CN111036040A - Condensation-adsorption integrated VOCs recycling system and recycling process - Google Patents
Condensation-adsorption integrated VOCs recycling system and recycling process Download PDFInfo
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- 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
- B01D53/14—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 absorption
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- 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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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- 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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- B01D53/14—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 absorption
- B01D53/1487—Removing organic compounds
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Abstract
The invention discloses a condensation-adsorption integrated VOCs (volatile organic compounds) recycling system and a recycling process, which comprises a water washing unit, a condensation recycling unit, an adsorption and desorption unit and a heat exchange unit connected with the condensation recycling unit or the adsorption and desorption unit; the water washing unit is arranged at an inlet of the mixed gas of the VOCs in the system; the condensation recovery unit comprises a primary cold box and a secondary cold box which are connected with each other and is used for recovering the cooled liquefied VOCs and conveying the unliquefied gaseous VOCs to the adsorption desorption unit; the adsorption and desorption unit comprises two adsorption and desorption towers and is used for enriching the VOCs which are not recovered by the adsorption and condensation recovery unit step by step and then desorbing and circularly conveying the adsorbed VOCs to the condensation recovery unit for recovery; the heat exchange unit comprises a second heat exchanger and a third heat exchanger. The invention adopts an adsorption method and a condensation method integrated process, can realize the advantage complementation of the adsorption method and the condensation method, and reduces or avoids the defects and potential safety hazard problems existing in the use process of a single method.
Description
Technical Field
The invention belongs to the field of VOCs recovery processing, and particularly relates to a condensation-adsorption integrated VOCs recycling system and a recycling process.
Background
The evaporation loss of crude oil and finished oil occurs in the whole storage and transportation process from an oil field to a refinery and then to a sales user, which not only causes huge economic loss, but also brings serious potential safety hazard and environmental hazard. Oil and gas belong to the typical Volatile Organic Compounds (VOCs), which are a category of atmospheric pollutants that countries have specifically focused on and monitored. From the viewpoint of technologies for controlling the discharge of VOCs, there are two types, one is a preventive measure mainly for preventing and suppressing the leakage of VOCs and even eliminating the discharge of VOCs, and the other is a controlled measure mainly for terminal treatment, and the first method is difficult to implement, so the second method is generally adopted. The second method is classified into two types, one of which is physically recovered by absorption, adsorption, condensation, and membrane, and the other of which is chemically recovered by plasma, photocatalysis, and combustion. At present, an absorption method, an adsorption method, a condensation method or a membrane method is generally adopted, each method has advantages and disadvantages, in actual operation, the single method is often not efficient, and good separation efficiency can be achieved only by combining multiple processes.
For the adsorption method, the adsorbent, which is generally in the form of particles or powder, is filled in an adsorption tower, generally needs to have larger adsorption capacity and adsorption capacity, and is generally recycled after desorption, that is, when the adsorbent is saturated or nearly saturated, desorption regeneration is performed, and the adsorption operation is switched to again after desorption. The most widely used active carbon is active carbon, but the active carbon has high adsorption heat and rapid temperature rise, thereby not only influencing the use performance, but also causing many potential safety hazards.
In practical application, the condensation method is generally indirect heat transfer and requires multi-stage refrigeration, so that a refrigeration process system is complex, and the investment and operation cost of the method are higher due to various requirements of practical application on the operation of the method.
For desorption, various desorption regeneration methods such as temperature-rising desorption, pressure-reducing desorption, displacement desorption and the like are commonly used at present, wherein the temperature-rising desorption and the pressure-reducing desorption are widely applied in industrial application. The superheated steam desorption method is one of temperature-rising desorption methods, is suitable for desorbing low-molecular hydrocarbons and aromatic organic compounds with low boiling points, but has weak desorption capacity for high-boiling-point substances and long desorption period. The method has the advantages of high and easily obtained vapor enthalpy of the heating medium and good economical efficiency, but the temperature and the pressure in the desorption tower need to be controlled well during desorption so as to prevent spontaneous combustion. In the practical application of enterprises, the in-situ adsorption and desorption can greatly reduce the operation cost, save resources, reduce pollution and greatly improve the operation safety factor of equipment.
Disclosure of Invention
Aiming at the problems, the invention provides a condensation-adsorption integrated VOCs recycling system and a recycling process.
The technical purpose is achieved, the technical effect is achieved, and the invention is realized through the following technical scheme:
the utility model provides a collection condensation-absorption's VOCs circulation recovery system which characterized in that: the device comprises a water washing unit, a condensation recovery unit, an adsorption and desorption unit and a heat exchange unit connected with the condensation recovery unit or the adsorption and desorption unit, wherein the water washing unit, the condensation recovery unit and the adsorption and desorption unit are sequentially arranged;
the water washing unit is arranged at an inlet of the mixed gas of the VOCs in the system and is used for removing ammonia in the mixed gas of the VOCs;
the condensation recovery unit comprises a primary cold box and a secondary cold box, wherein the primary cold box is refrigerated by a cold source, the secondary cold box is deeply refrigerated by a refrigerator, and the primary cold box and the secondary cold box are sequentially connected with each other and are used for outputting the cooled and liquefied VOCs to the VOCs recovery unit and conveying the unliquefied gaseous VOCs to the adsorption desorption unit through a circulating pipeline;
the adsorption and desorption unit comprises an adsorption and desorption tower A and an adsorption and desorption tower B and is used for enriching VOCs which are not recovered by the adsorption and condensation recovery unit and then desorbing the adsorbed VOCs and conveying the desorbed VOCs to the condensation recovery unit through a circulating pipeline for recovery;
the heat exchange unit comprises a second heat exchanger and a third heat exchanger; the second heat exchanger is arranged between the condensation recovery unit and the adsorption and desorption unit and is used for heat exchange between the non-liquefied gaseous VOCs output by the condensation recovery unit and the VOCs desorbed by the adsorption and desorption unit; the third heat exchanger is arranged between the second heat exchanger and the adsorption and desorption unit and is connected with a cold source.
As a further improvement of the invention, a gas outlet of the secondary cooling box is connected with a first adsorption pipeline, and a pipe layer passing through the second heat exchanger is connected with the adsorption and desorption tower A.
As a further improvement of the invention, the adsorption and desorption tower A is provided with a qualified gas discharge port, and qualified gas after adsorption treatment is discharged from the gas discharge port.
As a further improvement of the invention, the adsorption and desorption tower a further comprises a second adsorption pipeline connected with the adsorption and desorption tower B, the unqualified gas adsorbed by the adsorption and desorption tower a is connected to a gas inlet of the adsorption and desorption tower B through the second adsorption pipeline, and the adsorption and desorption tower B is provided with a qualified gas discharge port.
As a further improvement of the invention, when the gas treated by the adsorption and desorption tower B is unqualified, the gas is communicated with a first circulation pipeline, and the first circulation pipeline is connected to the shell inlet of the second heat exchanger and enters the gas inlet of the condensation and recovery unit through the second heat exchanger.
As a further improvement of the invention, the VOCs post-processing unit is connected with a first desorption pipeline after VOCs are recycled, the first desorption pipeline is connected with the inlets of the heat pipe layers of the adsorption and desorption tower A and the adsorption and desorption tower B through the outlet of the heat storage furnace, and the adsorption and desorption tower A and the adsorption and desorption tower B are thermally desorbed by heat generated by the heat storage furnace.
As a further improvement of the invention, the system also comprises a VOCs recovery processing unit, wherein the VOCs recovery processing unit recovers and processes VOCs liquid condensed and recovered by the heat exchange unit and the condensation recovery unit; still include the regenerator, the heat supply pipe of regenerator with the absorption desorption unit link to each other, the regenerator gets into the produced secondary VOCs of VOCs recovery processing unit and burns, the heat input of its production adsorbs in the desorption unit.
As a further improvement of the invention, the device also comprises a second desorption pipeline communicated with the shell layers of the adsorption and desorption tower A and the adsorption and desorption tower B, and the initial end of the second desorption pipeline is connected with a nitrogen purging device.
As a further improvement of the invention, a first heat exchanger is arranged between the water washing tower and the condensation recovery unit, and the first heat exchanger is connected with a cold source.
A VOCs recycling process integrating condensation and adsorption is characterized in that the VOCs recycling system is applied to sequentially carry out half-process operation and full-process operation to complete recycling;
the semi-flow operation is to close a first desorption pipeline and a second desorption pipeline of the adsorption and desorption unit and a VOCs post-treatment unit, and VOCs are circulated between an absorption tower A and an absorption tower B to adsorb and enrich adsorbate until the adsorbate is saturated;
the full-flow operation is used for communicating a first desorption pipeline and a second desorption pipeline of the adsorption and desorption unit and a VOCs post-processing unit, saturated adsorbates are desorbed by the first desorption pipeline and the second desorption pipeline of the adsorption and desorption unit, and the desorbed VOCs enter the condensation recovery unit and the adsorption and desorption unit again for cyclic recovery.
The invention has the beneficial effects that:
① the invention can remove ammonia and water from VOCs to prevent damage to absorption tower.
② the invention adopts the integration technology of adsorption method and condensation method, which can realize the complementary advantages of the adsorption method and the condensation method, and reduce or avoid the defects and potential safety hazard problems existing in the use process of a single method.
③ the invention adopts double condensation method to absorb in stages, which improves the condensation efficiency and reduces the energy consumption and the operation cost.
④ the invention adopts double adsorption towers to absorb VOCs step by step, thus fully and effectively utilizing the adsorbent and reducing resource waste.
⑤ the invention carries out heat storage combustion to the secondary VOCs generated by the processing unit after the VOCs are recovered, and desorbs the adsorption and desorption tower by recycling the generated heat, thereby not only solving the problem of difficult waste treatment of enterprises, but also recovering partial resources to be used as energy for continuous use, and playing the roles of protecting environment and reducing resource waste and economic loss.
⑥ the invention adopts normal temperature nitrogen to purge, which can completely exhaust the desorption gas, improve the desorption rate and prolong the service life of the equipment.
Drawings
FIG. 1 is a schematic structural diagram of an embodiment of the present invention;
wherein: 1-a water washing tower, 2-a primary cooling box, 3-a secondary cooling box, 401-an adsorption and desorption tower A, 402-an adsorption and desorption tower B, 501-a first adsorption pipeline, 502-a second adsorption pipeline, 503-a first circulation pipeline, 504-a first desorption pipeline, 505-a second circulation pipeline, 506-a second desorption pipeline, 601-a first heat exchanger, 602-a second heat exchanger, 603-a third heat exchanger, 7-a regenerator, 8-a vacuum pump and 9-a cold source.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is further described in detail with reference to the following embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
The following detailed description of the principles of the invention is provided in connection with the accompanying drawings.
As shown in the figure, the invention designs a condensation-adsorption-integrated VOCs recycling system, which is a VOCs recycling system integrating double condensation, double adsorption and desorption and comprises a water washing tower 1, a condensation recycling unit and an adsorption and desorption unit.
The water isThe washing tower 1 is provided with an inlet of the mixed gas of VOCs in the system; for removing a large amount of ammonia from the VOCs by water washing. In one embodiment of the present invention, the water washing tower 1 in the water washing device is vertical, has a height of 5m and a diameter of 1.5 m. The water storage tank is arranged below the water washing tower 1, the water washing tower 1 takes water through the water storage tank and the water replenishing port to spray, the water storage amount of the water storage tank is 0.5-5 tons, and the spraying amount is 12m3The amount of recovered ammonia was 75 kg/h. And a qualified gas discharge port is arranged at the top end of the water washing tower 1.
The condensation recovery unit comprises a first-stage cold box 3 and a second-stage cold box 4 which are connected with each other and are used for recovering the cooled liquefied VOCs and conveying the non-liquefied gaseous VOCs to the adsorption desorption unit. The primary cold box 320 adopts a refrigerant refrigeration cold box for primary condensation; the secondary cooling box 422 is a refrigeration cooling box of a variable frequency refrigeration compressor and is used for deep condensation.
The gas outlet of the secondary cooling box 4 is connected with the first adsorption pipeline 501, and the pipe layer passing through the second heat exchanger 602 is connected with the adsorption and desorption tower A401. .
The adsorption and desorption unit comprises an adsorption and desorption tower A401 and an adsorption and desorption tower B402 and is used for enriching VOCs which are not recovered by the adsorption and condensation recovery unit and desorbing the adsorbed VOCs to be conveyed to the condensation recovery unit through a circulating pipeline for recovery. The adsorption and desorption tower A401 or the adsorption and desorption tower B402 is provided with an access port connected with a plurality of pipelines, and the switching of adsorption and desorption can be carried out by switching the opening and closing and the direction of a valve arranged on the pipeline.
The specific connection mode is as follows:
the adsorption and desorption tower A401 is provided with a qualified gas discharge port, and qualified gas after adsorption treatment is discharged from the gas discharge port
The adsorption and desorption tower A401 comprises a second adsorption pipeline 502 connected with the adsorption and desorption tower B402, unqualified gas adsorbed and treated by the adsorption and desorption tower A401 passes through the second adsorption pipeline 502 and is connected to a gas inlet of the adsorption and desorption tower B402, and the adsorption and desorption tower B402 is provided with a qualified gas discharge port.
And thirdly, when the gas treated by the adsorption and desorption tower B402 is unqualified, communicating a first circulation pipeline 503, wherein the first circulation pipeline 503 is connected to the shell inlet of the second heat exchanger 602 and enters the gas inlet of the condensation recovery unit through the second heat exchanger 602.
In the embodiment of the invention, the adsorption and desorption tower is a vertical tower, the diameter of the tower is 1m, and the height of the tower is 3 m. And simultaneously, filling activated carbon in the tower as an adsorbent. The adsorption and desorption tower 5 is internally provided with a heating pipe for introducing high-temperature hot steam, and is used for carrying out high-temperature desorption on VOCs in the adsorbent after saturated adsorption. In the desorption process, the temperature of the high-temperature steam is controlled to be 120-150 ℃, the absolute pressure range is 0.5MPa, and the absolute pressure of the outlet gas is controlled to be 0.15 MPa.
The VOCs after analysis or cleaning enters the condensation recovery unit to be recovered again through the same outlet discharge arranged at the bottom end of the adsorption and desorption tower.
In order to improve the efficiency of condensation and recovery, a second heat exchanger 602 and a third heat exchanger 603 are also included; the second heat exchanger 602 is disposed between the condensation recovery unit and the adsorption desorption unit, and is used for heat exchange between the non-liquefied gaseous VOCs output by the condensation recovery unit and the VOCs desorbed by the adsorption desorption unit; the third heat exchanger 603 is arranged between the second heat exchanger 602 and the adsorption and desorption unit, and is connected with a cold source 9.
The secondary cooling box 3 further comprises a gas discharge pipe 401, the gas discharge pipe 401 is connected with a first inlet end of the second heat exchanger 602, and a first outlet end communicated with the first inlet end is connected with the adsorption and desorption tower 5. The second inlet end of the second heat exchanger 602 is connected to the outlet end of the third heat exchanger 603, and the second outlet end communicated with the second inlet end is connected to the first-stage cold box 2.
The system also comprises a first heat exchanger 601 arranged between the water washing tower 1 and the condensation recovery unit. The first heat exchanger 601 is a low-temperature heat exchanger and is used for drying the washed VOCs.
The first heat exchanger 601 or the third heat exchanger 603 of the primary cold box 3 comprises a pipeline for flowing in refrigerant, and the introduced VOCs exchange heat with the refrigerant in the pipeline. In the primary cold box 3, the first heat exchanger 601 and the third heat exchanger 60 adopt the same refrigerant and are connected by a cold carrying pipeline. The refrigerant enters each heat exchanger through the connected circulating pump to act, and then is discharged to be collected and recycled.
The refrigerant is provided by a cold source 9 filled with the refrigerant, and all the heat exchangers and the cold box are connected through cold carrying pipelines.
In the embodiment of the invention, DN15 is generally selected as the cold-carrying medium pipeline, the temperature of the cold-carrying medium is-25 ℃ to-10 ℃, and the flow of the cold-carrying medium is 3m3/h。
The invention also comprises a VOCs recovery processing unit, wherein the VOCs recovery processing unit recovers and processes VOCs liquid which is condensed and recovered by the heat exchange unit and the condensation recovery unit; still include regenerator 7, regenerator 7's heat supply pipe with adsorption desorption unit link to each other, regenerator 7 gets into the produced secondary waste gas of VOCs recovery processing unit and burns, and the heat input that its produced adsorbs in the desorption unit.
The top of the adsorption and desorption tower is also provided with a second desorption pipeline 506, the starting end of the second desorption pipeline 506 is connected with a nitrogen purging device, nitrogen is pressurized and then is purged into the tower through a cleaning gas inlet, VOCs in the tower is emptied, and meanwhile, activated carbon is cleaned.
The flow of gas or liquid in the present invention can be adjusted, and the desorption and adsorption process can be adjusted by controlling the opening of a valve disposed in the pipeline. Meanwhile, the system is also provided with a vacuum pump 8, and before the system is used for the first time, the desorption tower, the condensing device and the pipeline need to be vacuumized by the vacuum pump 8, so that the air tightness of the system is checked. In theory the vacuum pump 8 can be connected in any line of the system, but considering that the later purging of the adsorption and desorption column with nitrogen requires the adjustment of the pressure in the adsorption and desorption column, the vacuum pump 8 is preferably connected in the line close to the adsorption and desorption unit.
The foregoing shows and describes the general principles and broad features of the present invention and advantages thereof. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, which are described in the specification and illustrated only to illustrate the principle of the present invention, but that various changes and modifications may be made therein without departing from the spirit and scope of the present invention, which fall within the scope of the invention as claimed. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (10)
1. The utility model provides a collection condensation-absorption's VOCs circulation recovery system which characterized in that: the device comprises a water washing unit, a condensation recovery unit, an adsorption and desorption unit and a heat exchange unit connected with the condensation recovery unit or the adsorption and desorption unit, wherein the water washing unit, the condensation recovery unit and the adsorption and desorption unit are sequentially arranged;
the water washing unit is arranged at an inlet of the mixed gas of the VOCs in the system and is used for removing ammonia in the mixed gas of the VOCs;
the condensation recovery unit comprises a primary cold box (2) and a secondary cold box (3), wherein the primary cold box (2) is refrigerated by a cold source (9) and the secondary cold box (3) is deeply refrigerated by a refrigerator, which are sequentially connected with each other, and is used for outputting the cooled and liquefied VOCs to the VOCs recovery unit and conveying the unliquefied gaseous VOCs to the adsorption desorption unit through a circulating pipeline;
the adsorption and desorption unit comprises an adsorption and desorption tower A (401) and an adsorption and desorption tower B (402) and is used for enriching VOCs which are not recovered by the adsorption and condensation recovery unit and desorbing the adsorbed VOCs and conveying the desorbed VOCs to the condensation recovery unit through a circulating pipeline for recovery;
the heat exchange unit comprises a second heat exchanger (602) and a third heat exchanger (603); the second heat exchanger (602) is arranged between the condensation recovery unit and the adsorption desorption unit and is used for heat exchange between the non-liquefied gaseous VOCs output by the condensation recovery unit and the VOCs desorbed by the adsorption desorption unit; the third heat exchanger (603) is arranged between the second heat exchanger (602) and the adsorption and desorption unit and is connected with a cold source (9).
2. The recycling system of claim 1, wherein the recycling system comprises: and a gas outlet of the secondary cooling box (4) is connected with a first adsorption pipeline (501), and a pipe layer passing through a second heat exchanger (602) is connected with an adsorption and desorption tower A (401).
3. A recycling system for VOCs collected by condensation-adsorption as claimed in claim 1 or 2, wherein: the adsorption and desorption tower A (401) is provided with a qualified gas discharge port, and qualified gas after adsorption treatment is discharged from the gas discharge port.
4. A condensate-adsorption integrated VOCs recycling system according to claim 3, wherein: the adsorption and desorption tower A (401) further comprises a second adsorption pipeline (502) connected with the adsorption and desorption tower B (402), unqualified gas subjected to adsorption treatment of the adsorption and desorption tower A (401) is connected to a gas inlet of the adsorption and desorption tower B (402) through the second adsorption pipeline (502), and the adsorption and desorption tower B (402) is provided with a qualified gas discharge port.
5. The recycling system of claim 4, wherein the recycling system comprises: and when the gas treated by the adsorption and desorption tower B (402) is unqualified, the gas is communicated with a first circulating pipeline (503), and the first circulating pipeline (503) is connected to the shell layer inlet of the second heat exchanger (602) and enters the gas inlet of the condensation recovery unit through the second heat exchanger (602).
6. The recycling system of claim 1, wherein the recycling system comprises: VOCs aftertreatment unit connects first desorption pipeline (504) after carrying out VOCs recycle, first desorption pipeline (504) pass through regenerator (7) exit linkage adsorption and desorption tower A (401) and the heat pipe layer entry of adsorption and desorption tower B (402), the heat that utilizes the regenerator to produce is right adsorption and desorption tower A (401) and adsorption and desorption tower B (402) carry out thermal desorption.
7. The recycling system of claim 1, wherein the recycling system comprises: the VOCs recovery processing unit is used for recovering and processing VOCs liquid condensed and recovered by the heat exchange unit and the condensation recovery unit; still include regenerator (7), regenerator (7) the heat supply pipe with adsorption desorption unit link to each other, regenerator (7) get into the produced secondary VOCs of VOCs recovery processing unit and burn, in its heat input adsorption desorption unit that produces.
8. The recycling system of claim 1 or 7, wherein the recycling system comprises: the adsorption and desorption device further comprises a second desorption pipeline (506) communicated with the shell layers of the adsorption and desorption tower A (401) and the adsorption and desorption tower B (402), and the starting end of the second desorption pipeline (506) is connected with a nitrogen purging device.
9. The recycling system of claim 1, wherein the recycling system comprises: and the first heat exchanger (601) is arranged between the water washing tower (1) and the condensation recovery unit, and the first heat exchanger (601) is connected with a cold source (9).
10. A VOCs recycling technology integrating condensation-adsorption is characterized in that: the VOCs recovery system of any one of claims 1-9 is applied to sequentially perform half-process operation and full-process operation to complete recovery and recovery;
the semi-flow operation is to close a first desorption pipeline (504) and a second desorption pipeline (506) of the adsorption and desorption unit and a VOCs post-treatment unit, and VOCs circularly flow between an absorption tower A (401) and an absorption tower B (402) to adsorb and enrich adsorbate until the adsorbate is saturated;
the full-flow operation is used for communicating a first desorption pipeline (504) and a second desorption pipeline (506) of the adsorption and desorption unit and a VOCs post-processing unit, saturated adsorbates are desorbed by the first desorption pipeline (504) and the second desorption pipeline (506) of the adsorption and desorption unit, and the desorbed VOCs enter the condensation recovery unit and the adsorption and desorption unit again for cyclic recovery.
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| CN115089992A (en) * | 2022-07-07 | 2022-09-23 | 连云港市拓普科技发展有限公司 | Method for recycling VOCs (volatile organic compounds) gas through shallow cold adsorption desorption |
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