CN217568114U - Butadiene tail gas recovery system - Google Patents
Butadiene tail gas recovery system Download PDFInfo
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- CN217568114U CN217568114U CN202221128995.6U CN202221128995U CN217568114U CN 217568114 U CN217568114 U CN 217568114U CN 202221128995 U CN202221128995 U CN 202221128995U CN 217568114 U CN217568114 U CN 217568114U
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- heat exchanger
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- tail gas
- water washing
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- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 title claims abstract description 74
- 238000011084 recovery Methods 0.000 title claims abstract description 49
- 238000005406 washing Methods 0.000 claims abstract description 138
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 93
- 239000012071 phase Substances 0.000 claims abstract description 74
- 239000007791 liquid phase Substances 0.000 claims abstract description 36
- 238000000926 separation method Methods 0.000 claims abstract description 31
- 239000007788 liquid Substances 0.000 claims description 18
- 238000001816 cooling Methods 0.000 claims description 9
- 238000005070 sampling Methods 0.000 claims description 9
- 238000007789 sealing Methods 0.000 claims description 5
- 239000007789 gas Substances 0.000 abstract description 78
- 238000004519 manufacturing process Methods 0.000 abstract description 21
- 239000007792 gaseous phase Substances 0.000 abstract description 8
- 230000009467 reduction Effects 0.000 abstract description 3
- 238000013461 design Methods 0.000 description 20
- NLHHRLWOUZZQLW-UHFFFAOYSA-N Acrylonitrile Chemical compound C=CC#N NLHHRLWOUZZQLW-UHFFFAOYSA-N 0.000 description 15
- 238000012360 testing method Methods 0.000 description 10
- 238000004781 supercooling Methods 0.000 description 8
- 230000006835 compression Effects 0.000 description 4
- 238000007906 compression Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 239000010865 sewage Substances 0.000 description 4
- 238000001210 attenuated total reflectance infrared spectroscopy Methods 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 230000003749 cleanliness Effects 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 229920000459 Nitrile rubber Polymers 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- BSFODEXXVBBYOC-UHFFFAOYSA-N 8-[4-(dimethylamino)butan-2-ylamino]quinolin-6-ol Chemical compound C1=CN=C2C(NC(CCN(C)C)C)=CC(O)=CC2=C1 BSFODEXXVBBYOC-UHFFFAOYSA-N 0.000 description 1
- 241000282414 Homo sapiens Species 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- CERQOIWHTDAKMF-UHFFFAOYSA-N Methacrylic acid Chemical compound CC(=C)C(O)=O CERQOIWHTDAKMF-UHFFFAOYSA-N 0.000 description 1
- 239000012298 atmosphere Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000007123 defense Effects 0.000 description 1
- KWKXNDCHNDYVRT-UHFFFAOYSA-N dodecylbenzene Chemical group CCCCCCCCCCCCC1=CC=CC=C1 KWKXNDCHNDYVRT-UHFFFAOYSA-N 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000002372 labelling Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 230000029058 respiratory gaseous exchange Effects 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- BDHFUVZGWQCTTF-UHFFFAOYSA-M sulfonate Chemical compound [O-]S(=O)=O BDHFUVZGWQCTTF-UHFFFAOYSA-M 0.000 description 1
- 238000010257 thawing Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 230000007306 turnover Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Abstract
The utility model discloses a butadiene tail gas recovery system, including reation kettle, reation kettle passes through pipeline intercommunication cooler, the cooler passes through pipeline intercommunication condensate tank, the liquid phase of condensate tank passes through pipeline intercommunication recovery jar, the gaseous phase of condensate tank passes through pipeline intercommunication washing unit, the washing unit passes through pipeline intercommunication first compressor, first compressor passes through pipeline intercommunication buffer tank, the buffer tank passes through pipeline intercommunication second compressor, the second compressor passes through pipeline intercommunication separation unit, the liquid phase of separation unit passes through pipeline intercommunication three-phase separator, the gaseous phase of three-phase separator passes through pipeline intercommunication first compressor, the water of three-phase separator passes through pipeline intercommunication blowdown house steward, the liquid phase of three-phase separator passes through pipeline intercommunication recovery jar, the gaseous phase of separation unit passes through pipeline intercommunication RTO incinerator; the utility model discloses make butadiene recovery reuse in the tail gas, reduction in production cost is applicable to the tail gas treatment.
Description
Technical Field
The utility model belongs to the technical field of chemical industry equipment, concretely relates to butadiene recovery system.
Background
In the production of nitrile rubber, the main raw materials are butadiene and acrylonitrile, the production process relates to the air defense of a reaction kettle, the cooling of a vacuum pump and the breathing of an acrylonitrile storage tank, in the process, butadiene and acrylonitrile are discharged outside, and the tail gas can cause pollution to water, soil and atmosphere, thereby seriously affecting the production and life of human beings; moreover, the discharged tail gas contains butadiene, which causes waste of raw materials and increases the investment cost of the raw materials. Therefore, the method has important significance in recycling the tail gas generated in the production process of the nitrile rubber.
SUMMERY OF THE UTILITY MODEL
The utility model provides a not enough of above prior art, provide a butadiene recovery system who makes butadiene recovery reuse in the tail gas, reduction in production cost.
In order to achieve the above object, the utility model adopts the following technical scheme:
the utility model provides a butadiene tail gas recovery system, includes reation kettle, reation kettle passes through pipeline intercommunication cooler, the cooler passes through pipeline intercommunication condensate tank, the liquid phase of condensate tank passes through pipeline intercommunication recovery jar, the gaseous phase of condensate tank passes through pipeline intercommunication washing unit, the washing unit passes through pipeline intercommunication first compressor, first compressor passes through pipeline intercommunication buffer tank, the buffer tank passes through pipeline intercommunication second compressor, the second compressor passes through pipeline intercommunication separating unit, the liquid phase of separating unit passes through pipeline intercommunication three-phase separator, the gaseous phase of three-phase separator passes through pipeline intercommunication first compressor, the water of three-phase separator passes through pipeline intercommunication blowdown house steward, the liquid phase of three-phase separator passes through pipeline intercommunication recovery jar, the gaseous phase of separating unit passes through pipeline intercommunication RTO incinerator.
By way of limitation, the inlet temperature of the cooler is 30 ℃ and the outlet temperature of the cooler is 5 ℃.
As another kind of injecture, the washing unit is three tower washings, and three tower washings include one-level washing tower, second grade washing tower and tertiary washing tower, one-level washing tower passes through the pipeline intercommunication second grade washing tower, second grade washing tower passes through pipeline intercommunication tertiary washing tower, tertiary washing tower passes through pipeline intercommunication circulating pump, the circulating pump passes through pipeline intercommunication water source.
As another limitation, a first water washing circulating pump is arranged at the bottom of the first-stage water washing tower and is used for driving water washing liquid to be sent into the top of the first-stage water washing tower from the bottom of the first-stage water washing tower; the bottom of the second-stage washing tower is provided with a second washing circulating pump, and the second washing circulating pump is used for driving washing liquid to be sent into the top of the second-stage washing tower from the bottom of the second-stage washing tower; and a third washing circulating pump is arranged at the bottom of the third-stage washing tower and used for driving the washing liquid to be sent into the top of the third-stage washing tower from the bottom of the third-stage washing tower.
As another limitation, the number of the first water-washing circulation pump, the number of the second water-washing circulation pump, and the number of the third water-washing circulation pump are 2, and each of the first water-washing circulation pump, the second water-washing circulation pump, and the third water-washing circulation pump is 1, and 1.
As another limitation, the separation unit includes a heat regenerator, a primary heat exchanger, a secondary heat exchanger, a tertiary heat exchanger, and a separator, the heat regenerator is communicated with the second compressor through a pipeline, the heat regenerator is communicated with the primary heat exchanger through a pipeline, a liquid phase of the primary heat exchanger is communicated with the three-phase separator through a pipeline, a gas phase of the primary heat exchanger is communicated with the secondary heat exchanger through a pipeline, a liquid phase of the secondary heat exchanger is communicated with the three-phase separator through a pipeline, a gas phase of the secondary heat exchanger is communicated with the tertiary heat exchanger through a pipeline, a liquid phase of the tertiary heat exchanger is communicated with the three-phase separator through a pipeline, a gas phase of the separator is communicated with the heat regenerator through a pipeline, the heat regenerator is communicated with the RTO incinerator through a pipeline, and a liquid phase of the separator is communicated with the three-phase separator through a pipeline.
As another definition, the cooling temperature of the primary heat exchanger is up to 5 ℃; the cooling temperature of the secondary heat exchanger is-30 ℃; the cooling temperature of the tertiary heat exchanger is-105 ℃.
As another definition, the tertiary heat exchanger comprises a cryogenic heat exchanger and a supercooling heat exchanger, and the cryogenic heat exchanger is communicated with the supercooling heat exchanger through a pipeline.
As another limitation, the number of the first-stage heat exchanger, the number of the second-stage heat exchanger and the number of the third-stage heat exchanger are 2, each of the first-stage heat exchanger, the second-stage heat exchanger and the third-stage heat exchanger forms a first group and a second group, the first-stage heat exchanger, the second-stage heat exchanger and the third-stage heat exchanger of the first group are all communicated with the first-stage heat exchanger, the second-stage heat exchanger and the third-stage heat exchanger of the second group through pipelines, and the pipelines among the first-stage heat exchanger, the second-stage heat exchanger and the third-stage heat exchanger are all provided with valves, and each valve is used for opening or closing a corresponding pipeline.
As another definition, the recovery tank is provided with a sampling port provided with a closure cap for opening or closing the sampling port.
Compared with the prior art, the utility model, the technological progress who gains lies in:
the reaction kettle of the utility model is communicated with the cold area device through a pipeline, and the tail gas is cooled in the cooler; the cooler is communicated with the condensate tank through a pipeline, the cooled tail gas enters the condensate tank, gas-liquid separation is carried out in the condensate tank, and most of water and acrylonitrile in the tail gas are condensed into a liquid phase which is sent to the recovery tank; the liquid phase of the condensate tank is communicated with the recovery tank through a pipeline, the gas phase of the condensate tank is communicated with the water washing unit through a pipeline, and the water washing unit is used for removing impurities in the tail gas; the washing unit is communicated with the first compressor through a pipeline, the first compressor is communicated with the buffer tank through a pipeline, the first compressor can overcome the resistance of the pipeline, the recovery amount of tail gas is improved, and the recovery rate of butadiene is increased; the buffer tank is communicated with a second compressor through a pipeline, the second compressor is communicated with the separation unit through a pipeline, and the second compressor provides power to enable tail gas to enter the separation unit; the liquid phase of the separation unit is communicated with the three-phase separator through a pipeline, the gas phase of the three-phase separator is communicated with the first compressor through a pipeline, so that the gas phase flashed from the three-phase separator by the tail gas enters the buffer tank through the first compressor, the water of the three-phase separator is communicated with the sewage discharge main pipe through a pipeline, the liquid phase of the three-phase separator is communicated with the recovery tank through a pipeline, the liquid phase in the recovery tank is a mixed solution of water, butadiene and acrylonitrile, the mixed solution can be reused, the butadiene in the tail gas is recovered and reused, and the production cost is reduced; the gas phase of the separation unit is communicated with the RTO incinerator through a pipeline, and the tail gas passing through the separation unit enters the RTO incinerator for incineration treatment so as to reach the tail gas emission standard; to sum up, the utility model discloses butadiene is retrieved and is recycled in making tail gas, and reduction in production cost is applicable to the tail gas treatment.
Drawings
The accompanying drawings are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention, and together with the description serve to explain the invention and not to limit the invention.
In the drawings:
fig. 1 is a schematic structural view of the present invention;
FIG. 2 is a schematic structural diagram of a separation unit according to an embodiment of the present invention;
fig. 3 is a schematic structural diagram of a primary heat exchanger and a primary heat exchanger, a secondary heat exchanger and a secondary heat exchanger, and a tertiary heat exchanger according to an embodiment of the present invention;
FIG. 4 is a schematic structural diagram of a cryogenic heat exchanger and a supercooling heat exchanger according to an embodiment of the present invention;
fig. 5 is a schematic structural diagram of a water washing unit according to an embodiment of the present invention.
Labeling components: 1-reaction kettle, 2-cooler, 3-condensate tank, 4-recovery tank, 5-water washing unit, 501-first-stage water washing tower, 502-second-stage water washing tower, 503-third-stage water washing tower, 504-first water washing circulating pump, 505-second water washing circulating pump, 506-third water washing circulating pump, 6-first compressor, 7-buffer tank, 8-second compressor, 9-separation unit, 901-regenerator, 902-first-stage heat exchanger, 903-second-stage heat exchanger, 904-third-stage heat exchanger, 90401-cryogenic heat exchanger, 90402-supercooling heat exchanger, 905-separator, 10-three-phase separator, 11-RTO, 12-circulating pump, 13-valve, 14-sampling port, 15-sealing cover.
Detailed Description
The preferred embodiments of the present invention will be described below with reference to the accompanying drawings. It should be understood that the preferred embodiments described herein are for purposes of illustration and explanation only and are not intended to limit the invention.
Embodiment butadiene tail gas recovery system
The embodiment discloses butadiene tail gas recovery system, as shown in fig. 1, including reation kettle 1, distributed Control System (DCS) is connected to reation kettle 1, and reation kettle 1 passes through pipeline intercommunication cold zone ware 2, and DCS is connected to cooler 2, and tail gas cools down in cooler 2, makes tail gas cool down to 5 ℃, and the tail gas technical parameter of business turn over cooler 2 is: inlet flow rate: 2289Nm 3 H, outlet flow: 2289Nm 3 H, inlet pressure: 1.2bar (A), outlet pressure: 1.15bar (A), inlet temperature: 30 ℃, outlet temperature: 5 ℃; the cooler 2 is communicated with a condensate tank 3 through a pipeline, the condensate tank 3 is also called a buffer condensate tank (SRLS 20-049), and the product number is as follows: SRLS0025, design pressure: 0.1/0.3MPa, pressure resistance test pressure 0.38MPa, design temperature: 40 ℃, container weight 1530Kg, volume: 3.9m 3 The working medium: raw material gas, production unit: wuxi Shirayl heat exchange equipment Limited company, condensate tank 3 connects DCS, and tail gas carries out gas-liquid separation in condensate tank 3 and is prior art, and condensate tank 3's liquid phase passes through the pipeline and linksLeading to the recovery tank 4, the recovery tank 4 is also called a product intermediate tank (SRLS 20-052), and the product number is: 205108, pressure vessel class: II, design pressure: 0.6MPa, pressure resistance test pressure: 0.75MPa, design temperature: 40 ℃, container dead weight: 765Kg, volume: 2.35m 3 The working medium: coagulated product, manufacturing unit: the Snieshi Rayleigh heat exchange equipment Limited company, the recovery tank 4 is provided with a sampling port 14, the sampling port 14 is provided with a sealing cover 15, the sealing cover 15 is used for opening or closing the sampling port 14, and the setting can be used for conveniently taking out the condensate in the recovery tank 4 and detecting and analyzing the components of the condensate; make most water and acrylonitrile condensation become the liquid phase in the tail gas and carry recovery jar 4 through the pipeline, the gaseous phase of condensate jar 3 passes through pipeline intercommunication washing unit 5, washing unit 5 connects DCS, washing unit 5 is used for getting rid of the impurity in the tail gas, such as methacrylic acid, impurity such as dodecylbenzene ring sodium sulfonate, washing unit 5 passes through pipeline intercommunication first compressor 6, first compressor 6 connects DCS, first compressor 6 passes through pipeline intercommunication buffer tank 7, first compressor 6 makes the tail gas that passes through washing unit 5 get into buffer tank 7 and compress, the resistance of pipeline can be overcome to first compressor 6, improve the recovery of tail gas, increase the rate of recovery of butadiene, buffer tank 7 passes through pipeline intercommunication second compressor 8, second compressor 8 connects DCS, the tail gas in buffer tank 7 gets into separating element 9 after second compressor 8 pressure boost, separating element 9 connects DCS, second compressor 8 passes through pipeline intercommunication separating element 9, the tail gas incinerator further separates in separating element 9, the tail gas that passes through separating element 9 gets into RTO 11 and burns the processing, in order to reach the tail gas emission standard, RTO 11 connects RTO separating element 9, the product passes through the condensate phase separator 10 through the three-phase condensate separator 10, the gaseous phase separator LS 10 that the condensate unit communicates with the three-phase condensate, the three-phase condensate separator 051 product is: 205107, design pressure: tube side (jacket) 1.0MPa, shell side (shell) 0.6MPa, pressure vessel type: II, pressure resistance test pressure: 1.41MPa for tube side (jacket), 0.75MPa for shell side (shell), container dead weight: 2483Kg, design temperature: tube side (jacket) 250 ℃, shell side (shell) 40 ℃, working medium: tube side (jacket) steam, shell side (shell) condensate, manufacturing unit: wuxi Shirayl Heat transfer apparatus Co LtdThe phase separator 10 is connected with DCS, the liquid phase of the separation unit 9 enters the three-phase separator 10 through a pipeline, the liquid phase is separated in the three-phase separator 10, a small amount of gas phase separated in the three-phase separator 10 enters the buffer tank 7 through the first compressor 6, the gas phase of the three-phase separator 10 is communicated with the first compressor 6 through a pipeline, water generated by the three-phase separator 10 is communicated with the sewage drainage main pipe through a pipeline, the mixed liquid of butadiene and acrylonitrile generated by the three-phase separator 10 is sent to the recovery tank 4 for recovery and utilization, and the liquid phase of the three-phase separator 10 is communicated with the recovery tank 4 through a pipeline; during operation, firstly, tail gas generated by a reaction kettle 1 enters a cooler 2 through a pipeline for cooling, then, the cooled tail gas enters a condensate tank 3, gas-liquid separation is carried out in the condensate tank 3, most of separated water and acrylonitrile are condensed into liquid phase, the liquid phase enters a recovery tank 4 through a pipeline for recycling, the separated gas phase enters a water washing unit 5 through a pipeline, then, the tail gas passing through the water washing unit 5 enters a buffer tank 7 through a first compressor 6 for compression, the tail gas passing through the buffer tank 7 for compression enters a separation unit 9 through pressurization of a second compressor 8, then, the tail gas is further separated in the separation unit 9, the tail gas separated by the separation unit 9 enters an RTO incinerator 11 for incineration treatment, the liquid phase separated by the separation unit 9 enters a three-phase separator 10 through a pipeline, finally, the liquid phase is separated in the three-phase separator 10, the gas phase generated in the three-phase separator 10 enters the buffer tank 7 through the first compressor 6, water generated in the three-phase separator 6 is discharged from a sewage main pipe through a three-phase pipeline, and butadiene and acrylonitrile mixed liquid generated by the three-phase separator 10 are recycled to the recovery tank 4; therefore, the advantage of the embodiment is that the arrangement is adopted, so that the butadiene in the tail gas is recycled, and the production cost is reduced.
A preferred structure of the water washing unit 5 in this embodiment is, as shown in fig. 1 and 5, that the water washing unit 5 is a three-tower water washing, the water washing tower adopts an existing water washing tower, the three-tower water washing includes a first-stage water washing tower 501, a second-stage water washing tower 502 and a third-stage water washing tower 503, the first-stage water washing tower 501 is communicated with the second-stage water washing tower 502 through a pipeline, the second-stage water washing tower 502 is communicated with the third-stage water washing tower 503 through a pipeline, the third-stage water washing tower 503 is communicated with the circulating pump 12 through a pipeline, the circulating pump 12 is communicated with a water source through a pipeline, when the water washing liquid is replaced, the liquid is replenished from the bottom of the next-stage water washing tower to the previous-stage water washing tower through the circulating pump 12, and fresh water is replenished in the third-stage water washing tower 503 to ensure the cleanliness of outlet tail gas; the bottom of the first-stage water washing tower 501 is provided with a first water washing circulating pump 504, the first water washing circulating pump 504 is used for driving water washing liquid to be sent to the top of the first-stage water washing tower 501 from the bottom of the first-stage water washing tower 501, the bottom of the second-stage water washing tower 502 is provided with a second water washing circulating pump 505, the second water washing circulating pump 505 is used for driving water washing liquid to be sent to the top of the second-stage water washing tower 502 from the bottom of the second-stage water washing tower 502, the bottom of the third-stage water washing tower 503 is provided with a third water washing circulating pump 506, the third water washing circulating pump 506 is used for driving water washing liquid to be sent to the top of the third-stage water washing tower 503 from the bottom of the third-stage water washing tower 503 for circulation; the first washing circulating pump 504, the second washing circulating pump 505 and the third washing circulating pump 506 are 2, each washing tower is circularly provided with 2 water system circulating pumps, and the 2 water system circulating pumps are 1 for 1, so that the situation that when one washing circulating pump is damaged, a standby water system circulating pump is immediately switched to work is avoided, and the cleanliness of outlet tail gas is ensured; the advantage of this embodiment lies in that adopts above-mentioned setting, has guaranteed the cleanliness factor of export tail gas.
One preferred structure of the separation unit 9 of this embodiment is, as shown in fig. 1, 2, 3, and 4, that the separation unit 9 includes a regenerator 902, a regenerator 902 (SRLE 20-069), product number: 205122, design pressure: tube side (jacket) 0.6MPa, shell side (shell) 0.6MPa, pressure vessel type: II, pressure resistance test pressure: tube side (jacket) 0.75MPa, shell side (shell) 0.75MPa, container dead weight: 918Kg, design temperature: tube side (jacket) -100 ℃, shell side (shell) 60 ℃, heat exchange area: 28m 2 The distance between the baffle plates: 274mm, manufacturing unit: tin-free poem rayleigh heat exchange equipment ltd, primary heat exchanger 902 is also called precooling heat exchanger (SRLE 20-068), product number: 205121, design pressure: tube side (jacket) 2.2MPa, shell side (shell) 1.7MPa, pressure vessel type: II, pressure resistance test pressure: tube side (jacket) 2.75MPa, shell side: (Shell) 2.75MPa, container dead weight: 993Kg. Design temperature: tube side (jacket) -19 ℃, shell side (shell) 60 ℃, heat exchange area: 29m 2 The distance between the baffle plates: 401mm, manufacturing unit: wuxi shi rayl heat exchange equipment ltd, secondary heat exchanger 903 is also called shallow cold heat exchanger (SRLE 20-062B), product number: 205113, design pressure: tube side (jacket) 2.2MPa, shell side (shell) 1.7MPa, pressure vessel type: II, pressure resistance test pressure: tube side (jacket) 2.75MPa, shell side (shell) 2.75MPa, vessel dead weight: 1083Kg, design temperature: tube side (jacket) -60 ℃, shell side (shell) -60 ℃, heat exchange area: 41m 2 The distance between the baffle plates: 276mm, manufacturing unit: the Wuxi Rayleigh heat exchange equipment Co Ltd, the tertiary heat exchanger 904 can adopt cryogen heat exchanger II (SELE 20-070), the product number: 205123, design pressure: tube side (jacket) 2.2MPa, shell side (shell) 2.2MPa, pressure vessel type: II, pressure resistance test pressure: tube side (jacket) 2.75MPa, shell side (shell) 2.75MPa, vessel dead weight: 530Kg, design temperature: tube side (jacket) -80 ℃, shell side (shell) -130 ℃, heat exchange area: 12m 2 The distance between the baffle plates: 244mm, manufacturing unit: wuxi shi rayl heat exchange equipment ltd, separator 905, separator is also called high efficiency separator (SRLS 20-054), product number: 207092, pressure vessel class: i, design pressure: 0.6MPa, pressure resistance test pressure: 0.75MPa, design temperature: -130 ℃, container dead weight: 350Kg, volume: 0.58m 3 The manufacturing unit is as follows: the system comprises a Wunshi Rayleigh heat exchange equipment Co., ltd, 2 primary heat exchangers 902, 2 secondary heat exchangers 903 and 2 tertiary heat exchangers 904, wherein the first group comprises 1 primary heat exchanger 902, 1 secondary heat exchanger 903 and 1 tertiary heat exchanger 904, the second group comprises 1 primary heat exchanger 902, 1 secondary heat exchanger 903 and 1 tertiary heat exchanger 904,2, the air outlets of the primary heat exchangers 902 are communicated through pipelines, the pipelines are provided with valves 13, and the valves 13 are used for opening or closing the pipelines; the discharge ports of the 2 secondary heat exchangers 903 are communicated through a pipeline, the pipeline is provided with a valve 13, and the valve 13 is used for opening or closing the pipeline; the discharge ports of the 2 tertiary heat exchangers 904 are communicated through a pipeline, the pipeline is provided with a valve 13, and the valve 13 is used for opening or closing the pipeline; this arrangement is used in the first groupWhen the resistance is increased to an alarm value, the system automatically switches to a second group of heat exchangers to work, the system is a Distributed Control System (DCS), then the first group of heat exchangers are subjected to back flushing, unfreezing and defrosting work by utilizing the hot exhaust of a refrigeration compressor, and the operation is repeated in a circulating mode; the heat regenerator 901 is communicated with the second compressor 8 through a pipeline, the heat regenerator 901 is communicated with a first-stage heat exchanger 902 through a pipeline, the tail gas after washing is cooled to 5 ℃ through the heat regenerator 901 and the first-stage heat exchanger 902, the separated water, butadiene and a small amount of acrylonitrile are condensed into a liquid phase and sent to a three-phase separator 10, the gas phase tail gas passing through the heat regenerator 901 and the first-stage heat exchanger 902 enters a second-stage heat exchanger 903 through a pipeline, the tail gas is cooled to-30 ℃ in the second-stage heat exchanger 903, a part of butadiene and a small amount of acrylonitrile are condensed again and sent to the three-phase separator 10, the gas phase tail gas generated by the second-stage heat exchanger 903 passes through a pipeline third-stage heat exchanger 904, the third-stage heat exchanger 904 comprises a cryogenic heat exchanger 90401 and a supercooling heat exchanger 90402, a cryogenic heat exchanger 90401 (SRLE 20-063A), and the product number: 205114, design pressure: tube side (jacket) 2.2MPa, shell side (shell) 1.7MPa, pressure vessel type: II, pressure resistance test pressure: tube side (jacket) 2.75MPa, shell side (shell) 2.74MPa, vessel dead weight: 2082Kg, design temperature: tube side (jacket) -120 ℃, shell side (shell) -120 ℃, heat exchange area: 96m 2 The distance between the baffle plates: 310mm, manufacturing unit: snieless Rayleigh heat exchange equipment, inc., cryogenic heat exchanger 90401 is communicated with secondary heat exchanger 903 through a pipeline, cryogenic heat exchanger 90401 is communicated with supercooling heat exchanger 90402 through a pipeline, supercooling heat exchanger 90402 (SRLE 20-064B), product number: 205117, design pressure: tube side (jacket) 2.2MPa, shell side (shell) 1.7MPa, pressure vessel type: II, pressure resistance test pressure: tube side (jacket) 2.75MPa, shell side (shell) 2.75MPa, vessel dead weight: 1059Kg, design temperature: tube side (jacket) -140 ℃, shell side (shell) -140 ℃, heat exchange area: 41m 2 The distance between the baffle plates: 316mm, manufacturing unit: the tin-free Shirayley heat exchange equipment Limited, a supercooling heat exchanger 90402 is communicated with a separator 905 through a pipeline, tail gas is cooled to-105 ℃ in a three-stage heat exchanger 904 and is further condensed to obtain butadiene and trace acrylonitrile which are sent to a three-phase separator 10, gas-phase tail gas generated by the three-stage heat exchanger 904 enters the separator 905 through a pipeline, and the separator 905 is efficientThe tail gas is subjected to gas-liquid separation in the separator 905, the separated gas phase returns to the heat regenerator 901 through a pipeline and is reheated to normal temperature, the reheated tail gas is conveyed to the RTO incinerator 11 through a pipeline and is incinerated, so that more than 90% of butadiene and acrylonitrile in the tail gas can be condensed and separated out, and the liquid phase of the separator 905 is conveyed to the three-phase separator 10 through a pipeline; therefore, the advantage of the embodiment is that by adopting the arrangement, the recycling of butadiene in the tail gas is improved, and the production cost is reduced.
The embodiment of the utility model provides a theory of operation as follows:
during operation, firstly, tail gas generated by a reaction kettle 1 enters a cooler 2 through a pipeline for cooling, then, the cooled tail gas enters a condensate tank 3, gas-liquid separation is carried out in the condensate tank 3, most of separated water and acrylonitrile are condensed into a liquid phase, the liquid phase enters a recovery tank 4 through a pipeline for recycling, the separated gas phase enters a water washing unit 5 through a pipeline, then, the tail gas passing through the water washing unit 5 enters a buffer tank 7 through a first compressor 6 for compression, the tail gas passing through the buffer tank 7 for compression enters a separation unit 9 through pressurization of a second compressor 8, then, the tail gas is further separated in the separation unit 9, the tail gas separated through the separation unit 9 enters an RTO incinerator 44 for incineration treatment, the liquid phase separated out by the separation unit 9 enters a three-phase separator 10 through a pipeline, finally, the liquid phase is separated in the three-phase separator 10, the gas phase generated in the three-phase separator 10 enters the buffer tank 7 through the first compressor 6, water generated in the three-phase separator 10 is discharged from a sewage main pipe, and butadiene and acrylonitrile generated in the three-phase separator 10 are recycled to the recovery tank 4.
The system adopts a Distributed Control System (DCS) to monitor the process, automatically detects and adjusts important parameters in the process in a central control room, and ensures stable operation and safe production of the system; the automatic control adopts mature and is proved to be a reliable control scheme such as PID single loop, cascade, ratio and the like by practice.
The system is not described in detail, such as the buffer tank, the compressor, the valve arrangement, the connection of the distributed control system, and other arrangements, which are conventional in the art.
Finally, it should be noted that: although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications may be made to the embodiments described in the foregoing embodiments, or equivalents may be substituted for elements thereof. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the scope of the protection of the claims of the present invention.
Claims (10)
1. The utility model provides a butadiene tail gas recovery system, includes reation kettle (1), its characterized in that: the reaction kettle (1) is communicated with a cooler (2) through a pipeline, the cooler (2) is communicated with a condensate tank (3) through a pipeline, a liquid phase of the condensate tank (3) is communicated with a recovery tank (4) through a pipeline, a gas phase of the condensate tank (3) is communicated with a washing unit (5) through a pipeline, the washing unit (5) is communicated with a first compressor (6) through a pipeline, the first compressor (6) is communicated with a buffer tank (7) through a pipeline, the buffer tank (7) is communicated with a second compressor (8) through a pipeline, the second compressor (8) is communicated with a separation unit (9) through a pipeline, a liquid phase of the separation unit (9) is communicated with a three-phase separator (10) through a pipeline, a gas phase of the three-phase separator (10) is communicated with the first compressor (6) through a pipeline, water of the three-phase separator (10) is communicated with a blowdown header pipe through a pipeline, a liquid phase of the three-phase separator (10) is communicated with the recovery tank (4) through a pipeline, and a gas phase of the separation unit (9) is communicated with an RTO incinerator (11) through a pipeline.
2. The butadiene tail gas recovery system of claim 1, wherein: the inlet temperature of the cooler (2) is 30 ℃, and the outlet temperature of the cooler (2) is 5 ℃.
3. The butadiene tail gas recovery system of claim 1, wherein: washing unit (5) are three towers washing, and three towers washing includes one-level washing tower (501), second grade washing tower (502) and tertiary washing tower (503), one-level washing tower (501) pass through the pipeline intercommunication second grade washing tower (502), tertiary washing tower (503) of pipeline intercommunication is passed through in second grade washing tower (502), tertiary washing tower (503) pass through pipeline intercommunication tertiary washing tower (503), pipeline intercommunication circulating pump (12) are passed through in tertiary washing tower (503), circulating pump (12) pass through pipeline intercommunication water source.
4. The butadiene tail gas recovery system of claim 3, wherein: the bottom of the first-stage water washing tower (501) is provided with a first water washing circulating pump (504), and the first water washing circulating pump (504) is used for driving water washing liquid to be sent into the top of the first-stage water washing tower (501) from the bottom of the first-stage water washing tower (501); the bottom of the secondary water washing tower (502) is provided with a second water washing circulating pump (505), and the second water washing circulating pump (505) is used for driving water washing liquid to be sent into the top of the secondary water washing tower (502) from the bottom of the secondary water washing tower (502); and a third washing circulating pump (506) is arranged at the bottom of the third-stage washing tower (503), and the third washing circulating pump (506) is used for driving washing liquid to be sent into the top of the third-stage washing tower (503) from the bottom of the third-stage washing tower (503).
5. The butadiene tail gas recovery system of claim 4, wherein: the number of the first water washing circulating pump (504), the number of the second water washing circulating pump (505) and the number of the third water washing circulating pump (506) are 2, and each of the first water washing circulating pump (504), the second water washing circulating pump (505) and the third water washing circulating pump (506) is 1 for 1.
6. The butadiene tail gas recovery system of claim 1, wherein: the separation unit (9) comprises a heat regenerator (901), a primary heat exchanger (902), a secondary heat exchanger (903), a tertiary heat exchanger (904) and a separator (905), wherein the heat regenerator (901) is communicated with the second compressor (8) through a pipeline, the heat regenerator (901) is communicated with the primary heat exchanger (902) through a pipeline, a liquid phase of the primary heat exchanger (902) is communicated with the three-phase separator (10) through a pipeline, a gas phase of the primary heat exchanger (902) is communicated with the secondary heat exchanger (903) through a pipeline, a liquid phase of the secondary heat exchanger (903) is communicated with the three-phase separator (10) through a pipeline, a gas phase of the separator (905) is communicated with the heat regenerator (901) through a pipeline, the heat regenerator (901) is communicated with the RTO incinerator (11) through a pipeline, and a liquid phase of the separator (905) is communicated with the three-phase separator (10) through a pipeline.
7. The butadiene tail gas recovery system of claim 6, wherein: the cooling temperature of the primary heat exchanger (902) is 5 ℃; the cooling temperature of the secondary heat exchanger (903) is-30 ℃; the cooling temperature of the tertiary heat exchanger (904) is to-105 ℃.
8. The butadiene tail gas recovery system of claim 7, wherein: tertiary heat exchanger (904) includes cryogenic heat exchanger (90401) and subcooling heat exchanger (90402), cryogenic heat exchanger (90401) passes through the pipeline intercommunication subcooling heat exchanger (90402).
9. The butadiene tail gas recovery system of claim 8, wherein: the heat exchanger comprises a primary heat exchanger (902), a secondary heat exchanger (903) and a tertiary heat exchanger (904), wherein the primary heat exchanger (902), the secondary heat exchanger (903) and the tertiary heat exchanger (904) form a first group and a second group, the primary heat exchanger (902), the secondary heat exchanger (903) and the tertiary heat exchanger (904) of the first group are communicated with the primary heat exchanger (902), the secondary heat exchanger (903) and the tertiary heat exchanger (904) of the second group through pipelines, valves (13) are arranged on the pipelines among the primary heat exchanger (902), the secondary heat exchanger (903) and the tertiary heat exchanger (904), and the valves (13) are used for opening or closing corresponding pipelines.
10. The butadiene tail gas recovery system of claim 1, wherein: the recovery tank (4) is provided with a sampling port (14), the sampling port (14) is provided with a sealing cover (15), and the sealing cover (15) is used for opening or closing the sampling port (14).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221128995.6U CN217568114U (en) | 2022-05-11 | 2022-05-11 | Butadiene tail gas recovery system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221128995.6U CN217568114U (en) | 2022-05-11 | 2022-05-11 | Butadiene tail gas recovery system |
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| Publication Number | Publication Date |
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| CN217568114U true CN217568114U (en) | 2022-10-14 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202221128995.6U Active CN217568114U (en) | 2022-05-11 | 2022-05-11 | Butadiene tail gas recovery system |
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| CN (1) | CN217568114U (en) |
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