CN111197913B - Isobutane dehydrogenation cold box system separation equipment capable of refrigerating by latent heat of vaporization and separation method thereof - Google Patents
Isobutane dehydrogenation cold box system separation equipment capable of refrigerating by latent heat of vaporization and separation method thereof Download PDFInfo
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- CN111197913B CN111197913B CN202010077166.9A CN202010077166A CN111197913B CN 111197913 B CN111197913 B CN 111197913B CN 202010077166 A CN202010077166 A CN 202010077166A CN 111197913 B CN111197913 B CN 111197913B
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- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 title claims abstract description 70
- 238000000926 separation method Methods 0.000 title claims abstract description 41
- 239000001282 iso-butane Substances 0.000 title claims abstract description 34
- 238000009834 vaporization Methods 0.000 title claims abstract description 26
- 230000008016 vaporization Effects 0.000 title claims abstract description 26
- 238000006356 dehydrogenation reaction Methods 0.000 title claims abstract description 19
- 239000007788 liquid Substances 0.000 claims abstract description 85
- 238000005057 refrigeration Methods 0.000 claims abstract description 27
- 239000000463 material Substances 0.000 claims abstract description 24
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 16
- 239000001257 hydrogen Substances 0.000 claims abstract description 11
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 11
- 238000003303 reheating Methods 0.000 claims abstract description 11
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 7
- 238000011084 recovery Methods 0.000 claims abstract description 6
- 239000007789 gas Substances 0.000 claims description 65
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 33
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 33
- 239000011344 liquid material Substances 0.000 claims description 19
- 238000011143 downstream manufacturing Methods 0.000 claims description 14
- 239000000047 product Substances 0.000 claims description 12
- 239000003507 refrigerant Substances 0.000 claims description 12
- 239000012263 liquid product Substances 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 5
- 150000002431 hydrogen Chemical class 0.000 claims description 5
- 238000010992 reflux Methods 0.000 claims description 3
- 238000004781 supercooling Methods 0.000 claims description 2
- 238000000605 extraction Methods 0.000 claims 1
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 abstract description 16
- 238000000034 method Methods 0.000 abstract description 10
- 238000002156 mixing Methods 0.000 abstract description 5
- 238000002360 preparation method Methods 0.000 abstract description 3
- 238000004134 energy conservation Methods 0.000 abstract description 2
- 238000011027 product recovery Methods 0.000 abstract 1
- 238000005265 energy consumption Methods 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 238000009835 boiling Methods 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 238000011144 upstream manufacturing Methods 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000010168 coupling process Methods 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 239000013526 supercooled liquid Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 230000005501 phase interface Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
- F25J3/0655—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of hydrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
- F25J3/062—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B41/00—Fluid-circulation arrangements
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B41/00—Fluid-circulation arrangements
- F25B41/30—Expansion means; Dispositions thereof
- F25B41/31—Expansion valves
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B43/00—Arrangements for separating or purifying gases or liquids; Arrangements for vaporising the residuum of liquid refrigerant, e.g. by heat
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
- F25J3/065—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of CnHm with 4 carbon atoms or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/02—Mixing or blending of fluids to yield a certain product
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/04—Internal refrigeration with work-producing gas expansion loop
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/12—External refrigeration with liquid vaporising loop
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Power Engineering (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
A separation method and equipment of an isobutane dehydrogenation cold box system for refrigeration by vaporization latent heat, in particular to a method and equipment for fully separating isobutane, isobutene and the like in reaction products from hydrogen in a low-temperature heat exchange system; the main cold energy required by the low-temperature separation of the system is from the vaporization latent heat of isobutane and isobutene (accounting for about 90 percent of the total refrigerating energy of the cold box system), the preparation of the cold energy required by the low-temperature separation is realized in the cold box system, and the heat exchange meets the requirements of a separation process. The reaction product is connected with a first-stage gas-liquid separator after being cooled by a cold combined feeding heat exchanger; the liquid isobutane is cooled by a feed cooler and then is branched into two streams, one stream enters a secondary cooler, is premixed with circulating hydrogen after being cooled, throttled and decompressed, and the premixed stream returns to the secondary cooler for reheating, vaporization and cold recovery; mixing the reheated material flow with another strand of liquid isobutane; the separation method and the separation equipment have the characteristics of simple process flow, safety, high efficiency, energy conservation, easy operation, high operation elasticity, high product recovery rate and the like.
Description
Technical Field
The invention belongs to the field of low-temperature separation, and particularly relates to a separation method and equipment of an isobutane dehydrogenation cold box system by utilizing latent heat of vaporization refrigeration, which are mainly applicable to a cold box separation method for realizing effective separation of isobutane, isobutene and the like from hydrogen and cold recovery of reaction products after isobutane dehydrogenation of an Oleflex process of a UOP in a low-temperature environment.
Background
The invention relates to an isobutene preparation device based on an UOP (Uop) Oleflex process by isobutane catalytic dehydrogenation, which consists of a plurality of parts such as reaction, product compression, low-temperature separation, product refining and the like, wherein a low-temperature separation system is a key link for ensuring normal operation and product quality of an upstream product separation unit and a downstream product separation unit, and is also a core reaction and fractionation unit intersection center of the isobutene preparation device by isobutane dehydrogenation, and the cold and hot collecting flow is very concentrated. The method mainly separates mixed components after dehydrogenation reaction, and utilizes physical cooling components to fully separate isobutane, isobutene and hydrogen components to obtain isobutane, isobutene liquid products, dry gas products and the like. The main cold energy of the cold box system comes from the vaporization latent heat of isobutane entering and exiting the cold box and the vaporization latent heat of isobutane and isobutene in the flash steam (accounting for about 90 percent of the total refrigerating energy of the cold box system); and the flash evaporation material flows out of the cold box and then is directly compressed by the reaction product compressor and then returns to the cold box for recycling (an important refrigeration mode of the cold box system is the effect of low Wen Oudi cold supply of the cold box), and the refrigeration of the flash evaporation material flows and the coupling degree of the product compressor are high, so that the refrigeration and the product compressor are mutually influenced. In order to solve the above influencing factors, improve the heat exchange efficiency and reduce the energy consumption, a cold box system low-temperature separation method and a cold box system low-temperature separation device with few devices, high refrigeration heat exchange efficiency and high operation flexibility are researched and designed.
Disclosure of Invention
The invention aims to provide a low-temperature separation method and equipment for an isobutane dehydrogenation cold box system with safe and reliable process, high refrigeration efficiency, low energy consumption, convenient operation and low investment, which fully considers the refrigeration and heat exchange characteristics of a cold box low-temperature area, optimizes the relationship between the cold box separation system and the upstream and downstream processes by the principle of high-temperature high enthalpy drop of isentropic expansion, and optimally distributes low-temperature cold energy so that each plate-fin heat exchanger has ideal heat exchange performance, thereby well solving the contradiction of high coupling degree between flash evaporation logistics vaporization refrigeration and heat exchange separation and a reaction product compressor; the problem that the cooling capacity of the cold box system is insufficient and the heat load is not matched enough under the high-load working condition is solved; the energy consumption of the whole process device is effectively reduced. In order to achieve the purpose of the technology, the invention provides the following technical scheme: the device consists of a cold combined feed heat exchanger, a secondary cooler, a feed cooler, a first gas-liquid separator, a second gas-liquid separator, a flash tank, a compressor unit, an expansion unit and a low-temperature pump, wherein the cold combined feed heat exchanger is connected with the feed cooler through a pipeline, a valve is arranged on a connecting pipeline, the first gas-liquid separator is arranged between the cold combined feed heat exchanger and the secondary cooler, the secondary cooler is connected with the expansion unit, the expansion unit is connected with the second gas-liquid separator, the second gas-liquid separator is connected with the secondary cooler to form a first loop, the secondary cooler is connected with the feed cooler and the low-temperature pump through the flash tank respectively, the low-temperature pump is connected with the feed cooler to form a second loop,
As preferable: a hot flow channel and three cold flow channels are arranged in the cold combined feeding heat exchanger, wherein one cold flow channel is a reflux channel, and a propylene compressor and a cooler are arranged on the channels.
As preferable: the secondary cooler is provided with two hot flow channels and five cold flow channels, and the channels are respectively connected with the cold combined feeding heat exchanger, the feeding cooler, the second gas-liquid separator, the flash tank and the expansion unit.
As preferable: the feed cooler is provided with a hot flow channel and two cold flow channels which are respectively connected with the flash tank, the cold combined feed heat exchanger and the outside.
The separation method of the invention comprises the following steps: the method comprises the steps that a cold combined feeding heat exchanger is provided with a hot flow channel and three cold flow channels, a reaction product after pressurization and purification treatment is cooled to-20 to-25 ℃ through the cold combined feeding heat exchanger, the reaction product enters a first gas-liquid separator after partial condensation, the separated gas material flows are further cooled to-90 to-100 ℃ in a second-stage cooler, the gas material flows enter a second gas-liquid separator after partial condensation, the gas material flows separated by the second gas-liquid separator branch out a gas material flow and a dry gas material flow, and the two material flows are returned to the second-stage cooler for reheating and recycling cold energy; the gas stream is reheated to-80 to-85 ℃ in a secondary cooler, is extracted as a superheated gas stream and enters an expansion unit for isentropic expansion, the pressure is expanded from 0.4-0.6 MPa (G) to 0.18-0.33 MPa (G), and the temperature of the expanded gas stream is-95 to-105 ℃; the expanded gas stream branches off to recycle hydrogen and a gas stream, and the gas stream is throttled and depressurized to 0.04-0.07 MPa (G) to form a gas stream; the liquid material flow separated by the second gas-liquid separator branches into a liquid material flow and a liquid material flow, the liquid material flow is throttled and depressurized to 0.04-0.07 MPa (G), the obtained liquid material flow is mixed with the gas material flow, a refrigeration material flow is formed, the refrigeration material flow returns to the secondary cooler for reheating to minus 28-minus 32 ℃, and the refrigeration material flow is obtained after being led out; the feeding cooler is provided with a hot flow channel and two cold flow channels, and the secondary cooler is provided with two hot flow channels and five cold flow channels; after external liquid isobutane is cooled to-18 to-23 ℃ through a feed cooler, obtaining two streams of liquid isobutane after further supercooling, wherein one stream is a liquid stream accounting for 85-92% of the total flow of the liquid, the other stream accounting for 8-15% of the total flow of the liquid is cooled to-90 to-100 ℃ through a secondary cooler, the obtained liquid stream is throttled and depressurized to 0.18-0.33 MPa (G), the depressurized liquid stream is premixed with circulating hydrogen, a refrigerating stream is formed after premixing and returned to the secondary cooler for reheating to-28 to-32 ℃ for vaporization and cold recovery, and the obtained stream is led out; the liquid material flow is throttled and depressurized to 0.17-0.32 MPa (G), the obtained liquid material flow and the material flow are mixed to form combined feeding, the combined feeding is reheated to 30-35 ℃ by a cold combined feeding heat exchanger and is discharged out of a cold box, the combined feeding is used as the combined feeding to be sent to a downstream process, the external propylene gas is compressed to 1.8MPa (G) from 0.1MPa (G) by a propylene compressor, the obtained gas propylene is cooled to 40 ℃ by a cooler, the obtained liquid propylene is throttled and depressurized to 0.09-0.12 MPa (G), the temperature of minus 28-minus 32 ℃, the obtained propylene refrigerant enters the cold combined feeding heat exchanger to provide cold for reaction products, the propylene refrigerant is reheated to 30-35 ℃ and is gasified into propylene gas, and the propylene gas is pressurized, cooled and throttled and depressurized by the propylene compressor, so that the recycling of the propylene refrigerant is realized.
As preferable: the dry gas material flow is reheated to-22 to-28 ℃ by a secondary cooler, and then reheated to 30 to 35 ℃ by a cold combined feeding heat exchanger and discharged out of a cold box as a dry gas product to be sent into a downstream process.
As preferable: all liquid separated by the first gas-liquid separator is throttled and decompressed to 0.2-0.35 MPa (G) and then enters a flash tank; the liquid material flow separated by the second gas-liquid separator is throttled and depressurized to 0.2-0.35 MPa (G), and then is reheated to-22 to-28 ℃ by a secondary cooler and enters a flash tank; the flash tank separates out liquid at-10 to-30 ℃, the liquid is pressurized to 0.8-1.1 MPa (G) by a low-temperature pump, and then the liquid is reheated to 30-35 ℃ by a feed cooler and discharged out of the cold box to be used as a liquid product to be sent into a downstream process.
As preferable: the gas separated from the flash tank is throttled and depressurized to 0.04-0.07 MPa (G), the obtained gas stream is mixed with the refrigerant stream reheated by the secondary cooler to form a flash stream, the flash stream is reheated to 30-35 ℃ by the feed cooler and discharged out of the cold box to be used as a flash stream in a downstream process.
The beneficial effects of the invention are as follows: the invention provides a separation method and equipment for an isobutane dehydrogenation cold box system with latent heat of vaporization refrigeration, which have the advantages of high refrigeration efficiency and wide adjustment range, and solve the problems of insufficient system cold capacity and poor heat exchange effect of the cold box system under a high-load working condition; the energy consumption of the whole process device is effectively reduced. The flash evaporation material flows produced by the cold box low-temperature separation method and the equipment can well balance the relation between the cold box system and the reaction product compressor unit; the liquid products, the combined feeding and the dry gas products produced by the cold box low-temperature separation method and the equipment can meet the requirements of the upstream and downstream processes of the isobutane catalytic dehydrogenation, and the cold box low-temperature separation method and the equipment have the advantages of high recovery rate, low energy consumption, easiness in control and strong operability.
Drawings
FIG. 1 is a schematic flow chart of the present invention.
Detailed Description
The invention will be described in detail below with reference to the attached drawings: the device shown in figure 1 comprises a cold combined feed heat exchanger 2, a secondary cooler 6, a feed cooler 41, a first gas-liquid separator 4, a second gas-liquid separator 8, a flash tank 24, a compressor unit 62, an expansion unit 12 and a cryogenic pump 57, wherein the cold combined feed heat exchanger 2 is connected with the feed cooler 41 through a pipeline, a valve 48 is arranged on the connecting pipeline, the first gas-liquid separator 4 is arranged between the cold combined feed heat exchanger 2 and the secondary cooler 6, the secondary cooler 6 is connected with the expansion unit 12, the expansion unit 12 is connected with the second gas-liquid separator 8, the second gas-liquid separator 8 is connected with the secondary cooler 6 to form a first loop, the secondary cooler 6 is respectively connected with the feed cooler 41 and the cryogenic pump 57 through the flash tank 24, the cryogenic pump 57 is connected with the feed cooler 41 to form a second loop, one hot flow channel and three cold flow channels are arranged in the cold combined feed heat exchanger 2, one cold flow channel is a reflux channel, a propylene compressor and a cooler 64 are arranged on the channel, the secondary cooler 6 is provided with two hot flow channels and five cold flow channels, the channels are respectively connected with the cold combined feed heat exchanger 2, the feed cooler 41, the second gas-liquid separator 8, the flash tank 24 and the expansion unit 12, and the feed cooler 41 is provided with one hot flow channel and two cold flow channels which are respectively connected with the flash tank 24, the cold combined feed heat exchanger and the outside.
The cold combined feed heat exchanger 2 is provided with a hot flow channel and three cold flow channels, the reaction product 1 with the pressure of 0.63MPa (G) and the temperature of 40 ℃ below zero is cooled to 21 ℃ below zero by the cold combined feed heat exchanger 2, the gas-liquid mixture flow 3 is formed by partial condensation and enters the first gas-liquid separator 4, the separated gas flow 5 enters the secondary cooler 6 and is further cooled to 93 ℃ below zero, and the gas-liquid mixture flow 7 is formed by partial condensation and enters the second gas-liquid separator 8.
The feed cooler 41 is provided with one hot flow channel and two cold flow channels, and the secondary cooler 6 is provided with two hot flow channels and five cold flow channels; the liquid isobutane 40 with the pressure of 0.9MPa (G) and the temperature of 40 ℃ below zero is cooled to 19 ℃ below zero by a feed cooler 41 to obtain two streams of further supercooled liquid isobutane 42, one stream is a liquid stream 47 accounting for 91 percent of the total flow rate of the liquid, the other stream 43 accounting for 9 percent of the total flow rate of the liquid is cooled to 93 ℃ below zero by a secondary cooler 6, the liquid stream 44 is led out and is throttled and decompressed to 0.31 MPa (G) by a valve 45, the decompressed liquid stream 46 is premixed with circulating hydrogen 14, a refrigerant stream 50 is formed after premixing and is returned to the secondary cooler 6 for reheating to 28 ℃ below zero for vaporization and cold recovery, and a stream 51 is led out.
The liquid stream 47 is throttled down to-0.31 MPa (G) by valve 48 and the resulting liquid stream 49 is mixed with stream 51 to form combined feed 52 which is reheated to-34 ℃ by cold combined feed heat exchanger 2 and fed out of the cold box as combined feed 53 to the downstream process.
The external gas propylene 61 is compressed to 1.8MPa (G) from 0.1MPa (G) through a propylene compressor, the obtained gas propylene 63 is cooled to 40 ℃ through a cooler 64, the obtained liquid propylene 65 is throttled and decompressed to 0.11MPa (G) through a valve 66, the obtained propylene refrigerant 67 enters a cold combined feed heat exchanger 2 to provide cold energy for the material flow of the reaction product 1, the propylene refrigerant 67 is reheated to 34 ℃ and vaporized to obtain propylene gas 61, and the propylene gas is then returned to be pressurized, cooled, throttled and decompressed through the propylene compressor, so that the recycling of the propylene refrigerant is realized.
All liquid 21 separated by the first gas-liquid separator 4 is throttled and decompressed to 0.3MPa (G) by a valve 22 to obtain gas-liquid mixture
The material flow 23 enters a flash tank 24, the other liquid material flow 31 separated by the second gas-liquid separator 8 is throttled and decompressed to 0.3MPa (G) by a valve 32, the obtained liquid material flow 33 is reheated to-28 ℃ by a secondary cooler 6, and the obtained liquid material flow 34 enters the flash tank 24; the liquid 56 separated from flash tank 24 is pressurized to-1.0 MPa (G) by cryopump 57 to obtain liquid product 58, and liquid product 58 is reheated by feed cooler 41 to-34 ℃ and taken out of the cold box as liquid product 59 for downstream processing.
The gas stream 9 separated by the second gas-liquid separator 8 is branched into a gas stream 10 and a dry gas stream 18, and both streams are returned to the secondary cooler 6 for reheating and recovering cold; the gas stream 10 is reheated to-83 ℃ in the secondary cooler 6, and then is extracted into an expansion unit 12 to be expanded isentropically, the pressure is expanded from-0.60 MPa (G) to-0.31 MPa (G), and the temperature of the expanded gas stream 13 is-93 ℃. The dry gas material flow 18 is reheated to minus 28 ℃ through the secondary cooler 6, and then reheated to minus 34 ℃ through the cold combined feed heat exchanger 2, and then is discharged out of the cold box and is used as a dry gas product 55 to be sent into a downstream process.
The expanded gas stream 13 branches off a recycle hydrogen 14 and a gas stream 15, and the gas stream 15 is throttled and depressurized to 0.05MPa (G) by a valve 16 to obtain a gas stream 17; the liquid stream 25 separated by the second gas-liquid separator 8 branches into a liquid stream 26 and a liquid stream 31, and the liquid stream 26 is throttled and depressurized to-0.05 MPa (G) by a valve 27 to form a liquid stream 28. The gaseous stream 17 and the liquid stream 28 are mixed to form a refrigeration stream 29, the refrigeration stream 29 is returned to the secondary cooler 6 for reheating to minus 28 ℃ and is led out to obtain a liquid stream 30.
The gas 35 separated from the flash tank 24 is throttled and depressurized to 0.04MPa (G) by a valve 36, the obtained gas stream 37 and the refrigerant stream 30 reheated by the secondary cooler 6 are mixed to form a flash stream 38, and the flash stream 38 is reheated to-34 ℃ by a feed cooler 41 and discharged from the cold box as a flash stream 39 to be sent to a downstream process.
H 2 and C 4H10, cooling and vaporization refrigeration principle:
1) For example: 1kmol H 2 (-20 ℃, 500KPaA, superheated gas) and 1kmol C 4H10 (-20 ℃, 500KPaA, supercooled liquid) are mixed, the partial pressure of C 4H10 in the gas phase is 0KPa at the beginning of mixing, and the partial pressure of the gas-liquid phase interface is far greater than the partial pressure in the gas phase, so C 4H10 can be vaporized, the concentration of C 4H10 in the gas phase is increased along with the vaporization of C 4H10, the partial pressure is gradually increased, and simultaneously, trace H 2 is absorbed by C 4H10 to reach the gas-liquid phase balance. Since C 4H10 is far greater than H 2 absorbed, C 4H10 absorbs heat by vaporization according to energy conservation, and only the temperature of the fluid is reduced, since the latent heat of vaporization 378 KJ/kg of C 4H10 is far greater than the specific heat of constant pressure 2.15KJ/kg in this state, and the boiling points of C 4H10 (boiling point 37.44 ℃ C. In 500 kPaA) and H 2 (boiling point-246.1 ℃ C. In 500 kPaA) differ too much, the temperature at which isobutane is mixed with hydrogen is reduced to-33.27 ℃.
Along with the reduction of the temperature of H 2、C4H10 before mixing, the temperature after mixing is reduced (but the reduction amplitude is gradually reduced), and the heat exchange temperature difference (heat exchange driving force) is provided for heat exchange separation.
2) The mixture of H 2 and C 4H10 (the mixture of H 2 and C 4H10、C4H8) flows in the plate-fin heat exchanger channels to undergo a complex mass and heat transfer process of reheating, separating, mixing, reheating, separating and remixing …, and H 2 promotes the liquid C 4H10、C4H8 to be completely vaporized in the plate-fin heat exchanger channels, so as to provide main cold energy for cooling and separating the reaction product (1).
3) The lower the pressure is in favor of vaporization of C 4H10、C4H8 after C 4H10、C4H8 and H 2 are mixed, so that the refrigeration function of the vaporization latent heat is fully exerted.
Claims (8)
1. The utility model provides a cold box system separation equipment of isobutane dehydrogenation of latent heat of vaporization refrigeration, its characterized in that equipment is by cold joint feed heat exchanger (2), second grade cooler (6), feed cooler (41), first gas-liquid separator (4), second gas-liquid separator (8), flash tank (24), compressor unit (62), expansion unit (12), cryopump (57) are constituteed, cold joint feed heat exchanger (2) are connected through the pipeline with feed cooler (41) to be equipped with valve (48) on connecting pipeline, be equipped with first gas-liquid separator (4) between cold joint feed heat exchanger (2) and second grade cooler (6), second grade cooler (6) are connected with expansion unit (12), expansion unit (12) are connected with second gas-liquid separator (8), and second gas-liquid separator (8) are connected with second grade cooler (6) and are formed first circuit, second grade cooler (6) are connected with feed cooler (41) and cryopump (57) respectively through flash tank (24), second grade cooler (6) are connected with second circuit (57) are formed.
2. The separation device of an isobutane dehydrogenation cold box system refrigerated by vaporization latent heat according to claim 1, characterized in that one hot flow channel and three cold flow channels are arranged in the cold combined feed heat exchanger (2), one cold flow channel is a reflux channel, and a propylene compressor and a cooler (64) are arranged on the channels.
3. Isobutane dehydrogenation cold box system separation device according to claim 1, characterized in that the secondary cooler (6) is provided with two hot flow channels and five cold flow channels, which channels are connected to the cold combined feed heat exchanger (2), the feed cooler (41), the second gas-liquid separator (8), the flash tank (24), the expansion unit (12), respectively.
4. Isobutane dehydrogenation cold box system separation apparatus with latent heat of vaporization refrigeration according to claim 1, characterized in that the feed cooler (41) is provided with one hot flow channel and two cold flow channels, which channels are connected to the flash tank (24), the cold combined feed heat exchanger and the outside, respectively.
5. The separation method of the isobutane dehydrogenation cold box system separation device for latent heat of vaporization refrigeration according to any one of claims 1 to 4, comprising the steps of: the cold combined feeding heat exchanger (2) is provided with a hot flow channel and three cold flow channels, the pressurized and purified reaction product (1) is cooled to-20 to-25 ℃ through the cold combined feeding heat exchanger (2), the reaction product enters the first gas-liquid separator (4) after being partially condensed, the separated gas stream (5) is further cooled to-90 to-100 ℃ through the secondary cooler (6), the reaction product enters the second gas-liquid separator (8) after being partially condensed, the gas stream (9) separated by the second gas-liquid separator (8) is branched into a gas stream (10) and a dry gas stream (18), and the two streams are returned to the secondary cooler (6) for reheating and recovering cold quantity; the gas stream (10) is reheated to-80 to-85 ℃ in a secondary cooler (6), and then is taken as a superheated gas stream (11) to be pumped into an expansion unit (12) for isentropic expansion, the pressure is expanded from 0.4 to 0.6MPa (G) to 0.18 to 0.33 MPa (G), and the temperature of the expanded gas stream (13) is-95 to-105 ℃; the expanded gas stream (13) is branched into circulating hydrogen (14) and a gas stream (15), and the gas stream (15) is throttled and depressurized to 0.04-0.07 MPa (G) to form a gas stream (17); the liquid material flow (25) separated by the second gas-liquid separator (8) is branched into a liquid material flow (26) and a liquid material flow (31), the liquid material flow (26) is throttled and depressurized to 0.04-0.07 MPa (G), the obtained liquid material flow (28) is mixed with the gas material flow (17), a refrigeration material flow (29) is formed, and the refrigeration material flow (29) is returned to the secondary cooler (6) for reheating to minus 28-minus 32 ℃ and is led out to obtain a refrigeration material flow (30); the feeding cooler (41) is provided with a hot flow channel and two cold flow channels, and the secondary cooler (6) is provided with two hot flow channels and five cold flow channels; after the external liquid isobutane (40) is cooled to-18 to-23 ℃ through a feed cooler (41), two streams are branched out from the liquid isobutane (42) after further supercooling, one stream is a liquid stream (47) accounting for 85-92% of the total liquid flow, the other stream is cooled to-90 to-100 ℃ through a secondary cooler (6), the obtained liquid stream (44) is throttled and depressurized to 0.18-0.33 MPa (G), the depressurized liquid stream (46) is premixed with circulating hydrogen (14), a refrigerating stream (50) is formed after premixing, the preheated liquid stream is returned to the secondary cooler (6) to-28 to-32 ℃ for vaporization and cold recovery, and a stream (51) is obtained after extraction; the liquid material flow (47) is throttled and depressurized to 0.17-0.32 MPa (G), the obtained liquid material flow (49) is mixed with the material flow (51) to form a combined feed (52), the combined feed is reheated to 30-35 ℃ by a cold combined feed heat exchanger (2) and is discharged out of a cold box, the combined feed (53) is used as a downstream process, external propylene gas (61) is compressed to 1.8MPa (G) from 0.1MPa (G) by a propylene compressor, the obtained gas propylene (63) is cooled to 40 ℃ by a cooler (64), the obtained liquid propylene (65) is throttled and depressurized to 0.09-0.12 MPa (G), the temperature of-28 to-32 ℃ is reduced, the obtained propylene refrigerant (67) enters the cold combined feed heat exchanger (2) to provide cooling capacity for the reaction product (1), the propylene refrigerant (67) is reheated to 30-35 ℃ to be propylene gas (61), and the propylene gas is returned to be pressurized, cooled and depressurized by the propylene compressor, so that the propylene refrigerant is recycled.
6. The separation method of the separation equipment of the isobutane dehydrogenation cold box system with latent heat of vaporization refrigeration according to claim 5, wherein the dry gas stream (18) is reheated to-22 to-28 ℃ by a secondary cooler (6) and then reheated to 30 to 35 ℃ by a cold combined feed heat exchanger (2) to be discharged from a cold box as a dry gas product (55) to be sent to a downstream process.
7. The separation method of the isobutane dehydrogenation cold box system separation device with vaporization latent heat refrigeration according to claim 1, wherein all liquid (21) separated by the first gas-liquid separator (4) enters a flash tank (24) after being throttled and depressurized to 0.2-0.35 MPa (G); the liquid material flow (31) separated by the second gas-liquid separator (8) is throttled and decompressed to 0.2-0.35 MPa (G), and then is reheated to-22 to-28 ℃ by the secondary cooler (6) and enters the flash tank (24); the flash tank (24) separates liquid (56) at-10 to-30 ℃, the liquid is pressurized to 0.8-1.1 MPa (G) by a low-temperature pump (57), and the liquid is reheated to 30-35 ℃ by a feed cooler (41) and discharged from the cold box to be used as a liquid product (59) to be sent to a downstream process.
8. The separation method of a separation device of an isobutane dehydrogenation cold box system with vaporization latent heat refrigeration according to claim 7, wherein the gas (35) separated from the flash tank (24) is throttled and depressurized to 0.04-0.07 MPa (G), the obtained gas stream (37) is mixed with the refrigerating stream (30) reheated by the secondary cooler (6), and the flash stream (38) is formed and reheated to 30-35 ℃ by the feed cooler (41) to be discharged from the cold box and sent to a downstream process as a flash stream (39).
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| DE69915872D1 (en) * | 1998-12-08 | 2004-04-29 | Costain Oil Gas & Process Ltd | METHOD FOR SEPARATING HYDROCARBONS AT LOW TEMPERATURE |
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| EP3379187A1 (en) * | 2017-03-21 | 2018-09-26 | Linde Aktiengesellschaft | Generation of an input stream for alkane dehydration |
| CN212205333U (en) * | 2020-01-24 | 2020-12-22 | 杭州制氧机集团股份有限公司 | Isobutane dehydrogenation cold box system separation equipment adopting latent heat of vaporization refrigeration |
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| DE69915872D1 (en) * | 1998-12-08 | 2004-04-29 | Costain Oil Gas & Process Ltd | METHOD FOR SEPARATING HYDROCARBONS AT LOW TEMPERATURE |
| CN106766674A (en) * | 2016-12-09 | 2017-05-31 | 杭州杭氧股份有限公司 | A kind of ice chest deep cooling separating method of preparing isobutene through dehydrogenation of iso-butane project |
| EP3379187A1 (en) * | 2017-03-21 | 2018-09-26 | Linde Aktiengesellschaft | Generation of an input stream for alkane dehydration |
| CN108444214A (en) * | 2018-03-09 | 2018-08-24 | 中科瑞奥能源科技股份有限公司 | Dehydrogenation of isobutane technique and system |
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