WO2021093262A1 - Vocs recovery system and method integrating absorption, desorption and recovery - Google Patents

Vocs recovery system and method integrating absorption, desorption and recovery Download PDF

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Publication number
WO2021093262A1
WO2021093262A1 PCT/CN2020/084401 CN2020084401W WO2021093262A1 WO 2021093262 A1 WO2021093262 A1 WO 2021093262A1 CN 2020084401 W CN2020084401 W CN 2020084401W WO 2021093262 A1 WO2021093262 A1 WO 2021093262A1
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absorption
vocs
unit
temperature
tower
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PCT/CN2020/084401
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French (fr)
Chinese (zh)
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黄维秋
王鑫雅
黄洲乐
浮历沛
孙宪航
曹学明
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常州大学
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Priority to JP2020564664A priority Critical patent/JP2022510051A/en
Publication of WO2021093262A1 publication Critical patent/WO2021093262A1/en

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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
    • B01D53/14—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
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • 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
    • B01D53/14—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
    • B01D53/1406—Multiple stage absorption
    • 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
    • B01D53/14—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
    • B01D53/1425—Regeneration of liquid absorbents
    • 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
    • B01D53/14—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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B01D2257/708—Volatile organic compounds V.O.C.'s
    • 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
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters

Definitions

  • the invention belongs to the field of VOCs recovery processing, and specifically relates to a VOCs recovery system and method integrating absorption, desorption and recovery.
  • VOCs volatile organic compounds
  • its molecular structure also contains oxygen, nitrogen, sulfur, and chlorine, and its emissions It has brought many serious hazards to the society and enterprises. For example, when a large amount of VOCs evaporate and discharge, they will not only easily cause fire and explosion and other hazards due to the high density of VOCs, but also irritate the human respiratory tract and cause cancer and other hazards. In addition, it It is also the main reactant produced by photochemical smog, causing serious harm to ecology and the environment. my country's oil resources are limited, and it is also a big oil consumer and importer, so VOCs need to be effectively recovered.
  • the current recovery methods mainly use a single recovery method, including adsorption, absorption, condensation and membrane methods.
  • the single use of these methods will cause a series of problems and low recovery efficiency.
  • the absorption method has high requirements on the performance of the absorbent, the consumption of the absorbent is large, and the equipment occupies a large space, resulting in a low process recovery rate;
  • the adsorption method often selects adsorbents with relatively good adsorption performance and moderate prices, such as Activated carbon, but the adsorption heat of activated carbon is high, and the adsorption temperature rises rapidly, which reduces the adsorption performance and service life, and also increases safety hazards such as fire and explosion.
  • the condensation method requires high temperature and needs to condense the gas at a very low temperature. In order to achieve the ideal condensation effect, it has high requirements for materials and processes, and relatively high recovery and operating costs; membrane oil and gas recovery is a modern oil and gas separation technology that emerged in the late last century, and separation is achieved through different molecular sizes. It has a small footprint, safe operation and easy maintenance, but it usually needs to be combined with other processes to achieve good separation efficiency.
  • the technical problem to be solved by the present invention is: how to further improve the absorption efficiency of the VOCs recovery treatment system, and reduce energy consumption and operating costs.
  • a VOCs recovery system integrating absorption, desorption and recovery, including
  • Washing unit connected to the self-coupling pre-cooling unit, used to wash the VOCs intake air;
  • Self-coupling pre-cooling unit connected to the low-temperature absorption unit, used to condense the VOCs gas after washing;
  • Low-temperature absorption unit connected to the high-temperature desorption unit through the second heat exchanger 20, used to absorb the condensed VOCs gas;
  • High temperature desorption unit connected to the low temperature recovery unit through the heat exchanger 324, used to desorb the VOCs gas after low temperature absorption;
  • Low-temperature recovery unit connected to the low-temperature absorption unit, used to recover the liquefied VOCs, and at the same time, retransmit the unliquefied VOCs to the low-temperature absorption unit for processing.
  • the washing unit includes a washing tower 3, the washing tower is a segmented spray tower, including two layers of trays and two spray heads, the two spray heads are the washing tower, the first spray head 501 and the washing
  • the second-level spray head 502 of the tower, the first-level spray head 501 of the water washing tower and the second-level spray head 502 of the water washing tower are supplied by the first-level circulating spray pump 601 of the water washing tower and the second-level circulating spray pump 602 of the water washing tower respectively.
  • the layer tray is provided with a number of overflow small pipes 4. Realize the full water washing of more than 80% of the VOCs gas entering the water washing tower.
  • the self-coupling pre-cooling unit adopts an internal self-coupling one-to-two defrosting system; it includes a two-stage condensing device A 9, a two-stage condensing device B 10, and a first-stage condensing device 7.
  • the two-stage condensing device A, the two-stage condensing device B There are two connection modes between the condensing device B and the first condensing device: the first condensing circuit 2801 and the second condensing circuit 2802:
  • connection mode of the first condensing circuit is as follows: the inlet end of the secondary condensing device B is connected to the outlet end of the washing tower of the water washing unit; the outlet end of the secondary condensing device B is connected to the inlet end of the primary condensing device; the primary condensing device The outlet end of is connected to the inlet end of the secondary condensing device A; the outlet end of the secondary condensing device A is connected to the low-temperature absorption unit;
  • connection mode of the second condensing circuit is as follows: the inlet end of the second condensing device A is connected to the outlet end of the washing tower of the water washing unit; the outlet end of the second condensing device A is connected to the inlet end of the first condensing device; the first condensing device The outlet end of is connected to the inlet end of the secondary condensing device B; the outlet end of the secondary condensing device B is connected to the low-temperature absorption unit.
  • the primary condensing device, secondary condensing device A, and secondary condensing device B of the self-coupling pre-cooling unit are all connected to the liquid separation tank 11, the liquid separation tank 1 is divided by density, the middle is the buffer zone, and the left side is the organic matter Zone, the right side is the condensate zone.
  • the first condensing device is primary condensing
  • the second condensing device A and the second condensing device B are deep condensing.
  • the VOCs gas is deep condensed first, then the primary condensing, to avoid the frosting of the primary condensing device, and then through a deep condensing, the second
  • the two deep condensed gas outlet ends are the outlet ends of the self-coupling pre-cooling unit, and are connected to the inlet end of the low-temperature absorption unit.
  • the first condensing circuit When the secondary condensing device B is frosted and needs to be defrosted, the first condensing circuit is operated, and the VOCs gas is condensed through the secondary condensing device B, the primary condensing device and the secondary condensing device A in turn; when the secondary condensing device A is frosted When defrosting is required, the second condensing circuit is operated, and the VOCs gas is first condensed by the second condensing device A, and then condensed by the first condensing device and the second condensing device B in turn.
  • the low-temperature absorption unit includes an absorption tower 13.
  • the absorption tower is a segmented spray tower, including two layers of trays and two spray heads.
  • the gas inlet end of the absorption tower is set above the first layer of the absorption tower.
  • the second-layer tray of the absorption tower is provided with a number of overflow small pipes 14 for the transmission of VOCs gas and the overflow transmission of the second-layer absorption liquid.
  • the VOCs gas passes through the first layer of the absorption tower.
  • the spray head 1501 After the spray head 1501 is sprayed, it enters the second layer of the absorption tower from the overflow pipe 2 and is sprayed by the second layer spray head 1502 of the absorption tower to achieve full absorption of VOCs; the top of the absorption tower is also equipped with qualified Gas discharge port.
  • the cryogenic absorption unit includes a first self-circulating absorption liquid circuit 2803 and a second self-circulating absorption liquid circuit 2804:
  • the first self-circulating absorption liquid circuit the absorption liquid outlet of the first layer of the absorption tower is connected to the first-level spray head of the absorption tower through the first-stage circulating spray pump 1601 of the absorption tower to realize the spraying of VOCs gas;
  • the second self-circulating absorption liquid circuit the second-layer absorption liquid outlet of the absorption tower is connected to the second-layer spray head of the absorption tower through the absorption tower second-level circulating spray pump 1602 to realize further spraying of VOCs gas.
  • the high-temperature desorption unit includes a desorption tower 21, and the connection between the desorption tower and the absorption tower in the low-temperature absorption unit includes:
  • the first desorption circuit 2805 the absorption liquid outlet at the bottom of the absorption tower in the low-temperature absorption unit is connected to the absorption liquid inlet above the upper body of the desorption tower in the high-temperature desorption unit through the tube layer of the second heat exchanger;
  • the second desorption circuit 2806 the absorption liquid outlet under the bottom of the desorption tower in the high temperature desorption unit is connected to the inlet of the second self-circulating absorption liquid circuit in the low temperature absorption unit through the shell of the second heat exchanger;
  • the absorption liquid in the first self-circulating absorption liquid circuit, the second self-circulating absorption liquid circuit, the first desorption circuit and the second desorption circuit of the absorption tower and the absorption liquid in the absorption tower and the desorption tower constitute a flow balance.
  • the desorption tower in the high temperature desorption unit is connected to the absorption tower in the low temperature absorption unit through a recovery loop 2807.
  • the recovery loop is: the top outlet of the desorption tower is connected to the recovery horizontal tank 18 through the heat exchanger three and the vacuum pump 25 in turn, The top outlet of the recovery tank is connected to the inlet of the absorption tower.
  • the outlet end of the heat source 23 of the desorption tower in the high temperature desorption unit is connected to a steam trap 22.
  • the recovery horizontal tank of the low-temperature recovery unit is connected to the second liquid separation tank 19, the second liquid separation tank is divided by density, the middle is the buffer zone, the left side is the organic matter area, and the right side is the condensate water area.
  • the inlet end of the water washing unit is connected to the VOCs on-site gas through the flame arrestor 1; any unit and any pipeline are equipped with a gate valve 2 or an automatic control valve 8 or a ball valve 12 and a flow meter.
  • VOCs gas exchanges heat through the cold source 27 and the heat source to realize waste cooling recovery and condensation or vaporization of VOCs.
  • a heat exchanger 17 is provided between the absorption tower of the low-temperature absorption unit and the safety discharge port; the first heat exchanger uses the low-temperature gas discharged from the absorption tower of the low-temperature absorption unit for waste cooling recovery, and the self-coupling pre-cooling unit The latter cold source is supplemented with cold capacity;
  • a second heat exchanger is arranged between the absorption tower of the low-temperature absorption unit and the high-temperature desorption unit; the second heat exchanger utilizes the low-temperature absorption liquid discharged from the low-temperature absorption unit and the high-temperature absorption liquid desorbed from the high-temperature desorption unit for mutual heat recovery.
  • the primary condensing unit, secondary condensing unit A, secondary condensing unit B, heat exchanger 1, the internal heat exchanger in the absorption tower, and the internal heat exchanger in the recovery tank are all connected to the cold source through the recovery pump to desorb
  • the internal heat exchanger in the tower is connected with the heat source; the third heat exchanger is a circulating water heat exchanger.
  • a VOCs recovery method using a VOCs recovery processing system includes the following steps:
  • VOCs on-site air flow passes through the flame arrestor and the washing unit to remove ammonia, and then enters the self-coupling pre-cooling unit;
  • the low-temperature absorption unit runs the first self-circulating absorption liquid circuit and the second self-circulating absorption liquid circuit for absorption.
  • the first layer of rich absorption liquid of the absorption tower passes through the tube layer of heat exchanger 2 during the process of passing through the first desorption circuit. After the cold energy is recovered, it enters the desorption tower in the high temperature desorption unit for desorption; the desorbed fresh absorption liquid passes through the second desorption loop and passes through the shell of the heat exchanger 2 for heat recovery, and then the second layer of the absorption tower is lean Priority replenishment of absorbent;
  • the desorbed VOCs gas enters the recovery horizontal tank through the recovery loop to be condensed and liquefied for recovery, and the unliquefied VOCs gas is re-transmitted to the low-temperature absorption unit for absorption.
  • the present invention adopts the VOCs recovery method of water washing + self-coupling pre-cooling + low temperature absorption + high temperature desorption + low temperature recovery, and the advantages of multiple methods are combined and the disadvantages complement each other, which not only saves energy, but also realizes the recycling of absorption liquid, which greatly reduces Energy costs.
  • the present invention adopts a segmented washing tower and a segmented absorption tower to fully wash and absorb VOCs respectively.
  • Several overflow small pipes arranged on the two-layer tray realize the upward transmission of VOCs and the downward overflow transmission of liquid. Coupled with the self-circulating spray on the two layers of the tower, it not only improves the absorption efficiency and the use efficiency of the absorption liquid, but also reduces energy consumption and operating costs.
  • the invention adopts an internal self-coupling defrosting system, the three condensing devices are set up as one support and two types, and the internal circulating pipeline units are alternately operated according to the defrosting requirements, that is, two deep condensing devices are alternately used, which not only improves the pre-cooling efficiency It also uses the heat of the VOCs itself to alternately defrost the deep condensing device, which greatly saves energy consumption and avoids waste of energy consumption.
  • the first heat exchanger and the second heat exchanger in the present invention respectively recover the low-temperature gas and the low-temperature liquid of the absorption tower, thereby improving the heat utilization efficiency and reducing the energy consumption.
  • the self-coupling pre-cooling unit and the low-temperature recovery unit in the present invention are respectively provided with a liquid separation tank divided by density, the middle is a buffer zone, the left side is the organic matter area, and the right side is the condensate water area, which greatly improves the VOCs recovery rate and Use safety.
  • Figure 1 is a schematic diagram of the structural connection of a device according to an embodiment of the present invention.
  • 1-flame arrester 2-gate valve, 3-washing tower, 4-overflow small pipe one, 501-sprinkler head on the first floor of washing tower, 502-sprinkler head on the second stage of washing tower, and 601-first circulation of washing tower Spray pump, 602-water scrubber two-stage circulating spray pump, 7-stage condensing device, 8-automatic control valve, 9-stage condensing device A, 10-stage condensing device B, 11-separating tank 1 , 12-ball valve, 13-absorption tower, 14-overflow small pipe two, 1501- absorption tower first-level spray head, 1502- absorption tower second-level spray head, 1601- absorption tower first-level circulating spray pump, 1602- Absorption tower two-stage circulating spray pump, 17-heat exchanger one, 18-recovery horizontal tank, 19-separating tank two, 20-heat exchanger two, 21-desorption tower, 22-trap, 23-heat source, 24-heat exchanger three, 25-vacuum pump, 26-
  • FIG. 2 is a detailed structural connection diagram of a self-coupling pre-cooling unit in a device according to an embodiment of the present invention
  • Figure 3 is a schematic cross-sectional view of the overflow small pipe of the two-layer tray of the washing tower or the absorption tower in an embodiment of the present invention
  • Fig. 4 is a schematic diagram of the process of VOCs in an embodiment of the present invention passing through the overflow small pipe of the two-layer tray of the water washing tower or the absorption tower;
  • Figure 5 is a partial schematic diagram of the process of VOCs in an embodiment of the present invention passing through the two-layer tray overflow small pipe of the absorption tower;
  • a VOCs processing system of the present invention as shown in Figure 1, including
  • Washing unit connected to the self-coupling pre-cooling unit, used to wash the VOCs intake air;
  • Self-coupling pre-cooling unit connected to the low-temperature absorption unit, used to condense the VOCs gas after washing;
  • Low-temperature absorption unit connected to the high-temperature desorption unit through the second heat exchanger 20, used to absorb the condensed VOCs gas;
  • High temperature desorption unit connected to the low temperature recovery unit through the heat exchanger 324, used to desorb the VOCs gas after low temperature absorption;
  • Low-temperature recovery unit connected to the low-temperature absorption unit, used to recover the liquefied VOCs, and at the same time, re-send the non-liquefied VOCs to the low-temperature absorption unit for processing.
  • the washing unit as shown in Figures 3 and 4 includes a washing tower 3.
  • the washing tower is a segmented spray tower and includes two layers of trays and two spray heads.
  • the two spray heads are one layer of the washing tower.
  • the spray head 501 and the second-level spray head 502 of the washing tower, the first-level spray head 501 of the water-washing tower and the second-level spray head 502 of the water-washing tower are respectively sprayed by the first-level circulating spray pump 601 of the water-washing tower and the second-level circulating spray of the water-washing tower.
  • the pump 602 supplies water, and the second layer of tray is provided with a number of overflow small pipes 4. Realize the full water washing of more than 80% of the VOCs gas entering the water washing tower.
  • the self-coupling pre-cooling unit as shown in Figure 2 adopts an internal self-coupling one-to-two defrosting system; it includes a secondary condensing device A 9, a secondary condensing device B 10, and a primary condensing device 7.
  • the secondary condensing device A There are two connection modes between the second condensing device B and the first condensing device: the first condensing circuit 2801 and the second condensing circuit 2802:
  • connection mode of the first condensing circuit is as follows: the inlet end of the secondary condensing device B is connected to the outlet end of the washing tower of the water washing unit; the outlet end of the secondary condensing device B is connected to the inlet end of the primary condensing device; the primary condensing device The outlet end of is connected to the inlet end of the secondary condensing device A; the outlet end of the secondary condensing device A is connected to the low-temperature absorption unit;
  • connection mode of the second condensing circuit is as follows: the inlet end of the second condensing device A is connected to the outlet end of the washing tower of the water washing unit; the outlet end of the second condensing device A is connected to the inlet end of the first condensing device; the first condensing device The outlet end of is connected to the inlet end of the secondary condensing device B; the outlet end of the secondary condensing device B is connected to the low-temperature absorption unit.
  • the primary condensing device, secondary condensing device A, and secondary condensing device B of the self-coupling pre-cooling unit are all connected to the liquid separation tank 11, the liquid separation tank 1 is divided by density, the middle is the buffer zone, and the left side is the organic matter Zone, the right side is the condensate zone.
  • the first condensing device is primary condensing
  • the second condensing device A and the second condensing device B are deep condensing.
  • the VOCs gas is deep condensed first, then the primary condensing, to avoid the frosting of the primary condensing device, and then through a deep condensing, the second
  • the two deep condensed gas outlet ends are the outlet ends of the self-coupling pre-cooling unit, and are connected to the inlet end of the low-temperature absorption unit.
  • the first condensing circuit When the secondary condensing device B is frosted and needs to be defrosted, the first condensing circuit is operated, and the VOCs gas is condensed through the secondary condensing device B, the primary condensing device and the secondary condensing device A in turn; when the secondary condensing device A is frosted When defrosting is required, the second condensing circuit is operated, and the VOCs gas is first condensed by the second condensing device A, and then condensed by the first condensing device and the second condensing device B in turn.
  • the low-temperature absorption unit as shown in Figures 3, 4, and 5 includes an absorption tower 13, which is a segmented spray tower and includes two trays and two spray heads.
  • the gas inlet of the absorption tower is set at The first layer of the absorption tower is higher than the upper level of the absorption liquid.
  • the second layer of the absorption tower is provided with a number of overflow small pipes 14 for the transmission of VOCs gas and the overflow transmission of the second layer of absorption liquid.
  • the VOCs gas After being sprayed by the spray nozzle 1501 on the first layer of the absorption tower, the VOCs gas enters the second layer of the absorption tower from the second overflow pipe, and then sprayed by the spray nozzle 1502 on the second layer of the absorption tower to realize the full absorption of VOCs.
  • the top of the absorption tower is also equipped with a qualified gas discharge port.
  • the cryogenic absorption unit includes a first self-circulating absorption liquid circuit 2803 and a second self-circulating absorption liquid circuit 2804:
  • the first self-circulating absorption liquid circuit the absorption liquid outlet of the first layer of the absorption tower is connected to the first-level spray head of the absorption tower through the first-stage circulating spray pump 1601 of the absorption tower to realize the spraying of VOCs gas;
  • the second self-circulating absorption liquid circuit the second-layer absorption liquid outlet of the absorption tower is connected to the second-layer spray head of the absorption tower through the absorption tower second-level circulating spray pump 1602 to realize further spraying of VOCs gas.
  • the high-temperature desorption unit includes a desorption tower 21, and the connection between the desorption tower and the absorption tower in the low-temperature absorption unit includes:
  • the first desorption circuit 2805 the absorption liquid outlet at the bottom of the absorption tower in the low-temperature absorption unit is connected to the absorption liquid inlet on the upper body of the desorption tower in the high-temperature desorption unit through the tube layer of the second heat exchanger;
  • the second desorption circuit 2806 the absorption liquid outlet under the bottom of the desorption tower in the high temperature desorption unit is connected to the inlet of the second self-circulating absorption liquid circuit in the low temperature absorption unit through the shell of the second heat exchanger;
  • the absorption liquid in the first self-circulating absorption liquid circuit, the second self-circulating absorption liquid circuit, the first desorption circuit and the second desorption circuit of the absorption tower and the absorption liquid in the absorption tower and the desorption tower constitute a flow balance.
  • the desorption tower in the high temperature desorption unit is connected to the absorption tower in the low temperature absorption unit through a recovery loop 2807.
  • the recovery loop is: the top outlet of the desorption tower is connected to the recovery horizontal tank 18 through the heat exchanger three and the vacuum pump 25 in turn, The top outlet of the recovery tank is connected to the inlet of the absorption tower.
  • the recovery horizontal tank of the low-temperature recovery unit is connected to the second liquid separation tank 19, the second liquid separation tank is divided by density, the middle is the buffer zone, the left side is the organic matter area, and the right side is the condensate water area.
  • the inlet end of the water washing unit is connected to the VOCs on-site gas through the flame arrestor 1; any unit and any pipeline are equipped with gate valves 2 or automatic control valves 8 or ball valves 12 and flow meters; the heat source of the desorption tower in the high temperature desorption unit 23 is connected to a steam trap 22 at the outlet end.
  • VOCs gas exchanges heat through the cold source 27 and the heat source to realize waste cooling recovery and condensation or vaporization of VOCs.
  • a VOCs recovery method integrating absorption, desorption and recovery includes the following steps:
  • VOCs on-site air flow passes through the flame arrestor and the washing unit to remove ammonia, and then enters the self-coupling pre-cooling unit;
  • the low-temperature absorption unit runs the first self-circulating absorption liquid circuit and the second self-circulating absorption liquid circuit for absorption.
  • the first layer of rich absorption liquid of the absorption tower passes through the tube layer of heat exchanger 2 during the process of passing through the first desorption circuit. After the cold energy is recovered, it enters the desorption tower in the high temperature desorption unit for desorption; the desorbed fresh absorption liquid passes through the second desorption loop and passes through the shell of the heat exchanger 2 for heat recovery, and then the second layer of the absorption tower is lean Priority replenishment of absorbent;
  • the desorbed VOCs gas enters the recovery horizontal tank through the recovery loop to be condensed and liquefied for recovery, and the unliquefied VOCs gas is re-transmitted to the low-temperature absorption unit for absorption.
  • the VOCs gas enters the secondary condensing unit B, and then passes through the primary condensing unit 7 and the secondary condensing unit A to condense and remove water from the VOCs, and then the uncondensed VOCs gas enters the low-temperature absorption unit Absorption tower.
  • the VOCs gas is first sprayed and absorbed in the first layer of the absorption tower. At this time, a large amount of VOCs is absorbed by the absorption liquid; the remaining VOCs gas enters the second layer of the absorption tower through the overflow tube 2 for fresh absorption liquid spraying. The water is absorbed deeply, and the qualified gas is discharged from the safety discharge port through the heat exchanger.
  • step 3 in addition to spraying the second-layer absorption liquid of the absorption tower, when the liquid level exceeds the second overflow port of the overflow small pipe, the absorption liquid overflows into the first-layer rich absorption liquid of the absorption tower.
  • the high-temperature VOCs gas is recovered from the top outlet of the desorption tower 21 through the recovery loop, that is, the circulating water is initially cooled through the heat exchanger three, and then enters the low-temperature recovery tank through the vacuum pump 25 to make the gaseous state VOCs are liquefied, the liquefied VOCs are recovered, and the unliquefied VOCs are re-entered into the absorption tower to continue processing.
  • the heat exchange equipment includes:
  • the heat exchanger 17 arranged between the low-temperature absorption unit and the safety discharge port is connected to the cold source through the recovery pump 26. In order to recover the residual cold of the discharged low-temperature gas, it supplements the cold source cold from the self-coupling pre-cooling unit. the amount;
  • the second heat exchanger is arranged between the absorption tower of the low-temperature absorption unit and the high-temperature desorption unit; one end of any heat exchange pipeline in the second heat exchanger is connected to the low-temperature absorption unit, and the other end is connected to the low-temperature absorption unit.
  • the high temperature desorption unit is connected.
  • the second heat exchanger utilizes the low-temperature absorption liquid discharged from the low-temperature absorption unit and the high-temperature absorption liquid desorbed by the high-temperature desorption unit to mutually recover heat;
  • Heat exchanger three arranged between the high-temperature desorption unit and the low-temperature recovery unit;
  • the third heat exchanger is a circulating water heat exchanger, in order to prevent high-temperature VOCs from damaging the vacuum pump.
  • the low-temperature VOCs cooled by the heat exchanger 3 are transported to the recovery horizontal tank by the vacuum pump and then further condensed, and the VOCs converted into liquid are stored in the liquid separation tank 2 of the low-temperature recovery unit;
  • the primary condensing device, secondary condensing device A, and secondary condensing device B arranged in the self-coupling pre-cooling unit; the primary condensing device, secondary condensing device A, and secondary condensing device B pass through the recovery pump Connected to the cold source;
  • It also includes internal heat exchangers built into the absorption tower, desorption tower, and recovery tank, and heat exchange circulation pipelines in the heat exchange unit.
  • the internal heat exchangers in the absorption tower and the recovery tank are connected to the cooling system through the recovery pump.
  • the source is connected, and the internal heat exchanger in the desorption tower is connected with the heat source.
  • the cold source is a refrigerant
  • the heat source is water vapor with a temperature higher than 100°C.
  • the VOCs recovery system specifically includes:
  • Gate valve water washing tower, first-level spray head of water washing tower, second-level spray head of water washing tower, water storage tank, first-level circulating spray pump of water washing tower and second-level circulating spray pump of water washing tower constitute a water washing unit, which passes through the flame arrester.
  • VOCs need to go through a water washing device, the purpose is to remove ammonia and wash away a large amount of water-soluble impurities through water washing.
  • the washing tower is vertical, with a height of 3m ⁇ 15m and a diameter of 0.5m ⁇ 3m.
  • the washing tower is designed as a segmented spray type.
  • the two-layer tray is equipped with a number of overflow small pipes.
  • the diameter of the overflow pipes is The height is 5mm ⁇ 10mm, and the total cross-sectional area is 5% ⁇ 15% of the cross-sectional area of the tray.
  • the first floor of the washing tower is equipped with a water storage tank with a water storage capacity of 0.5 to 10 tons, and the spraying capacity is 5m 3 /h ⁇ 50m 3 /h
  • the second-layer water source of the washing tower is supplied through the water replenishment port
  • the replenishing water volume is 1m 3 /h ⁇ 5m 3 /h
  • the spraying volume is 5m 3 /h ⁇ 50m 3 /h
  • the water washing tower recovers the amount of ammonia (water) It is 5kg/h ⁇ 100kg/h.
  • the top of the absorption tower is equipped with a VOCs outlet, and there is a VOCs inlet below the tower body and above the highest liquid level of the absorption liquid.
  • the gas enters from below and contacts the sprayed absorption liquid in a reverse direction to achieve full absorption.
  • the absorption tower is also designed as a segmented spray type.
  • the two-layer tray is equipped with a number of overflow small pipes.
  • the diameter of the overflow small pipes is The height is 5mm ⁇ 10mm, and the total cross-sectional area is 5% ⁇ 15% of the cross-sectional area of the tray; the diameter of the tower body is generally determined according to the amount of oil and gas processed, and the height of the tower body is generally 3m ⁇ 15m, and the diameter is 0.5m ⁇ 3m.
  • the storage height is 0.3m ⁇ 4m
  • the design operating temperature of the tower is -25°C ⁇ -5°C
  • the flow rate of the cold source in the internal heat exchanger is 0.5m 3 /h 2 ⁇ 3m 3 /h 2
  • the amount of spraying on the first layer is equal to
  • the spray rate of the second layer is 5m 3 /h ⁇ 50m 3 /h.
  • the desorption tower uses high temperature steam as the heat medium.
  • the diameter of the tower is 0.1m ⁇ 3m, the height is 0.5m ⁇ 5m, the high temperature steam temperature is 120°C ⁇ 150°C, the steam consumption is 1kg/h ⁇ 5kg/h, and the desorption capacity is 0.5kg/h ⁇ 50kg/h.
  • the recovery horizontal tank has a diameter of 0.2m-3m, a length of 0.5m-5m, and a recovered liquid volume of 0.5kg/h-50kg/h.
  • the circulating water temperature in the heat exchanger three is 10°C ⁇ 100°C, and the flow rate is 0.01m 3 /h ⁇ 2m 3 /h.
  • the refrigerant pipeline connected to the cold source is generally DN10 ⁇ DN20, the temperature of the refrigerant is -25°C ⁇ -10°C, and the flow of the refrigerant is 1m 3 /h ⁇ 20m 3 /h .

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Abstract

Disclosed are a VOCs recovery system and method integrating absorption, desorption and recovery. The recovery system comprises a washing unit, which is connected to a self-coupling pre-cooling unit and is used for washing VOCs inlet gas; the self-coupling pre-cooling unit, which is connected to a low-temperature absorption unit and is used for condensing the washed VOCs gas; the low-temperature absorption unit, which is connected to a high-temperature desorption unit by means of a heat exchanger II (20) and is used for absorbing the condensed VOCs gas; the high-temperature desorption unit, which is connected to a low-temperature recovery unit by means of a heat exchanger III (24) and is used for desorbing the VOCs gas subjected to low-temperature absorption; and the low-temperature recovery unit, which is connected to the low-temperature absorption unit and is used for recovering liquefied VOCs and conveying un-liquefied VOCs to the low-temperature absorption unit again for treatment. Not only is a high amount of energy saved, the cyclic utilization of absorption liquid is also realized.

Description

一种集吸收、解吸和回收为一体VOCs回收系统及方法VOCs recovery system and method integrating absorption, desorption and recovery 技术领域Technical field
本发明属于VOCs回收处理领域，具体涉及一种集吸收、解吸和回收为一体VOCs回收系统及方法。The invention belongs to the field of VOCs recovery processing, and specifically relates to a VOCs recovery system and method integrating absorption, desorption and recovery.
背景技术Background technique
在各种工业生产及有关过程中，常常会出现一种挥发性有机物，即VOCs(volatile organic compounds)，其分子结构除碳和氢以外，还包含有氧、氮、硫、氯，它的排放给社会和企业带来了许多严重危害，如大量的VOCs蒸发排放时，因密度大漂浮聚集在地表空间，不仅很容易引起火灾爆炸等危险，还会刺激人体呼吸道，造成致癌等危险，另外它还是光化学烟雾产生的主要反应物，对生态和环境造成严重危害。我国石油资源有限，又是石油消费和进口大国，故需对VOCs进行有效回收。当前回收方法主要采用单一的回收方法，包括吸附法、吸收法、冷凝法和膜法，但在实际操作中，这几种方法单一使用会产生一系列问题，回收效率低。例如吸收法对吸收剂的性能要求高，吸收剂消耗量大，其设备占地空间大，导致工艺回收率低；吸附法在实际应用中常选用吸附性能相对较好且价格适中的吸附剂，如活性炭，但活性炭吸附热较高，吸附温度上升迅速，导致吸附性能和使用寿命降低，而且还会增加火灾爆炸等安全性隐患；冷凝法对温度要求高，需要在极低的温度下对气体冷凝才能达到理想的冷凝效果，故其对材质和工艺有较高的要求，而且回收和运行成本相对较高；膜法油气回收是上世纪后期崛起的现代油气分离技术，通过分子大小不同实现分离，其占地面积小，运行安全，维护容易，但通常需要与其他工艺相结合才能达到好的分离效率。In various industrial production and related processes, a kind of volatile organic compounds, namely VOCs (volatile organic compounds), is often present. In addition to carbon and hydrogen, its molecular structure also contains oxygen, nitrogen, sulfur, and chlorine, and its emissions It has brought many serious hazards to the society and enterprises. For example, when a large amount of VOCs evaporate and discharge, they will not only easily cause fire and explosion and other hazards due to the high density of VOCs, but also irritate the human respiratory tract and cause cancer and other hazards. In addition, it It is also the main reactant produced by photochemical smog, causing serious harm to ecology and the environment. my country's oil resources are limited, and it is also a big oil consumer and importer, so VOCs need to be effectively recovered. The current recovery methods mainly use a single recovery method, including adsorption, absorption, condensation and membrane methods. However, in actual operation, the single use of these methods will cause a series of problems and low recovery efficiency. For example, the absorption method has high requirements on the performance of the absorbent, the consumption of the absorbent is large, and the equipment occupies a large space, resulting in a low process recovery rate; in the actual application, the adsorption method often selects adsorbents with relatively good adsorption performance and moderate prices, such as Activated carbon, but the adsorption heat of activated carbon is high, and the adsorption temperature rises rapidly, which reduces the adsorption performance and service life, and also increases safety hazards such as fire and explosion. The condensation method requires high temperature and needs to condense the gas at a very low temperature. In order to achieve the ideal condensation effect, it has high requirements for materials and processes, and relatively high recovery and operating costs; membrane oil and gas recovery is a modern oil and gas separation technology that emerged in the late last century, and separation is achieved through different molecular sizes. It has a small footprint, safe operation and easy maintenance, but it usually needs to be combined with other processes to achieve good separation efficiency.
发明内容Summary of the invention
本发明所要解决的技术问题是：如何进一步提高VOCs回收处理系统的吸收效率，降低能耗和运行成本。The technical problem to be solved by the present invention is: how to further improve the absorption efficiency of the VOCs recovery treatment system, and reduce energy consumption and operating costs.
为解决上述技术问题，本发明通过以下技术方案实现：In order to solve the above technical problems, the present invention is implemented through the following technical solutions:
一种集吸收、解吸和回收为一体VOCs回收系统，包括A VOCs recovery system integrating absorption, desorption and recovery, including
水洗单元：与自耦合预冷单元连接，用于对VOCs进气进行水洗；Washing unit: connected to the self-coupling pre-cooling unit, used to wash the VOCs intake air;
自耦合预冷单元：连接至低温吸收单元，用于对水洗后的VOCs气体进行冷凝；Self-coupling pre-cooling unit: connected to the low-temperature absorption unit, used to condense the VOCs gas after washing;
低温吸收单元：通过换热器二20连接至高温解吸单元，用于对冷凝后的VOCs气体进行吸收；Low-temperature absorption unit: connected to the high-temperature desorption unit through the second heat exchanger 20, used to absorb the condensed VOCs gas;
高温解吸单元：通过换热器三24连接至低温回收单元，用于对低温吸收后的VOCs气体进行解吸；High temperature desorption unit: connected to the low temperature recovery unit through the heat exchanger 324, used to desorb the VOCs gas after low temperature absorption;
低温回收单元：连接至低温吸收单元，用于回收液化后的VOCs，同时将未液化的VOCs重新输送至低温吸收单元处理。Low-temperature recovery unit: connected to the low-temperature absorption unit, used to recover the liquefied VOCs, and at the same time, retransmit the unliquefied VOCs to the low-temperature absorption unit for processing.
所述水洗单元包括水洗塔3，所述水洗塔为分段式喷淋塔，包括两层塔板和两个喷淋头，两个喷淋头分别为水洗塔一层喷淋头501和水洗塔二层喷淋头502，水洗塔一层喷淋头501和水洗塔二层喷淋头502分别由水洗塔一级循环喷淋泵601、水洗塔二级循环喷淋泵602供水，第二层塔板设有若干溢流小管一4。实现对进入水洗塔的80％以上的VOCs气体进行充分水洗。The washing unit includes a washing tower 3, the washing tower is a segmented spray tower, including two layers of trays and two spray heads, the two spray heads are the washing tower, the first spray head 501 and the washing The second-level spray head 502 of the tower, the first-level spray head 501 of the water washing tower and the second-level spray head 502 of the water washing tower are supplied by the first-level circulating spray pump 601 of the water washing tower and the second-level circulating spray pump 602 of the water washing tower respectively. The layer tray is provided with a number of overflow small pipes 4. Realize the full water washing of more than 80% of the VOCs gas entering the water washing tower.
所述自耦合预冷单元采用内部自耦合一托二式除霜系统；包括二级冷凝装置A 9、二级冷凝装置B 10和一级冷凝装置7，所述二级冷凝装置A、二级冷凝装置B和一级冷凝装置之间有第一冷凝回路2801和第二冷凝回路2802两种连接方式：The self-coupling pre-cooling unit adopts an internal self-coupling one-to-two defrosting system; it includes a two-stage condensing device A 9, a two-stage condensing device B 10, and a first-stage condensing device 7. The two-stage condensing device A, the two-stage condensing device B There are two connection modes between the condensing device B and the first condensing device: the first condensing circuit 2801 and the second condensing circuit 2802:
所述第一冷凝回路的连接方式为：二级冷凝装置B的进口端连接水洗单元的水洗塔的出口端；二级冷凝装置B的出口端连接一级冷凝装置的进口端；一级冷凝装置的出口端连接二级冷凝装置A的进口端；二级冷凝装置A的出口端连接至低温吸收单元；The connection mode of the first condensing circuit is as follows: the inlet end of the secondary condensing device B is connected to the outlet end of the washing tower of the water washing unit; the outlet end of the secondary condensing device B is connected to the inlet end of the primary condensing device; the primary condensing device The outlet end of is connected to the inlet end of the secondary condensing device A; the outlet end of the secondary condensing device A is connected to the low-temperature absorption unit;
所述第二冷凝回路的连接方式为：二级冷凝装置A的进口端连接水洗单元的水洗塔的出口端；二级冷凝装置A的出口端连接一级冷凝装置的进口端；一级冷凝装置的出口端连接二级冷凝装置B的进口端；二级冷凝装置B的出口端连接至低温吸收单元。The connection mode of the second condensing circuit is as follows: the inlet end of the second condensing device A is connected to the outlet end of the washing tower of the water washing unit; the outlet end of the second condensing device A is connected to the inlet end of the first condensing device; the first condensing device The outlet end of is connected to the inlet end of the secondary condensing device B; the outlet end of the secondary condensing device B is connected to the low-temperature absorption unit.
所述自耦合预冷单元的一级冷凝装置、二级冷凝装置A、二级冷凝装置B均与分液罐一11连接，分液罐一由密度分流，中间为缓冲区，左侧为有机物区，右侧为冷凝水区。The primary condensing device, secondary condensing device A, and secondary condensing device B of the self-coupling pre-cooling unit are all connected to the liquid separation tank 11, the liquid separation tank 1 is divided by density, the middle is the buffer zone, and the left side is the organic matter Zone, the right side is the condensate zone.
一级冷凝装置为初级冷凝，二级冷凝装置A和二级冷凝装置B为深度冷凝，VOCs气体先经过深度冷凝，再经初级冷凝，避免初级冷凝装置结霜，再经一个深度冷凝，第二个深度冷凝气体出口端即为自耦合预冷单元的出口端，与所述低温吸收单元入口端相连。The first condensing device is primary condensing, the second condensing device A and the second condensing device B are deep condensing. The VOCs gas is deep condensed first, then the primary condensing, to avoid the frosting of the primary condensing device, and then through a deep condensing, the second The two deep condensed gas outlet ends are the outlet ends of the self-coupling pre-cooling unit, and are connected to the inlet end of the low-temperature absorption unit.
当二级冷凝装置B结霜需要除霜时，运行第一冷凝回路，VOCs气体依次通过二级冷凝装置B、一级冷凝装置和二级冷凝装置A进行冷凝；当二级冷凝装置A结霜需要除霜时，运行第二冷凝回路，VOCs气体首先通过二级冷凝装置A进行冷凝，再依次通过一级冷凝装置和二级冷凝装置B进行冷凝。When the secondary condensing device B is frosted and needs to be defrosted, the first condensing circuit is operated, and the VOCs gas is condensed through the secondary condensing device B, the primary condensing device and the secondary condensing device A in turn; when the secondary condensing device A is frosted When defrosting is required, the second condensing circuit is operated, and the VOCs gas is first condensed by the second condensing device A, and then condensed by the first condensing device and the second condensing device B in turn.
所述低温吸收单元包括吸收塔13，所述吸收塔为分段式喷淋塔，包括两层塔板和两个喷淋头，吸收塔的气体入口端设置在吸收塔的第一层高于吸收液液面上方处，所述吸收塔的第二层塔板设有若干溢流小管二14，用于VOCs气体的传送和第二层吸收液的溢流传送，VOCs气体经吸收塔一层喷淋头1501喷淋后，由溢流小管二进入吸收塔第二层，再经吸收塔二层喷淋头1502喷淋，实现VOCs气体的充分吸收；所述吸收塔塔顶还设有合格气体排放口。The low-temperature absorption unit includes an absorption tower 13. The absorption tower is a segmented spray tower, including two layers of trays and two spray heads. The gas inlet end of the absorption tower is set above the first layer of the absorption tower. Above the liquid level of the absorption liquid, the second-layer tray of the absorption tower is provided with a number of overflow small pipes 14 for the transmission of VOCs gas and the overflow transmission of the second-layer absorption liquid. The VOCs gas passes through the first layer of the absorption tower. After the spray head 1501 is sprayed, it enters the second layer of the absorption tower from the overflow pipe 2 and is sprayed by the second layer spray head 1502 of the absorption tower to achieve full absorption of VOCs; the top of the absorption tower is also equipped with qualified Gas discharge port.
低温吸收单元包括第一自循环吸收液回路2803和第二自循环吸收液回路2804：The cryogenic absorption unit includes a first self-circulating absorption liquid circuit 2803 and a second self-circulating absorption liquid circuit 2804:
第一自循环吸收液回路：吸收塔一层吸收液出口经吸收塔一级循环喷淋泵1601连接至吸收塔一层喷淋头，实现对VOCs气体的喷淋；The first self-circulating absorption liquid circuit: the absorption liquid outlet of the first layer of the absorption tower is connected to the first-level spray head of the absorption tower through the first-stage circulating spray pump 1601 of the absorption tower to realize the spraying of VOCs gas;
第二自循环吸收液回路：吸收塔二层吸收液出口经吸收塔二级循环喷淋泵1602连接至吸收塔二层喷淋头，实现对VOCs气体的进一步喷淋。The second self-circulating absorption liquid circuit: the second-layer absorption liquid outlet of the absorption tower is connected to the second-layer spray head of the absorption tower through the absorption tower second-level circulating spray pump 1602 to realize further spraying of VOCs gas.
所述高温解吸单元包括解吸塔21，所述解吸塔与所述低温吸收单元中的吸收塔之间的连接方式包括：The high-temperature desorption unit includes a desorption tower 21, and the connection between the desorption tower and the absorption tower in the low-temperature absorption unit includes:
第一解吸回路2805：低温吸收单元中的吸收塔塔底吸收液出口，经过换热器 二的管层连接至高温解吸单元中的解吸塔塔身上方的吸收液进口端；The first desorption circuit 2805: the absorption liquid outlet at the bottom of the absorption tower in the low-temperature absorption unit is connected to the absorption liquid inlet above the upper body of the desorption tower in the high-temperature desorption unit through the tube layer of the second heat exchanger;
第二解吸回路2806：高温解吸单元中的解吸塔塔底下方吸收液出口，经过换热器二的壳层连接至低温吸收单元中的第二自循环吸收液回路的入口；The second desorption circuit 2806: the absorption liquid outlet under the bottom of the desorption tower in the high temperature desorption unit is connected to the inlet of the second self-circulating absorption liquid circuit in the low temperature absorption unit through the shell of the second heat exchanger;
吸收塔的第一自循环吸收液回路、第二自循环吸收液回路、第一解吸回路和第二解吸回路内的吸收液及吸收塔和解吸塔内的吸收液构成流量平衡。The absorption liquid in the first self-circulating absorption liquid circuit, the second self-circulating absorption liquid circuit, the first desorption circuit and the second desorption circuit of the absorption tower and the absorption liquid in the absorption tower and the desorption tower constitute a flow balance.
所述高温解吸单元中的解吸塔通过回收回路2807连接至低温吸收单元中的吸收塔，所述回收回路为：解吸塔的顶端出口依次经过换热器三、真空泵25连接至回收卧罐18，回收卧罐的顶端出口连接至吸收塔的入口端。The desorption tower in the high temperature desorption unit is connected to the absorption tower in the low temperature absorption unit through a recovery loop 2807. The recovery loop is: the top outlet of the desorption tower is connected to the recovery horizontal tank 18 through the heat exchanger three and the vacuum pump 25 in turn, The top outlet of the recovery tank is connected to the inlet of the absorption tower.
所述高温解吸单元中的解吸塔的热源23出口端连接一疏水器22。The outlet end of the heat source 23 of the desorption tower in the high temperature desorption unit is connected to a steam trap 22.
所述低温回收单元的回收卧罐与分液罐二19连接，分液罐二由密度分流，中间为缓冲区，左侧为有机物区，右侧为冷凝水区。The recovery horizontal tank of the low-temperature recovery unit is connected to the second liquid separation tank 19, the second liquid separation tank is divided by density, the middle is the buffer zone, the left side is the organic matter area, and the right side is the condensate water area.
水洗单元入口端通过阻火器1连接VOCs现场来气；任一单元和任一管路均设有闸阀2或自动控制阀8或球阀12和流量计。The inlet end of the water washing unit is connected to the VOCs on-site gas through the flame arrestor 1; any unit and any pipeline are equipped with a gate valve 2 or an automatic control valve 8 or a ball valve 12 and a flow meter.
VOCs气体通过冷源27和热源进行热量交换，实现余冷回收和VOCs的冷凝或汽化。The VOCs gas exchanges heat through the cold source 27 and the heat source to realize waste cooling recovery and condensation or vaporization of VOCs.
在低温吸收单元的吸收塔与安全排放口之间设置有换热器一17；所述换热器一利用低温吸收单元的吸收塔排放出的低温气体进行余冷回收，对自耦合预冷单元后的冷源进行冷量补充；A heat exchanger 17 is provided between the absorption tower of the low-temperature absorption unit and the safety discharge port; the first heat exchanger uses the low-temperature gas discharged from the absorption tower of the low-temperature absorption unit for waste cooling recovery, and the self-coupling pre-cooling unit The latter cold source is supplemented with cold capacity;
低温吸收单元的吸收塔与高温解吸单元之间设置有换热器二；所述换热器二利用低温吸收单元排出的低温吸收液与高温解吸单元解吸出的高温吸收液互相进行热量回收。A second heat exchanger is arranged between the absorption tower of the low-temperature absorption unit and the high-temperature desorption unit; the second heat exchanger utilizes the low-temperature absorption liquid discharged from the low-temperature absorption unit and the high-temperature absorption liquid desorbed from the high-temperature desorption unit for mutual heat recovery.
一级冷凝装置、二级冷凝装置A、二级冷凝装置B、换热器一、吸收塔中的内置换热器、回收卧罐中的内置换热器均通过回收泵与冷源相连，解吸塔中的内置换热器与热源相连；所述换热器三为循环水换热器。The primary condensing unit, secondary condensing unit A, secondary condensing unit B, heat exchanger 1, the internal heat exchanger in the absorption tower, and the internal heat exchanger in the recovery tank are all connected to the cold source through the recovery pump to desorb The internal heat exchanger in the tower is connected with the heat source; the third heat exchanger is a circulating water heat exchanger.
一种利用VOCs回收处理系统的VOCs回收方法，包括以下步骤：A VOCs recovery method using a VOCs recovery processing system includes the following steps:
1)VOCs现场来气依次经过阻火器、水洗单元除氨后,进入自耦合预冷单元；1) The VOCs on-site air flow passes through the flame arrestor and the washing unit to remove ammonia, and then enters the self-coupling pre-cooling unit;
2)自耦合预冷单元对VOCs气体进行脱水处理后，进入低温吸收单元；2) After the self-coupling pre-cooling unit dehydrates the VOCs gas, it enters the low-temperature absorption unit;
3)低温吸收单元运行第一自循环吸收液回路和第二自循环吸收液回路进行吸收，吸收塔的第一层富级吸收液通过第一解吸回路过程中，经过换热器二的管层进行冷量回收后，进入高温解吸单元中的解吸塔进行解吸；解吸出来的新鲜吸收液通过第二解吸回路经过换热器二的壳层进行热量回收后，对吸收塔的第二层贫级吸收液优先补充；3) The low-temperature absorption unit runs the first self-circulating absorption liquid circuit and the second self-circulating absorption liquid circuit for absorption. The first layer of rich absorption liquid of the absorption tower passes through the tube layer of heat exchanger 2 during the process of passing through the first desorption circuit. After the cold energy is recovered, it enters the desorption tower in the high temperature desorption unit for desorption; the desorbed fresh absorption liquid passes through the second desorption loop and passes through the shell of the heat exchanger 2 for heat recovery, and then the second layer of the absorption tower is lean Priority replenishment of absorbent;
4)解吸出来的VOCs气体通过回收回路进入回收卧罐中冷凝液化回收，未液化的VOCs气体重新输送至低温吸收单元中吸收。4) The desorbed VOCs gas enters the recovery horizontal tank through the recovery loop to be condensed and liquefied for recovery, and the unliquefied VOCs gas is re-transmitted to the low-temperature absorption unit for absorption.
本发明所达的有益效果：The beneficial effects achieved by the present invention:
本发明采用水洗+自耦合预冷+低温吸收+高温解吸+低温回收于一体的VOCs回收方法，利用多方法优势结合和劣势互补，不仅高度节能，还实现了吸收液的循环利用，大大减少了能耗成本。The present invention adopts the VOCs recovery method of water washing + self-coupling pre-cooling + low temperature absorption + high temperature desorption + low temperature recovery, and the advantages of multiple methods are combined and the disadvantages complement each other, which not only saves energy, but also realizes the recycling of absorption liquid, which greatly reduces Energy costs.
本发明采用分段式水洗塔和分段式吸收塔分别对VOCs进行充分水洗和吸收，二层塔板设置的若干溢流小管实现对VOCs的向上传送和对液体的向下溢流传送，再加上塔两层的自我循环喷淋，不仅提高了吸收效率、吸收液的使用效率，还降低能耗和运行成本。The present invention adopts a segmented washing tower and a segmented absorption tower to fully wash and absorb VOCs respectively. Several overflow small pipes arranged on the two-layer tray realize the upward transmission of VOCs and the downward overflow transmission of liquid. Coupled with the self-circulating spray on the two layers of the tower, it not only improves the absorption efficiency and the use efficiency of the absorption liquid, but also reduces energy consumption and operating costs.
本发明采用内部自耦合除霜系统，三台冷凝装置设置为一托二式，内部的循环管路单元根据除霜所需交替运行，即两台深度冷凝装置交替使用，不仅提高了预冷效率，还利用VOCs本身的热量交替对深度冷凝装置进行除霜，大大节约了能耗使用和避免了能耗浪费。The invention adopts an internal self-coupling defrosting system, the three condensing devices are set up as one support and two types, and the internal circulating pipeline units are alternately operated according to the defrosting requirements, that is, two deep condensing devices are alternately used, which not only improves the pre-cooling efficiency It also uses the heat of the VOCs itself to alternately defrost the deep condensing device, which greatly saves energy consumption and avoids waste of energy consumption.
本发明中的换热器一和换热器二分别对吸收塔的低温气体和低温液体进行余冷回收，提高了热量的利用效率，减少了能耗使用。The first heat exchanger and the second heat exchanger in the present invention respectively recover the low-temperature gas and the low-temperature liquid of the absorption tower, thereby improving the heat utilization efficiency and reducing the energy consumption.
本发明中的自耦合预冷单元和低温回收单元均分别设有由密度分流的分液罐，中间为缓冲区，左侧为有机物区，右侧为冷凝水区，大大提高了VOCs回收率和使用安全性。The self-coupling pre-cooling unit and the low-temperature recovery unit in the present invention are respectively provided with a liquid separation tank divided by density, the middle is a buffer zone, the left side is the organic matter area, and the right side is the condensate water area, which greatly improves the VOCs recovery rate and Use safety.
附图说明Description of the drawings
图1为本发明一种实施例装置的结构连接示意图；Figure 1 is a schematic diagram of the structural connection of a device according to an embodiment of the present invention;
其中：1-阻火器，2-闸阀，3-水洗塔，4-溢流小管一，501-水洗塔一层喷淋头，502-水洗塔二层喷淋头，601-水洗塔一级循环喷淋泵，602-水洗塔二级循环喷淋泵，7-一级冷凝装置，8-自动控制阀，9-二级冷凝装置A，10-二级冷凝装置B，11-分液罐一，12-球阀，13-吸收塔，14-溢流小管二，1501-吸收塔一层喷淋头，1502-吸收塔二层喷淋头，1601-吸收塔一级循环喷淋泵，1602-吸收塔二级循环喷淋泵，17-换热器一，18-回收卧罐，19-分液罐二，20-换热器二，21-解吸塔，22-疏水器，23-热源，24-换热器三，25-真空泵，26-回收泵，27-冷源，2801-第一冷凝回路，2802-第二冷凝回路，2803-第一自循环吸收液回路，2804-第二自循环吸收液回路，2805-第一解吸回路，2806-第二解吸回路，2807-回收回路。Among them: 1-flame arrester, 2-gate valve, 3-washing tower, 4-overflow small pipe one, 501-sprinkler head on the first floor of washing tower, 502-sprinkler head on the second stage of washing tower, and 601-first circulation of washing tower Spray pump, 602-water scrubber two-stage circulating spray pump, 7-stage condensing device, 8-automatic control valve, 9-stage condensing device A, 10-stage condensing device B, 11-separating tank 1 , 12-ball valve, 13-absorption tower, 14-overflow small pipe two, 1501- absorption tower first-level spray head, 1502- absorption tower second-level spray head, 1601- absorption tower first-level circulating spray pump, 1602- Absorption tower two-stage circulating spray pump, 17-heat exchanger one, 18-recovery horizontal tank, 19-separating tank two, 20-heat exchanger two, 21-desorption tower, 22-trap, 23-heat source, 24-heat exchanger three, 25-vacuum pump, 26-recovery pump, 27-cold source, 2801-first condensing circuit, 2802-second condensing circuit, 2803-first self-circulating absorption liquid circuit, 2804-second self Circulating absorption liquid loop, 2805-first desorption loop, 2806-second desorption loop, 2807-recovery loop.
图2为本发明一种实施例装置中的自耦合预冷单元详细结构连接示意图；2 is a detailed structural connection diagram of a self-coupling pre-cooling unit in a device according to an embodiment of the present invention;
图3为本发明一种实施例装置中的水洗塔或吸收塔二层塔板的溢流小管横截面示意图；Figure 3 is a schematic cross-sectional view of the overflow small pipe of the two-layer tray of the washing tower or the absorption tower in an embodiment of the present invention;
图4为本发明一种实施例装置中的VOCs经过水洗塔或吸收塔二层塔板的溢流小管过程示意图；Fig. 4 is a schematic diagram of the process of VOCs in an embodiment of the present invention passing through the overflow small pipe of the two-layer tray of the water washing tower or the absorption tower;
图5为本发明一种实施例装置中的VOCs经过吸收塔二层塔板溢流小管过程局部示意图；Figure 5 is a partial schematic diagram of the process of VOCs in an embodiment of the present invention passing through the two-layer tray overflow small pipe of the absorption tower;
具体实施方式Detailed ways
为了使本发明的目的、技术方案及优点更加清楚明白，以下结合实施例，对本发明进行进一步详细说明。应当理解，此处所描述的具体实施例仅仅用以解释本发明，并不用于限定本发明。In order to make the objectives, technical solutions, and advantages of the present invention clearer, the following further describes the present invention in detail with reference to embodiments. It should be understood that the specific embodiments described here are only used to explain the present invention, but not to limit the present invention.
下面结合附图对本发明的应用原理作详细的描述。The application principle of the present invention will be described in detail below in conjunction with the accompanying drawings.
如图1所述的本发明的一种VOCs处理系统，包括A VOCs processing system of the present invention as shown in Figure 1, including
水洗单元：与自耦合预冷单元连接，用于对VOCs进气进行水洗；Washing unit: connected to the self-coupling pre-cooling unit, used to wash the VOCs intake air;
自耦合预冷单元：连接至低温吸收单元，用于对进行水洗后的VOCs气体进行冷凝；Self-coupling pre-cooling unit: connected to the low-temperature absorption unit, used to condense the VOCs gas after washing;
低温吸收单元：通过换热器二20连接至高温解吸单元，用于对冷凝后的VOCs气体进行吸收；Low-temperature absorption unit: connected to the high-temperature desorption unit through the second heat exchanger 20, used to absorb the condensed VOCs gas;
高温解吸单元：通过换热器三24连接至低温回收单元，用于对低温吸收后的VOCs气体进行解吸；High temperature desorption unit: connected to the low temperature recovery unit through the heat exchanger 324, used to desorb the VOCs gas after low temperature absorption;
低温回收单元：连接至低温吸收单元，用于回收液化后的VOCs，同时将未液化的VOCs则重新送至低温吸收单元处理。Low-temperature recovery unit: connected to the low-temperature absorption unit, used to recover the liquefied VOCs, and at the same time, re-send the non-liquefied VOCs to the low-temperature absorption unit for processing.
如图3、4所述的水洗单元包括水洗塔3，所述水洗塔为分段式喷淋塔，包括两层塔板和两个喷淋头，两个喷淋头分别为水洗塔一层喷淋头501和水洗塔二层喷淋头502，水洗塔一层喷淋头501和水洗塔二层喷淋头502分别由水洗塔一级循环喷淋泵601、水洗塔二级循环喷淋泵602供水，第二层塔板设有若干溢流小管一4。实现对进入水洗塔的80％以上的VOCs气体进行充分水洗。The washing unit as shown in Figures 3 and 4 includes a washing tower 3. The washing tower is a segmented spray tower and includes two layers of trays and two spray heads. The two spray heads are one layer of the washing tower. The spray head 501 and the second-level spray head 502 of the washing tower, the first-level spray head 501 of the water-washing tower and the second-level spray head 502 of the water-washing tower are respectively sprayed by the first-level circulating spray pump 601 of the water-washing tower and the second-level circulating spray of the water-washing tower. The pump 602 supplies water, and the second layer of tray is provided with a number of overflow small pipes 4. Realize the full water washing of more than 80% of the VOCs gas entering the water washing tower.
如图2所述的自耦合预冷单元采用内部自耦合一托二式除霜系统；包括二级冷凝装置A 9、二级冷凝装置B 10和一级冷凝装置7，所述二级冷凝装置A、二级冷凝装置B和一级冷凝装置之间有第一冷凝回路2801和第二冷凝回路2802两种连接方式：The self-coupling pre-cooling unit as shown in Figure 2 adopts an internal self-coupling one-to-two defrosting system; it includes a secondary condensing device A 9, a secondary condensing device B 10, and a primary condensing device 7. The secondary condensing device A. There are two connection modes between the second condensing device B and the first condensing device: the first condensing circuit 2801 and the second condensing circuit 2802:
所述第一冷凝回路的连接方式为：二级冷凝装置B的进口端连接水洗单元的水洗塔的出口端；二级冷凝装置B的出口端连接一级冷凝装置的进口端；一级冷凝装置的出口端连接二级冷凝装置A的进口端；二级冷凝装置A的出口端连接至低温吸收单元；The connection mode of the first condensing circuit is as follows: the inlet end of the secondary condensing device B is connected to the outlet end of the washing tower of the water washing unit; the outlet end of the secondary condensing device B is connected to the inlet end of the primary condensing device; the primary condensing device The outlet end of is connected to the inlet end of the secondary condensing device A; the outlet end of the secondary condensing device A is connected to the low-temperature absorption unit;
所述第二冷凝回路的连接方式为：二级冷凝装置A的进口端连接水洗单元的水洗塔的出口端；二级冷凝装置A的出口端连接一级冷凝装置的进口端；一级冷凝装置的出口端连接二级冷凝装置B的进口端；二级冷凝装置B的出口端连接至低温吸收单元。The connection mode of the second condensing circuit is as follows: the inlet end of the second condensing device A is connected to the outlet end of the washing tower of the water washing unit; the outlet end of the second condensing device A is connected to the inlet end of the first condensing device; the first condensing device The outlet end of is connected to the inlet end of the secondary condensing device B; the outlet end of the secondary condensing device B is connected to the low-temperature absorption unit.
所述自耦合预冷单元的一级冷凝装置、二级冷凝装置A、二级冷凝装置B均与分液罐一11连接，分液罐一由密度分流，中间为缓冲区，左侧为有机物区，右侧为冷凝水区。The primary condensing device, secondary condensing device A, and secondary condensing device B of the self-coupling pre-cooling unit are all connected to the liquid separation tank 11, the liquid separation tank 1 is divided by density, the middle is the buffer zone, and the left side is the organic matter Zone, the right side is the condensate zone.
一级冷凝装置为初级冷凝，二级冷凝装置A和二级冷凝装置B为深度冷凝，VOCs气体先经过深度冷凝，再经初级冷凝，避免初级冷凝装置结霜，再经一个深度冷凝，第二个深度冷凝气体出口端即为自耦合预冷单元的出口端，与所述低温吸收单元入口端相连。The first condensing device is primary condensing, the second condensing device A and the second condensing device B are deep condensing. The VOCs gas is deep condensed first, then the primary condensing, to avoid the frosting of the primary condensing device, and then through a deep condensing, the second The two deep condensed gas outlet ends are the outlet ends of the self-coupling pre-cooling unit, and are connected to the inlet end of the low-temperature absorption unit.
当二级冷凝装置B结霜需要除霜时，运行第一冷凝回路，VOCs气体依次通过二级冷凝装置B、一级冷凝装置和二级冷凝装置A进行冷凝；当二级冷凝装置A结霜需要除霜时，运行第二冷凝回路，VOCs气体首先通过二级冷凝装置A进行冷凝，再依次通过一级冷凝装置和二级冷凝装置B进行冷凝。When the secondary condensing device B is frosted and needs to be defrosted, the first condensing circuit is operated, and the VOCs gas is condensed through the secondary condensing device B, the primary condensing device and the secondary condensing device A in turn; when the secondary condensing device A is frosted When defrosting is required, the second condensing circuit is operated, and the VOCs gas is first condensed by the second condensing device A, and then condensed by the first condensing device and the second condensing device B in turn.
如图3、4、5所述的低温吸收单元包括吸收塔13，所述吸收塔为分段式喷淋塔，包括两层塔板和两个喷淋头，吸收塔的气体入口端设置在吸收塔的第一层高于吸收液液面上方处，所述吸收塔的第二层塔板设有若干溢流小管二14，用于VOCs气体的传送和第二层吸收液的溢流传送，VOCs气体经吸收塔一层喷淋头1501喷淋后，由溢流小管二进入吸收塔第二层，再经吸收塔二层喷淋头1502喷淋，实现VOCs气体的充分吸收，所述吸收塔塔顶还设有合格气体排放口。The low-temperature absorption unit as shown in Figures 3, 4, and 5 includes an absorption tower 13, which is a segmented spray tower and includes two trays and two spray heads. The gas inlet of the absorption tower is set at The first layer of the absorption tower is higher than the upper level of the absorption liquid. The second layer of the absorption tower is provided with a number of overflow small pipes 14 for the transmission of VOCs gas and the overflow transmission of the second layer of absorption liquid. After being sprayed by the spray nozzle 1501 on the first layer of the absorption tower, the VOCs gas enters the second layer of the absorption tower from the second overflow pipe, and then sprayed by the spray nozzle 1502 on the second layer of the absorption tower to realize the full absorption of VOCs. The top of the absorption tower is also equipped with a qualified gas discharge port.
低温吸收单元包括第一自循环吸收液回路2803和第二自循环吸收液回路2804：The cryogenic absorption unit includes a first self-circulating absorption liquid circuit 2803 and a second self-circulating absorption liquid circuit 2804:
第一自循环吸收液回路：吸收塔一层吸收液出口经吸收塔一级循环喷淋泵1601连接至吸收塔一层喷淋头，实现对VOCs气体的喷淋；The first self-circulating absorption liquid circuit: the absorption liquid outlet of the first layer of the absorption tower is connected to the first-level spray head of the absorption tower through the first-stage circulating spray pump 1601 of the absorption tower to realize the spraying of VOCs gas;
第二自循环吸收液回路：吸收塔二层吸收液出口经吸收塔二级循环喷淋泵1602连接至吸收塔二层喷淋头，实现对VOCs气体的进一步喷淋。The second self-circulating absorption liquid circuit: the second-layer absorption liquid outlet of the absorption tower is connected to the second-layer spray head of the absorption tower through the absorption tower second-level circulating spray pump 1602 to realize further spraying of VOCs gas.
所述高温解吸单元包括解吸塔21，所述解吸塔与所述低温吸收单元中的吸收塔之间的连接方式包括：The high-temperature desorption unit includes a desorption tower 21, and the connection between the desorption tower and the absorption tower in the low-temperature absorption unit includes:
第一解吸回路2805：低温吸收单元中的吸收塔塔底吸收液出口，经过换热器二的管层连接至高温解吸单元中的解吸塔塔身上方的吸收液进口端；The first desorption circuit 2805: the absorption liquid outlet at the bottom of the absorption tower in the low-temperature absorption unit is connected to the absorption liquid inlet on the upper body of the desorption tower in the high-temperature desorption unit through the tube layer of the second heat exchanger;
第二解吸回路2806：高温解吸单元中的解吸塔塔底下方吸收液出口，经过换热器二的壳层连接至低温吸收单元中的第二自循环吸收液回路的入口；The second desorption circuit 2806: the absorption liquid outlet under the bottom of the desorption tower in the high temperature desorption unit is connected to the inlet of the second self-circulating absorption liquid circuit in the low temperature absorption unit through the shell of the second heat exchanger;
吸收塔的第一自循环吸收液回路、第二自循环吸收液回路、第一解吸回路和第二解吸回路内的吸收液及吸收塔和解吸塔内的吸收液构成流量平衡。The absorption liquid in the first self-circulating absorption liquid circuit, the second self-circulating absorption liquid circuit, the first desorption circuit and the second desorption circuit of the absorption tower and the absorption liquid in the absorption tower and the desorption tower constitute a flow balance.
所述高温解吸单元中的解吸塔通过回收回路2807连接至低温吸收单元中的吸收塔，所述回收回路为：解吸塔的顶端出口依次经过换热器三、真空泵25连接至回收卧罐18，回收卧罐的顶端出口连接至吸收塔的入口端。The desorption tower in the high temperature desorption unit is connected to the absorption tower in the low temperature absorption unit through a recovery loop 2807. The recovery loop is: the top outlet of the desorption tower is connected to the recovery horizontal tank 18 through the heat exchanger three and the vacuum pump 25 in turn, The top outlet of the recovery tank is connected to the inlet of the absorption tower.
所述低温回收单元的回收卧罐与分液罐二19连接，分液罐二由密度分流，中间为缓冲区，左侧为有机物区，右侧为冷凝水区。The recovery horizontal tank of the low-temperature recovery unit is connected to the second liquid separation tank 19, the second liquid separation tank is divided by density, the middle is the buffer zone, the left side is the organic matter area, and the right side is the condensate water area.
水洗单元入口端通过阻火器1连接VOCs现场来气；任一单元和任一管路均设有闸阀2或自动控制阀8或球阀12和流量计；所述高温解吸单元中的解吸塔的热源23出口端连接一疏水器22。The inlet end of the water washing unit is connected to the VOCs on-site gas through the flame arrestor 1; any unit and any pipeline are equipped with gate valves 2 or automatic control valves 8 or ball valves 12 and flow meters; the heat source of the desorption tower in the high temperature desorption unit 23 is connected to a steam trap 22 at the outlet end.
VOCs气体通过冷源27和热源进行热量交换，实现余冷回收和VOCs的冷凝或汽化。The VOCs gas exchanges heat through the cold source 27 and the heat source to realize waste cooling recovery and condensation or vaporization of VOCs.
一种集吸收、解吸和回收为一体VOCs回收方法，包括以下步骤：A VOCs recovery method integrating absorption, desorption and recovery includes the following steps:
1)VOCs现场来气依次经过阻火器、水洗单元除氨后,进入自耦合预冷单元；1) The VOCs on-site air flow passes through the flame arrestor and the washing unit to remove ammonia, and then enters the self-coupling pre-cooling unit;
2)自耦合预冷单元对VOCs气体进行脱水处理后，进入低温吸收单元；2) After the self-coupling pre-cooling unit dehydrates the VOCs gas, it enters the low-temperature absorption unit;
3)低温吸收单元运行第一自循环吸收液回路和第二自循环吸收液回路进行吸收，吸收塔的第一层富级吸收液通过第一解吸回路过程中，经过换热器二的管层进行冷量回收后，进入高温解吸单元中的解吸塔进行解吸；解吸出来的新鲜吸收液通过第二解吸回路经过换热器二的壳层进行热量回收后，对吸收塔的第二层贫级吸收液优先补充；3) The low-temperature absorption unit runs the first self-circulating absorption liquid circuit and the second self-circulating absorption liquid circuit for absorption. The first layer of rich absorption liquid of the absorption tower passes through the tube layer of heat exchanger 2 during the process of passing through the first desorption circuit. After the cold energy is recovered, it enters the desorption tower in the high temperature desorption unit for desorption; the desorbed fresh absorption liquid passes through the second desorption loop and passes through the shell of the heat exchanger 2 for heat recovery, and then the second layer of the absorption tower is lean Priority replenishment of absorbent;
4)解吸出来的VOCs气体通过回收回路进入回收卧罐中冷凝液化回收，未液化的VOCs气体重新输送至低温吸收单元中吸收。4) The desorbed VOCs gas enters the recovery horizontal tank through the recovery loop to be condensed and liquefied for recovery, and the unliquefied VOCs gas is re-transmitted to the low-temperature absorption unit for absorption.
在所述步骤2)中，VOCs气体进入二级冷凝装置B，然后依次经过一级冷凝装置7和二级冷凝装置A对VOCs进行冷凝和除水，随后未冷凝的VOCs气体进入低温吸收单元的吸收塔。In the step 2), the VOCs gas enters the secondary condensing unit B, and then passes through the primary condensing unit 7 and the secondary condensing unit A to condense and remove water from the VOCs, and then the uncondensed VOCs gas enters the low-temperature absorption unit Absorption tower.
在所述步骤3)中，VOCs气体首先在吸收塔一层进行喷淋吸收，此时大量 的VOCs被吸收液吸收；剩余VOCs气体再通过溢流小管二进入吸收塔二层进行新鲜吸收液喷淋的深度吸收，合格后的气体经换热器一由安全排放口排放。In the step 3), the VOCs gas is first sprayed and absorbed in the first layer of the absorption tower. At this time, a large amount of VOCs is absorbed by the absorption liquid; the remaining VOCs gas enters the second layer of the absorption tower through the overflow tube 2 for fresh absorption liquid spraying. The water is absorbed deeply, and the qualified gas is discharged from the safety discharge port through the heat exchanger.
在所述步骤3)中，吸收塔的二层吸收液除了自身喷淋外，当液位超过溢流小管二溢流口时，吸收液溢流进入吸收塔的一层富级吸收液。In the step 3), in addition to spraying the second-layer absorption liquid of the absorption tower, when the liquid level exceeds the second overflow port of the overflow small pipe, the absorption liquid overflows into the first-layer rich absorption liquid of the absorption tower.
在所述步骤4)中，高温VOCs气体则从解吸塔21塔顶出口通过回收回路进行回收，即先经过换热器三进行循环水初步降温，然后通过真空泵25进入低温回收罐卧，使气态VOCs液化，液化后的VOCs回收，未液化的VOCs则重新进入吸收塔继续处理。In the step 4), the high-temperature VOCs gas is recovered from the top outlet of the desorption tower 21 through the recovery loop, that is, the circulating water is initially cooled through the heat exchanger three, and then enters the low-temperature recovery tank through the vacuum pump 25 to make the gaseous state VOCs are liquefied, the liquefied VOCs are recovered, and the unliquefied VOCs are re-entered into the absorption tower to continue processing.
为了实现吸收质VOCs的气液两种状态的转换和利用气液转换进行分离，提高分离效率，换热设备包括：In order to achieve the conversion of the gas-liquid state of the absorbing VOCs and the separation of the gas-liquid conversion to improve the separation efficiency, the heat exchange equipment includes:
设置在低温吸收单元和安全排放口之间的换热器一17，通过回收泵26与冷源相连，为了对排放出的低温气体进行余冷回收，补充自耦合预冷单元出来的冷源冷量；The heat exchanger 17 arranged between the low-temperature absorption unit and the safety discharge port is connected to the cold source through the recovery pump 26. In order to recover the residual cold of the discharged low-temperature gas, it supplements the cold source cold from the self-coupling pre-cooling unit. the amount;
设置在低温吸收单元的吸收塔与高温解吸单元之间的换热器二；所述换热器二中的任一热交换管路的一端与所述的低温吸收单元相连，另一端与所述的高温解吸单元相连。The second heat exchanger is arranged between the absorption tower of the low-temperature absorption unit and the high-temperature desorption unit; one end of any heat exchange pipeline in the second heat exchanger is connected to the low-temperature absorption unit, and the other end is connected to the low-temperature absorption unit. The high temperature desorption unit is connected.
所述换热器二利用低温吸收单元排出的低温吸收液与高温解吸单元解吸出的高温吸收液互相进行热量回收；The second heat exchanger utilizes the low-temperature absorption liquid discharged from the low-temperature absorption unit and the high-temperature absorption liquid desorbed by the high-temperature desorption unit to mutually recover heat;
设置在高温解吸单元和低温回收单元之间的换热器三；Heat exchanger three arranged between the high-temperature desorption unit and the low-temperature recovery unit;
换热器三为循环水换热器，为了防止高温VOCs对真空泵的损害。经换热器三降温后的低温VOCs通过真空泵输送到回收卧罐后进一步冷凝，转化为液体的VOCs存储在低温回收单元的分液罐二中；The third heat exchanger is a circulating water heat exchanger, in order to prevent high-temperature VOCs from damaging the vacuum pump. The low-temperature VOCs cooled by the heat exchanger 3 are transported to the recovery horizontal tank by the vacuum pump and then further condensed, and the VOCs converted into liquid are stored in the liquid separation tank 2 of the low-temperature recovery unit;
设置在所述自耦合预冷单元中的一级冷凝装置、二级冷凝装置A、二级冷凝装置B；所述的一级冷凝装置、二级冷凝装置A和二级冷凝装置B通过回收泵与冷源相连；The primary condensing device, secondary condensing device A, and secondary condensing device B arranged in the self-coupling pre-cooling unit; the primary condensing device, secondary condensing device A, and secondary condensing device B pass through the recovery pump Connected to the cold source;
还包括分别内置在吸收塔、解吸塔和回收卧罐中的内置换热器和换热单元中 的换热循环管路，其中吸收塔和回收卧罐中的内置换热器通过回收泵与冷源相连，所述的解吸塔中的内置换热器与热源相连。It also includes internal heat exchangers built into the absorption tower, desorption tower, and recovery tank, and heat exchange circulation pipelines in the heat exchange unit. The internal heat exchangers in the absorption tower and the recovery tank are connected to the cooling system through the recovery pump. The source is connected, and the internal heat exchanger in the desorption tower is connected with the heat source.
在本发明的一种实施例中，所述的冷源为载冷剂，所述的热源为温度高于100℃的水蒸汽。In an embodiment of the present invention, the cold source is a refrigerant, and the heat source is water vapor with a temperature higher than 100°C.
在本发明的实施例中，VOCs回收系统具体包括：In the embodiment of the present invention, the VOCs recovery system specifically includes:
闸阀、水洗塔、水洗塔一层喷淋头、水洗塔二层喷淋头、储水罐、水洗塔一级循环喷淋泵和水洗塔二级循环喷淋泵组成水洗单元，经过阻火器的VOCs需经过水洗装置，目的是通过水洗进行除氨和洗去大量溶于水的杂质。Gate valve, water washing tower, first-level spray head of water washing tower, second-level spray head of water washing tower, water storage tank, first-level circulating spray pump of water washing tower and second-level circulating spray pump of water washing tower constitute a water washing unit, which passes through the flame arrester. VOCs need to go through a water washing device, the purpose is to remove ammonia and wash away a large amount of water-soluble impurities through water washing.
水洗塔选用立式，高度为3m～15m，直径为0.5m～3m。水洗塔设计为分段式喷淋式，二层塔板设有若干溢流小管一，溢流小管一直径为
Figure PCTCN2020084401-appb-000001
高度为5mm～10mm，总截面积为塔板截面积的5％～15％，水洗塔一层设有储水量在0.5吨～10吨的储水罐，喷淋量为5m 3/h～50m 3/h，水洗塔二层水源通过补水口进行供给，补水量为1m 3/h～5m 3/h，喷淋量为5m 3/h～50m 3/h，水洗塔回收氨(水)量为5kg/h～100kg/h。 The washing tower is vertical, with a height of 3m～15m and a diameter of 0.5m～3m. The washing tower is designed as a segmented spray type. The two-layer tray is equipped with a number of overflow small pipes. The diameter of the overflow pipes is
Figure PCTCN2020084401-appb-000001
The height is 5mm～10mm, and the total cross-sectional area is 5%～15% of the cross-sectional area of the tray. The first floor of the washing tower is equipped with a water storage tank with a water storage capacity of 0.5 to 10 tons, and the spraying capacity is 5m 3 /h～50m 3 /h, the second-layer water source of the washing tower is supplied through the water replenishment port, the replenishing water volume is 1m 3 /h～5m 3 /h, the spraying volume is 5m 3 /h～50m 3 /h, the water washing tower recovers the amount of ammonia (water) It is 5kg/h～100kg/h.
吸收塔塔顶设有VOCs出口，塔身下方、吸收液最高液面上方设有VOCs进口，气体从下方进入，与喷淋的吸收液呈逆向接触，从而实现充分吸收。吸收塔也设计为分段式喷淋式，二层塔板设有若干溢流小管二，溢流小管二直径为
Figure PCTCN2020084401-appb-000002
高度为5mm～10mm，总截面积为塔板截面积的5％～15％；塔身直径一般根据所处理的油气量而定，一般塔身高度为3m～15m，直径为0.5m～3m，存储高度为0.3m～4m，塔设计操作温度为-25℃～-5℃，内置换热器中的冷源流量为0.5m 3/h 2～3m 3/h 2，一层喷淋量和二层喷淋量为5m 3/h～50m 3/h。 The top of the absorption tower is equipped with a VOCs outlet, and there is a VOCs inlet below the tower body and above the highest liquid level of the absorption liquid. The gas enters from below and contacts the sprayed absorption liquid in a reverse direction to achieve full absorption. The absorption tower is also designed as a segmented spray type. The two-layer tray is equipped with a number of overflow small pipes. The diameter of the overflow small pipes is
Figure PCTCN2020084401-appb-000002
The height is 5mm～10mm, and the total cross-sectional area is 5%～15% of the cross-sectional area of the tray; the diameter of the tower body is generally determined according to the amount of oil and gas processed, and the height of the tower body is generally 3m～15m, and the diameter is 0.5m～3m. The storage height is 0.3m～4m, the design operating temperature of the tower is -25℃～-5℃, the flow rate of the cold source in the internal heat exchanger is 0.5m 3 /h 2 ～3m 3 /h 2 , and the amount of spraying on the first layer is equal to The spray rate of the second layer is 5m 3 /h～50m 3 /h.
解吸塔是利用高温蒸汽作为热媒介质，塔径为0.1m～3m，高度为0.5m～5m，高温蒸汽温度为120℃～150℃，蒸汽用量为1kg/h～5kg/h，解吸量为0.5kg/h～50kg/h。The desorption tower uses high temperature steam as the heat medium. The diameter of the tower is 0.1m～3m, the height is 0.5m～5m, the high temperature steam temperature is 120℃～150℃, the steam consumption is 1kg/h～5kg/h, and the desorption capacity is 0.5kg/h～50kg/h.
回收卧罐直径为0.2m～3m，长度为0.5m～5m，回收液量为0.5kg/h～50kg/h。The recovery horizontal tank has a diameter of 0.2m-3m, a length of 0.5m-5m, and a recovered liquid volume of 0.5kg/h-50kg/h.
换热器三中的循环水温度为10℃～100℃，流量为0.01m 3/h～2m 3/h。 The circulating water temperature in the heat exchanger three is 10℃～100℃, and the flow rate is 0.01m 3 /h～2m 3 /h.
在本发明的VOCs回收系统中，冷源相连的载冷剂管道一般选用DN10～DN20， 载冷剂温度为-25℃～-10℃，载冷剂流量为1m 3/h～20m 3/h。 In the VOCs recovery system of the present invention, the refrigerant pipeline connected to the cold source is generally DN10～DN20, the temperature of the refrigerant is -25℃～-10℃, and the flow of the refrigerant is 1m 3 /h～20m 3 /h .
以上显示和描述了本发明的基本原理和主要特征和本发明的优点。本行业的技术人员应该了解，本发明不受上述实施例的限制，上述实施例和说明书中描述的只是说明本发明的原理，在不脱离本发明精神和范围的前提下，本发明还会有各种变化和改进，这些变化和改进都落入要求保护的本发明范围内。本发明要求保护范围由所附的权利要求书及其等效物界定。The basic principles and main features of the present invention and the advantages of the present invention have been shown and described above. Those skilled in the industry should understand that the present invention is not limited by the above-mentioned embodiments. The above-mentioned embodiments and descriptions only illustrate the principles of the present invention. Without departing from the spirit and scope of the present invention, the present invention may have Various changes and improvements fall within the scope of the claimed invention. The scope of protection claimed by the present invention is defined by the appended claims and their equivalents.

Claims (17)

  1. 一种集吸收、解吸和回收为一体VOCs回收系统，其特征在于：包括A VOCs recovery system integrating absorption, desorption and recovery, which is characterized in that:
    水洗单元：与自耦合预冷单元连接，用于对VOCs进气进行水洗；Washing unit: connected to the self-coupling pre-cooling unit, used to wash the VOCs intake air;
    自耦合预冷单元：连接至低温吸收单元，用于对水洗后的VOCs气体进行冷凝；Self-coupling pre-cooling unit: connected to the low-temperature absorption unit, used to condense the VOCs gas after washing;
    低温吸收单元：通过换热器二连接至高温解吸单元，用于对冷凝后的VOCs气体进行吸收；Low-temperature absorption unit: connected to the high-temperature desorption unit through the second heat exchanger, used to absorb the condensed VOCs gas;
    高温解吸单元：通过换热器三连接至低温回收单元，用于对低温吸收后的VOCs气体进行解吸；High-temperature desorption unit: connected to the low-temperature recovery unit through heat exchanger 3, used to desorb the VOCs gas after low-temperature absorption;
    低温回收单元：连接至低温吸收单元，用于回收液化后的VOCs，同时将未液化的VOCs重新输送至低温吸收单元处理。Low-temperature recovery unit: connected to the low-temperature absorption unit, used to recover the liquefied VOCs, and at the same time, retransmit the unliquefied VOCs to the low-temperature absorption unit for processing.
  2. 根据权利要求1所述的集吸收、解吸和回收为一体VOCs回收系统，其特征在于：所述水洗单元包括水洗塔，所述水洗塔为分段式喷淋塔，包括两层塔板和两个喷淋头。The VOCs recovery system integrating absorption, desorption and recovery according to claim 1, characterized in that: the washing unit includes a washing tower, and the washing tower is a segmented spray tower, including two trays and two A shower head.
  3. 根据权利要求1所述的集吸收、解吸和回收为一体VOCs回收系统，其特征在于：所述自耦合预冷单元包括二级冷凝装置A、二级冷凝装置B和一级冷凝装置，所述二级冷凝装置A、二级冷凝装置B和一级冷凝装置之间有第一冷凝回路和第二冷凝回路两种连接方式：The VOCs recovery system integrating absorption, desorption, and recovery according to claim 1, wherein the self-coupling pre-cooling unit includes a secondary condensation device A, a secondary condensation device B, and a primary condensation device. There are two connection modes between the second condensing device A, the second condensing device B and the first condensing device: the first condensing circuit and the second condensing circuit:
    所述第一冷凝回路的连接方式为：二级冷凝装置B的进口端连接水洗单元的水洗塔的出口端；二级冷凝装置B的出口端连接一级冷凝装置的进口端；一级冷凝装置的出口端连接二级冷凝装置A的进口端；二级冷凝装置A的出口端连接至低温吸收单元；The connection mode of the first condensing circuit is as follows: the inlet end of the secondary condensing device B is connected to the outlet end of the washing tower of the water washing unit; the outlet end of the secondary condensing device B is connected to the inlet end of the primary condensing device; the primary condensing device The outlet end of is connected to the inlet end of the secondary condensing device A; the outlet end of the secondary condensing device A is connected to the low-temperature absorption unit;
    所述第二冷凝回路的连接方式为：二级冷凝装置A的进口端连接水洗单元的水洗塔的出口端；二级冷凝装置A的出口端连接一级冷凝装置的进口端；一级冷凝装置的出口端连接二级冷凝装置B的进口端；二级冷凝装置B的出口端连接至低温吸收单元。The connection mode of the second condensing circuit is as follows: the inlet end of the second condensing device A is connected to the outlet end of the washing tower of the water washing unit; the outlet end of the second condensing device A is connected to the inlet end of the first condensing device; the first condensing device The outlet end of is connected to the inlet end of the secondary condensing device B; the outlet end of the secondary condensing device B is connected to the low-temperature absorption unit.
  4. 根据权利要求3所述的集吸收、解吸和回收为一体VOCs回收系统，其特 征在于：所述自耦合预冷单元的一级冷凝装置、二级冷凝装置A、二级冷凝装置B均与分液罐一连接。The VOCs recovery system integrating absorption, desorption, and recovery according to claim 3, characterized in that: the first-stage condensation device, the second-stage condensation device A, and the second-stage condensation device B of the self-coupling pre-cooling unit are all combined with each other. One connection of the liquid tank.
  5. 根据权利要求1所述的集吸收、解吸和回收为一体VOCs回收系统，其特征在于：所述低温吸收单元包括吸收塔，所述吸收塔为分段式喷淋塔，包括两层塔板和两个喷淋头，吸收塔的气体入口端设置在吸收塔的第一层高于吸收液液面上方处，所述吸收塔的第二层塔板设有若干溢流小管二，用于VOCs气体的传送和第二层吸收液的溢流传送，VOCs气体经吸收塔一层喷淋头喷淋后，由溢流小管二进入吸收塔第二层，再经吸收塔二层喷淋头喷淋，实现VOCs气体的充分吸收。The VOCs recovery system integrating absorption, desorption and recovery according to claim 1, characterized in that: the low-temperature absorption unit includes an absorption tower, and the absorption tower is a segmented spray tower, including two-layer trays and Two spray heads, the gas inlet end of the absorption tower is set on the first layer of the absorption tower above the level of the absorption liquid, and the second layer of the absorption tower is provided with a number of overflow small pipes two for VOCs The gas transmission and the overflow transmission of the second layer of absorption liquid. After being sprayed by the first-level spray head of the absorption tower, the VOCs gas enters the second layer of the absorption tower from the overflow pipe two, and then sprays through the second-level spray head of the absorption tower. To achieve full absorption of VOCs gas.
  6. 根据权利要求5所述的集吸收、解吸和回收为一体VOCs回收系统，其特征在于：在低温吸收单元的吸收塔与安全排放口之间设置有换热器一；所述换热器一利用低温吸收单元的吸收塔排放出的低温气体进行余冷回收，对自耦合预冷单元后的冷源进行冷量补充。The VOCs recovery system integrating absorption, desorption and recovery according to claim 5, characterized in that: a heat exchanger is arranged between the absorption tower of the low-temperature absorption unit and the safety discharge port; the heat exchanger is used The low-temperature gas discharged from the absorption tower of the low-temperature absorption unit undergoes waste cooling recovery to supplement the cooling capacity of the cold source after the self-coupling pre-cooling unit.
  7. 根据权利要求1所述的集吸收、解吸和回收为一体VOCs回收系统，其特征在于：低温吸收单元包括第一自循环吸收液回路和第二自循环吸收液回路；The VOCs recovery system integrating absorption, desorption and recovery according to claim 1, wherein the low-temperature absorption unit includes a first self-circulating absorption liquid circuit and a second self-circulating absorption liquid circuit;
    第一自循环吸收液回路：吸收塔一层吸收液出口经吸收塔一级循环喷淋泵连接至吸收塔一层喷淋头，实现对VOCs气体的喷淋；The first self-circulating absorption liquid circuit: the absorption liquid outlet of the first layer of the absorption tower is connected to the spray head of the first layer of the absorption tower through the first-stage circulating spray pump of the absorption tower to realize the spraying of VOCs gas;
    第二自循环吸收液回路：吸收塔二层吸收液出口经吸收塔二级循环喷淋泵连接至吸收塔二层喷淋头，实现对VOCs气体的进一步喷淋。The second self-circulating absorption liquid circuit: the second-layer absorption liquid outlet of the absorption tower is connected to the second-layer spray head of the absorption tower through the second-stage circulating spray pump of the absorption tower to realize further spraying of VOCs gas.
  8. 根据权利要求1所述的集吸收、解吸和回收为一体VOCs回收系统，其特征在于：所述高温解吸单元包括解吸塔，所述解吸塔与所述低温吸收单元中的吸收塔之间的连接方式包括：The VOCs recovery system integrating absorption, desorption and recovery according to claim 1, wherein the high temperature desorption unit comprises a desorption tower, and the connection between the desorption tower and the absorption tower in the low temperature absorption unit Ways include:
    第一解吸回路：低温吸收单元中的吸收塔塔底吸收液出口，经过换热器二的管层连接至高温解吸单元中的解吸塔塔身上方的吸收液进口端；The first desorption circuit: the absorption liquid outlet at the bottom of the absorption tower in the low-temperature absorption unit is connected to the absorption liquid inlet above the upper body of the desorption tower in the high-temperature desorption unit through the tube layer of the heat exchanger 2;
    第二解吸回路：高温解吸单元中的解吸塔塔底下方吸收液出口，经过换热器二的壳层连接至低温吸收单元中的第二自循环吸收液回路的入口；The second desorption loop: the outlet of the absorption liquid under the bottom of the desorption tower in the high-temperature desorption unit is connected to the inlet of the second self-circulating absorption liquid loop in the low-temperature absorption unit through the shell of the second heat exchanger;
    吸收塔的第一自循环吸收液回路、第二自循环吸收液回路、第一解吸回路和第二解吸回路内的吸收液及吸收塔和解吸塔内的吸收液构成流量平衡。The absorption liquid in the first self-circulating absorption liquid circuit, the second self-circulating absorption liquid circuit, the first desorption circuit and the second desorption circuit of the absorption tower and the absorption liquid in the absorption tower and the desorption tower constitute a flow balance.
  9. 根据权利要求1所述的集吸收、解吸和回收为一体VOCs回收系统，其特征在于：所述高温解吸单元中的解吸塔通过回收回路连接至低温吸收单元中的吸收塔，所述回收回路为：解吸塔的顶端出口依次经过换热器三、真空泵连接至回收卧罐，回收卧罐的顶端出口连接至吸收塔的入口端。The VOCs recovery system integrating absorption, desorption and recovery according to claim 1, wherein the desorption tower in the high temperature desorption unit is connected to the absorption tower in the low temperature absorption unit through a recovery loop, and the recovery loop is : The top outlet of the desorption tower passes through the heat exchanger in turn. Third, the vacuum pump is connected to the recovery horizontal tank, and the top outlet of the recovery horizontal tank is connected to the inlet end of the absorption tower.
  10. 根据权利要求9所述的集吸收、解吸和回收为一体VOCs回收系统，其特征在于：所述低温回收单元的回收卧罐与分液罐二连接。The VOCs recovery system integrating absorption, desorption and recovery according to claim 9, characterized in that: the recovery horizontal tank of the low-temperature recovery unit is connected to the second liquid separation tank.
  11. 根据权利要求5所述的集吸收、解吸和回收为一体VOCs回收系统，其特征在于：低温吸收单元的吸收塔与高温解吸单元之间设置有换热器二,所述换热器二利用低温吸收单元排出的低温吸收液与高温解吸单元解吸出的高温吸收液互相进行热量回收。The VOCs recovery system integrating absorption, desorption and recovery according to claim 5, characterized in that: a second heat exchanger is provided between the absorption tower of the low temperature absorption unit and the high temperature desorption unit, and the second heat exchanger uses low temperature The low-temperature absorption liquid discharged from the absorption unit and the high-temperature absorption liquid desorbed by the high-temperature desorption unit recover heat from each other.
  12. 一种利用VOCs回收系统的VOCs回收方法，其特征在于：包括以下步骤：A VOCs recovery method using a VOCs recovery system is characterized in that it comprises the following steps:
    1)VOCs现场来气依次经过阻火器、水洗单元除氨后,进入自耦合预冷单元；1) The VOCs on-site air flow passes through the flame arrestor and the washing unit to remove ammonia, and then enters the self-coupling pre-cooling unit;
    2)自耦合预冷单元对VOCs气体进行脱水处理后，进入低温吸收单元；2) After the self-coupling pre-cooling unit dehydrates the VOCs gas, it enters the low-temperature absorption unit;
    3)低温吸收单元运行第一自循环吸收液回路和第二自循环吸收液回路进行吸收，吸收塔的第一层富级吸收液通过第一解吸回路过程中，经过换热器二的管层进行冷量回收后，进入高温解吸单元中的解吸塔进行解吸；解吸出来的新鲜吸收液通过第二解吸回路经过换热器二的壳层进行热量回收后，对吸收塔的第二层贫级吸收液优先补充；3) The low-temperature absorption unit runs the first self-circulating absorption liquid circuit and the second self-circulating absorption liquid circuit for absorption. The first layer of rich absorption liquid of the absorption tower passes through the tube layer of heat exchanger 2 during the process of passing through the first desorption circuit. After the cold energy is recovered, it enters the desorption tower in the high temperature desorption unit for desorption; the desorbed fresh absorption liquid passes through the second desorption loop and passes through the shell of the heat exchanger 2 for heat recovery, and then the second layer of the absorption tower is lean Priority replenishment of absorbent;
    4)解吸出来的VOCs气体通过回收回路进入回收卧罐中冷凝液化回收，未液化的VOCs气体重新输送至低温吸收单元中吸收。4) The desorbed VOCs gas enters the recovery horizontal tank through the recovery loop to be condensed and liquefied for recovery, and the unliquefied VOCs gas is re-transmitted to the low-temperature absorption unit for absorption.
  13. 根据权利要求12所述的利用VOCs回收系统的VOCs回收方法，其特征在于：在所述步骤2)中，当二级冷凝装置B结霜需要除霜时，运行第一冷凝回路，VOCs气体依次通过二级冷凝装置B、一级冷凝装置和二级冷凝装置A进行冷凝；当二级冷凝装置A结霜需要除霜时，运行第二冷凝回路，VOCs气体首先 通过二级冷凝装置A进行冷凝，再依次通过一级冷凝装置和二级冷凝装置B进行冷凝。The VOCs recovery method using a VOCs recovery system according to claim 12, characterized in that: in the step 2), when the secondary condensing device B is frosted and needs to be defrosted, the first condensing circuit is operated, and the VOCs gas is sequentially Condensate through the secondary condenser B, primary condenser and secondary condenser A; when the secondary condenser A is frosted and needs to be defrosted, the second condensing circuit is operated, and the VOCs gas is first condensed through the secondary condenser A , And then pass through the first condensing device and the second condensing device B in turn for condensation.
  14. 根据权利要求13所述的利用VOCs回收系统的VOCs回收方法，其特征在于：在所述步骤2)中，VOCs气体运行第一冷凝回路或第二冷凝回路时，一级冷凝装置、二级冷凝装置B和二级冷凝装置A分别对VOCs进行冷凝和除水，随后未冷凝的VOCs气体进入低温吸收单元的吸收塔。The VOCs recovery method using the VOCs recovery system according to claim 13, characterized in that: in the step 2), when the VOCs gas runs the first condensing circuit or the second condensing circuit, the primary condensing device and the secondary condensing Device B and secondary condensation device A respectively condense and remove water from VOCs, and then the uncondensed VOCs gas enters the absorption tower of the low-temperature absorption unit.
  15. 根据权利要求12所述的利用VOCs回收系统的VOCs回收方法，其特征在于：在所述步骤3)中，VOCs气体首先在吸收塔一层进行喷淋吸收，此时大量的VOCs被吸收液吸收；剩余VOCs气体再通过溢流小管进入吸收塔二层进行新鲜吸收液喷淋的深度吸收，合格后的气体经换热器一由安全排放口排放。The VOCs recovery method using a VOCs recovery system according to claim 12, characterized in that: in the step 3), the VOCs gas is first sprayed and absorbed on the first layer of the absorption tower, and a large amount of VOCs are absorbed by the absorption liquid. ; The remaining VOCs gas enters the second layer of the absorption tower through the overflow tube for deep absorption of fresh absorption liquid spray, and the qualified gas is discharged from the safety discharge port through the heat exchanger 1.
  16. 根据权利要求12所述的利用VOCs回收系统的VOCs回收方法，其特征在于：在所述步骤3)中，吸收塔的二层吸收液除了自身喷淋外，当液位超过溢流小管二溢流口时，吸收液溢流进入吸收塔的一层富级吸收液。The VOCs recovery method using the VOCs recovery system according to claim 12, characterized in that: in the step 3), the second-layer absorption liquid of the absorption tower is sprayed by itself, when the liquid level exceeds the overflow small pipe, the second overflow When flowing out, the absorption liquid overflows into a layer of rich absorption liquid in the absorption tower.
  17. 根据权利要求12所述的利用VOCs回收系统的VOCs回收方法，其特征在于：在所述步骤4)中，高温VOCs气体则从解吸塔塔顶出口通过回收回路进行回收，即先经过换热器三进行循环水初步降温，然后通过真空泵进入低温回收卧罐，使气态VOCs液化，液化后的VOCs回收，未液化的VOCs则重新进入吸收塔继续处理。The VOCs recovery method using a VOCs recovery system according to claim 12, characterized in that: in the step 4), the high-temperature VOCs gas is recovered from the top outlet of the desorption tower through the recovery loop, that is, first passes through the heat exchanger Third, the circulating water is initially cooled, and then enters the low-temperature recovery horizontal tank through the vacuum pump to liquefy the gaseous VOCs. The liquefied VOCs are recovered, and the unliquefied VOCs are re-entered into the absorption tower to continue processing.
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