank inner exhaust gas and nitrogen form is discharged by groove top exhaust pipe, and sends into burning and exhausting in the torch through mixing with coal gas behind the fireproof tempering device.The processing of the benzene vapour when this method is unsuitable for entrucking.
CN200720108765.2 " 3 benzene waste gas differential absorbing and purifying device " discloses a kind of 3 benzene waste gas differential absorbing and purifying device, mainly is the technical problem that solves absorption liquid, absorption equipment structure and mist control etc. in the existing in prior technology liquid absorption method.The rate of recovery of the rate of recovery absorption process of absorption process is lower than 99%, and this method purifies back tail gas benzene concentration, can't reach 12mg/m
3The standard limited value requirement.
CN200610051688.1 " a kind of method that reclaims toluene " discloses a kind of method that reclaims toluene, and the major technique measure of being taked specifically comprises the following steps: (1) dedusting; (2) cooling; (3) charcoal absorption (4) steam desorption; The toluene gas of the high concentration that (5) frees is along with water vapour enters condenser, and through cooling water temperature, mist becomes the mixed liquor of toluene and water; (6) separation of toluene in the mixed liquor; (7) toluene reuse.This method is with the toluene that adsorbs on the steam desorption active carbon, produces a large amount of toluene waste water that contain, and problem of secondary pollution is arranged.
CN200620127053.0 " toluene absorbing recovery device " discloses a kind of toluene absorbing recovery device, two-stage absorption, and adsorption efficiency reaches more than 99%, and the discharge capacity of toluene meets the current standard of country about the toluene discharging.This method is only applicable to contain the processing of toluene waste gas, does not relate to the removal of benzene and dimethylbenzene waste gas.
CN87100454 " a kind of method that reclaims dimethylbenzene in the waste gas " discloses a kind of method that reclaims dimethylbenzene in the waste gas, absorbs dimethylbenzene in the waste gas with absorbent earlier, carries out air-distillation then and reclaims dimethylbenzene.The rate of recovery of absorption process is lower than 99%, and this method purifies back tail gas benzene concentration, can't reach 12mg/m
3The standard limited value requirement.
Summary of the invention
At the deficiencies in the prior art, the utility model provides the cryogenic temperature condensation-adsorption and enrichment reclaimer that contains the rudimentary aromatic hydrocarbon gas of high concentration in a kind of air, adopt absorption of general refrigeration technique and silica gel absorber and suitable regeneration techniques, control tail gas qualified discharge, realize effective recovery of aromatic hydrocarbon, processing cost is cheap.
Cryogenic temperature condensation-absorbing recovery device that the utility model contains rudimentary aromatic hydrocarbon waste gases comprises one-level condensing zone, B-grade condensation district, adsorption zone successively, adsorption zone comprises that at least two absorbers carry out the adsorption-regeneration handover operation, heater is set in the adsorption zone, regenerative operation adopts vacuum regeneration, the discharging gas of vacuum regeneration loops back one-level condensing zone inlet, and regeneration time control refrigerating/heating apparatus makes the temperature of adsorption zone reach 60 ℃～90 ℃.
In the utility model device, one-level condensing zone control gas temperature is reduced to 7 ℃～5 ℃, and B-grade condensation district control gas temperature is reduced to-30 ℃～-40 ℃, and the temperature of control adsorption zone is 70 ℃～80 ℃ during adsorption zone regeneration.
In the utility model device, the B-grade condensation district is set to identical two B-grade condensation districts arranged side by side, the B-grade condensation district is provided with water vapour heating defrosting pipeline, when a B-grade condensation district carries out condensation work, defrost operation is heated in another B-grade condensation district, the operating temperature of heating defrosting is preferably 10～20 ℃ for 8～50 ℃ of the temperature in control B-grade condensation district.
In the utility model device, catch box is set communicates with one-level condensing zone, B-grade condensation district.
In the utility model device, the desorption pump adopts dry vacuum pump, and the absolute pressure≤50Pa after vacuumizing gets final product.
In the utility model device, adsorption zone can use conventional adsorbent, and as water-fast silica gel etc., the consumption of adsorbent is determined according to the content of rudimentary aromatic hydrocarbon in the waste gas and the regeneration period of design.The regeneration period of design is shorter, i.e. when regeneration was frequent, the adsorbent consumption was less, and the regeneration period of design is longer, and when promptly regeneration frequency was low, the adsorbent consumption was more, generally can by regeneration in per 24 hours once or regeneration in 48 hours once design.
In the utility model device, the heater in the adsorption zone can be steam heater, electric heater etc.
Adopt direct condensation method to reclaim the technology of rudimentary aromatic hydrocarbon in the waste gas, because benzene is in one section temperature range more than-37 ℃, exist the distillation phenomenon, gas benzene in this temperature range, directly condensation becomes solid benzene, easily by the gas condensing zone of carrying under one's arms out, the concentration of benzene can't reach 12mg/m to superfine little benzene solid particle in the discharge tail gas
3The emission limit requirement.And for the absorbing process of routine, because the concentration height of rudimentary aromatic hydrocarbon in the waste gas, for reaching 12mg/m
3The emission limit requirement, the adsorption tanks volume is very big, and adsorption process and regenerative process need frequent the switching, and the expense of regenerative operation is higher.Rudimentary aromatic hydrocarbon reaches the emission limit requirement in the discharging tail gas in order to satisfy, also reduce simultaneously investment cost and operating cost, the utility model device combines condensation method and absorption method, adopt the cryogenic temperature condensation technology, reclaim the rudimentary aromatic hydrocarbon gas of gas middle and high concentration, adopt modified silica-gel adsorbents adsorb technology, control tail gas qualified discharge.Experimental studies results shows, under suitable temperature, adopts the method that vacuumizes, and rudimentary aromatic hydrocarbon is desorption from the silica gel absorber easily, can obtain high desorption rate in the short time.Because in the gas after the condensing zone processing, rudimentary aromatic hydrocarbon concentration is very low, therefore, the adsorbance that absorber is born is very little, and the adsorbent use amount is also few, and the absorber relative set is very little, and investment and operating cost are all low.
The overall cost of device is cheap.The utility model device can effectively reclaim the rudimentary aromatic hydrocarbon gas of the high concentration that contains in the gas, and the rate of recovery of benzene is more than 99.99%, and the emission limit that processing back exhaust emissions concentration reaches benzene is 12mg/m
3, toluene emission limit be 40mg/m
3, dimethylbenzene emission limit be 70mg/m
3Requirement.
Description of drawings
Fig. 1 is the cryogenic temperature condensation-trap filter reclaimer structural relation schematic diagram of the utility model volatile organic steam.
The specific embodiment
The utility model use is as follows: from containing of airtight collection conduit rudimentary aromatic hydrocarbon gas at first enter first-stage condenser, in first-stage condenser, gas is cooled to about 7 ℃～5 ℃, and water vapour and rudimentary aromatic hydrocarbon major part are removed in the gas, and condensation water drains into the hydrops case.
Leave the not noncondensing gas of first-stage condenser, enter in two secondary condensers arranged side by side, in this secondary condenser, be cooled to-30 ℃～-40 ℃, through behind the certain hour, change the valve opening and closing state that is communicated with, change gas flow, the not noncondensing gas that leaves first-stage condenser enters another in two secondary condensers arranged side by side, is cooled to-30 ℃～-40 ℃ in this secondary condenser.The secondary condenser of replacing enters the defrost stage; its corresponding two stage cooler group outage is shut down; water vapour is by this secondary condenser of pipeline indirect; when temperature 〉=10 in this secondary condenser ℃, stop the water vapour heating, finish defrost process; liquid enters hydrops case 7; and start corresponding two stage cooler group, and this secondary condenser is carried out refrigeration cool-down, temperature is reduced to-30 ℃～-40 ℃.Behind the process certain hour, change the valve opening and closing state that is communicated with, change gas flow, the not noncondensing gas that leaves first-stage condenser enters the secondary condenser that defrost is laid equal stress on and newly freezed, and is cooled to-30 ℃～-40 ℃ in this secondary condenser.And another secondary condenser of replacing enters the defrost stage; its corresponding two stage cooler group outage is shut down; water vapour is by this secondary condenser of pipeline indirect; when temperature 〉=10 in this secondary condenser ℃, stop the water vapour heating, finish defrost process; liquid enters hydrops case 7; and start corresponding two stage cooler group, and this secondary condenser is carried out refrigeration cool-down, temperature is reduced to-30 ℃～-40 ℃.Above-mentioned process of refrigerastion and defrost process, two secondary condensers in parallel hocket.
When rudimentary aromatic hydrocarbon gas enters first-stage condenser from containing of airtight collection conduit, start adsorption pump.The secondary condenser exit gas enters in two absorbers arranged side by side one by adsorption pump, and the rudimentary aromatic hydrocarbon gas that contains in the gas is adsorbed agent absorption, purified gas qualified discharge.Behind absorber adsorption treatment certain volume gas, change to be communicated with the valve open and-shut mode, to change gas flow, the secondary condenser exit gas enters in two absorbers arranged side by side another by adsorption pump, the rudimentary aromatic hydrocarbon gas that contains in the gas is adsorbed agent absorption, purified gas qualified discharge.Finished and once adsorbed and be replaced the absorber that gets off, enter the desorption and regeneration state, at first water vapour passes through the adsorbent bed of coil pipe indirect absorber, adsorbent bed temperature reaches 70 ℃～80 ℃, by the desorption pump, vacuumizes the rudimentary aromatic hydrocarbon that adsorbs on the desorption adsorbent, the rudimentary aromatic hydrocarbon rich gas that is got off by desorption, send into the first-stage condenser import and recycle, during the desorption pump operation, control adsorbent bed temperature≤90 ℃.Through behind the certain hour, stop the water vapour heating, stop the desorption pump operation, finish a desorption and regeneration process of this absorber, and standby.Behind another absorber adsorption treatment certain volume gas, change the valve opening and closing state that is communicated with, change gas flow, the secondary condenser exit gas enters the absorber that desorption and regeneration has been got well by adsorption pump, the rudimentary aromatic hydrocarbon gas that contains in the gas is adsorbed agent absorption, purified gas qualified discharge.Finished and once adsorbed and be replaced another absorber of getting off, enter the desorption and regeneration state, at first water vapour passes through the adsorbent bed of coil pipe indirect absorber, when adsorbent bed temperature reaches 70 ℃～80 ℃, start the desorption pump, vacuumize the rudimentary aromatic hydrocarbon that adsorbs on the desorption adsorbent, the rudimentary aromatic hydrocarbon rich gas that is got off by desorption, send into the first-stage condenser import and recycle, during the desorption pump operation, control adsorbent bed temperature≤90 ℃.Through behind the certain hour, stop the water vapour heating, stop the desorption pump operation, finish a desorption and regeneration process of this absorber, and standby.Adsorption process and desorption and standby process, two absorbers in parallel hocket.
The utility model is described in further detail to reclaim the waste gas containing benzene specific embodiment that benzene entrucking process produces below.
Referring to Fig. 1, connect the power supply of one-level refrigeration unit 2 earlier, the power supply of two stage cooler group A4, the power supply of two stage cooler group B6, by the temperature of setting each condenser is carried out refrigeration cool-down, with the temperature-30 of 7 ℃～5 ℃ of temperature keeping first-stage condenser 1 and secondary condenser A3, secondary condenser B5 ℃～-40 ℃, condenser can be selected the equipment of this area routine.
When benzene entrucking process, the waste gas containing benzene of generation enters first-stage condenser 1 by closed gas pipeline 17, starts adsorption pump 8, and waste gas containing benzene is cooled to 7 ℃～5 ℃ in first-stage condenser 1, condensation water from the row of conduits of first-stage condenser 1 bottom to catch box 7.
Leave the not noncondensing gas of first-stage condenser 1, enter secondary condenser A3, in secondary condenser A3, be cooled to-30 ℃～-40 ℃, through behind the certain hour, change the valve opening and closing state that the B-grade condensation district is communicated with, change gas flow, the not noncondensing gas that leaves first-stage condenser 1 enters secondary condenser B5, is cooled to-30 ℃～-40 ℃ in secondary condenser B5.Secondary condenser A3 enters the defrost stage; the two stage cooler group A4 shutdown of cutting off the power supply; water vapour 12 is by pipeline indirect secondary condenser A3; when temperature 〉=10 in the secondary condenser A3 ℃, stop water vapour 12 heating, finish defrost process; liquid enters hydrops case 7; and start two stage cooler group A4, and secondary condenser A3 is carried out refrigeration cool-down, the temperature of secondary condenser A3 is reduced to-30 ℃～-40 ℃.Through behind the certain hour, change the valve opening and closing state that the B-grade condensation district is communicated with, change gas flow, the not noncondensing gas that leaves first-stage condenser 1 enters secondary condenser A3, is cooled to-30 ℃～-40 ℃ in secondary condenser A3.Secondary condenser B5 enters the defrost stage; the two stage cooler group B6 shutdown of cutting off the power supply; water vapour 13 is by pipeline indirect secondary condenser B5; when temperature 〉=10 in the secondary condenser B5 ℃, stop water vapour 13 heating, finish defrost process; liquid enters hydrops case 7; and start two stage cooler group B6, and secondary condenser B5 is carried out refrigeration cool-down, the temperature of secondary condenser B5 is reduced to-30 ℃～-40 ℃.Above-mentioned process of refrigerastion and defrost process, secondary condenser A3 and secondary condenser B5 hocket.
The exit gas of secondary condenser A3 or secondary condenser B5 enters absorber A9 by adsorption pump 8, and the rudimentary aromatic hydrocarbon that contains in the gas is adsorbed agent absorption, tail gas qualified discharge.Behind absorber A9 adsorption treatment certain volume gas, change the valve opening and closing state that adsorption zone is communicated with, change gas flow, the exit gas of secondary condenser A3 or secondary condenser B5 enters absorber B10 by adsorption pump 8, the rudimentary aromatic hydrocarbon that contains in the gas is adsorbed agent absorption, purified gas qualified discharge.Absorber A9 enters the desorption and regeneration state, at first water vapour 14 passes through the adsorbent bed of coil pipe indirect absorber A9, when adsorbent bed temperature reaches 70 ℃～80 ℃, start desorption pump 11, vacuumize the rudimentary aromatic hydrocarbon that adsorbs on the desorption adsorbent,, send into first-stage condenser 1 import and recycle by the rudimentary aromatic hydrocarbon rich gas that desorption gets off, desorption pump 11 run durations, adsorbent bed temperature≤80 of control absorber A9 ℃.Behind the desorption pump operation certain hour, stop the heating of water vapour 14, stop 11 operations of desorption pump, finish the desorption and regeneration process of absorber A9, and standby.Behind absorber B10 adsorption treatment certain volume gas, change the valve opening and closing state that adsorption zone is communicated with, change gas flow, the exit gas of secondary condenser A3 or secondary condenser B5 enters absorber A9 by adsorption pump 8, the rudimentary aromatic hydrocarbon that contains in the gas is adsorbed agent absorption, purified gas qualified discharge.Absorber B10 enters the desorption and regeneration state, at first water vapour 15 passes through the adsorbent bed of coil pipe indirect absorber B10, when adsorbent bed temperature reaches 70 ℃～80 ℃, start desorption pump 11, vacuumize the rudimentary aromatic hydrocarbon that adsorbs on the desorption adsorbent,, send into first-stage condenser 1 import and recycle by the rudimentary aromatic hydrocarbon rich gas that desorption gets off, desorption pump 11 run durations, the adsorbent bed temperature of control absorber B10≤80 ℃.Through behind the certain hour, stop water vapour 15 heating, stop adsorption pump 11 operations, finish the desorption and regeneration process of absorber B10, and standby.Adsorption process and desorption and regeneration and standby process, two absorbers in parallel hocket.
Claims (10)
1. cryogenic temperature condensation-absorbing recovery device that contains rudimentary aromatic hydrocarbon waste gases, it is characterized in that: this device comprises one-level condensing zone, B-grade condensation district, adsorption zone successively, adsorption zone comprises that at least two absorbers carry out the adsorption-regeneration handover operation, heater is set in the adsorption zone, regenerative operation adopts and vacuumizes regeneration, and the discharging gas of vacuum regeneration loops back one-level condensing zone inlet.
2. according to the described device of claim 1, it is characterized in that: regeneration time control refrigerating/heating apparatus makes the temperature of adsorption zone reach 60 ℃～90 ℃.
3. according to the described device of claim 1, it is characterized in that: one-level condensing zone control gas temperature is reduced to 7 ℃～5 ℃, and B-grade condensation district control gas temperature is reduced to-30 ℃～-40 ℃, and the temperature of control adsorption zone is 70 ℃～80 ℃ during adsorption zone regeneration.
4. according to claim 1 or 3 described devices, it is characterized in that: the B-grade condensation district is set to identical two B-grade condensation districts arranged side by side, the B-grade condensation district is provided with water vapour heating defrosting pipeline, when a B-grade condensation district carried out condensation work, defrost operation was heated in another B-grade condensation district.
5. according to the described device of claim 4, it is characterized in that: the operating temperature of heating defrosting is 10～50 ℃ of the temperature in control B-grade condensation district.
6. according to the described device of claim 1, it is characterized in that: catch box is set communicates with one-level condensing zone, B-grade condensation district.
7. according to the described device of claim 1, it is characterized in that: the desorption pump adopts dry vacuum pump.
8. according to the described device of claim 1, it is characterized in that: adsorption zone can water-fast silica gel.
9. according to the described device of claim 1, it is characterized in that: the heater in the adsorption zone is steam heater or electric heater.
10. according to the described device of claim 1, it is characterized in that: the operating temperature of heating defrosting is 10～20 ℃ for the temperature in control B-grade condensation district.
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| CN 200920247547 CN201578875U (en) | 2009-10-27 | 2009-10-27 | Low-temperature condensation and adsorption recovery device containing high-concentration low-level aromatic hydrocarbon exhaust gas |
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| CN102205197A (en) * | 2011-03-17 | 2011-10-05 | 杰智环境科技股份有限公司 | Organic waste gas purifying system and method for preventing surface of absorbing material from condensing and caking |
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