CN220153070U - Carbon dioxide rectification stability control system - Google Patents
Carbon dioxide rectification stability control system Download PDFInfo
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- CN220153070U CN220153070U CN202321534898.1U CN202321534898U CN220153070U CN 220153070 U CN220153070 U CN 220153070U CN 202321534898 U CN202321534898 U CN 202321534898U CN 220153070 U CN220153070 U CN 220153070U
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 120
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 60
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 60
- 238000009833 condensation Methods 0.000 claims abstract description 150
- 230000005494 condensation Effects 0.000 claims abstract description 150
- 239000003507 refrigerant Substances 0.000 claims abstract description 106
- 239000012071 phase Substances 0.000 claims abstract description 69
- 239000007788 liquid Substances 0.000 claims abstract description 59
- 238000000926 separation method Methods 0.000 claims abstract description 54
- 239000007791 liquid phase Substances 0.000 claims abstract description 45
- 238000003860 storage Methods 0.000 claims abstract description 32
- 238000010992 reflux Methods 0.000 claims description 14
- 238000012544 monitoring process Methods 0.000 claims description 4
- 238000007654 immersion Methods 0.000 claims description 3
- 230000006641 stabilisation Effects 0.000 claims 6
- 238000011105 stabilization Methods 0.000 claims 6
- 238000000034 method Methods 0.000 abstract description 13
- 230000008569 process Effects 0.000 abstract description 13
- 238000012546 transfer Methods 0.000 abstract description 6
- 230000002411 adverse Effects 0.000 abstract description 3
- 230000000694 effects Effects 0.000 abstract description 2
- 230000001276 controlling effect Effects 0.000 description 6
- 239000000463 material Substances 0.000 description 5
- 238000009826 distribution Methods 0.000 description 3
- 238000013461 design Methods 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 230000009965 odorless effect Effects 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- HSFWRNGVRCDJHI-UHFFFAOYSA-N Acetylene Chemical compound C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010000 carbonizing Methods 0.000 description 1
- 238000012993 chemical processing Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009920 food preservation Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000008635 plant growth Effects 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 235000014214 soft drink Nutrition 0.000 description 1
- 235000019614 sour taste Nutrition 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000004781 supercooling 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
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0266—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of carbon dioxide
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
-
- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
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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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
- F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
-
- 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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/80—Separating impurities from carbon dioxide, e.g. H2O or water-soluble contaminants
- F25J2220/82—Separating low boiling, i.e. more volatile components, e.g. He, H2, CO, Air gases, CH4
-
- 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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
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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
-
- 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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/34—Details about subcooling of liquids
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The utility model relates to a carbon dioxide rectification stability control system, which comprises a refrigerant storage tank, wherein an outlet of the refrigerant storage tank is connected with a multi-stage condensation and separation unit, the condensation and separation unit comprises a submerged heat exchanger, and the submerged heat exchanger comprises a shell and a heat exchanger arranged in the shell; the gas-phase carbon dioxide pipeline is connected with the condensation separator through a heat exchanger, a shell inlet of the immersed heat exchanger is arranged on a shell of the immersed heat exchanger and is connected with an outlet of the refrigerant storage tank, and a shell gas-phase outlet is arranged at the top of the shell of the immersed heat exchanger; the heat exchanger is soaked in the liquid-phase refrigerant, so that continuous and stable cold energy can be provided for the heat exchanger, and the rectification mass transfer heat exchange process is stable, so that the purposes of small system fluctuation and stable and controllable product quality and yield are realized; the refrigerant can have enough space in the shell of the immersed heat exchanger to carry out gas-liquid separation so as to reduce the problem of liquid carrying of the gas phase outlet of the shell and avoid adverse effects on a subsequent ice machine.
Description
Technical Field
The utility model relates to the technical field of carbon dioxide production, in particular to a carbon dioxide rectification stability control system.
Background
Carbon dioxide (CO) 2 The chemical formula weight is 44.0095, and the gas is colorless, odorless or colorless and odorless at normal temperature and normal pressure, and the aqueous solution of the gas has slightly sour taste; the carbon dioxide gas has wide application in carbonizing soft drink, chemical processing, food preservation, inert protection in chemical and food processing, welding gas and plant growth stimulant.
At present, a rectification mode is generally adopted for purifying carbon dioxide, gas phase generated by rectification needs to be subjected to gas-liquid separation through a condensation and separation unit, tail gas treatment is carried out at the later stage of the gas phase, and liquid phase flows back to a rectification tower; specifically, in the prior art, the structure of the condenser generally adopts a plate fin type or a tube type, the refrigerant of the first-stage condenser comes from a refrigerant storage tank, one part enters the first-stage condenser after first-stage throttling, the other part enters the second-stage condenser after second-stage throttling, and part of the refrigerant after second-stage throttling enters the third-stage condenser after third-stage throttling; above-mentioned one-level throttle governing valve is used for controlling the liquid level of one-level condenser, two-level throttle governing valve is used for controlling the liquid level of second grade condenser, three-level throttle governing valve is used for controlling the liquid level of third grade condenser, second grade condenser refrigerant is got from one-level condenser refrigerant import, consequently cause one-level condenser refrigerant liquid level fluctuation easily, the hot material gas phase fraction of one-level condenser grow when the refrigerant quantity is little, lead to the heat load increase of second grade condenser, three-level condenser, if the cold volume is adjusted untimely, can lead to the tail gas blowdown increase, rectifying column top reflux liquid reduces, product quality and output all will be influenced. The refrigerant consumption of the tertiary condenser also affects the secondary condenser; namely: when the structural form of the condenser is matched with the corresponding regulating valve, one condenser generates fluctuation or causes instability of the whole condensation separation unit system, the instability directly leads to the increase of tail gas emptying, the reflux liquid at the top of the rectifying tower is reduced, and the quality and the yield of the product are influenced.
Disclosure of Invention
The utility model aims to provide a carbon dioxide rectification stability control system for solving the problems in the background technology.
In order to achieve the above purpose, the present utility model provides the following technical solutions:
the carbon dioxide rectification stability control system comprises a refrigerant storage tank, wherein an outlet of the refrigerant storage tank is connected with a multi-stage condensation and separation unit, the condensation and separation unit comprises a submerged heat exchanger, and the submerged heat exchanger comprises a shell and a heat exchanger arranged inside the shell; the gas-phase carbon dioxide pipeline is connected with the condensation separator through the heat exchanger, a shell inlet and an outlet of the refrigerant storage tank are arranged on the shell of the immersed heat exchanger, and a shell gas-phase outlet is arranged at the top of the shell of the immersed heat exchanger.
The beneficial effects of the utility model are as follows: the heat exchanger of the utility model adopts an immersed heat exchanger, namely: the liquid-phase refrigerant is arranged in the shell and is submerged in the heat exchanger arranged in the shell, so that continuous and stable cold energy can be provided for the heat exchanger, and carbon dioxide rectification stability is realized; in the multistage condensation separation unit, the flow direction of a gas-phase carbon dioxide pipeline is set to be of a conventional design, the gas-phase carbon dioxide pipeline firstly enters a heat exchanger of a first-stage condensation separation unit for condensation, then passes through a condensation separator of the first-stage condensation separation unit, flows back to a rectifying tower through a liquid phase separated by the condensation separator, and enters a heat exchanger of a next condensation separation unit for condensation through a separated gas phase; namely, multistage condensation and separation units are arranged in series in the flow direction of the gas-phase carbon dioxide pipeline; the relation between the refrigerant storage tank and the shell of the multistage condensation separation unit can be parallel or series; namely: the outlet of the refrigerant storage tank is respectively connected with the shell of the immersed heat exchanger in the multi-stage condensation and separation unit, or the outlet of the refrigerant storage tank is connected with the shell of the primary condensation and separation unit, and the liquid phase of the shell of the primary condensation and separation unit is connected with the shell of the next condensation and separation unit; compared with the prior art, the technical scheme has the advantages that the shell of the condensation separation unit is soaked in the liquid-phase refrigerant through the heat exchanger, so that continuous and stable cold energy can be provided for the heat exchanger, the rectification mass transfer heat exchange process is stable, and the purposes of small system fluctuation and stable and controllable product quality and yield are realized; meanwhile, the refrigerant can have enough space in the shell of the immersed heat exchanger to carry out gas-liquid separation, so that the problem of liquid carrying of a gas phase outlet of the shell is solved, and adverse effects on a subsequent ice machine are avoided.
Preferably, the bottom of the shell of the immersed heat exchanger is respectively provided with a shell liquid phase outlet, the shells of the immersed heat exchangers in the multistage condensation separation units are connected in series, and a first throttle valve is arranged at the inlet of the shell.
Preferably, a first liquid level sensor for monitoring the liquid level of the liquid-phase refrigerant is arranged on the shell of the immersed heat exchanger.
Preferably, the multistage condensation separation unit is a three-stage condensation unit, an outlet of the refrigerant storage tank is connected with a shell inlet of the submerged heat exchanger in the first-stage condensation unit, a shell liquid phase outlet of the submerged heat exchanger in the first-stage condensation unit is connected with a shell inlet of the submerged heat exchanger in the second-stage condensation unit, and a shell liquid phase outlet of the submerged heat exchanger in the second-stage condensation unit is connected with a shell inlet of the submerged heat exchanger in the third-stage condensation unit; the shell gas phase outlet of the immersed heat exchanger in the primary condensation unit is connected with the first ice machine, the shell gas phase outlet of the immersed heat exchanger in the secondary condensation unit is connected with the second ice machine, and the shell gas phase outlet of the immersed heat exchanger in the tertiary condensation unit is connected with the third ice machine.
Preferably, the gas-phase carbon dioxide pipeline is connected with the condensation separator in the first-stage condensation unit through the heat exchanger of the immersed heat exchanger in the first-stage condensation unit, the liquid-phase outlet of the condensation separator in the first-stage condensation unit is connected with the reflux pipeline of the rectifying tower, the gas-phase outlet of the condensation separator in the first-stage condensation unit is connected with the condensation separator in the second-stage condensation unit through the heat exchanger of the immersed heat exchanger in the second-stage condensation unit, the liquid-phase outlet of the condensation separator in the second-stage condensation unit is connected with the reflux pipeline of the rectifying tower, the gas-phase outlet of the condensation separator in the third-stage condensation unit is connected with the tail gas treatment device.
Preferably, a tee joint is arranged between a shell liquid phase outlet of the submerged heat exchanger in the primary condensing unit and a shell inlet of the submerged heat exchanger in the secondary condensing unit, and a third end of the tee joint is connected with a second ice machine through a second throttle valve and a cold side channel of the subcooler; the hot side channel inlet of the subcooler is connected with a carbon dioxide product pipeline, and the hot side channel outlet of the subcooler is connected with a carbon dioxide product storage tank.
The utility model also comprises a PLC control system, wherein the signal input end of the PLC control system is respectively connected with the first liquid level sensor and the second liquid level sensor, the signal output end of the PLC control system is respectively connected with the first throttle valve and the second throttle valve, and the second liquid level sensor is arranged on the subcooler.
The stable control system for carbon dioxide rectification is manufactured according to the scheme, and by using the immersed heat exchanger, namely: the shell is internally provided with a liquid-phase refrigerant which is submerged in the heat exchanger arranged in the shell, so that continuous and stable cold energy can be provided for the heat exchanger, and the stability of the carbon dioxide rectifying system is realized; compared with the prior art, the utility model can realize the stable control of the refrigerant liquid level of the condenser at each level, so as to realize reasonable refrigerant consumption distribution, the reflux liquid of the rectifying tower can be regulated stably according to the requirement, the rectifying mass transfer heat exchange process is stable, the system fluctuation is small, and the product quality and yield are stable and controllable; furthermore, the immersed heat exchanger is adopted to realize that hot materials can fully exchange heat with the refrigerant, meanwhile, a shell liquid phase outlet is formed in the bottom of the shell, and abundant refrigerant is discharged from the bottom and enters the immersed heat exchanger shell of the next condensation separation unit, so that the throttle valve can realize the stability control of the liquid level of the condenser refrigerant, and the stability control is not influenced by other factors; in addition, the utility model can also convey abundant refrigerant to the subcooler in the carbon dioxide product pipeline for condensation, so as to realize the supercooling of the carbon dioxide product for convenient storage.
Drawings
Fig. 1 is a schematic diagram of a prior art structure.
Fig. 2 is a schematic structural view of the present utility model.
Fig. 3 is a schematic structural view of an submerged heat exchanger in a primary condensing unit according to the present utility model.
Fig. 4 is a control schematic of the present utility model.
In the figure: 1. a cryogen storage tank; 2. a housing; 3. a heat exchanger; 4. a gas phase carbon dioxide pipeline; 5. a condensation separator; 6. a housing inlet; 7, a shell gas phase outlet; 8. a housing liquid phase outlet; 9. a first throttle valve; 10. a first liquid level sensor; 11. a first ice maker; 12. a second ice maker; 13. a third ice maker; 14. a rectifying tower reflux pipeline; 15. a tail gas treatment device; 16. a tee joint; 17. a second throttle valve; 18. a subcooler; 19. a carbon dioxide product conduit; 20. a carbon dioxide product storage tank; 21. a PLC control system; 22. and a second liquid level sensor.
Detailed Description
The technical solutions in the embodiments of the present utility model will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present utility model.
Referring to fig. 2 and 3, the utility model relates to a carbon dioxide rectification stability control system, which comprises a refrigerant storage tank 1, wherein an outlet of the refrigerant storage tank 1 is connected with a multi-stage condensation separation unit, the condensation separation unit comprises a submerged heat exchanger, and the submerged heat exchanger comprises a shell 2 and a heat exchanger 3 arranged inside the shell 2; the gas-phase carbon dioxide pipeline 4 is connected with the condensation separator 5 through the heat exchanger 3, a shell inlet 6 and an outlet of the refrigerant storage tank 1 are arranged on the shell 2 of the immersed heat exchanger, and a shell gas-phase outlet 7 is arranged at the top of the shell 2 of the immersed heat exchanger. At present, a rectification mode is generally adopted for purifying carbon dioxide, gas phase generated by rectification needs to be subjected to gas-liquid separation through a condensation and separation unit, tail gas treatment is carried out at the later stage of the gas phase, and liquid phase flows back to a rectification tower; referring specifically to fig. 1 of the prior art, fig. 1 is a schematic view of the prior art, in which the condenser structure generally adopts a plate fin type or a tube type, the refrigerant of the first-stage condenser comes from a refrigerant storage tank, one part enters the first-stage condenser after first-stage throttling, the other part enters the second-stage condenser after second-stage throttling, and part of the refrigerant after second-stage throttling enters the third-stage condenser after third-stage throttling; above-mentioned one-level throttle governing valve is used for controlling the liquid level of one-level condenser, two-level throttle governing valve is used for controlling the liquid level of second grade condenser, three-level throttle governing valve is used for controlling the liquid level of third grade condenser, second grade condenser refrigerant is got from one-level condenser refrigerant import, consequently cause one-level condenser refrigerant liquid level fluctuation easily, the hot material gas phase fraction of one-level condenser grow when the refrigerant quantity is little, lead to the heat load increase of second grade condenser, three-level condenser, if the cold volume is adjusted untimely, can lead to the tail gas blowdown increase, rectifying column top reflux liquid reduces, product quality and output all will be influenced. As shown in fig. 2 and 3, the heat exchanger adopted by the utility model adopts a submerged heat exchanger, namely: the liquid-phase refrigerant is arranged in the shell and is submerged in the heat exchanger arranged in the shell, so that continuous and stable cold energy can be provided for the heat exchanger, and carbon dioxide rectification stability is realized; in the multistage condensation separation unit, the flow direction of a gas-phase carbon dioxide pipeline is set to be of a conventional design, the gas-phase carbon dioxide pipeline firstly enters a heat exchanger of a first-stage condensation separation unit for condensation, then passes through a condensation separator of the first-stage condensation separation unit, flows back to a rectifying tower through a liquid phase separated by the condensation separator, and enters a heat exchanger of a next condensation separation unit for condensation through a separated gas phase; namely, multistage condensation and separation units are arranged in series in the flow direction of the gas-phase carbon dioxide pipeline; the relation between the refrigerant storage tank and the shell of the multistage condensation separation unit can be parallel or series; namely: the outlet of the refrigerant storage tank is respectively connected with the shell of the immersed heat exchanger in the multi-stage condensation and separation unit, or the outlet of the refrigerant storage tank is connected with the shell of the primary condensation and separation unit, and the liquid phase of the shell of the primary condensation and separation unit is connected with the shell of the next condensation and separation unit; compared with the prior art, the technical scheme has the advantages that the shell of the condensation separation unit is soaked in the liquid-phase refrigerant through the heat exchanger, so that continuous and stable cold energy can be provided for the heat exchanger, the rectification mass transfer heat exchange process is stable, and the purposes of small system fluctuation and stable and controllable product quality and yield are realized; meanwhile, the refrigerant can have enough space in the shell of the immersed heat exchanger to carry out gas-liquid separation, so that the problem of liquid carrying of a gas phase outlet of the shell is reduced, and the subsequent ice machine is adversely affected.
Further, the bottom of the shell 2 of the immersed heat exchanger is respectively provided with a shell liquid phase outlet 8, the shells 2 of the immersed heat exchangers in the multi-stage condensation separation unit are connected in series, and a first throttle valve 9 is arranged at the shell inlet 6. The utility model preferably adopts the serial connection mode, so that the rich refrigerant in the upper stage condensation and separation unit shell is discharged from the liquid phase outlet 8 of the part shell and enters the immersed heat exchanger shell of the next condensation and separation unit, the flow, the liquid level and the temperature of the refrigerant can be controlled through the first throttle valve 9 arranged at the inlet 6 of the shell, and the temperature in the upper stage condensation and separation unit shell is preferably higher than the temperature in the next condensation and separation unit shell.
Further, a first liquid level sensor 10 for monitoring the liquid level of the liquid phase refrigerant is arranged on the shell 2 of the immersion heat exchanger. The utility model adopts the immersed heat exchanger, which is different from the prior art in that the key point is that the liquid level of the refrigerant in the shell 2 is controlled, specifically, the liquid level in the corresponding shell 2 is detected by the first liquid level sensor 10, the stability of the refrigerant liquid level of the condensers at all levels is realized, the reasonable distribution of the refrigerant dosage is realized, and the stability of the rectification mass transfer heat exchange process is ensured.
Further, referring to fig. 2 and 3, the multi-stage condensation separation unit is a three-stage condensation unit, an outlet of the refrigerant storage tank 1 is connected with a shell inlet 6 of the submerged heat exchanger in the first-stage condensation unit, a shell liquid phase outlet 8 of the submerged heat exchanger in the first-stage condensation unit is connected with a shell inlet 6 of the submerged heat exchanger in the second-stage condensation unit, and a shell liquid phase outlet 8 of the submerged heat exchanger in the second-stage condensation unit is connected with a shell inlet 6 of the submerged heat exchanger in the third-stage condensation unit; the shell gas phase outlet 7 of the immersed heat exchanger in the primary condensation unit is connected with the first ice machine 11, the shell gas phase outlet 7 of the immersed heat exchanger in the secondary condensation unit is connected with the second ice machine 12, and the shell gas phase outlet 7 of the immersed heat exchanger in the tertiary condensation unit is connected with the third ice machine 13. Taking a three-stage condensing unit as an example, the refrigerant from a refrigerant storage tank 1 enters a shell 2 through a shell inlet 6 of a submerged heat exchanger after being subjected to primary throttling through a first throttle valve 9 in the primary condensing unit, so that the heat exchanger 3 is completely soaked in the refrigerant, and part of the refrigerant is gasified and discharged from a shell gas phase outlet 7 of the submerged heat exchanger in the primary condensing unit to enter a first ice machine 11 to realize the reutilization of the refrigerant; the abundant refrigerant in the shell 2 in the first-stage condensing unit enters the shell in the second-stage condensing unit after being subjected to second-stage throttling through the first throttle valve 9 in the second-stage condensing unit, so that the heat exchanger 3 is completely soaked in the refrigerant, and part of the refrigerant is gasified and discharged from the shell gas phase outlet 7 of the immersed heat exchanger in the second-stage condensing unit to enter the second ice machine 12 to realize the reutilization of the refrigerant; the abundant refrigerant in the shell 2 in the secondary condensation unit enters the shell in the primary condensation unit after three-stage throttling through the first throttle valve 9 in the tertiary condensation unit, the heat exchanger 3 is completely soaked in the refrigerant, and part of the refrigerant is gasified and discharged from the shell gas phase outlet 7 of the immersed heat exchanger in the tertiary condensation unit to enter the third ice machine 13 to realize the recycling of the refrigerant. The heat exchanger 3 is fully soaked in the refrigerant in the process, so that hot materials can fully exchange heat with the refrigerant, meanwhile, the abundant refrigerant is discharged from the bottom and enters the shell of the subsequent condensing unit, the throttle valve can realize the stability control of the refrigerant liquid level in the shell 2 and cannot be influenced by other factors, in addition, the refrigerant can have enough space in the shell 2 to perform gas-liquid separation, the ice machine is not easy to carry liquid, and the flow of reflux liquid of the rectifying tower is stable, so that the whole rectification process is stable and controllable.
Further, the gas-phase carbon dioxide pipeline 4 is connected with the condensation separator 5 in the first-stage condensation unit through the heat exchanger 3 of the immersed heat exchanger in the first-stage condensation unit, the liquid-phase outlet of the condensation separator 5 in the first-stage condensation unit is connected with the reflux pipeline 14 of the rectifying tower, the gas-phase outlet of the condensation separator 5 in the first-stage condensation unit is connected with the condensation separator 5 in the second-stage condensation unit through the heat exchanger 3 of the immersed heat exchanger in the second-stage condensation unit, the liquid-phase outlet of the condensation separator 5 in the second-stage condensation unit is connected with the reflux pipeline 14 of the rectifying tower, the gas-phase outlet of the condensation separator 5 in the third-stage condensation unit is connected with the tail gas treatment device 15. The gas phase in the rectifying tower firstly enters a heat exchanger 3 of an immersed heat exchanger in the primary condensing unit through a gas phase carbon dioxide pipeline 4 to exchange heat with external refrigerant, the gas phase enters a condensation separator 5 to carry out gas-liquid separation after the heat exchange is completed, the liquid phase flows back into the rectifying tower, the gas phase enters the heat exchanger 3 of the immersed heat exchanger in the secondary condensing unit and exchanges heat with the refrigerant in a shell 2 in the secondary condensing unit, the gas phase enters the condensation separator 5 to carry out gas-liquid separation after the heat exchange is completed, the liquid phase flows back into the rectifying tower, the gas phase enters the heat exchanger 3 of the immersed heat exchanger in the tertiary condensing unit and exchanges heat with the refrigerant in the shell 2 in the tertiary condensing unit, the liquid phase flows back into the rectifying tower, and the gas phase enters a tail gas treatment device 15 to carry out tail gas treatment.
Further, a tee joint 16 is arranged between a shell liquid phase outlet 8 of the submerged heat exchanger in the primary condensation unit and a shell inlet 6 of the submerged heat exchanger in the secondary condensation unit, and a third end of the tee joint 16 is connected with the second ice machine 12 through a second throttle valve 17 and a cold side channel of a subcooler 18; the hot side channel inlet of the subcooler 18 is connected to a carbon dioxide product conduit 19 and the hot side channel outlet of the subcooler 18 is connected to a carbon dioxide product tank 20. The utility model can also enable the surplus cold in the immersed heat exchanger shell 2 in the primary condensing unit to enter the subcooler 18 to exchange heat and cool with the carbon dioxide product from the carbon dioxide product pipeline 19, so as to realize the purpose of convenient product preservation.
As shown in fig. 4, the utility model further comprises a PLC control system 21, wherein the signal input end of the PLC control system 21 is respectively connected with the first liquid level sensor 10 and the second liquid level sensor 22, the signal output end of the PLC control system is respectively connected with the first throttle valve 9 and the second throttle valve 17, and the second liquid level sensor 22 is arranged on the subcooler 18. The utility model can realize stable control of carbon dioxide rectification in an automatic control mode, specifically, the first liquid level sensor 10 and the second liquid level sensor 22 are used for monitoring the liquid level of the shell 2 and the subcooler 18, and when the liquid level is low, the corresponding first throttle valve 9 and the second throttle valve 17 are controlled by the PLC control system 21 to realize replenishment of liquid-phase refrigerant so as to achieve the aim of stabilizing the system; it should be noted that the second level sensor 22 described in the present disclosure is used to monitor the level of the refrigerant in the subcooler 18.
The working principle of the utility model is as follows: the utility model comprises two sets of processes, one is a gas-phase carbon dioxide process which enters a gas-phase carbon dioxide pipeline 4 after rectification in a rectifying tower, and the other is a process which provides cold energy for a carbon dioxide rectifying system by a refrigerant storage tank, wherein the two processes are operated simultaneously; specifically, the gas phase carbon dioxide flow is that the gas phase in the rectifying tower firstly enters a heat exchanger 3 of an immersed heat exchanger in a first-stage condensing unit through a gas phase carbon dioxide pipeline 4 to exchange heat with external refrigerant, the gas phase enters a condensation separator 5 to perform gas-liquid separation after the heat exchange is completed, the liquid phase flows back into the rectifying tower, the gas phase enters the heat exchanger 3 of the immersed heat exchanger in a second-stage condensing unit to exchange heat with the refrigerant in a shell 2 in the second-stage condensing unit, the gas phase enters the condensation separator 5 to perform gas-liquid separation after the heat exchange is completed, the liquid phase flows back into the rectifying tower, the gas phase enters the heat exchanger 3 of the immersed heat exchanger in a third-stage condensing unit to exchange heat with the refrigerant in the shell 2 in the third-stage condensing unit, the liquid phase flows back into the rectifying tower, and the gas phase enters a tail gas treatment device 15 to perform tail gas treatment; the flow of providing cold energy for the carbon dioxide rectification system by the refrigerant storage tank is as follows: the refrigerant from the refrigerant storage tank 1 enters the shell 2 through the shell inlet 6 of the immersed heat exchanger after being subjected to primary throttling through the first throttle valve 9 in the primary condensing unit, so that the heat exchanger 3 is completely immersed in the refrigerant, and part of the refrigerant is gasified and discharged from the shell gas phase outlet 7 of the immersed heat exchanger in the primary condensing unit to enter the first ice machine 11 to realize the reutilization of the refrigerant; the abundant refrigerant in the shell 2 in the first-stage condensing unit enters the shell in the second-stage condensing unit after being subjected to second-stage throttling through the first throttle valve 9 in the second-stage condensing unit, so that the heat exchanger 3 is completely soaked in the refrigerant, and part of the refrigerant is gasified and discharged from the shell gas phase outlet 7 of the immersed heat exchanger in the second-stage condensing unit to enter the second ice machine 12 to realize the reutilization of the refrigerant; the abundant refrigerant in the shell 2 in the secondary condensation unit enters the shell in the primary condensation unit after three-stage throttling through the first throttle valve 9 in the three-stage condensation unit, so that the heat exchanger 3 is completely soaked in the refrigerant, and part of the refrigerant is gasified and discharged from the shell gas phase outlet 7 of the immersed heat exchanger in the three-stage condensation unit to enter the third ice machine 13 to realize the reutilization of the refrigerant; the process of providing cold energy further comprises that the abundant cold energy in the immersed heat exchanger shell 2 in the primary condensing unit enters the subcooler 18 to exchange heat and cool with the carbon dioxide product from the carbon dioxide product pipeline 19, so as to achieve the purpose of conveniently preserving the product, and meanwhile, the cold energy can enter the second ice machine 12 after being gasified. The utility model adopts the structure of the immersion heat exchanger, the refrigerant is stored in the shell 2 of the condensing unit and fully submerges the heat exchanger, so that hot materials can exchange heat with the refrigerant fully, the bottom of the shell 2 is provided with the shell liquid phase outlet 8, so that abundant refrigerant can be discharged from the bottom into the shell 2 of the subsequent condensing unit, the first throttle valve 9 can realize the stability control of the condenser refrigerant liquid level and is not influenced by other factors, the utility model has the characteristics of realizing the stable control of the refrigerant dosage distribution of the refrigerant liquid level of each stage of condensing unit, stable regulation of the reflux liquid of the rectifying tower according to the requirement, stable rectifying mass transfer heat exchange process, small system fluctuation, and stable and controllable product quality and yield.
Although embodiments of the present utility model have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the utility model, the scope of which is defined in the appended claims and their equivalents.
Claims (7)
1. The utility model provides a carbon dioxide rectification stable control system, includes refrigerant storage tank (1), its characterized in that: the outlet of the refrigerant storage tank (1) is connected with the multistage condensation separation unit,
the condensation separation unit comprises an immersed heat exchanger, the immersed heat exchanger comprises a shell (2) and a heat exchanger (3) arranged inside the shell (2);
the gas-phase carbon dioxide pipeline (4) is connected with the condensation separator (5) through the heat exchanger (3),
the shell (2) of the immersed heat exchanger is provided with a shell inlet (6) and an outlet of the refrigerant storage tank (1), and the top of the shell (2) of the immersed heat exchanger is provided with a shell gas phase outlet (7).
2. The carbon dioxide rectification stabilization control system according to claim 1, wherein: the bottom of the shell (2) of the immersed heat exchanger is respectively provided with a shell liquid phase outlet (8), the shells (2) of the immersed heat exchangers in the multistage condensation separation units are connected in series, and a first throttle valve (9) is arranged at the shell inlet (6).
3. The carbon dioxide rectification stabilization control system according to claim 1, wherein: a first liquid level sensor (10) for monitoring the liquid level of the liquid-phase refrigerant is arranged on a shell (2) of the immersion type heat exchanger.
4. The carbon dioxide rectification stabilization control system according to claim 2, wherein: the multistage condensation separation unit is a three-stage condensation unit, an outlet of the refrigerant storage tank (1) is connected with a shell inlet (6) of the immersed heat exchanger in the first-stage condensation unit, a shell liquid phase outlet (8) of the immersed heat exchanger in the first-stage condensation unit is connected with a shell inlet (6) of the immersed heat exchanger in the second-stage condensation unit, and a shell liquid phase outlet (8) of the immersed heat exchanger in the second-stage condensation unit is connected with a shell inlet (6) of the immersed heat exchanger in the third-stage condensation unit;
the shell gas phase outlet (7) of the immersed heat exchanger in the primary condensation unit is connected with the first ice machine (11), the shell gas phase outlet (7) of the immersed heat exchanger in the secondary condensation unit is connected with the second ice machine (12), and the shell gas phase outlet (7) of the immersed heat exchanger in the tertiary condensation unit is connected with the third ice machine (13).
5. The carbon dioxide rectification stabilization control system according to claim 4, wherein: the gas-phase carbon dioxide pipeline (4) is connected with the condensation separator (5) in the primary condensation unit through the heat exchanger (3) of the immersed heat exchanger in the primary condensation unit, the liquid phase outlet of the condensation separator (5) in the primary condensation unit is connected with the rectifying tower reflux pipeline (14), the gas phase outlet of the condensation separator (5) in the primary condensation unit is connected with the condensation separator (5) in the secondary condensation unit through the heat exchanger (3) of the immersed heat exchanger in the secondary condensation unit, the liquid phase outlet of the condensation separator (5) in the secondary condensation unit is connected with the rectifying tower reflux pipeline (14), the gas phase outlet of the condensation separator (5) in the secondary condensation unit is connected with the condensation separator (5) in the tertiary condensation unit through the heat exchanger (3) of the immersed heat exchanger in the tertiary condensation unit, the liquid phase outlet of the condensation separator (5) in the tertiary condensation unit is connected with the rectifying tower reflux pipeline (14), and the gas phase outlet of the condensation separator (5) in the tertiary condensation unit is connected with the tail gas treatment device (15).
6. The carbon dioxide rectification stabilization control system according to claim 4, wherein: a tee joint (16) is arranged between a shell liquid phase outlet (8) of the submerged heat exchanger in the primary condensation unit and a shell inlet (6) of the submerged heat exchanger in the secondary condensation unit, and a third end of the tee joint (16) is connected with a second ice machine (12) through a second throttle valve (17) and a cold side channel of a subcooler (18);
the hot side channel inlet of the subcooler (18) is connected with a carbon dioxide product pipeline (19), and the hot side channel outlet of the subcooler (18) is connected with a carbon dioxide product storage tank (20).
7. The carbon dioxide rectification stabilization control system according to claim 1, wherein: the device also comprises a PLC control system (21), the signal input end of the PLC control system (21) is respectively connected with the first liquid level sensor (10) and the second liquid level sensor (22), the signal output end of the PLC control system is respectively connected with the first throttle valve (9) and the second throttle valve (17),
a second liquid level sensor (22) is provided on the subcooler (18).
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| Application Number | Priority Date | Filing Date | Title |
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| CN202321534898.1U CN220153070U (en) | 2023-06-15 | 2023-06-15 | Carbon dioxide rectification stability control system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321534898.1U CN220153070U (en) | 2023-06-15 | 2023-06-15 | Carbon dioxide rectification stability control system |
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| CN220153070U true CN220153070U (en) | 2023-12-08 |
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| CN202321534898.1U Active CN220153070U (en) | 2023-06-15 | 2023-06-15 | Carbon dioxide rectification stability control system |
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| CN (1) | CN220153070U (en) |
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