CN114017994A - Process for purifying carbon dioxide from alcohol tail gas - Google Patents
Process for purifying carbon dioxide from alcohol tail gas Download PDFInfo
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- CN114017994A CN114017994A CN202111314287.1A CN202111314287A CN114017994A CN 114017994 A CN114017994 A CN 114017994A CN 202111314287 A CN202111314287 A CN 202111314287A CN 114017994 A CN114017994 A CN 114017994A
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- gas
- rectifying tower
- liquid
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- tail gas
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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
- F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/80—Carbon dioxide
Abstract
The invention provides a process for purifying carbon dioxide from alcohol tail gas, which comprises the following steps: A. pre-cooling and compressing the raw materials before compression; B. pre-cooling the raw materials after desulfurization and compression; C. liquefying and purifying raw materials: a first rectifying tower, a second rectifying tower and a cold circulating system are arranged in the cold box, and gas separated after gas-liquid separation treatment after compression firstly enters the first rectifying tower for rectification; after the gas is rectified by the first rectifying tower, the gas gathered at the tower top of the first rectifying tower enters the second rectifying tower after passing through a cold circulation system, secondary rectification is carried out in the second rectifying tower, and food-grade liquid CO is obtained in a tower kettle of the second rectifying tower after the gas is rectified by the second rectifying tower2Mixing the food-grade liquid CO2The feed grade CO is compressed by a subcooler and a throttle reducing valve2And (4) storing in a storage tank. The invention adopts a double-tower rectification and refrigeration combined process, heavy components with the boiling point higher than that of carbon dioxide are separated and removed in a first rectification tower in a rectification mode, and CO is improved2The purity of (2).
Description
Technical Field
The invention relates to the technical field of alcohol tail gas purification treatment, in particular to a process for purifying carbon dioxide from alcohol tail gas.
Background
The tail gas produced in the alcohol production process is a mixed gas with carbon dioxide as a main component, and comprises 94% of carbon dioxide, 1.7% of oxygen, 3.1% of nitrogen, 0.12% of ethanol, 0.32% of unknown organic matters and the balance of sulfur, hydrogen, nitrogen oxides, sulfur dioxide, hydrogen sulfide, carbonyl sulfide, acetaldehyde and the like. The carbon dioxide in the tail gas is recycled, so that great economic benefit is generated, and great contribution is made to environmental protection.
At present, the recovery of alcohol tail gas generally adopts the mode of water absorption, and this mode needs to use steam, and this mode is generally only done and is retrieved alcohols material, and still can smuggle gases such as ethanol in the implementation in the steam, leads to recovery efficiency low, and adopts prior art can not carry out effectual recovery to carbon dioxide, causes the waste of resource, and the mode of adopting direct evacuation will cause the influence to atmospheric environment again.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides a process for purifying carbon dioxide from alcohol tail gas, which comprises the following steps:
A. pre-cooling and compressing raw materials before compression: firstly, precooling the tail gas before compression, then carrying out gas-liquid separation treatment on the tail gas after precooling before compression, and then enabling the tail gas to enter a compressor to compress the tail gas to 2.5 MpaG-2.9 MpaG;
B. pre-cooling after desulfurization and compression of raw materials: sending the compressed tail gas into a desulfurizing tower, compressing the tail gas and then pre-cooling the tail gas after desulfurization is finished, then compressing the pre-cooled tail gas before compression and then carrying out gas-liquid separation treatment, recovering the separated light wine, and feeding the separated gas into a cold box;
C. liquefying and purifying raw materials: a first rectifying tower, a second rectifying tower and a cold circulating system are arranged in the cold box, and gas separated after gas-liquid separation treatment after compression firstly enters the first rectifying tower for rectification; after the high boiling point impurities in the tail gas are rectified by the first rectifying towerColumn bottom build-up of CO from the column2And low boiling point gas is gathered at the top of the first rectifying tower; gas gathered at the tower top of the first rectifying tower passes through a cold circulation system and then enters the second rectifying tower, secondary rectification is carried out in the second rectifying tower, and food-grade liquid CO is obtained in the tower kettle of the second rectifying tower after rectification in the second rectifying tower2Mixing the food-grade liquid CO2The feed grade CO is compressed by a subcooler and a throttle reducing valve2And (4) storing in a storage tank.
In step B, the gas separated after the gas-liquid separation treatment after the compression is finished passes through a parking dryer before entering the cold box.
Preferably, in the step C, a product extraction outlet is formed in the middle of the second rectifying tower, and the product extraction outlet is connected with industrial grade CO2The storage tanks are connected.
As optimization, the method also comprises the following steps of D: the waste material generated after the heavy material is removed by the first rectifying tower and the waste material generated after the light material is removed by the second rectifying tower are both connected to a sewage discharge pipeline.
As optimization, cold circulating system includes one-level condenser, second grade condenser, the gas outlet of first rectifying column passes through the condenser pipe and links to each other with one-level condenser, and one-level condenser passes through the condenser pipe and links to each other with second grade condenser, and second grade condenser passes through the inlet of condenser pipe and second rectifying column and links to each other.
As optimization, a first-stage gas-liquid separator is communicated between the first-stage condenser and the second-stage condenser, a gas discharge port of the first-stage gas-liquid separator is connected with the second-stage condenser, and a liquid discharge port of the first-stage gas-liquid separator is connected with a liquid inlet of the second rectifying tower;
and a second-stage gas-liquid separator is communicated and arranged between the second-stage condenser and the second rectifying tower, a liquid discharge port of the second-stage gas-liquid separator is connected with a liquid inlet of the second rectifying tower, and a gas discharge port of the second-stage gas-liquid separator refluxes and is discharged after passing through a refrigerator.
As optimization, an ice machine refrigerating system is arranged outside the cold box, and comprises an ammonia storage tank and an ammonia liquid separator; liquid ammonia is filled in the ammonia storage tank; the ammonia storage tank is connected with the ammonia-liquid separator, one liquid phase outlet of the ammonia-liquid separator is connected with the precooler, the other liquid phase outlet of the ammonia-liquid separator is connected with the first-stage condenser, and the gas phase outlet of the first-stage condenser is connected with the standard working condition ice machine.
Preferably, the gas-phase outlet of the ammonia-liquid separator and the gas outlet of the precooler are both connected to one end of a converging pipe through branch pipes, the other end of the converging pipe is connected with two branch pipes, one branch pipe is connected with a reboiler in the first rectifying tower, and the other branch pipe is connected with a reboiler in the second rectifying tower.
Preferably, the cooling liquid discharged from the reboiler in the first rectifying tower and the cooling liquid discharged from the reboiler in the second rectifying tower are both subjected to gas-liquid separation treatment, and the liquid phase subjected to the gas-liquid separation treatment flows back to the first-stage condenser.
Compared with the prior art, the invention mainly has the following beneficial effects:
1. the rectification process of the application adopts an original double-tower rectification technology, the previous drying, dealkylation and dealcoholization equipment is concentrated in one rectification tower, high boiling point substances are gathered at a tower kettle in the first rectification tower, low boiling point substances are gathered at the tower top, the waste liquid at the tower kettle is recovered with cold energy, residual liquid containing a large amount of ethanol is recovered, and heavy components such as water, alcohols and the like in the raw material gas are removed; the tower top gas rectified by the first rectifying tower flows back to the second rectifying tower after multi-stage refrigeration, and food grade liquid CO with the purity of more than or equal to 99.995 percent is obtained in the tower kettle of the second rectifying tower after rectification again2Throttling and decompressing after supercooling, and finally entering a storage tank for storage.
2. The product extraction port is designed in the middle of the second rectifying tower, and interchange and random proportion switching of industrial and food-grade products can be achieved.
3. This application is with first rectifying column, second rectifying column and cold circulating system and through various pipeline, valve even as a whole, installs in a cold box in unison, makes the flow tend to the perfection, makes cold volume loss of cold circulating system lower simultaneously.
4. In the application, all light components (such as hydrocarbon) lower than the boiling point of carbon dioxide are separated and removed in a second rectifying tower in a rectifying mode, a traditional catalytic oxidation hydrocarbon removing device and an adsorption system are not needed, the requirement of food-grade purification can be met, a large amount of investment cost and operation cost are saved, the product quality is far higher than the quality index of the traditional process, the product basically belongs to a high-purity carbon dioxide product, in addition, the equipment arrangement and operation are greatly simplified, and the investment and the operation manpower are saved.
Drawings
In order to more clearly illustrate the embodiments of the present invention, the drawings, which are required to be used in the embodiments, will be briefly described below. In all the drawings, the elements or parts are not necessarily drawn to actual scale.
FIG. 1 is a schematic flow diagram of the present invention;
FIG. 2 is a schematic diagram of the structure of the raw materials of the present invention before entering the cold box;
fig. 3 is a schematic view of the internal structure of the cold box of the present invention.
Reference numerals:
1-a front precooler, 2-a compressor, 3-a front gas-liquid separator, 4-a desulfurizing tower and 5-a cold box;
6-cold box, 61-first rectifying tower, 62-second rectifying tower, 621-product extraction and outlet, 63-cold circulation system, 631-primary condenser, 632-secondary condenser, 633-primary gas-liquid separator, 634-secondary gas-liquid separator, 635-ammonia storage tank, 636-ammonia-liquid separator, 637-branch pipe, 638-confluence pipe and 639-branch pipe;
7-a post precooler and 8-a post gas-liquid separator;
91-food grade CO2Storage tank, 92-technical grade CO2A storage tank;
11-refrigerator.
Detailed Description
Embodiments of the present invention will be described in detail below with reference to the accompanying drawings. The following examples are only for illustrating the technical solutions of the present invention more clearly, and therefore are only examples, and the protection scope of the present invention is not limited thereby.
Example (b): as shown in fig. 1 to 3, a process for purifying carbon dioxide from alcohol off-gas includes the following steps:
A. pre-cooling and compressing raw materials before compression: firstly, precooling the tail gas before compression, then carrying out gas-liquid separation treatment on the tail gas after precooling before compression, then leading the tail gas to enter a compressor 2, and compressing the tail gas to 2.5 MpaG-2.9 MpaG; in the present application, the pre-cooler 1 is used for pre-cooling before compression, and the pre-gas-liquid separator 3 is used for gas-liquid separation before compression.
B. Pre-cooling after desulfurization and compression of raw materials: sending the compressed tail gas into a desulfurizing tower 4, compressing the tail gas and then pre-cooling the tail gas after desulfurization is finished, then compressing the pre-cooled tail gas before compression and then carrying out gas-liquid separation treatment, recovering the separated light wine, and feeding the separated gas into a cold box 5; in the application, a post-precooler 7 is used for precooling treatment after compression, and a post-gas-liquid separator 8 is used for gas-liquid separation treatment after compression.
C. Liquefying and purifying raw materials: a first rectifying tower 61, a second rectifying tower 62 and a cold circulating system 63 are arranged in the cold box 6, and gas separated after gas-liquid separation treatment after compression firstly enters the first rectifying tower 61 for rectification; after the rectification in the first rectification tower 61, the high boiling point impurities in the tail gas are gathered in the tower kettle of the first rectification tower 61, and CO is generated2And the low boiling point gas is accumulated at the top of the first rectifying column 61; the gas gathered at the top of the first rectifying tower 61 passes through a cooling circulation system 63 and then enters a second rectifying tower 62, secondary rectification is carried out in the second rectifying tower 62, and food-grade liquid CO is obtained in the tower kettle of the second rectifying tower 62 after rectification in the second rectifying tower 622Mixing the food-grade liquid CO2The feed grade CO is compressed by a subcooler and a throttle reducing valve2The storage tank 91 stores. In this application, the subcooler is a primary condenser 631.
Specifically, in step B, the gas separated after the gas-liquid separation process after the compression is completed passes through a shutdown dryer before entering the cold box 6. The parking dryer is used only when the apparatus is driven or parked, and is not required to be used in a normal operation.
Specifically, in step C, a product extraction outlet 621 is formed in the middle of the second rectifying tower 62, and the product extraction outlet 621 and the industrial grade CO are connected to each other2The storage tank 92 is connected.
Specifically, the method further comprises the following steps of D, waste treatment: the waste material produced after the heavy material is removed by the first rectifying tower 61 and the waste material produced after the light material is removed by the second rectifying tower 62 are connected to a sewage pipeline.
Specifically, cold circulation system 63 includes one-level condenser 631, second grade condenser 632, the gas outlet of first rectifying column 61 passes through the condenser pipe and links to each other with one-level condenser 631, and one-level condenser 631 passes through the condenser pipe and links to each other with second grade condenser 632, and second grade condenser 632 passes through the condenser pipe and links to each other with the inlet of second rectifying column 62.
Specifically, a primary gas-liquid separator 633 is communicated between the primary condenser 631 and the secondary condenser 632, a gas discharge port of the primary gas-liquid separator 633 is connected with the secondary condenser 632, and a liquid discharge port of the primary gas-liquid separator 633 is connected with a liquid inlet of the second rectifying tower 62;
a second-stage gas-liquid separator 634 is arranged between the second-stage condenser 632 and the second rectifying tower 62 in a communicating manner, a liquid discharge port of the second-stage gas-liquid separator 634 is connected with a liquid inlet of the second rectifying tower 62, and a gas discharge port of the second-stage gas-liquid separator 634 reflows to be discharged after passing through the refrigerator 11.
Specifically, an ice maker refrigeration system is arranged outside the cold box 6, and comprises an ammonia storage tank 635 and an ammonia liquid separator 636; the ammonia storage tank 635 is filled with liquid ammonia; the ammonia storage tank 635 is connected with an ammonia liquid separator 636, one liquid phase outlet of the ammonia liquid separator 636 is connected with a precooler, the other liquid phase outlet of the ammonia liquid separator 636 is connected with a first-stage condenser 631, and the gas phase outlet of the first-stage condenser 631 is connected with a standard working condition ice machine. In the present application, the precooler may be a pre-precooler 1.
Specifically, the gas phase outlet of the ammonia liquid separator 636 and the gas outlet of the precooler are both connected to one end of a confluence pipe 638 via a branch pipe 637, and the other end of the confluence pipe 638 is connected to two branch pipes 639, wherein one branch pipe 639 is connected to the reboiler in the first rectifying column 61, and the other branch pipe 639 is connected to the reboiler in the second rectifying column 62. In the present application, the precooler may be a pre-precooler 1.
Specifically, the cooling liquid discharged from the reboiler in the first rectifying tower 61 and the cooling liquid discharged from the reboiler in the second rectifying tower 62 are both subjected to gas-liquid separation, and the liquid phase subjected to the gas-liquid separation is returned to the first-stage condenser 631.
The above examples are only intended to illustrate the technical solution of the present invention, but not to limit it; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; such modifications and substitutions do not depart from the spirit and scope of the present invention, and they should be construed as being included in the following claims and description.
Claims (9)
1. The process for purifying carbon dioxide from alcohol tail gas is characterized by comprising the following steps of:
A. pre-cooling and compressing raw materials before compression: firstly, precooling the tail gas before compression, then carrying out gas-liquid separation treatment on the tail gas after precooling before compression, and then enabling the tail gas to enter a compressor to compress the tail gas to 2.5 MpaG-2.9 MpaG;
B. pre-cooling after desulfurization and compression of raw materials: sending the compressed tail gas into a desulfurizing tower, compressing the tail gas and then pre-cooling the tail gas after desulfurization is finished, then compressing the pre-cooled tail gas before compression and then carrying out gas-liquid separation treatment, recovering the separated light wine, and feeding the separated gas into a cold box;
C. liquefying and purifying raw materials: a first rectifying tower, a second rectifying tower and a cold circulating system are arranged in the cold box, and gas separated after gas-liquid separation treatment after compression firstly enters the first rectifying tower for rectification; after the distillation of the first rectifying tower, the high boiling point impurities in the tail gas are gathered in the tower kettle of the first rectifying towerCO Collection2And low boiling point gas is gathered at the top of the first rectifying tower; gas gathered at the tower top of the first rectifying tower passes through a cold circulation system and then enters the second rectifying tower, secondary rectification is carried out in the second rectifying tower, and food-grade liquid CO is obtained in the tower kettle of the second rectifying tower after rectification in the second rectifying tower2Mixing the food-grade liquid CO2The feed grade CO is compressed by a subcooler and a throttle reducing valve2And (4) storing in a storage tank.
2. The process for purifying carbon dioxide from alcohol off-gas as claimed in claim 1, wherein in step B, the gas separated after the gas-liquid separation treatment after the compression is performed is passed through a shutdown dryer before entering the cold box.
3. The process for purifying carbon dioxide from alcohol tail gas as claimed in claim 1, wherein in the step C, a product extraction port is opened at the middle part of the second rectifying tower, and the product extraction port is connected with industrial grade CO2The storage tanks are connected.
4. The process for purifying carbon dioxide from alcohol off-gas as claimed in claim 1, further comprising step D, waste treatment: the waste material generated after the heavy material is removed by the first rectifying tower and the waste material generated after the light material is removed by the second rectifying tower are both connected to a sewage discharge pipeline.
5. The process for purifying carbon dioxide from alcohol tail gas as claimed in claim 1, wherein the cold circulation system comprises a first-stage condenser and a second-stage condenser, the gas outlet of the first distillation column is connected with the first-stage condenser through a condensation pipe, the first-stage condenser is connected with the second-stage condenser through a condensation pipe, and the second-stage condenser is connected with the liquid inlet of the second distillation column through a condensation pipe.
6. The process for purifying carbon dioxide from alcohol tail gas as claimed in claim 5, wherein a primary gas-liquid separator is communicated between the primary condenser and the secondary condenser, a gas discharge port of the primary gas-liquid separator is connected with the secondary condenser, and a liquid discharge port of the primary gas-liquid separator is connected with a liquid inlet of the second rectifying tower;
and a second-stage gas-liquid separator is communicated and arranged between the second-stage condenser and the second rectifying tower, a liquid discharge port of the second-stage gas-liquid separator is connected with a liquid inlet of the second rectifying tower, and a gas discharge port of the second-stage gas-liquid separator refluxes and is discharged after passing through a refrigerator.
7. The process for purifying carbon dioxide from alcohol tail gas as claimed in claim 5, wherein an ice machine refrigerating system is arranged outside the cold box, and the ice machine refrigerating system comprises an ammonia storage tank and an ammonia-liquid separator; liquid ammonia is filled in the ammonia storage tank; the ammonia storage tank is connected with the ammonia-liquid separator, one liquid phase outlet of the ammonia-liquid separator is connected with the precooler, the other liquid phase outlet of the ammonia-liquid separator is connected with the first-stage condenser, and the gas phase outlet of the first-stage condenser is connected with the standard working condition ice machine.
8. The process for purifying carbon dioxide from alcohol tail gas as claimed in claim 7, wherein the gas phase outlet of the ammonia-liquid separator and the gas outlet of the precooler are connected to one end of a converging pipe through branch pipes, the other end of the converging pipe is connected with two branch pipes, one branch pipe is connected with a reboiler in the first rectifying tower, and the other branch pipe is connected with a reboiler in the second rectifying tower.
9. The process for purifying carbon dioxide from alcohol tail gas as claimed in claim 8, wherein the cooling liquid discharged from the reboiler in the first distillation column and the cooling liquid discharged from the reboiler in the second distillation column are both subjected to gas-liquid separation, and the liquid phase after the gas-liquid separation is returned to the first-stage condenser.
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| CN202111314287.1A CN114017994B (en) | 2021-11-08 | 2021-11-08 | Process for purifying carbon dioxide from alcohol tail gas |
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| CN202111314287.1A CN114017994B (en) | 2021-11-08 | 2021-11-08 | Process for purifying carbon dioxide from alcohol tail gas |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114570158A (en) * | 2022-05-06 | 2022-06-03 | 山东神驰化工集团有限公司 | Methanol hydrogen production carbon dioxide recovery device and recovery method thereof |
| CN117482688A (en) * | 2023-11-02 | 2024-02-02 | 江苏罗迈特生物科技有限公司 | Process and device for producing high-purity food-grade carbon dioxide by utilizing alcohol fermentation waste gas |
| CN117482688B (en) * | 2023-11-02 | 2024-05-14 | 江苏罗迈特生物科技有限公司 | Process and device for producing high-purity food-grade carbon dioxide by utilizing alcohol fermentation waste gas |
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| CN101607708A (en) * | 2009-07-27 | 2009-12-23 | 申屠晶 | The co-production of technical grade and food-class liquid CO 2 and device |
| US20100150802A1 (en) * | 2008-12-11 | 2010-06-17 | Gilliam Ryan J | Processing co2 utilizing a recirculating solution |
| CN210197865U (en) * | 2019-03-19 | 2020-03-27 | 河南心连心深冷能源股份有限公司 | Cold box capable of producing food-grade carbon dioxide |
| CN214620294U (en) * | 2021-09-26 | 2021-11-05 | 河南心连心深冷能源股份有限公司 | Device for producing industrial grade and food grade carbon dioxide by adopting double-tower rectification |
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2021
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| US20100150802A1 (en) * | 2008-12-11 | 2010-06-17 | Gilliam Ryan J | Processing co2 utilizing a recirculating solution |
| CN101607708A (en) * | 2009-07-27 | 2009-12-23 | 申屠晶 | The co-production of technical grade and food-class liquid CO 2 and device |
| CN210197865U (en) * | 2019-03-19 | 2020-03-27 | 河南心连心深冷能源股份有限公司 | Cold box capable of producing food-grade carbon dioxide |
| CN214620294U (en) * | 2021-09-26 | 2021-11-05 | 河南心连心深冷能源股份有限公司 | Device for producing industrial grade and food grade carbon dioxide by adopting double-tower rectification |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114570158A (en) * | 2022-05-06 | 2022-06-03 | 山东神驰化工集团有限公司 | Methanol hydrogen production carbon dioxide recovery device and recovery method thereof |
| CN117482688A (en) * | 2023-11-02 | 2024-02-02 | 江苏罗迈特生物科技有限公司 | Process and device for producing high-purity food-grade carbon dioxide by utilizing alcohol fermentation waste gas |
| CN117482688B (en) * | 2023-11-02 | 2024-05-14 | 江苏罗迈特生物科技有限公司 | Process and device for producing high-purity food-grade carbon dioxide by utilizing alcohol fermentation waste gas |
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| CN114017994B (en) | 2023-03-10 |
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