CN204513904U - Utilize two-tower rectification to purify and produce the device of food-class liquid CO 2 - Google Patents
Utilize two-tower rectification to purify and produce the device of food-class liquid CO 2 Download PDFInfo
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- CN204513904U CN204513904U CN201520092261.0U CN201520092261U CN204513904U CN 204513904 U CN204513904 U CN 204513904U CN 201520092261 U CN201520092261 U CN 201520092261U CN 204513904 U CN204513904 U CN 204513904U
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Abstract
The utility model belongs to a kind of device utilizing two-tower rectification purification to produce food-class liquid CO 2, comprise the outlet of air inlet surge tank to be connected with the import of unstripped gas four-stage compressor, the outlet of unstripped gas four-stage compressor is connected by the raw material gas inlet of the first reboiler with the first rectifying column middle and lower part, the liquid-phase outlet of the first rectifier bottoms is connected with collector, the gaseous phase outlet at the first rectifying column top is connected with the gas phase import of overhead condenser, the liquid-phase outlet of overhead condenser is connected by the fluid inlet of pipeline with the first rectifier, pipeline between the liquid-phase outlet of overhead condenser and the fluid inlet of the first rectifier is provided with the first threeway, 3rd end of the first threeway is connected with inlet in the middle part of Second distillation column, liquid-phase outlet bottom Second distillation column is connected with the inlet of First Heat Exchanger by pipeline, and the liquid outlet of First Heat Exchanger is connected with carbon dioxide storage tank, there is technological process simple, easy and simple to handle, the advantage of stable and low energy consumption.
Description
Technical field
The utility model belongs to carbon dioxide production technical field, is specifically related to a kind of device utilizing two-tower rectification purification to produce food-class liquid CO 2.
Background technology
The production of traditional food grade carbon-dioxide generally adopts molecular sieve dehydration dealcoholysis and Production by Catalytic Combustion Process to take off hydrocarbon device and technique thereof; Wherein, need a large amount of heats for thermal regeneration gas in the molecular sieve dehydration dealcoholysis stage, energy consumption is higher, and dehydration dealcoholysis then needs successively through release, regeneration, cold blowing, all press, and operating process is complicated; Need the equipment dropped into containing sequencing valve, adsorbent, adsorption tower, electric heater etc. one-time investment is larger; Production by Catalytic Combustion Process takes off the hydrocarbon stage and adopts platinum, palladium series catalyst and patent equipment, and price is higher, and its material needs cold through preheating, heating, de-hydrocarbon, water-cooled and ammonia successively, and energy consumption is higher.Above-mentioned technical process not only brings white elephant to manufacturing enterprise, also for using enterprise to add production cost.
Utility model content
The purpose of this utility model is to overcome defect of the prior art, and provide that a kind of flow process is simple, reasonable in design, easy to operate, stable, energy consumption is low and disposable less investment utilize two-tower rectification to purify to produce the device of food-class liquid CO 2.
The purpose of this utility model is achieved in that and comprises air inlet surge tank, the outlet of air inlet surge tank is connected by the import of pipeline with unstripped gas four-stage compressor, the outlet of unstripped gas four-stage compressor is connected by the raw material gas inlet of the first reboiler with the first rectifying column middle and lower part, the liquid-phase outlet of the first rectifier bottoms is connected with collector, the gaseous phase outlet at the first rectifying column top is connected with the gas phase import of overhead condenser, the liquid-phase outlet of overhead condenser is connected by the fluid inlet of pipeline with the first rectifier, pipeline between the liquid-phase outlet of overhead condenser and the fluid inlet of the first rectifier is provided with the first threeway, 3rd end of the first threeway by pipeline successively with the second reboiler, first control valve is connected with inlet in the middle part of Second distillation column, liquid-phase outlet bottom Second distillation column is connected with the inlet of First Heat Exchanger by pipeline, and the liquid outlet of First Heat Exchanger is connected with carbon dioxide storage tank, the gaseous phase outlet at described overhead condenser top is connected with gas-liquid separator with the shell side of the second heat exchanger by the second threeway, liquid-phase outlet bottom gas-liquid separator is connected by the fluid inlet of pipeline with Second distillation column top, the gaseous phase outlet at gas-liquid separator top is connected with the first gas phase import of First Heat Exchanger, and the first gaseous phase outlet of First Heat Exchanger is connected with waste gas header, the gaseous phase outlet at described Second distillation column top is connected with the 3rd end of the second threeway by pipeline, pipeline between described second reboiler and the first control valve is provided with the 3rd threeway, 3rd end of described 3rd threeway is connected with the second gas phase import of First Heat Exchanger with the tube side of the second heat exchanger by the second control valve, and the second gaseous phase outlet of First Heat Exchanger is connected with the two-stage compression air inlet of unstripped gas four-stage compressor by pipeline.
For catalyst, pass into oxygen with noble metal (palladium molybdenum) catalyst in traditional food grade carbon-dioxide production process, under 425 DEG C of conditions, benzene, hydrocarbon compound are oxidized to carbon dioxide and water, whole process must be heated to 425 DEG C through electric heater.Food-grade carbon-dioxide is produced after the incoagulable gas such as the gas after catalytic oxidation, through again cooling, enters cryogenic system and carries out cryogenic rectification after molecular sieve drying, removing oxygen.The utility model overcomes the employing of above-mentioned traditional concept, by compressor, unstripped gas is pressurized to 4.8MPa, unstripped gas after pressurization regulates its temperature by the water-cooled of additional multiple line, pass into the first reboiler of the first rectifier bottoms, maintain rectifying column column bottom temperature between 50 ~ 75 DEG C by multiple line valve opening.Enter in the middle part of the first rectifying column from the first reboiler unstripped gas out, high boiling substance discharges system from tower reactor, overhead condensation liquid partial reflux, major part condensed fluid to enter to bottom Second distillation column the second reboiler for rectifying provides cold, then be divided into two strands, one throttling enters Second distillation column as after 3.5MPa, another meropodium flow to 1.2MPa for the second heat exchanger cold is provided after enter First Heat Exchanger, enter compressor secondary inlet after recovery section cold.The second heat exchanger shell pass is entered after Second distillation column top fixed gas and the first rectifying column top fixed gas bout, gas-liquid separator is entered after partial liquefaction, liquid-phase reflux is in Second distillation column, and gas-liquid separator top fixed gas enters First Heat Exchanger, discharges system after reclaiming cold; Bottom Second distillation column high-pureness carbon dioxide enter First Heat Exchanger cross cold after enter in carbon dioxide storage tank, there is technological process simple, easy and simple to handle, the advantage of stable and low energy consumption.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model.
Detailed description of the invention
As shown in Figure 1, the utility model is for comprising air inlet surge tank 22, air inlet surge tank 22 is exported and is connected by the import of pipeline with unstripped gas four-stage compressor 1, the outlet of unstripped gas four-stage compressor 1 is connected by the raw material gas inlet of the first reboiler 2 with the first rectifying column 3 middle and lower part, liquid-phase outlet bottom first rectifying column 3 is connected with collector 4, the gaseous phase outlet at the first rectifying column 3 top is connected with the gas phase import of overhead condenser 5, the liquid-phase outlet of overhead condenser 5 is connected by the fluid inlet of pipeline with the first rectifying column 3 top, pipeline between the liquid-phase outlet of overhead condenser 5 and the fluid inlet on the first rectifying column 3 top is provided with the first threeway 13, 3rd end of the first threeway 13 by pipeline successively with the second reboiler 8, first control valve 10 is connected with inlet in the middle part of Second distillation column 9, liquid-phase outlet bottom Second distillation column 9 is connected by the inlet of pipeline with First Heat Exchanger 12, and the liquid outlet of First Heat Exchanger 12 is connected with carbon dioxide storage tank 16, the gaseous phase outlet at described overhead condenser 5 top is connected with gas-liquid separator 7 with the shell side of the second heat exchanger 6 by the second threeway 14, liquid-phase outlet bottom gas-liquid separator 7 is connected by the fluid inlet of pipeline with Second distillation column 9 top, the gaseous phase outlet at gas-liquid separator 7 top is connected with the first gas phase import 18 of First Heat Exchanger 12, and the first gaseous phase outlet 19 of First Heat Exchanger 12 is connected with waste gas header 17, the gaseous phase outlet at described Second distillation column 9 top is connected with the 3rd end of the second threeway 14 by pipeline, pipeline between described second reboiler 8 and the first control valve 10 is provided with the 3rd threeway 15,3rd end of described 3rd threeway 15 is connected with the second gas phase import 20 of First Heat Exchanger 12 with the tube side of the second heat exchanger 6 by the second control valve 11, and the second gaseous phase outlet 21 of First Heat Exchanger 12 is connected with the two-stage compression air inlet of unstripped gas four-stage compressor 1 by pipeline.
Operation principle of the present utility model comprises the steps: step one: unstripped gas enters the first reboiler 2 import by air inlet surge tank 22 and unstripped gas four-stage compressor 1, the component of described unstripped gas is: carbon dioxide 95 ~ 99%, water 0.4 ~ 2%, alcohol 0.1 ~ 2%, hydrocarbon 0.1 ~ 1%, temperature is: 10 ~ 40 DEG C, and pressure is: 0.1 ~ 0.2Mpa; Described unstripped gas by the temperature after unstripped gas four-stage compressor 1 is: 90 ~ 120 DEG C, and pressure is 4 ~ 6Mpa; Step 2: make to enter the first reboiler 2 imported materials gas described in step one and enter in the first rectifying column 3 by the raw material gas inlet of the first reboiler 2 and the first rectifying column 3 middle and lower part; The raw material gas inlet of described first rectifying column 3 middle and lower part goes out unstripped gas temperature and is: 30 ~ 80 DEG C; Step 3: make to enter described in step 2 unstripped gas in the first rectifying column 3 and overhead condenser 5 and carry out mass-and heat-transfer by the low-boiling point material entering the first rectifying column 3 in the fluid inlet on the first threeway 13 and the first rectifying column 3 top, high boiling substance after mass-and heat-transfer enters in collector 4 by the liquid-phase outlet bottom the first rectifying column 3 after condensation, and its low-boiling point material enters in overhead condenser 5 by the gaseous phase outlet at the first rectifying column 3 top and the gas phase import of overhead condenser 5; High boiling substance component in the described collector 4 entered is: carbon dioxide 30 ~ 35%, alcohol 5 ~ 11%, water 40 ~ 60%, hydro carbons 0.1 ~ 1%, and temperature is: 50 ~ 80 DEG C, and pressure is 4 ~ 6Mpa; Step 4: make the liquid phase of the low-boiling point material in overhead condenser 5 described in step 3 by the first threeway 13, the liquid phase of part low-boiling point material enters in the first rectifying column 3 in the fluid inlet on the first rectifying column 3 top carries out mass-and heat-transfer with the unstripped gas in the first rectifying column 3, the liquid phase of another part low-boiling point material is divided into two-way, and first via inlet in the middle part of the second reboiler 8, the 3rd threeway 15, first control valve 10 and Second distillation column 9 enters the inside of Second distillation column 9; Second tunnel second reboiler the 8, the 3rd threeway 15 and the second control valve 11 enter the tube side of the second heat exchanger 6; The described liquidus temperature entering the low-boiling point material of Second distillation column 9 inside is: 5 ~-10 DEG C, and pressure is 4 ~ 6Mpa, and flow is 748Nm
3/ h; The liquid phase component of low-boiling point material in described rectifying column overhead condenser 5: carbon dioxide 99.3%, foreign gas 0.7%, temperature is 5 ~-10 DEG C, and pressure is 4.8Mpa; The liquidus temperature entering the low-boiling point material of the second heat exchanger 6 tube side is :-30 ~-45 DEG C, and pressure is 1.0 ~ 2.0Mpa; Step 5: the carbon dioxide rich solution that the liquid phase of the low-boiling point material entering Second distillation column 9 inside described in step 4 and the fluid inlet by the liquid-phase outlet bottom gas-liquid separator 7 and Second distillation column 9 top are entered in Second distillation column 9 carries out mass-and heat-transfer, after mass-and heat-transfer, the gas phase of secondary low-boiling point material discharges Second distillation column 9 by the gaseous phase outlet at Second distillation column 9 top, and its secondary high boiling substance enters in carbon dioxide storage tank 16 by the inlet of the liquid-phase outlet bottom Second distillation column 9, First Heat Exchanger 12 and the liquid outlet of First Heat Exchanger 12; Liquid-phase outlet secondary high boiling substance component bottom described Second distillation column 9 is: carbon dioxide 99.99%, flow is: 666Nm
3/ h, temperature is :-10 ~-20 DEG C, and pressure is 1.5 ~ 3.0Mpa; The temperature of the secondary high boiling substance of the inlet of described First Heat Exchanger 12 is :-10 ~-20 DEG C, and pressure is: 1.5 ~ 3.0Mpa; The temperature of the liquid outlet secondary high boiling substance of described First Heat Exchanger 12 is :-15 DEG C ~-20 DEG C, pressure is: 1.5 ~ 3.0Mpa; The described secondary high boiling substance entered in carbon dioxide storage tank 16 is food-grade carbon-dioxide, and its carbon dioxide content is 99.99%; Step 6: make the gas phase of the low-boiling point material in overhead condenser 5 described in step 3 enter in the shell side of the second heat exchanger 6 by overhead condenser 5 gaseous phase outlet and the second threeway 14, the gas phase of the secondary low-boiling point material of discharging Second distillation column 9 described in step 5 is entered in the shell side of the second heat exchanger 6 by the second threeway 14, makes the gas phase of the gas phase of the gas phase of low-boiling point material and secondary low-boiling point material in the shell side of the second heat exchanger 6 after mixed heat transfer enter in gas-liquid separator 7; The gaseous component of the low-boiling point material of described overhead condenser 5 gaseous phase outlet is carbon dioxide 50 ~ 65%, and temperature is: 0 ~-10 DEG C, pressure is: 4.8Mpa; The gaseous component of the secondary low-boiling point material of described Second distillation column 9 is: carbon dioxide 91%, hydrogen 1%, oxygen 2.1%, nitrogen 5.9%, and temperature is: 0 ~-15 DEG C, and pressure is 1.0 ~ 2.5Mpa; Gas temperature in described second heat exchanger 6 shell side after mixed heat transfer is :-30 DEG C, pressure is: 1.26Mpa; Step 7: make the gas phase entered described in step 6 in gas-liquid separator 7 after mixed heat transfer carry out gas-liquid separation, carbon dioxide rich solution after gas-liquid separation enters in Second distillation column 9 by the fluid inlet on the liquid-phase outlet bottom gas-liquid separator 7 and Second distillation column 9 top, and the waste gas after gas-liquid separation enters waste gas header 17 by the first gaseous phase outlet 19 of the gaseous phase outlet at gas-liquid separator 7 top, the first gas phase import 18 of First Heat Exchanger 12 and First Heat Exchanger 12; Described go out the carbon dioxide rich solution component of liquid-phase outlet bottom gas-liquid separator 7 be: carbon dioxide 80 ~ 90%, temperature is :-10 ~-32 DEG C, and pressure is 1.5 ~ 3.0MPa; Described go out the waste gas component of gaseous phase outlet at gas-liquid separator 7 top be: carbon dioxide 30 ~ 52%, temperature is-10 ~-32 DEG C, and pressure is 1.5 ~ 3.0MPa; Step 8: make the liquid phase of the low-boiling point material entering the second heat exchanger 6 tube side described in step 4 be entered the two-stage compression air inlet of unstripped gas four-stage compressor 1 successively by the second gas phase import 20 of the second heat exchanger 6 tube side, First Heat Exchanger 12 and the second gaseous phase outlet 21 of First Heat Exchanger 12; The described liquidus temperature entering the low-boiling point material of the two-stage compression air inlet of unstripped gas four-stage compressor 1 is :-14 DEG C, and pressure is 1.0 ~ 2.0Mpa.
Claims (1)
1. the device utilizing two-tower rectification purification to produce food-class liquid CO 2, it is characterized in that: this device comprises air inlet surge tank (22), air inlet surge tank (22) outlet is connected by the import of pipeline with unstripped gas four-stage compressor (1), the outlet of unstripped gas four-stage compressor (1) is connected by the raw material gas inlet of the first reboiler (2) with the first rectifying column (3) middle and lower part, the liquid-phase outlet of the first rectifying column (3) bottom is connected with collector (4), the gaseous phase outlet at the first rectifying column (3) top is connected with the gas phase import of overhead condenser (5), the liquid-phase outlet of overhead condenser (5) is connected by the fluid inlet of pipeline with the first rectifying column (3) top, pipeline between the liquid-phase outlet of overhead condenser (5) and the fluid inlet on the first rectifying column (3) top is provided with the first threeway (13), 3rd end of the first threeway (13) by pipeline successively with the second reboiler (8), first control valve (10) is connected with Second distillation column (9) middle part inlet, the liquid-phase outlet of Second distillation column (9) bottom is connected by the inlet of pipeline with First Heat Exchanger (12), and the liquid outlet of First Heat Exchanger (12) is connected with carbon dioxide storage tank (16), the gaseous phase outlet at described overhead condenser (5) top is connected with gas-liquid separator (7) with the shell side of the second heat exchanger (6) by the second threeway (14), the liquid-phase outlet of gas-liquid separator (7) bottom is connected by the fluid inlet of pipeline with Second distillation column (9) top, the gaseous phase outlet at gas-liquid separator (7) top is connected with the first gas phase import (18) of First Heat Exchanger (12), and first gaseous phase outlet (19) of First Heat Exchanger (12) is connected with waste gas header (17), the gaseous phase outlet at described Second distillation column (9) top is connected with the 3rd end of the second threeway (14) by pipeline, pipeline between described second reboiler (8) and the first control valve (10) is provided with the 3rd threeway (15), 3rd end of described 3rd threeway (15) is connected with the second gas phase import (20) of First Heat Exchanger (12) with the tube side of the second heat exchanger (6) by the second control valve (11), and second gaseous phase outlet (21) of First Heat Exchanger (12) is connected by the two-stage compression air inlet of pipeline with unstripped gas four-stage compressor (1).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520092261.0U CN204513904U (en) | 2015-02-02 | 2015-02-02 | Utilize two-tower rectification to purify and produce the device of food-class liquid CO 2 |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201520092261.0U CN204513904U (en) | 2015-02-02 | 2015-02-02 | Utilize two-tower rectification to purify and produce the device of food-class liquid CO 2 |
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| CN204513904U true CN204513904U (en) | 2015-07-29 |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104654739A (en) * | 2015-02-02 | 2015-05-27 | 河南心连心深冷能源股份有限公司 | Device and method for preparing food-grade liquid carbon dioxide by rectification and purification with double towers |
| CN106744956A (en) * | 2016-12-22 | 2017-05-31 | 乐陵胜利新能源有限责任公司 | A kind of high-pressure washing methane purification carbon dioxide in process recovery process |
| CN111256432A (en) * | 2020-03-12 | 2020-06-09 | 金昌隆博气体有限责任公司 | Device and method for treating carbon dioxide rectification separation waste liquid |
| CN111895724A (en) * | 2020-07-01 | 2020-11-06 | 陕西裕隆气体有限公司 | Carbon dioxide dehydration method |
-
2015
- 2015-02-02 CN CN201520092261.0U patent/CN204513904U/en not_active Withdrawn - After Issue
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104654739A (en) * | 2015-02-02 | 2015-05-27 | 河南心连心深冷能源股份有限公司 | Device and method for preparing food-grade liquid carbon dioxide by rectification and purification with double towers |
| CN106744956A (en) * | 2016-12-22 | 2017-05-31 | 乐陵胜利新能源有限责任公司 | A kind of high-pressure washing methane purification carbon dioxide in process recovery process |
| CN111256432A (en) * | 2020-03-12 | 2020-06-09 | 金昌隆博气体有限责任公司 | Device and method for treating carbon dioxide rectification separation waste liquid |
| CN111256432B (en) * | 2020-03-12 | 2024-03-08 | 金昌隆博气体有限责任公司 | Device and method for treating waste liquid from carbon dioxide rectification separation |
| CN111895724A (en) * | 2020-07-01 | 2020-11-06 | 陕西裕隆气体有限公司 | Carbon dioxide dehydration method |
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| C14 | Grant of patent or utility model | ||
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Granted publication date: 20150729 Effective date of abandoning: 20170405 |
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| AV01 | Patent right actively abandoned |