CN115254078A - VOCs recovery system and method using double-bed purification purge gas - Google Patents
VOCs recovery system and method using double-bed purification purge gas Download PDFInfo
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/30—Processes for preparing, regenerating, or reactivating
- B01J20/34—Regenerating or reactivating
- B01J20/345—Regenerating or reactivating using a particular desorbing compound or mixture
- B01J20/3458—Regenerating or reactivating using a particular desorbing compound or mixture in the gas phase
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
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- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
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- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Abstract
The invention discloses a VOCs recovery system utilizing double-bed purification purge gas, which comprises a desorption bed, a first purification bed, a second purification bed and desorption condensation auxiliary equipment, wherein the desorption bed, the first purification bed and the second purification bed are connected in parallel, the desorption condensation auxiliary equipment comprises a VOCs condenser, a gas-liquid separator, a desorption fan, a heater and a nitrogen source, the VOCs condenser, the gas-liquid separator, the desorption fan and the heater are sequentially connected, and the desorption bed, the first purification bed and the second purification bed are all communicated with the desorption condensation auxiliary equipment. According to the invention, the double purification beds are arranged in the closed cycle desorption system, so that the concentration of VOCs in carrier gas can be effectively controlled, the high purification and deep regeneration of cycle desorption nitrogen are realized, the ultralow concentration discharge after adsorption purification is ensured under the condition of VOCs condensation recovery with high condensation temperature and low energy consumption, the condensation temperature can be increased, and near zero emission of organic waste gas is realized.
Description
Technical Field
The invention relates to the technical field of environmental protection, in particular to a VOCs recovery system and a method thereof by utilizing double-bed purification purge gas.
Background
Along with the continuous development of the industrialization level in China, a large amount of discharged industrial organic waste gas becomes one of the main sources of air pollution in China. Volatile Organic Compounds (VOCs) are used as main pollutant components of organic waste gas, and provide serious challenges for human health and ecological environment.
The destruction and recovery are two main approaches for the treatment of industrial organic waste gas. The disposal method based on the destruction method is generally used for decomposing VOCs by an oxidation method, so that the applicability is wide, but the oxidation and decomposition of VOCs are usually accompanied by the generation of harmful byproducts such as NOx, dioxin, secondary organic aerosol and the like, so that the secondary pollution of the atmospheric environment is caused, and meanwhile, the destruction method inevitably discharges a large amount of CO into the environment 2 Therefore, the destruction method is not a low-carbon and green VOCs treatment method. The recycling method realizes the recycling of resources on the basis of retaining the structure of the VOCs substances through a physical separation mode, and particularly has higher economical efficiency on high-value organic components. Specifically, the recovery method mainly comprises the technologies of absorption, condensation, membrane separation, adsorption and the like, wherein the combined method of adsorbing and concentrating VOCs and then thermal desorption, condensation and recovery has the advantages of high recovery rate, good economic benefit and the like, and is an industrial organic waste gas treatment method recommended by the industry. Meanwhile, in recent years, a centralized treatment technology of activated carbon is gradually developed, and activated carbon which is absorbed and penetrated in each factory is transported to a regeneration station for centralized treatment, so that the realization form of an absorption-condensation recovery mode is expanded.
The invention discloses a system and a method for recovering VOCs (volatile organic compounds) by normal temperature condensation, wherein the system and the method for recovering VOCs by normal temperature condensation are provided by Chinese invention patent (CN 114558420A), the normal temperature condensation of VOCs is realized by parallel connection of four activated carbon adsorption beds and high-temperature and high-pressure steam desorption, the condensation temperature of the system can be effectively improved, but the recovery of part of VOCs with low boiling points is difficult to realize, and meanwhile, as the steam desorption is adopted, the recovered product contains a large amount of liquid water and has the problems of secondary condensate water pollution and the like;
another invention patent (CN 109985485 a) proposes a device and method for high concentration gas adsorption recovery purification, in which a regeneration system is arranged in parallel with an adsorption system for recovering gas components and regenerating an adsorbent, and its main component is an auxiliary adsorber, and the high efficiency adsorption recovery of high concentration organic gas is realized by adsorbing and desorbing the residual amount by the auxiliary adsorber; however, the two auxiliary adsorber regeneration modes provided by the system adopt single-bed-based hot nitrogen cyclic desorption, and the VOCs concentration of the purge gas at the inlet of the desorption bed is higher in the desorption process, so that the re-adsorption process faces a larger penetration risk.
At the present stage, the VOCs normal atmospheric temperature condensation recovery system who adopts closed circulation desorption often faces the problem of circulation nitrogen gas area concentration desorption, and the addition of purification bed can reduce the VOCs content in the nitrogen gas purge gas by a wide margin, improves the desorption degree, but the single bed regeneration process of purification bed leads to the unable complete desorption of its export, and purification bed export still remains the VOCs of certain concentration in the purification process, reduces the VOCs treatment effeciency of adsorption process, easily leads to discharging the risk that exceeds standard. Especially in the normal temperature condensation process of low boiling point VOCs, this risk is obvious aggravation, has reduced the reliability of absorption purification, for this reason, we propose a VOCs recovery system and its method that utilizes the twin-bed purification purge gas.
Disclosure of Invention
The invention aims to provide a VOCs recovery system and a VOCs recovery method by using double-bed purification purge gas, so as to solve the problems to be solved in the background art.
In order to achieve the purpose, the invention provides the following technical scheme: the utility model provides an utilize VOCs recovery system of two bed purification purge gas, includes desorption bed, first purification bed, second purification bed and desorption condensation auxiliary assembly, desorption bed, first purification bed and second purification bed parallel connection, desorption condensation auxiliary assembly is including the nitrogen gas source, VOCs condenser, vapour and liquid separator, desorption fan and the heater that connect gradually, desorption bed, first purification bed and second purification bed all are linked together with desorption condensation auxiliary assembly, set up first valve and second valve around the desorption bed respectively, first purification bed front and back end is provided with third valve, fourth valve, seventh valve and eighth valve respectively, second purification bed front and back end is provided with fifth valve, sixth valve, ninth valve and tenth valve respectively, the fixed intercommunication in exit position of desorption fan has three pipelines, wherein two pipelines are fixed respectively and are linked together in the both sides of first purification bed and second purification bed, be provided with the eleventh valve between two pipelines, the top of nitrogen gas source is provided with nitrogen gas and replenishes the valve, another group pipeline and heater intercommunication each other.
Preferably, the top and the bottom of desorption bed run through respectively and are provided with first connecting pipe and second connecting pipe, the top and the bottom of first purification bed run through respectively and are provided with third connecting pipe and fourth connecting pipe, the top and the bottom of second purification bed run through respectively and are provided with fifth connecting pipe and sixth connecting pipe, the fixed intercommunication in bottom of second connecting pipe, fourth connecting pipe and sixth connecting pipe has the eighth connecting pipe, the fixed intercommunication in one end of eighth connecting pipe has the seventh connecting pipe, the fixed intercommunication of seventh connecting pipe and nitrogen gas source, the one end and the fixed intercommunication of VOCs condenser of eighth connecting pipe, the fixed intercommunication in proper order of the one end that the eighth connecting pipe was kept away from to the VOCs condenser has vapour and liquid separator and desorption fan, the fixed intercommunication in one end of desorption fan has the tenth connecting pipe, the fixed intercommunication in one end of tenth connecting pipe has the ninth connecting pipe, the fixed intercommunication of one end of ninth connecting pipe has the heater, just the top and the fixed intercommunication of ninth connecting pipe of first connecting pipe, third connecting pipe and fifth connecting pipe.
Preferably, an eleventh connecting pipe is fixedly communicated with the top of the tenth connecting pipe, one end of the eleventh connecting pipe is fixedly communicated with the sixth connecting pipe, a twelfth connecting pipe is fixedly communicated with the fourth connecting pipe and fixedly communicated with the top of the eleventh connecting pipe, a thirteenth connecting pipe is fixedly communicated with the top of the tenth connecting pipe and positioned on one side of the eleventh connecting pipe, and a fourteenth connecting pipe and a fifteenth connecting pipe are fixedly communicated with the fifth connecting pipe and the third connecting pipe respectively and fixedly communicated with one end of the thirteenth connecting pipe through a tee.
Preferably, the surfaces of the first connecting pipe, the third connecting pipe and the fifth connecting pipe are respectively provided with a first valve, a third valve and a fifth valve, the surfaces of the second connecting pipe, the fourth connecting pipe and the sixth connecting pipe are respectively provided with a second valve, a fourth valve and a sixth valve, a nitrogen supplementary valve is arranged between the nitrogen gas source and the seventh connecting pipe, an eleventh valve is arranged on the surface of the tenth connecting pipe and between the eleventh connecting pipe and the thirteenth connecting pipe, a tenth valve is arranged on the surface of the eleventh connecting pipe and between the eleventh connecting pipe and the sixth connecting pipe, an eighth valve is arranged on the surface of the twelfth connecting pipe, one end of the twelfth connecting pipe is installed on the surface of the fourth connecting pipe in a penetrating manner, the installation position of the twelfth connecting pipe is between the first purifying bed and the fourth valve, a ninth valve is arranged on the surface of the fourteenth connecting pipe, a seventh valve is arranged on the surface of the fifteenth connecting pipe, the fifteenth connecting pipe is installed on the surface of the third connecting pipe, and the installation position of the fifteenth connecting pipe is between the first purifying bed and the third valve.
Preferably, the first purification bed and the second purification bed are provided as a low-temperature adsorption bed using condensed residual heat, and the first purification bed and the second purification bed have the same adsorbent filling amount, and the packing heights of the packing inside the first purification bed and the second purification bed are the same.
Preferably, the operation condition of the desorption bed is a closed desorption and cooling process; the operation conditions of the first purification bed and the second purification bed comprise nitrogen purification, closed desorption and cooling processes.
Preferably, the desorption and condensation auxiliary equipment adopts a natural cold source for treating the high-boiling-point VOCs, and adopts a refrigerating unit or liquid nitrogen for refrigerating for treating the low-boiling-point VOCs.
A VOCs recovery method using a double-bed purification purge gas comprises the following steps:
s1: firstly, debugging equipment, closing all valves except a first valve, a second valve, a seventh valve, an eighth valve and an eleventh valve, opening a nitrogen supplementing valve, then connecting a nitrogen source into the nitrogen supplementing valve, then replacing all pipelines and equipment in the whole system with nitrogen, and closing all valves and the nitrogen source when an online oxygen content detector shows that the oxygen content is lower than 5%;
s2: then, the seventh valve and the eighth valve are closed, and the desorption fan, the VOCs condenser, the gas-liquid separator and the heater are sequentially opened, so that the desorption bed can be desorbed, and simultaneously, high-concentration VOCs in the desorption gas can be condensed and recovered until the desorption concentration reaches a first concentration threshold value;
s3: opening a seventh valve and an eighth valve, closing an eleventh valve, introducing the non-condensable gas at the outlet of the VOCs condenser into the first purification bed for nitrogen purification, heating the purified nitrogen again by a heater, and then deeply desorbing the heated nitrogen by a desorption bed;
s4: when the concentration of the VOCs at the outlet of the condenser is lower than a second concentration threshold value, the heater is closed, and the desorption bed is cooled;
s5: after the cooling process of the desorption bed in the step S is finished, opening the eleventh valve, and closing the seventh valve, the eighth valve and the desorption condensation auxiliary equipment, so that the desorption condensation recovery process of the desorption bed can be finished;
s6: repeating the steps S1-S5 until the first purification bed is penetrated by adsorption;
s7: closing all valves except the third valve, the fourth valve, the ninth valve, the tenth valve and the eleventh valve, opening a nitrogen gas supplementing valve, then opening a nitrogen gas source, replacing gas in a system pipeline and equipment with nitrogen gas, and closing all valves and the nitrogen gas source when the online oxygen content detector shows that the oxygen content is lower than percent;
s8: then closing the ninth valve and the tenth valve, sequentially opening a desorption fan, a VOCs condenser, a gas-liquid separator and a heater, beginning to desorb the first purification bed, and simultaneously condensing and recovering high-concentration VOCs in the desorption gas until the desorption concentration reaches a first concentration threshold value;
s9: opening a ninth valve and a tenth valve, closing an eleventh valve, introducing the non-condensable gas at the outlet of the VOCs condenser into a second purification bed for nitrogen purification, heating the purified nitrogen again by a heater, and introducing the purified nitrogen into the first purification bed for deep desorption;
s10: when the concentration of the VOCs at the outlet of the condenser is lower than a second concentration threshold value, the heater is closed, and the first purification bed is cooled;
s11: after the cooling process of the S first purification bed is finished, opening the eleventh valve, closing the ninth valve and the tenth valve, and closing the rest of the desorption condensation auxiliary equipment, so that the desorption condensation recovery process of the first purification bed can be finished;
s12: repeating the steps S-S until the second purification bed is penetrated by adsorption;
s13: and repeating the step S-S, wherein the opening and closing states of the corresponding valves of the first purification bed and the second purification bed are interchanged, and the deep desorption, condensation and recovery of the second purification bed are completed through the purification transfer function of the first purification bed, so that the cyclic operation of the system can be completed.
Preferably, the first concentration threshold is a determination concentration after the condensation recovery process is finished, and the concentration range is 1-3 times of the saturated concentration of the VOCs at the condensation temperature, and the second concentration threshold is a determination concentration after the nitrogen purification process is finished, and the concentration range is 0.1-1 times of the adsorption concentration.
Preferably, the first purification bed and the second purification bed have the same filling amount of the adsorbent, and the filling amount needs to be calculated according to adsorption isotherms at the desorption temperature and the condensation temperature and a saturation pressure curve of the VOCs, and a specific calculation method of the filling amount is shown as the following formula:
wherein Tde is a desorption temperature, tcd is a condensation temperature, ccd is a saturated condensation concentration, H is a design height of the purification bed, H is a height of the mass transfer zone, q is an adsorption capacity, the height of the mass transfer zone is set to be 0.1-0.3m, and the apparent wind speeds of the first purification bed and the second purification bed are set to be 0.05-0.6m/s.
Compared with the prior art, the invention has the following beneficial effects: according to the invention, a closed nitrogen circulating desorption adsorbent regeneration mode is adopted, compared with the existing steam desorption mode (CN 109985485A), the desorption temperature and the desorption degree are improved, the subsequent adsorption is effectively ensured to be discharged up to the standard, and the problems of secondary pollution of condensed water and the like are avoided. In addition, compared with the existing single-bed auxiliary purification system (CN 109985485A), the invention ensures that the regeneration process of the purification bed body is always zero-concentration cyclic nitrogen desorption through the way of double-bed alternation and mutual purification by arranging double purification beds in the closed cyclic desorption system, ensures the deep regeneration of the adsorbent at the outlet of the purification bed, further ensures the purification effect, realizes the deep regeneration of the desorption bed and the efficient purification of the adsorption process, and ensures the near-zero concentration discharge of VOCs. The invention adopts a double purification bed design, can effectively reduce the concentration of VOCs in desorption carrier gas, realizes high purification of nitrogen and deep regeneration of adsorbent in the cyclic desorption process, ensures ultralow concentration discharge after adsorption purification under the condition of VOCs condensation recovery with high condensation temperature and low energy consumption, can improve condensation temperature, has obvious energy-saving advantage compared with deep cooling and the like, and simultaneously realizes near zero emission of organic waste gas.
Drawings
FIG. 1 is a schematic view of the connection structure of the present invention.
In the figure: the device comprises a desorption bed 1, a first purification bed 2, a second purification bed 3, a 4VOCs condenser, a 5 gas-liquid separator, a 6 desorption fan, a 7 heater, an 8 nitrogen gas source, a 9 first valve, a 10 second valve, a 11 third valve, a 12 fourth valve, a 13 fifth valve, a 14 sixth valve, a 15 seventh valve, a 16 eighth valve, a 17 ninth valve, a 18 tenth valve, a 19 eleventh valve, a 20 nitrogen gas supplementing valve, a 21 first connecting pipe, a 22 second connecting pipe, a 23 third connecting pipe, a 24 fourth connecting pipe, a 25 fifth connecting pipe, a 26 sixth connecting pipe, a 27 seventh connecting pipe, a 28 eighth connecting pipe, a 29 ninth connecting pipe, a 30 tenth connecting pipe, a 31 eleventh connecting pipe, a 32 twelfth connecting pipe, a 33 thirteenth connecting pipe, a 34 fourteenth connecting pipe and a 35 fifteenth connecting pipe.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Referring to fig. 1, the present invention provides a technical solution: the utility model provides an utilize VOCs recovery system of two beds purification sweep gas, includes desorption bed 1, first purification bed 2, second purification bed 3 and desorption condensation auxiliary assembly, desorption bed 1, first purification bed 2 and the 3 parallel connection of second purification bed, desorption condensation auxiliary assembly includes VOCs condenser 4, vapour and liquid separator 5, desorption fan 6, heater 7 and nitrogen gas source 8, VOCs condenser 4, vapour and liquid separator 5, desorption fan 6 and heater 7 connect gradually, desorption bed 1, first purification bed 2 and second purification bed 3 all are linked together with desorption condensation auxiliary assembly, set up first valve 9 and second valve 10 respectively before desorption bed 1, first purification bed 2 front and back end sets up the third valve 11, the fourth valve 12 that switch the desorption mode respectively and switch seventh valve 15, the eighth valve 16 of purification mode, second purification bed 3 front and back end sets up the fifth valve 13, the sixth valve 14 and switch the ninth valve 17 that switch the purification mode respectively and the fixed valve 17, the fixed valve 18 that the purification bed 18 that the purification mode was provided with two nitrogen gas source outlet pipeline in the purification bed 3, the fixed valve 19 intercommunication of the ten two purification beds of desorption bed 3 between the purification bed 3.
The method comprises the following steps of regenerating a desorption bed 1 by adopting hot nitrogen cyclic desorption, simultaneously realizing condensation recovery of high-concentration VOCs in desorption gas, and separating residual VOCs from nitrogen purge gas by switching a valve when the desorption concentration reaches a first concentration threshold value, wherein non-condensable gas enters a first purification bed 2, so that the concentration of a desorption inlet of the desorption bed 1 is always kept zero, and the desorption bed 1 is ensured to be completely removed; after the desorption gas of the desorption bed 1 is purified for a plurality of times, when the first purification bed 2 is absorbed and penetrated or is close to penetrating, the second purification bed 3 alternately undertakes purification work through the combined switching of a plurality of groups of valves; then, carrying out hot nitrogen cyclic desorption on the first purification bed 2, simultaneously realizing condensation and recovery of high-concentration VOCs in the desorption gas, starting the nitrogen purification function of the second purification bed 3 through valve switching when the desorption concentration reaches a first concentration threshold value, realizing deep regeneration of the first purification bed 2, and ensuring that the outlet concentration is zero when the first purification bed 2 runs next round; the desorption process of the desorption bed 1 is repeated until the second purification bed 3 is absorbed and penetrated or is close to penetrating, and the first purification bed 2 alternately undertakes purification work through valve switching, so that one complete cycle between the first purification bed 2 and the second purification bed 3 is completed, and the organic waste gas treatment standard emission at high condensation temperature is realized.
The top and the bottom of desorption bed 1 run through respectively and are provided with first connecting pipe 21 and second connecting pipe 22, the top and the bottom of first purification bed 2 run through respectively and are provided with third connecting pipe 23 and fourth connecting pipe 24, the top and the bottom of second purification bed 3 run through respectively and are provided with fifth connecting pipe 25 and sixth connecting pipe 26, the fixed intercommunication in bottom of second connecting pipe 22, fourth connecting pipe 24 and sixth connecting pipe 26 has eighth connecting pipe 28, the fixed intercommunication in one end of eighth connecting pipe 28 has seventh connecting pipe 27, seventh connecting pipe 27 and the fixed intercommunication of nitrogen gas source 8, the one end and the fixed intercommunication of VOCs condenser 4 of eighth connecting pipe 28, the fixed intercommunication in proper order of the one end that the eighth connecting pipe 28 was kept away from to VOCs condenser 4 has gas-liquid separator 5 and desorption fan 6, the fixed intercommunication in one end of desorption fan 6 has tenth connecting pipe 30, the fixed intercommunication in one end of tenth connecting pipe 30 has ninth connecting pipe 29, the fixed intercommunication of one end of ninth connecting pipe 29 has heater 7, just the fixed intercommunication of first connecting pipe 21, third connecting pipe 23 and the top of fifth connecting pipe 25 and ninth connecting pipe 29.
Preferably, an eleventh connection pipe 31 is fixedly communicated with a top portion of the tenth connection pipe 30, one end of the eleventh connection pipe 31 is fixedly communicated with the sixth connection pipe 26, a twelfth connection pipe 32 is fixedly communicated with the fourth connection pipe 24, a thirteenth connection pipe 33 is fixedly communicated with a top portion of the tenth connection pipe 30 and positioned on one side of the eleventh connection pipe 31, and a fourteenth connection pipe 34 is fixedly communicated with the fifth connection pipe 25 and a fifteenth connection pipe 35 is fixedly communicated with the third connection pipe 23.
Preferably, the first, third and fifth connection pipes 21, 23 and 25 are respectively provided with a first valve 9, a third valve 11 and a fifth valve 13 on the surface thereof, the second, fourth and sixth connection pipes 22, 24 and 26 are respectively provided with a second valve 10, a fourth valve 12 and a sixth valve 14 on the surface thereof, a nitrogen supplement valve 20 is provided between the nitrogen source 8 and the seventh connection pipe 27, an eleventh valve 19 is provided on the surface of the tenth connection pipe 30 and between the eleventh connection pipe 31 and the thirteenth connection pipe 33, a tenth valve 18 is provided on the surface of the eleventh connection pipe 31 and between the eleventh connection pipe 31 and the sixth connection pipe 26, an eighth valve 16 is provided on the surface of the twelfth connection pipe 32, one end of the twelfth connection pipe 32 is installed on the surface of the fourth connection pipe 24 in a penetrating manner, the installation position is between the first purification bed 2 and the fourth valve 12, a ninth valve 17 is provided on the surface of the fourteenth connection pipe 34, a seventh valve 15 is provided on the surface of the fifteenth connection pipe 35, a fifteenth connection pipe 35 is installed on the surface of the third connection pipe 23, and the installation position is between the purification bed 2 and the third valve 11.
Preferably, the first purification bed 2 and the second purification bed 3 are provided as a low-temperature adsorption bed using condensed residual heat, and the first purification bed 2 and the second purification bed 3 have the same adsorbent filling amount, and the packing heights of the packing inside the first purification bed 2 and the second purification bed 3 are the same.
Preferably, the operation condition of the desorption bed 1 is a closed desorption and cooling process; the operation conditions of the first purification bed 2 and the second purification bed 3 comprise nitrogen purification, closed desorption and cooling processes.
Preferably, the desorption and condensation auxiliary equipment adopts a natural cold source for treating the high-boiling-point VOCs, and adopts a refrigerating unit or liquid nitrogen for refrigerating for treating the low-boiling-point VOCs.
A VOCs recovery method using double-bed purification purge gas comprises the following steps:
s1: firstly, debugging equipment, closing all valves except a first valve 9, a second valve 10, a seventh valve 15, an eighth valve 16 and an eleventh valve 19, opening a nitrogen supplementing valve 20, then connecting a nitrogen source into the nitrogen supplementing valve 20, then replacing all the gas in all the pipelines and equipment of the whole system with nitrogen, and closing all the valves and the nitrogen source when an online oxygen content detector shows that the oxygen content is lower than 5%;
s2: then, the seventh valve 15 and the eighth valve 16 are closed, and the desorption fan 6, the VOCs condenser 4, the gas-liquid separator 5 and the heater 7 are sequentially opened, so that the desorption bed 1 can be desorbed, and simultaneously, high-concentration VOCs in the desorption gas can be condensed and recovered until the desorption concentration reaches a first concentration threshold value;
s3: opening a seventh valve 15 and an eighth valve 16, closing an eleventh valve 19, introducing the non-condensable gas at the outlet of the VOCs condenser 4 into the first purification bed 2 for nitrogen purification, heating the purified nitrogen by the heater 7 again, and then deeply desorbing the heated nitrogen by the desorption bed 1;
s4: when the concentration of the outlet of the VOCs condenser 4 is lower than a second concentration threshold value, the heater 7 is closed, and the desorption bed 1 is cooled;
s5: when the cooling process of the desorption bed 1 in the step S4 is finished, the eleventh valve 19 is opened, the seventh valve 15, the eighth valve 16 and the desorption condensation auxiliary equipment are closed, so that the desorption condensation recovery process of the desorption bed 1 can be completed;
s6: repeating the steps S1 to S5 until the first purification bed 2 is penetrated by adsorption;
s7: then closing all valves except a third valve 11, a fourth valve 12, a ninth valve 17, a tenth valve 18 and an eleventh valve 19, opening a nitrogen supplementing valve 20, then opening a nitrogen source, replacing the gas in the system pipeline and the equipment with nitrogen, and closing all valves and the nitrogen source when the online oxygen content detector shows that the oxygen content is lower than 5%;
s8: then closing the ninth valve 17 and the tenth valve 18, and opening the desorption fan 6, the VOCs condenser 4, the gas-liquid separator 5 and the heater 7 in sequence to begin to desorb the first purification bed 2, and simultaneously condensing and recovering high-concentration VOCs in the desorbed gas until the desorption concentration reaches a first concentration threshold value;
s9: opening a ninth valve 17 and a tenth valve 18, closing an eleventh valve 19, introducing the non-condensable gas at the outlet of the VOCs condenser 4 into the second purification bed 3 for nitrogen purification, heating the purified nitrogen again by the heater 7, and introducing the purified nitrogen into the first purification bed 2 for deep desorption;
s10: when the concentration of the VOCs at the outlet of the condenser 4 is lower than the second concentration threshold, the heater 7 is closed, and the first purification bed 2 is cooled;
s11: after the cooling process of the first purification bed 2 in S10 is finished, the eleventh valve 19 is opened, the ninth valve 17 and the tenth valve 18 are closed, and the rest of the desorption condensation auxiliary devices are closed, so that the desorption condensation recovery process of the first purification bed 2 can be completed;
s12: repeating the steps S1 to S5 until the second purification bed 3 is penetrated by adsorption;
s13: and (4) repeating the steps S7-S11, wherein the opening and closing states of corresponding valves of the first purification bed 2 and the second purification bed 3 are interchanged, and the deep desorption, condensation and recovery of the second purification bed 3 are completed through the purification transfer function of the first purification bed 2, so that the circulating operation of the system can be completed.
Preferably, the first concentration threshold is a determination concentration after the condensation recovery process is finished, the concentration range is 1 to 3 times of the saturated concentration of the VOCs at the condensation temperature, the second concentration threshold is a determination concentration after the nitrogen purification process is finished, and the concentration range is 0.1 to 1 time of the adsorption concentration.
Wherein, first concentration threshold value is through carrying out concentration value range to operating time, desorption degree and purification efficiency when selecting and select, and specific concentration selection range refers to following table 1:
| cold condensation spot | 0.5 times of | 1 times of | 2 times of | 3 times of | 4 times of |
| Run time | 9.33h | 5.47h | 3.20h | 2.40h | 1.98h |
| Degree of desorption | 95.20％ | 92.50％ | 86.27％ | 83.99％ | 68.35％ |
| Purification efficiency | 99.12％ | 97.80％ | 95.53％ | 92.21％ | 80.87％ |
TABLE 1
As can be seen from the above table, when the concentration of the first concentration threshold is lower than 1 time, the purification efficiency is not significantly improved, and the operation time is significantly increased, such a decrease in concentration of the condensation end point means an increase in operation energy consumption, and when the concentration of the selected condensation end point is higher than 3 times, the desorption degree is significantly decreased, and the purification efficiency is lower than 90% of the standard, so that the first concentration threshold is selected to be 1-3 times of the saturated concentration of the VOCs at the condensation temperature, and the setting of the second concentration threshold has higher requirements on the desorption degree and the purification efficiency, and for this reason, the second concentration threshold is selected to be 0.1-1 times of the saturated concentration of the VOCs at the condensation temperature.
Preferably, the first purification bed 2 and the second purification bed 3 have the same filling amount of the adsorbent, and the filling amount is calculated according to the adsorption isotherm at the desorption temperature and the condensation temperature and the saturation pressure curve of the VOCs, and the specific calculation method of the filling amount is shown in the following formula:
wherein Tde is a desorption temperature, tcd is a condensation temperature, ccd is a saturated condensation concentration, H is a design height of the purification bed, H is a height of a mass transfer zone, q is an adsorption capacity, the height of the mass transfer zone is set to be 0.1-0.3m, and the apparent wind speeds of the first purification bed 2 and the second purification bed 3 are set to be 0.05-0.6m/s.
The adsorbents arranged in the adsorption bed 1, the first purification bed 2 and the second purification bed 3 comprise active carbon, molecular sieves, resin, silica gel and the like.
When the device is used, firstly, the desorption bed 1 is regenerated by adopting hot nitrogen circulating desorption, high-concentration VOCs in desorption gas are condensed and recovered, and when the desorption concentration reaches a first concentration threshold value, non-condensable gas enters the first purification bed 2 through valve switching, residual VOCs are separated from nitrogen purge gas, so that the concentration of a desorption inlet of the desorption bed 1 is always kept zero, and the desorption bed 1 is ensured to be completely removed; after the desorption gas of the desorption bed 1 is purified for a plurality of times, when the first purification bed 2 is absorbed and penetrated or is close to penetrating, the second purification bed 3 alternately undertakes purification work through the combined switching of a plurality of groups of valves; then, carrying out hot nitrogen cyclic desorption on the first purification bed 2, simultaneously realizing condensation and recovery of high-concentration VOCs in the desorption gas, starting the nitrogen purification function of the second purification bed 3 through valve switching when the desorption concentration reaches a first concentration threshold value, realizing deep regeneration of the first purification bed 2, and ensuring that the outlet concentration is zero when the first purification bed 2 runs next round; the desorption process of the desorption bed 1 is repeated until the second purification bed 3 is absorbed and penetrated or is close to penetrating, and the first purification bed 2 alternately undertakes purification work through valve switching, so that one complete cycle between the first purification bed 2 and the second purification bed 3 is completed, and the organic waste gas treatment standard emission at high condensation temperature is realized.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (10)
1. The utility model provides an utilize VOCs recovery system of two bed purification purge gas, includes desorption bed (1), first purification bed (2), second purification bed (3) and desorption condensation auxiliary assembly, its characterized in that: desorption bed (1), first purification bed (2) and second purification bed (3) parallel connection, desorption condensation auxiliary assembly is including nitrogen gas source (8), VOCs condenser (4), vapour and liquid separator (5), desorption fan (6) and heater (7) that connect gradually, desorption bed (1), first purification bed (2) and second purification bed (3) all are linked together with desorption condensation auxiliary assembly, set up first valve (9) and second valve (10) around desorption bed (1) respectively, first purification bed (2) preceding rear end is provided with third valve (11), fourth valve (12), seventh valve (15) and eighth valve (16) respectively, second purification bed (3) front and back end is provided with fifth valve (13), sixth valve (14), ninth valve (17) and tenth valve (18) respectively, the fixed intercommunication in exit position of desorption fan (6) has three pipelines, and wherein two pipelines are fixed respectively communicate in first purification bed (2) and second purification bed (3) preceding both sides are provided with the purification bed (7) between the purification bed (7) each other pipeline is provided with the purification pipeline (20), another purification bed top is provided with the nitrogen gas source intercommunication.
2. A system for recovering VOCs using a dual bed purification purge gas as claimed in claim 1 wherein: the top and the bottom of the desorption bed (1) are respectively provided with a first connecting pipe (21) and a second connecting pipe (22) in a penetrating way, the top and the bottom of the first purifying bed (2) are respectively provided with a third connecting pipe (23) and a fourth connecting pipe (24) in a penetrating way, the top and the bottom of the second purifying bed (3) are respectively provided with a fifth connecting pipe (25) and a sixth connecting pipe (26) in a penetrating way, the bottoms of the second connecting pipe (22), the fourth connecting pipe (24) and the sixth connecting pipe (26) are fixedly communicated with an eighth connecting pipe (28), one end of the eighth connecting pipe (28) is fixedly communicated with a seventh connecting pipe (27), the seventh connecting pipe (27) is fixedly communicated with a nitrogen gas source (8), one end of the eighth connecting pipe (28) is fixedly communicated with the VOCs condenser (4), one end of the VOCs condenser (4) far away from the eighth connecting pipe (28) is sequentially and fixedly communicated with a gas-liquid separator (5) and a desorption fan (6), one end of the desorption fan (6) is fixedly communicated with a tenth connecting pipe (30), one end of the tenth connecting pipe (30) is fixedly communicated with a ninth connecting pipe (29), one end of the ninth connecting pipe (29) is fixedly communicated with a heater (7), and the top parts of the first connecting pipe (21), the third connecting pipe (23) and the fifth connecting pipe (25) are fixedly communicated with a ninth connecting pipe (29).
3. A system for recovery of VOCs using a dual bed purification purge gas as claimed in claim 2 wherein: an eleventh connecting pipe (31) is fixedly communicated with the top of the tenth connecting pipe (30), one end of the eleventh connecting pipe (31) is fixedly communicated with the sixth connecting pipe (26), a twelfth connecting pipe (32) is fixedly communicated with the fourth connecting pipe (24) and is fixedly communicated with the top of the eleventh connecting pipe (31), a thirteenth connecting pipe (33) is fixedly communicated with the top of the tenth connecting pipe (30) and one side of the eleventh connecting pipe (31), and a fourteenth connecting pipe (34) fixedly communicated with the fifth connecting pipe (25) and a fifteenth connecting pipe (35) fixedly communicated with the third connecting pipe (23) are fixedly communicated with one end of the thirteenth connecting pipe (33) through a tee joint.
4. A system for recovery of VOCs using a dual bed purification purge gas as claimed in claim 3 wherein: the surfaces of the first connecting pipe (21), the third connecting pipe (23) and the fifth connecting pipe (25) are respectively provided with a first valve (9), a third valve (11) and a fifth valve (13), the surfaces of the second connecting pipe (22), the fourth connecting pipe (24) and the sixth connecting pipe (26) are respectively provided with a second valve (10), a fourth valve (12) and a sixth valve (14), a nitrogen supplementing valve (20) is arranged between the nitrogen source (8) and the seventh connecting pipe (27), the surface of the tenth connecting pipe (30) is arranged between the eleventh connecting pipe (31) and the thirteenth connecting pipe (33) and is provided with an eleventh valve (19), the surface of the eleventh connecting pipe (31) is arranged between the eleventh connecting pipe (31) and the sixth connecting pipe (26) and is provided with a tenth valve (18), the surface of the twelfth connecting pipe (32) is provided with an eighth valve (16), one end of the twelfth connecting pipe (32) penetrates through and is mounted on the surface of the fourth connecting pipe (24), the mounting position is arranged between the first bed (2) and the fourth bed (12), and the surface of the fourteenth valve (17) is provided with a fifteenth valve (17), the fifteenth connecting pipe (35) is installed on the surface of the third connecting pipe (23) at a position between the first purification bed (2) and the third valve (11).
5. A VOCs recovery system using a dual bed purification purge gas as claimed in claim 4 wherein: the first purification bed (2) and the second purification bed (3) are arranged as low-temperature adsorption beds using the residual cold of condensation, and the first purification bed (2) and the second purification bed (3) have the same adsorbent filling amount, and the packing heights of the fillers inside the first purification bed (2) and the second purification bed (3) are the same.
6. A system for recovering VOCs using a dual bed purification purge gas as claimed in claim 4 wherein: the operation working condition of the desorption bed (1) is a closed desorption and cooling process; the operation conditions of the first purification bed (2) and the second purification bed (3) comprise nitrogen purification, closed desorption and cooling processes.
7. A system for recovering VOCs using a dual bed purification purge gas as claimed in claim 1 wherein: the desorption condensation auxiliary equipment adopts a natural cold source for treating the high-boiling-point VOCs, and adopts a refrigerating unit or liquid nitrogen for refrigerating for treating the low-boiling-point VOCs.
8. A VOCs recovery method using double-bed purification purge gas is characterized in that: the method comprises the following steps:
s1: closing all valves except the first valve (9), the second valve (10), the seventh valve (15), the eighth valve (16) and the eleventh valve (19), opening a nitrogen supplementing valve (20), connecting a nitrogen source into the nitrogen supplementing valve (20), replacing the gas in all pipelines and equipment of the whole system with nitrogen, and closing all valves and the nitrogen source when an online oxygen content detector shows that the oxygen content is lower than 5%;
s2: closing the seventh valve (15) and the eighth valve (16), and sequentially opening the desorption fan (6), the VOCs condenser (4), the gas-liquid separator (5) and the heater (7), and then condensing and recovering high-concentration VOCs in the desorption gas while beginning desorption of the desorption bed (1) until the desorption concentration reaches a first concentration threshold value;
s3: opening a seventh valve (15) and an eighth valve (16), closing an eleventh valve (19), introducing non-condensable gas at the outlet of the VOCs condenser (4) into the first purification bed (2) for nitrogen purification, heating the purified nitrogen again by a heater (7), and deeply desorbing the heated nitrogen by the desorption bed (1);
s4: when the concentration of the outlet of the VOCs condenser (4) is lower than a second concentration threshold value, the heater (7) is closed, and the desorption bed (1) is cooled;
s5: after the cooling process of the desorption bed (1) in the step S4 is finished, opening the eleventh valve (19), and closing the seventh valve (15), the eighth valve (16) and the desorption condensation auxiliary equipment, so that the desorption condensation recovery process of the desorption bed (1) can be finished;
s6: repeating the steps S1-S5 until the first purification bed (2) is penetrated by adsorption;
s7: closing all valves except a third valve (11), a fourth valve (12), a ninth valve (17), a tenth valve (18) and an eleventh valve (19), opening a nitrogen supplement valve (20), then opening a nitrogen source, replacing the gas in the system pipeline and the equipment with nitrogen, and closing all valves and the nitrogen source when the online oxygen content detector shows that the oxygen content is lower than 5%;
s8: closing the ninth valve (17) and the tenth valve (18), and sequentially opening the desorption fan (6), the VOCs condenser (4), the gas-liquid separator (5) and the heater (7), starting to desorb the first purification bed (2), and simultaneously condensing and recovering high-concentration VOCs in the desorption gas until the desorption concentration reaches a first concentration threshold value;
s9: a ninth valve (17) and a tenth valve (18), the eleventh valve (19) is closed, the noncondensable gas at the outlet of the VOCs condenser (4) is firstly introduced into the second purification bed (3) for nitrogen purification, the purified nitrogen is heated by the heater (7) again, and enters the first purification bed (2) for deep desorption;
s10: when the concentration of the outlet of the VOCs condenser (4) is lower than a second concentration threshold value, the heater (7) is closed, and the first purification bed (2) is cooled;
s11: after the cooling process of the first purification bed (2) in the S10 is finished, opening an eleventh valve (19), closing a ninth valve (17) and a tenth valve (18), and closing the rest of the desorption and condensation auxiliary equipment, so that the desorption and condensation recovery process of the first purification bed (2) can be finished;
s12: repeating the steps S1 to S5 until the second purification bed (3) is penetrated by adsorption;
s13: and (7) repeating the steps S7-S11, wherein the opening and closing states of corresponding valves of the first purification bed (2) and the second purification bed (3) are interchanged, and deep desorption, condensation and recovery of the second purification bed (3) are completed through the purification transfer function of the first purification bed (2), so that the cyclic operation of the system can be completed.
9. A method of recovering VOCs using a dual bed purification purge gas as claimed in claim 6 wherein: the first concentration threshold value is the judgment concentration after the condensation recovery process is finished, the concentration range is 1-3 times of the saturated concentration of the VOCs at the condensation temperature, the second concentration threshold value is the judgment concentration after the nitrogen purification process is finished, and the concentration range is 0.1-1 times of the adsorption concentration.
10. A method of recovering VOCs using a dual bed purification purge gas as claimed in claim 7 wherein: the first purification bed (2) and the second purification bed (3) have the same filling amount of the adsorbent, the filling amount needs to be calculated according to adsorption isotherms at the desorption temperature and the condensation temperature and saturation pressure curves of VOCs, and the specific calculation method of the filling amount is shown as the following formula:
wherein Tde is a desorption temperature, tcd is a condensation temperature, ccd is a saturated condensation concentration, H is a design height of the purification bed, H is a height of a mass transfer zone, q is an adsorption capacity, the height of the mass transfer zone is set to be 0.1-0.3m, and apparent wind speeds of the first purification bed (2) and the second purification bed (3) are set to be 0.05-0.6m/s.
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