CN220496334U - Isobutane normal reaction waste gas recovery system - Google Patents
Isobutane normal reaction waste gas recovery system Download PDFInfo
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- CN220496334U CN220496334U CN202322033684.2U CN202322033684U CN220496334U CN 220496334 U CN220496334 U CN 220496334U CN 202322033684 U CN202322033684 U CN 202322033684U CN 220496334 U CN220496334 U CN 220496334U
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- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 title claims abstract description 80
- 238000011084 recovery Methods 0.000 title claims abstract description 44
- 239000001282 iso-butane Substances 0.000 title claims abstract description 40
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 28
- 239000002912 waste gas Substances 0.000 title claims abstract description 20
- 238000006356 dehydrogenation reaction Methods 0.000 claims abstract description 84
- 238000000926 separation method Methods 0.000 claims abstract description 61
- 239000001257 hydrogen Substances 0.000 claims abstract description 53
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 53
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 48
- 230000000087 stabilizing effect Effects 0.000 claims abstract description 9
- 239000007788 liquid Substances 0.000 claims description 62
- 239000003381 stabilizer Substances 0.000 claims description 45
- 239000007789 gas Substances 0.000 claims description 39
- 239000012071 phase Substances 0.000 claims description 35
- 239000000110 cooling liquid Substances 0.000 claims description 31
- 239000007791 liquid phase Substances 0.000 claims description 29
- 238000001816 cooling Methods 0.000 claims description 26
- 238000010992 reflux Methods 0.000 claims description 23
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 13
- 239000003507 refrigerant Substances 0.000 claims description 9
- 150000002431 hydrogen Chemical class 0.000 abstract description 7
- 229910052799 carbon Inorganic materials 0.000 description 15
- 239000007795 chemical reaction product Substances 0.000 description 12
- 238000005755 formation reaction Methods 0.000 description 11
- 238000004064 recycling Methods 0.000 description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 10
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 7
- 238000009833 condensation Methods 0.000 description 6
- 230000005494 condensation Effects 0.000 description 6
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 6
- YEJRWHAVMIAJKC-UHFFFAOYSA-N 4-Butyrolactone Chemical compound O=C1CCCO1 YEJRWHAVMIAJKC-UHFFFAOYSA-N 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 4
- 239000012530 fluid Substances 0.000 description 4
- 239000007809 chemical reaction catalyst Substances 0.000 description 3
- 230000008021 deposition Effects 0.000 description 3
- 230000002349 favourable effect Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000009835 boiling Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000007792 gaseous phase Substances 0.000 description 2
- FPYJFEHAWHCUMM-UHFFFAOYSA-N maleic anhydride Chemical compound O=C1OC(=O)C=C1 FPYJFEHAWHCUMM-UHFFFAOYSA-N 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 230000006641 stabilisation Effects 0.000 description 2
- 238000011105 stabilization Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
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Abstract
The utility model relates to an isobutane normal reaction waste gas recovery system which comprises a normal system, a dehydrogenation tower and a stabilizing tower, wherein the dehydrogenation tower is connected with a discharge port of the normal system through a pipeline, a separation unit is arranged between the dehydrogenation tower and the stabilizing tower and is respectively connected with the dehydrogenation tower and the stabilizing tower, the separation unit is connected with the normal system through a circulating device, and the circulating device is used for sending circulating hydrogen into the normal system. Compared with the prior art, the utility model has the advantages of cost saving, high purity of the recovered hydrogen, and the like.
Description
Technical Field
The utility model relates to an exhaust gas recovery system, in particular to an isobutane normal reaction exhaust gas recovery system.
Background
N-butane is an important organic chemical raw material, and is mainly used for preparing maleic anhydride and gamma-butyrolactone, and along with the continuous increase of the demand of the maleic anhydride and the gamma-butyrolactone, the demand of the n-butane is also continuously increased. At present, n-butane is mainly obtained through normal formation reaction of isobutane, and a reactor of the normal formation reaction device of isobutane is subjected to catalytic reaction under the condition of hydrogen at a certain temperature and under a certain pressure, so that a product n-butane is generated.
At present, waste gas generated in the normal formation reaction of isobutane is mainly used as fuel gas for combustion treatment, and some unreacted complete hydrogen exists in the waste gas, so that the waste gas is used as fuel and is low in energy consumption due to high cost of hydrogen, thereby wasting hydrogen resources and greatly increasing raw material cost; in addition, because of the existence of low-carbon alkane in the normal reaction product, when the hydrogen is recovered for recycling, the purity of the hydrogen is low, and certain influence is generated on the normal reaction.
Disclosure of Invention
The utility model aims to provide an isobutane normal reaction waste gas recovery system which is cost-saving and high in purity of recovered hydrogen.
The utility model provides an normal reaction waste gas recovery system of isobutane, includes normal system, dehydrogenation tower and stabilizer, the dehydrogenation tower passes through the discharge gate of pipeline with normal system to be connected, be equipped with separation unit between dehydrogenation tower and the stabilizer, separation unit respectively with dehydrogenation tower and stabilizer are connected, separation unit pass through circulating device with normal system connects, circulating device is used for sending circulating hydrogen into in the normal system.
In the technical scheme, the waste gas recovery system suitable for the isobutane normal reaction system comprises a normal system, a dehydrogenation tower and a stabilizer, wherein the normal system, the dehydrogenation tower and the stabilizer are sequentially arranged and form a circulation, the dehydrogenation tower is connected with a discharge port of the isobutane normal system through a pipeline, a normal reaction product enters the dehydrogenation tower through the pipeline, the normal reaction product is divided into a light component containing hydrogen and a heavy component containing low-carbon alkane in the dehydrogenation tower, the light component is positioned at the upper part of the dehydrogenation tower, the heavy component is positioned at the lower part of the dehydrogenation tower, the hydrogen and the low-carbon alkane in the normal reaction product can be separated, the separation unit is connected with the top of the dehydrogenation tower, the light component at the top of the dehydrogenation tower enters the separation unit through a pipeline, the separation unit can separate the hydrogen in the light component and send the hydrogen into a circulation device connected with the separation unit, and the circulation device sends the hydrogen into the isobutane normal system, so that the hydrogen and the hydrogen is completely used and the recycling cost is reduced, and the recycling cost is fully realized; in addition, this application isobutane normal reaction waste gas recovery system is through the dehydrogenation tower that sets up, can carry out preliminary separation with normal formation reaction product, obtain light component and heavy component that contains hydrogen, then rethread the separation unit further separates, makes the hydrogen further purification and separates out to make the hydrogen purity that obtains improve by a wide margin, send back after the normal system of isobutane is favorable to improving the yield of normal formation main reaction, also can avoid the carbon deposition of main reaction catalyst simultaneously, prolongs its life.
Further, as a preferable technical scheme, the separation unit comprises a cooling device and a deep cooling device, the cooling device comprises a cooler and a cooling liquid separating tank, the deep cooling device comprises a deep cooler and a deep cooling liquid separating tank, and the cooler, the cooling liquid separating tank, the deep cooler and the deep cooling liquid separating tank are sequentially arranged.
In the above technical scheme, the separation unit includes cooling device and cryogenic device, cooling device and cryogenic device set gradually, the light fraction of dehydrogenation tower top gets into in proper order through the pipeline cooling device and cryogenic device, cooling device includes cooler and cooling liquid separating pot, the cooler is used for the light fraction of cooling entering, and the light fraction is under the condensation of cooler the preliminary separation is liquid phase and gaseous phase in the cooling liquid separating pot, cryogenic device includes cryogenic device and cryogenic liquid separating pot, the cryogenic device is used for to the noncondensable or the noncondensable steam after the cooler cooling carries out further condensation, through gaseous phase and liquid phase that the cryogenic device condensation obtained get into in the cryogenic liquid separating pot, cooler, cooling liquid separating pot, cryogenic device and cryogenic liquid separating pot set gradually in proper order and connect.
Further, as a preferable technical scheme, a feed inlet of the cooler is connected with the dehydrogenation tower, a discharge outlet of the cooler is connected with an inlet of the cooling liquid separating tank, a gas phase outlet of the cooling liquid separating tank is connected with the cryocooler, a gas phase outlet of the cryogenic liquid separating tank is connected with the circulating device, and a liquid phase outlet of the cryogenic liquid separating tank is connected with the stabilizer.
According to the technical scheme, the feeding port of the cooler is connected with the top of the dehydrogenation tower, the discharging port of the cooler is connected with the inlet of the cooling liquid separating tank, light components in the dehydrogenation tower enter the cooler through a pipeline to be cooled, the gas phase outlet at the top of the cooling liquid separating tank is connected with the cryogenic cooler, the light components condensed by the cooler are separated into gas phase and liquid phase in the cooling liquid separating tank, the gas phase enters the cryogenic cooler through the pipeline, the gas phase which is not completely condensed is further condensed by the cryogenic cooler to obtain hydrogen and liquid phase containing carbon-containing alkane, and the hydrogen can be completely separated through the further treatment of the cryogenic cooler and the cryogenic liquid separating tank, so that the purity of the hydrogen is effectively improved; and the hydrogen obtained by separation in the cryogenic liquid separation tank enters the circulating device through a gas phase outlet at the top, the hydrogen is sent into an isobutane normal system by the circulating device for recycling, and the rest liquid phase part containing carbon-containing alkane is sent into the stabilizer through a liquid phase outlet at the bottom of the cryogenic liquid separation tank for subsequent recovery treatment.
Further, as a preferable technical scheme, the separation unit further comprises a reflux pump, wherein an inlet end of the reflux pump is connected with a liquid phase outlet of the cooling liquid separating tank, and an outlet end of the reflux pump is connected with the dehydrogenation tower.
In the above technical scheme, the separation unit is further provided with a reflux pump, the inlet end and the outlet end of the reflux pump are respectively connected with the liquid phase outlet at the bottom of the cooling liquid separating tank and the dehydrogenation tower, the reflux pump is used for refluxing the liquid phase part obtained by cooling in the cooling liquid separating tank into the dehydrogenation tower, and the reflux is arranged to effectively improve the separation effect of the dehydrogenation tower, so that the subsequent recovery of low-carbon alkane is facilitated.
Further, as an optimal technical scheme, the circulating device comprises a circulating liquid separating tank and a compressor, wherein the circulating liquid separating tank is connected with a gas phase outlet of the cryogenic liquid separating tank, and the compressor is respectively connected with the circulating liquid separating tank and the normal system.
According to the technical scheme, the circulating liquid separating tank and the compressor are sequentially arranged, the circulating liquid separating tank is connected with a gas phase outlet at the top of the cryogenic liquid separating tank, hydrogen obtained after being processed by the cooler and the cryogenic device enters the circulating liquid separating tank for storage, and then the hydrogen is pressurized by the compressor and is sent into the isobutane normal system for recycling.
Further, as a preferable technical scheme, the cooler and the cryocooler are both provided with a liquid inlet and a liquid outlet, and the liquid inlet and the liquid outlet are used for the inlet and the outlet of the refrigerant.
In the above technical scheme, the cooler and the cryocooler are both provided with a liquid inlet and a liquid outlet, and the liquid inlet and the liquid outlet are used for providing a passage for the refrigerant, and the low boiling point components in the cooler and the cryocooler are condensed through the refrigerant so as to ensure that the hydrogen can be completely separated.
Further, as a preferable technical scheme, the dehydrogenation tower is connected with the stabilizer tower through a pipeline, the stabilizer tower is connected with a recovery device, and the recovery device is used for recovering the light alkane in the stabilizer tower.
In the above technical scheme, the dehydrogenation tower bottom is connected with the stabilizer through the pipeline, heavy components at the dehydrogenation tower bottom enter the stabilizer through the pipeline, the bottom of the stabilizer is connected with a recovery device, the recovery device is used for recovering alkane, wherein the heavy components at the bottom of the stabilizer comprise C4 alkane, the liquid phase part in the cryogenic liquid separation tank comprises C3 alkane, and after the heavy components are sent into the stabilizer, the heavy components are recovered and collected through the recovery device, so that the full utilization of resources is realized, and certain economic benefit is promoted for enterprises.
Further, as a preferable technical scheme, the stabilizer is also connected with an incineration device, and the incineration device is connected with a gas phase outlet of the stabilizer.
In the above technical scheme, the incineration device is connected to the top of the stabilizer, and the waste gas in the stabilizer enters the incineration device from a gas phase outlet at the top of the stabilizer, and is subjected to concentrated incineration treatment by the incineration device.
Further, as a preferable technical scheme, the dehydrogenation tower is provided with a heat exchange device, and the heat exchange device is connected with the dehydrogenation tower.
In the technical scheme, one side of the dehydrogenation tower is connected with a heat exchange device, and the heat exchange device is used for exchanging heat of materials in the dehydrogenation tower.
Compared with the prior art, the isobutane normal system waste gas has the following beneficial effects:
cost is practiced thrift, this application through the separation unit that sets up, can separate out the hydrogen in the normal formation reaction product of isobutane, and send into with in the circulating device that separation unit is connected, by again in circulating device sends hydrogen into the normal formation system of isobutane, accomplish the recovery and the cyclic utilization of hydrogen, realize the make full use of resource, effectively reduce cost.
The hydrogen recovery purity is high, the dehydrogenation tower that this application set up can carry out preliminary separation with normal formation reaction product, obtains light component and heavy component that contains hydrogen, later rethread separation unit further separates to make hydrogen and low-carbon alkane further separate, make the hydrogen purity that obtains improve by a wide margin, send back behind the normal system of isobutane, be favorable to improving normal formation main reaction's yield, also can avoid the carbon deposition of main reaction catalyst simultaneously, prolong its life.
Drawings
FIG. 1 is a schematic diagram of an embodiment of an isobutane normal reaction waste gas recovery system.
Reference numerals in the drawings illustrate:
t1-dehydrogenation column; t2-stabilizer; l1-a cooler; l2-chiller; f1-cooling a liquid separating tank; f2-a cryogenic liquid separation tank; f3-circulating liquid separating tank; b1-a reflux pump; y1-compressor; s1, a recovery device; s2-an incineration device; h1-heat exchange device.
Detailed Description
The isobutane normal reaction offgas recovery system according to the present utility model will be described in further detail with reference to specific examples and drawings.
Referring to fig. 1, in a preferred embodiment of the present utility model, an isobutane normal reaction waste gas recovery system includes a normal system, a dehydrogenation tower T1 and a stabilizer tower T2, wherein the dehydrogenation tower T1 is connected to a discharge port of the normal system through a pipeline, a separation unit is disposed between the dehydrogenation tower T1 and the stabilizer tower T2, the separation unit is connected to the dehydrogenation tower T1 and the stabilizer tower T2, respectively, and the separation unit is connected to the normal system through a circulation device, and the circulation device is used for sending circulated hydrogen into the normal system.
In the above embodiment, the application is an exhaust gas recovery system suitable for an isobutane normal reaction system, including a normal system, a dehydrogenation tower T1 and a stabilizer tower T2, where the normal system, the dehydrogenation tower T1 and the stabilizer tower T2 are sequentially arranged and form a cycle, the dehydrogenation tower T1 is connected with a discharge port of the isobutane normal reaction system through a pipeline, a normal reaction product enters the dehydrogenation tower T1 through a pipeline, the normal reaction product is separated into a light component containing hydrogen and a heavy component containing low-carbon alkane in the dehydrogenation tower T1, the light component is located at the upper part of the dehydrogenation tower T1, the heavy component is located at the lower part of the dehydrogenation tower T1, hydrogen and low-carbon alkane in the normal reaction product can be separated, the separation unit is connected with the top of the dehydrogenation tower T1, the light component at the top of the dehydrogenation tower T1 enters the separation unit through a pipeline, the separation unit can separate the hydrogen in the light component, and sends the light component into the separation unit to the circulation device connected with the separation unit, and the hydrogen is sent into the circulation device to complete recycling of the normal butane, thereby realizing full utilization of the hydrogen and recycling by the circulation device; in addition, this application isobutane normal reaction waste gas recovery system is through setting up dehydrogenation tower T1, can carry out preliminary separation with normal formation reaction product, obtain light component and heavy component that contains hydrogen, later rethread separation unit further separates, makes the hydrogen further purification and separates out to make the hydrogen purity that obtains improve by a wide margin, after sending back the normal system of isobutane, be favorable to improving the yield of normal formation main reaction, also can avoid the carbon deposition of main reaction catalyst simultaneously, prolong its life.
Referring to fig. 1, in a preferred embodiment of the present utility model, the separation unit includes a cooling device including a cooler L1 and a cooling liquid-separating tank F1, and a cryogenic device including a cryogenic device L2 and a cryogenic liquid-separating tank F2, and the cooler L1, the cooling liquid-separating tank F1, the cryogenic device L2 and the cryogenic liquid-separating tank F2 are sequentially disposed.
In the above embodiment, the separation unit includes a cooling device and a cryogenic device, the cooling device and the cryogenic device are sequentially disposed, light components at the top of the dehydrogenation tower T1 sequentially enter the cooling device and the cryogenic device through pipelines, the cooling device includes a cooler L1 and a cooling liquid separating tank F1, the cooler L1 is used for cooling the entering light components, the light components are primarily separated into a liquid phase and a gas phase in the cooling liquid separating tank F1 under the condensation action of the cooler L1, the cryogenic device includes a cryogenic device L2 and a cryogenic liquid separating tank F2, the cryogenic device L2 is used for further condensing noncondensable or noncondensable liquid after being cooled by the cooler L1, the gas phase and the liquid phase obtained by condensation of the cryogenic device L2 enter the cryogenic liquid separating tank F2, and the cooler L1, the cooling liquid separating tank F1, the cryogenic device L2 and the cryogenic liquid separating tank F2 are sequentially disposed and connected.
Referring to fig. 1, in a preferred embodiment of the present utility model, a feed inlet of the cooler L1 is connected to the dehydrogenation tower T1, a discharge outlet is connected to an inlet of the cooling liquid separating tank F1, a gas phase outlet of the cooling liquid separating tank F1 is connected to the chiller L2, a gas phase outlet of the cryogenic liquid separating tank F2 is connected to the circulation device, and a liquid phase outlet of the cryogenic liquid separating tank F2 is connected to the stabilization tower T2.
In the above embodiment, the feed inlet of the cooler L1 is connected to the top of the dehydrogenation tower T1, the discharge outlet is connected to the inlet of the cooling liquid separating tank F1, the light component in the dehydrogenation tower T1 enters the cooler L1 through a pipeline to be cooled, the gas phase outlet at the top of the cooling liquid separating tank F1 is connected to the chiller L2, the light component condensed by the cooler L1 is separated into a gas phase and a liquid phase in the cooling liquid separating tank F1, the gas phase enters the chiller L2 through the pipeline, the gas phase which is not completely condensed is further condensed by the chiller L2 to obtain hydrogen and a liquid phase containing carbon-containing alkane, and the hydrogen can be completely separated through the further treatment of the chiller L2 and the cryogenic liquid separating tank F2, so that the purity of the hydrogen is effectively improved; the hydrogen separated in the cryogenic liquid separation tank F2 enters the circulating device through a gas phase outlet at the top, the hydrogen is sent into an isobutane normal system for recycling by the circulating device, and the rest liquid phase part containing carbon-containing alkane is sent into the stabilizing tower T2 through a liquid phase outlet at the bottom of the cryogenic liquid separation tank F2 for subsequent recovery treatment.
Referring to fig. 1, in a preferred embodiment of the present utility model, the separation unit further includes a reflux pump B1, an inlet end of the reflux pump B1 is connected to the liquid phase outlet of the cooling liquid separating tank F1, and an outlet end of the reflux pump B1 is connected to the dehydrogenation tower T1.
In the above embodiment, the separation unit is further provided with a reflux pump B1, an inlet end and an outlet end of the reflux pump B1 are respectively connected with a liquid phase outlet at the bottom of the cooling liquid separation tank F1 and the dehydrogenation tower T1, the reflux pump B1 is used for refluxing a liquid phase part obtained by cooling in the cooling liquid separation tank F1 into the dehydrogenation tower T1, and the reflux pump B1 is used as reflux of the dehydrogenation tower T1, so that the separation effect of the dehydrogenation tower T1 can be effectively improved by setting reflux, and the subsequent recovery of low-carbon alkane is facilitated.
Referring to fig. 1, in a preferred embodiment of the present utility model, the circulating device includes a circulating fluid tank F3 and a compressor Y1, the circulating fluid tank F3 is connected to the gas phase outlet of the cryogenic fluid tank F2, and the compressor Y1 is connected to the circulating fluid tank F3 and the normal system, respectively.
In the above embodiment, the circulating liquid separation tank F3 and the compressor Y1 are sequentially disposed, the circulating liquid separation tank F3 is connected to a gas phase outlet at the top of the cryogenic liquid separation tank F2, and the hydrogen obtained after condensation treatment by the cooler L1 and the cryogenic device L2 enters the circulating liquid separation tank F3 to be stored, and is then pressurized by the compressor Y1, and is sent into the isobutane normal system to be recycled.
Referring to fig. 1, in a preferred embodiment of the present utility model, the cooler L1 and the chiller L2 are provided with a liquid inlet and a liquid outlet, which are used for the inlet and outlet of the refrigerant.
In the above embodiment, the cooler L1 and the chiller L2 are both provided with a liquid inlet and a liquid outlet, and the liquid inlet and the liquid outlet are used for providing a passage for the refrigerant, and the low boiling components in the cooler L1 and the chiller L2 are condensed by the refrigerant, so that the hydrogen can be completely separated.
In this embodiment, preferably, the refrigerant of the cooler L1 is circulating water, the refrigerant of the chiller L2 is chilled water, CWS in fig. 1 represents the water supply of the circulating water, CWR represents the water return of the circulating water, BWS represents the water supply of the chilled water, and BWR represents the water return of the chilled water.
Referring to fig. 1, in a preferred embodiment of the present utility model, the dehydrogenation tower T1 is connected to the stabilizer tower T2 through a pipeline, and the stabilizer tower T2 is connected to a recovery device S1, and the recovery device S1 is used for recovering the lower alkane in the stabilizer tower T2.
In the above embodiment, the bottom of the dehydrogenation tower T1 is connected with the stabilizer tower T2 through a pipeline, heavy components at the bottom of the dehydrogenation tower T1 enter the stabilizer tower T2 through a pipeline, the bottom of the stabilizer tower T2 is connected with a recovery device S1, the recovery device S1 is used for recovering alkane, wherein heavy components at the bottom of the stabilizer tower T2 comprise C4 alkane, liquid phase parts in the cryogenic liquid separation tank F2 comprise C3 alkane, and after both are sent into the stabilizer tower T2, the heavy components are recovered and collected through the recovery device S1, so that full utilization of resources is realized, and certain economic benefits are promoted for enterprises.
In this embodiment, preferably, the heavy component at the bottom of the dehydrogenation tower T1 and the liquid phase in the cryogenic liquid separation tank F2 enter the stabilization tower T2 at the same time, so that the recovery device S1 is convenient for recovery.
Referring to fig. 1, in a preferred embodiment of the present utility model, the stabilizer T2 is further connected to an incinerator S2, and the incinerator S2 is connected to the gas phase outlet of the stabilizer T2.
In the above embodiment, the incineration device S2 is connected to the top of the stabilizer T2, and the exhaust gas in the stabilizer T2 enters the incineration device S2 from the gas phase outlet at the top of the stabilizer T2, and is subjected to centralized incineration treatment by the incineration device S2.
Referring to fig. 1, in a preferred embodiment of the present utility model, the dehydrogenation tower T1 is provided with a heat exchange device H1, and the heat exchange device H1 is connected to the dehydrogenation tower T1.
In the above embodiment, preferably, a heat exchange device H1 is connected to one side of the dehydrogenation tower T1, and the heat exchange device H1 is used for exchanging heat of the material in the dehydrogenation tower T1; in this embodiment, preferably, one end of the heat exchange device H1 is connected to the bottom of the dehydrogenation tower T1, and the other end is connected to the side of the dehydrogenation tower T1, so that materials can conveniently enter the heat exchange device H1 to exchange heat.
The specific working flow of the isobutane normal reaction waste gas recovery system is as follows:
firstly, normal reaction products in an isobutane normal system enter the dehydrogenation tower T1 through a pipeline and are separated into light components and heavy components in the dehydrogenation tower T1, wherein the light components are positioned at the top layer of the dehydrogenation tower T1, the heavy components are positioned at the bottom layer of the dehydrogenation tower T1, then, the heavy components at the bottom of the dehydrogenation tower T1 enter the stabilizing tower T2 through a pipeline at the bottom of the tower, the light components at the top of the dehydrogenation tower T1 firstly enter the cooler L1, gas-liquid separation is carried out under the cooling action of the cooler L1, a gas phase and a liquid phase are formed in the cooling liquid separating tank F1, the liquid phase in the cooling liquid separating tank F1 flows back into the dehydrogenation tower T1 through the reflux pump B1, the gas phase enters the cryogenic liquid separating tank F2 for further cryogenic treatment, the gas phase and the liquid phase are formed in the cryogenic liquid separating tank F2, the liquid phase in the cryogenic liquid separating tank F2 enters the stabilizing tower T2, the gas phase enters the circulating liquid separating tank F3 for separation, the separated gas phase enters the top of the circulating liquid separating tank F3 and the top of the circulating tower F1 for recycling the hydrogen gas phase, and the hydrogen gas phase enters the top of the compressor Y1, and the top of the hydrogen recycling device is recycled by the top of the compressor 1.
In the description of the present utility model, it should be understood that the terms such as "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", etc. indicate orientations or positional relationships based on the drawings, are merely for convenience in describing the present utility model and simplifying the description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present utility model.
In the present utility model, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communicated with the inside of two elements or the interaction relationship of the two elements. The specific meaning of the above terms in the present utility model can be understood by those of ordinary skill in the art according to the specific circumstances.
While the utility model has been described in conjunction with the specific embodiments above, it is evident that many alternatives, modifications and variations will be apparent to those skilled in the art in light of the foregoing description. Accordingly, all such alternatives, modifications, and variations are included within the spirit and scope of the following claims.
Claims (9)
1. The isobutane normal reaction waste gas recovery system is characterized by comprising a normal system, a dehydrogenation tower and a stabilizing tower, wherein the dehydrogenation tower is connected with a discharge port of the normal system through a pipeline, a separation unit is arranged between the dehydrogenation tower and the stabilizing tower and is respectively connected with the dehydrogenation tower and the stabilizing tower, the separation unit is connected with the normal system through a circulating device, and the circulating device is used for conveying circulating hydrogen into the normal system.
2. The isobutane normal reaction off-gas recovery system according to claim 1, wherein the separation unit comprises a cooling device and a cryogenic device, the cooling device comprises a cooler and a cooling liquid-separating tank, the cryogenic device comprises a cryogenic device and a cryogenic liquid-separating tank, and the cooler, the cooling liquid-separating tank, the cryogenic device and the cryogenic liquid-separating tank are sequentially arranged.
3. The isobutane normal reaction waste gas recovery system according to claim 2, wherein a feed inlet of the cooler is connected with the dehydrogenation tower, a discharge outlet of the cooler is connected with an inlet of the cooling liquid separating tank, a gas phase outlet of the cooling liquid separating tank is connected with the cryogenic cooler, a gas phase outlet of the cryogenic liquid separating tank is connected with the circulating device, and a liquid phase outlet of the cryogenic liquid separating tank is connected with the stabilizer tower.
4. The isobutane normal reaction off-gas recovery system according to claim 2, wherein the separation unit further comprises a reflux pump, an inlet end of the reflux pump is connected to the liquid phase outlet of the cooling liquid separation tank, and an outlet end of the reflux pump is connected to the dehydrogenation tower.
5. The isobutane normal reaction waste gas recovery system according to claim 2, wherein the circulation device comprises a circulation liquid separation tank connected to the gas phase outlet of the cryogenic liquid separation tank and a compressor connected to the circulation liquid separation tank and normal system, respectively.
6. The isobutane normal reaction waste gas recovery system according to claim 2, wherein the cooler and the cryocooler are provided with a liquid inlet and a liquid outlet for the ingress and egress of a refrigerant.
7. The isobutane normal reaction offgas recovery system according to claim 1, characterized in that the dehydrogenation tower is connected to the stabilizer tower through a pipeline, the stabilizer tower is connected to a recovery device for recovering lower alkane in the stabilizer tower.
8. The isobutane normal reaction offgas recovery system according to claim 7, characterized in that the stabilizer is further connected with an incinerator connected to a gas phase outlet of the stabilizer.
9. The isobutane normal reaction offgas recovery system according to claim 1, characterized in that the dehydrogenation tower is provided with a heat exchange device, which is connected to the dehydrogenation tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322033684.2U CN220496334U (en) | 2023-07-31 | 2023-07-31 | Isobutane normal reaction waste gas recovery system |
Applications Claiming Priority (1)
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