CN215288580U - System for preparing methanol by carbon dioxide hydrogenation - Google Patents
System for preparing methanol by carbon dioxide hydrogenation Download PDFInfo
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- CN215288580U CN215288580U CN202120925525.1U CN202120925525U CN215288580U CN 215288580 U CN215288580 U CN 215288580U CN 202120925525 U CN202120925525 U CN 202120925525U CN 215288580 U CN215288580 U CN 215288580U
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Abstract
The utility model discloses a system for preparing methanol by carbon dioxide hydrogenation, which comprises at least three stages of methanol preparation units connected in series, wherein each methanol preparation unit comprises a tower preheater, a methanol synthesis tower, a methanol water cooler and a methanol separator; a raw material inlet of the tower preheater is communicated with a purified raw material mixed gas pipe, and a raw material outlet of the tower preheater is communicated with a gas inlet of the methanol synthesis tower; the gas outlet of the methanol synthesis tower is communicated with the high-temperature gas inlet of the tower preheater, the high-temperature gas outlet of the tower preheater is communicated with the feed inlet of the methanol water cooler, and the discharge outlet of the methanol water cooler is communicated with the feed inlet of the methanol separator; the gas outlet of the methanol separator of the previous stage methanol preparation unit is communicated with the raw material gas inlet of the tower-entering preheater of the next stage methanol preparation unit; the gas outlet of the methanol separator of the last stage of methanol preparation unit is communicated with the gas inlet of the methanol water washing tower. A recycle gas compressor is omitted, the non-recycle cycle of the methanol prepared by carbon dioxide hydrogenation is realized, and the compression work is saved.
Description
Technical Field
The utility model relates to a system for carbon dioxide hydrogenation preparation methyl alcohol belongs to methyl alcohol preparation system and technology technical field.
Background
Methanol is an important chemical basic raw material and an important fuel, and currently, the methanol is mainly synthesized gas (H) from natural gas or coal2+ CO) preparation. Recently, with the proposition of the target of 'carbon peak reaching and carbon neutralization', a technical route for preparing methanol by carbon dioxide hydrogenation, which is one of large-scale utilization ways of carbon dioxide, is increasingly emphasized, and the technical route also has an important supporting function on the development of a CCUS industrial chain, so that on one hand, the emission of greenhouse gases can be reduced, and the cyclic utilization of carbon and hydrogen sources is realized; on the other hand, the method can be linked with new energy such as hydrogen production by electrolysis, chlor-alkali and the like, realizes the storage of hydrogen energy, provides a brand new and convenient idea for methanol production and energy storage, and has good economic and social benefits.
A typical flow of the technology for preparing methanol by hydrogenating carbon dioxide comprises a gas compression system, a synthesis reaction system, a rectification system and the like. The working pressure of the synthesis reaction tower is 4.0MPa to 10.0MPa, and the working temperature is 230 ℃ to 265 ℃.
In a reaction system for preparing methanol by hydrogenating carbon dioxide, the main chemical reaction formula is as follows:
at present, a synthesis gas circulation process is generally adopted in a device for preparing methanol by carbon dioxide hydrogenation to control the reaction temperature of a methanol synthesis tower and realize complete conversion of the synthesis gas, and the process comprises the steps of recovering heat from the synthesis gas after the methanol synthesis reaction, cooling and separating out crude methanol, sending the rest unreacted synthesis gas (which is used as a part of purge gas discharge for keeping the balance of inert gas of a system and preventing accumulation) to a circulation gas compressor, mixing and boosting the rest unreacted synthesis gas and fresh raw material gas, and then sending the mixture to the methanol synthesis tower for circular production. The use of a recycle compressor leads to increased operating costs and complicated operation and maintenance.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a system for carbon dioxide hydrogenation preparation methyl alcohol does not adopt the circulation flow, has cancelled circulation gas compressor to reduce manufacturing cost, be convenient for operation maintenance, operation safety and stability.
In order to solve the technical problem, the utility model discloses a following technical scheme:
a system for preparing methanol by carbon dioxide hydrogenation comprises at least three stages of methanol preparation units connected in series, wherein each methanol preparation unit comprises an inlet tower preheater, a methanol synthesis tower, a methanol water cooler and a methanol separator; a raw material inlet of the tower preheater is communicated with a purified raw material mixed gas pipe, and a raw material outlet of the tower preheater is communicated with a gas inlet of the methanol synthesis tower; the gas outlet of the methanol synthesis tower is communicated with the high-temperature gas inlet of the tower preheater, the high-temperature gas outlet of the tower preheater is communicated with the feed inlet of the methanol water cooler, and the discharge outlet of the methanol water cooler is communicated with the feed inlet of the methanol separator; the gas outlet of the methanol separator of the previous stage methanol preparation unit is communicated with the raw material gas inlet of the tower-entering preheater of the next stage methanol preparation unit; the gas outlet of the methanol separator of the last stage of methanol preparation unit is communicated with the gas inlet of the methanol water washing tower; liquid outlets of the methanol separators of all stages of methanol preparation units are communicated with a liquid inlet of the methanol flash tank; the liquid outlet of the methanol water washing tower is communicated with the liquid inlet of the methanol flash tank.
In the system for preparing methanol by hydrogenating carbon dioxide, the liquid inlet of the methanol water washing tower is communicated with the desalted water supply device.
In the system for preparing methanol by carbon dioxide hydrogenation, the gas outlet of the methanol water washing tower is communicated with the hydrogen recovery device.
In the system for preparing methanol by hydrogenating carbon dioxide, the liquid outlet of the methanol flash tank is communicated with the methanol rectification system.
In the foregoing system for preparing methanol by hydrogenating carbon dioxide, the system includes three to eight stages of methanol preparation units connected in series.
The process for preparing the methanol by hydrogenating the carbon dioxide comprises the following steps: adding raw material mixed gas into a raw material gas inlet of an inlet tower preheater of a first-stage methanol preparation unit, heating the raw material mixed gas in the inlet tower preheater to a specified temperature, then introducing the heated raw material mixed gas into a methanol synthesis tower, and taking tower outlet gas after reaction of the methanol synthesis tower as a heat source to enter a high-temperature gas inlet of the inlet tower preheater; discharging the reacted tower outlet gas from the tower inlet preheater, reducing the temperature to a specified temperature through a methanol water cooler, introducing the cooled tower outlet gas into a methanol separator, introducing the separated crude methanol into a methanol flash tank, and introducing unreacted gas into a next-stage methanol preparation unit; the next stage of methanol preparation unit repeats the process until the mixed gas which is not reacted after being treated by the last stage of methanol preparation unit recovers methanol in a gas phase through a methanol washing tower, and then the mixed gas is discharged after being extracted by a hydrogen recovery device.
The process for preparing methanol by hydrogenating carbon dioxide further comprises the following steps: methanol in the gas phase is absorbed by desalted water in a water wash column, and then the wash water is led to a methanol flash drum to recover methanol absorbed by desalted water.
In the above-mentioned process for preparing methanol by hydrogenating carbon dioxide, the hydrogen-carbon ratio (H) of the raw material gas mixture introduced into the tower preheater of the first stage methanol preparation unit2+CO)/(CO+CO2) 2.5 to 3.5, the reaction temperature in the methanol synthesis tower is 230 to 265 ℃, and the methanol water cooler reduces the tower outlet gas after the reaction to 35 to 45 ℃.
In the above-mentioned process for preparing methanol by hydrogenating carbon dioxide, the hydrogen-carbon ratio (H) of the raw material gas mixture introduced into the tower preheater of the first stage methanol preparation unit2+CO)/(CO+CO2) 3.05 to 3.1, the reaction temperature in the methanol synthesis tower is 240 to 250 ℃, and the methanol water cooler reduces the tower outlet gas after the reaction to 40 ℃.
Compared with the prior art, the utility model discloses methanol synthesis tower adopts the form of establishing ties, and the former one-level synthetic tower exhaust process gas is as the feed gas of next stage synthetic tower after cooling separation coarse methanol, and the play tower gas of final stage synthetic tower is arranged outside after the recovery hydrogen through the methanol in the demineralized water absorption gas phase, the speed of releasing. Thereby saving a recycle gas compressor, realizing the non-recycle of the methanol synthesis and saving the compression work. By adopting the scheme, the energy consumption can be reduced by about 25%, and the number of the methanol preparation units connected in series can be set according to different requirements.
Drawings
Fig. 1 is a schematic structural diagram of an embodiment of the present invention;
FIG. 2 is a schematic diagram of the structure of a methanol production unit.
Reference numerals: the system comprises a 1-methanol preparation unit, a 2-methanol water washing tower, a 3-methanol flash tank, a 4-methanol synthesis tower, a 5-methanol water cooler, a 6-methanol separator and a 7-tower preheater.
The present invention will be further described with reference to the accompanying drawings and the detailed description.
Detailed Description
The system embodiment of the utility model 1: a system for preparing methanol by carbon dioxide hydrogenation comprises a methanol preparation unit 1 with at least three stages connected in series, wherein the methanol preparation unit 1 comprises an inlet tower preheater 7, a methanol synthesis tower 4, a methanol water cooler 5 and a methanol separator 6; a raw material inlet of the tower preheater 7 is communicated with the purified raw material mixed gas pipe, and a raw material outlet of the tower preheater 7 is communicated with a gas inlet of the methanol synthesis tower 4; the gas outlet of the methanol synthesis tower 4 is communicated with the high-temperature gas inlet of the tower preheater 7, the high-temperature gas outlet of the tower preheater 7 is communicated with the feed inlet of the methanol water cooler 5, and the discharge outlet of the methanol water cooler 5 is communicated with the feed inlet of the methanol separator 6; the gas outlet of the methanol separator 6 of the previous stage methanol preparation unit 1 is communicated with the raw material gas inlet of the tower-entering preheater 7 of the next stage methanol preparation unit 1; the gas outlet of the methanol separator 6 of the last stage of the methanol preparation unit 1 is communicated with the gas inlet of the methanol water washing tower 2; the liquid outlet of the methanol separator 6 of each stage of the methanol preparation unit 1 is communicated with the liquid inlet of the methanol flash tank 3; the liquid outlet of the methanol water washing tower 2 is communicated with the liquid inlet of the methanol flash tank 3. The liquid inlet of the methanol water washing tower 2 is communicated with a desalted water supply device. The gas outlet of the methanol water washing tower 2 is communicated with a hydrogen recovery device. And a liquid outlet of the methanol flash tank 3 is communicated with a methanol rectification system. The system comprises three to eight stages of methanol preparation units 1 connected in series.
Process example 1: a process for preparing methanol by hydrogenating carbon dioxide, which adopts the system for preparing methanol by hydrogenating carbon dioxide as described in example 1, and comprises the following steps: adding raw material mixed gas into a raw material gas inlet of a tower entering preheater 7 of a first-stage methanol preparation unit 1, heating the raw material mixed gas in the tower entering preheater 7 to a specified temperature, then introducing the heated raw material mixed gas into a methanol synthesis tower 4, reacting the synthesis gas in a catalytic bed layer of the methanol synthesis tower, removing reaction heat from boiler water to obtain byproduct steam, and taking tower outlet gas after the reaction of the methanol synthesis tower 4 as a heat source to enter a high-temperature gas inlet of the tower entering preheater 7; the reacted tower gas is discharged from a tower preheater 7, then is reduced to a specified temperature through a methanol water cooler 5, then is guided into a methanol separator 6, the separated crude methanol enters a methanol flash tank, and the unreacted gas enters a next-stage methanol preparation unit 1; the next-stage methanol preparation unit 1 repeats the process until the unreacted mixed gas treated by the last-stage methanol preparation unit 1 passes through a methanol washing tower to recover methanol in a gas phase, and then is discharged after hydrogen is extracted by a hydrogen recovery device.
The process also includes the following steps: methanol in the gas phase is absorbed by desalted water in a water wash column, and then the wash water is led to a methanol flash drum to recover methanol absorbed by desalted water. The hydrogen-to-carbon ratio (H) of the raw material mixture introduced into the column preheater 7 of the first-stage methanol production unit 12+CO)/(CO+CO2) Is 2.5, reaction in the methanol Synthesis column 4The temperature is 230 ℃, and the methanol water cooler 5 reduces the reacted tower gas to 35 ℃.
Process example 2: a process for preparing methanol by hydrogenating carbon dioxide, which adopts the system for preparing methanol by hydrogenating carbon dioxide as described in example 1, and comprises the following steps: adding raw material mixed gas into a raw material gas inlet of a tower entering preheater 7 of a first-stage methanol preparation unit 1, heating the raw material mixed gas in the tower entering preheater 7 to a specified temperature, then introducing the heated raw material mixed gas into a methanol synthesis tower 4, reacting the synthesis gas in a catalytic bed layer of the methanol synthesis tower, removing reaction heat from boiler water to obtain byproduct steam, and taking tower outlet gas after the reaction of the methanol synthesis tower 4 as a heat source to enter a high-temperature gas inlet of the tower entering preheater 7; the reacted tower gas is discharged from a tower preheater 7, then is reduced to a specified temperature through a methanol water cooler 5, then is guided into a methanol separator 6, the separated crude methanol enters a methanol flash tank, and the unreacted gas enters a next-stage methanol preparation unit 1; the next-stage methanol preparation unit 1 repeats the process until the mixed gas which is not reacted after being treated by the last-stage methanol preparation unit 1 absorbs methanol in a gas phase through a methanol water washing tower, and then the mixed gas is discharged after being extracted by a hydrogen recovery device.
The process also includes the following steps: methanol in the gas phase is absorbed by desalted water in a water wash column, and then the wash water is led to a methanol flash drum to recover methanol absorbed by desalted water. The hydrogen-to-carbon ratio (H) of the raw material mixture introduced into the column preheater 7 of the first-stage methanol production unit 12+CO)/(CO+CO2) 3.5, the reaction temperature in the methanol synthesis tower 4 is 265 ℃, and the methanol water cooler 5 reduces the tower gas after the reaction to 45 ℃.
Process example 3: a process for preparing methanol by hydrogenating carbon dioxide, which adopts the system for preparing methanol by hydrogenating carbon dioxide as described in example 1, and comprises the following steps: adding raw material mixed gas into a raw material gas inlet of a tower entering preheater 7 of a first-stage methanol preparation unit 1, heating the raw material mixed gas in the tower entering preheater 7 to a specified temperature, then introducing the heated raw material mixed gas into a methanol synthesis tower 4, reacting the synthesis gas in a catalytic bed layer of the methanol synthesis tower, removing reaction heat from boiler water to obtain byproduct steam, and taking tower outlet gas after the reaction of the methanol synthesis tower 4 as a heat source to enter a high-temperature gas inlet of the tower entering preheater 7; the reacted tower gas is discharged from a tower preheater 7, then is reduced to a specified temperature through a methanol water cooler 5, then is guided into a methanol separator 6, the separated crude methanol enters a methanol flash tank, and the unreacted gas enters a next-stage methanol preparation unit 1; the next-stage methanol preparation unit 1 repeats the process until the mixed gas which is not reacted after being treated by the last-stage methanol preparation unit 1 absorbs methanol in a gas phase through a methanol water washing tower, and then the mixed gas is discharged after being extracted by a hydrogen recovery device.
The process also includes the following steps: methanol in the gas phase is absorbed by desalted water in a water wash column, and then the wash water is led to a methanol flash drum to recover methanol absorbed by desalted water. The hydrogen-to-carbon ratio (H) of the raw material mixture introduced into the column preheater 7 of the first-stage methanol production unit 12+CO)/(CO+CO2) 3.05, the reaction temperature in the methanol synthesis tower 4 is 240 ℃, and the methanol water cooler 5 reduces the tower gas after the reaction to 40 ℃.
Process example 4: a process for preparing methanol by hydrogenating carbon dioxide, which adopts the system for preparing methanol by hydrogenating carbon dioxide as described in example 1, and comprises the following steps: adding raw material mixed gas into a raw material gas inlet of a tower entering preheater 7 of a first-stage methanol preparation unit 1, heating the raw material mixed gas in the tower entering preheater 7 to a specified temperature, then introducing the heated raw material mixed gas into a methanol synthesis tower 4, reacting the synthesis gas in a catalytic bed layer of the methanol synthesis tower, removing reaction heat from boiler water to obtain byproduct steam, and taking tower outlet gas after the reaction of the methanol synthesis tower 4 as a heat source to enter a high-temperature gas inlet of the tower entering preheater 7; the reacted tower gas is discharged from a tower preheater 7, then is reduced to a specified temperature through a methanol water cooler 5, then is guided into a methanol separator 6, the separated crude methanol enters a methanol flash tank, and the unreacted gas enters a next-stage methanol preparation unit 1; the next-stage methanol preparation unit 1 repeats the process until the mixed gas which is not reacted after being treated by the last-stage methanol preparation unit 1 absorbs methanol in a gas phase through a methanol water washing tower, and then the mixed gas is discharged after being extracted by a hydrogen recovery device.
The process also includes the following steps: methanol in the gas phase is absorbed by desalted water in a water wash column, and then the wash water is led to a methanol flash drum to recover methanol absorbed by desalted water. The hydrogen-to-carbon ratio (H) of the raw material mixture introduced into the column preheater 7 of the first-stage methanol production unit 12+CO)/(CO+CO2) 3.1, the reaction temperature in the methanol synthesis tower 4 is 250 ℃, and the methanol water cooler 5 reduces the tower gas after the reaction to 40 ℃.
Claims (5)
1. The system for preparing the methanol by hydrogenating the carbon dioxide is characterized by comprising at least three stages of methanol preparation units (1) connected in series, wherein each methanol preparation unit (1) comprises an inlet tower preheater (7), a methanol synthesis tower (4), a methanol water cooler (5) and a methanol separator (6); a raw material inlet of the tower preheater (7) is communicated with the purified raw material mixed gas pipe, and a raw material outlet of the tower preheater (7) is communicated with a gas inlet of the methanol synthesis tower (4); the gas outlet of the methanol synthesis tower (4) is communicated with the high-temperature gas inlet of the tower preheater (7), the high-temperature gas outlet of the tower preheater (7) is communicated with the feed inlet of the methanol water cooler (5), and the discharge outlet of the methanol water cooler (5) is communicated with the feed inlet of the methanol separator (6); the gas outlet of the methanol separator (6) of the previous stage methanol preparation unit (1) is communicated with the raw material gas inlet of the tower-entering preheater (7) of the next stage methanol preparation unit (1); the gas outlet of the methanol separator (6) of the last stage of methanol preparation unit (1) is communicated with the gas inlet of the methanol water washing tower (2); liquid outlets of the methanol separators (6) of the methanol preparation units (1) are communicated with a liquid inlet of the methanol flash tank (3); the liquid outlet of the methanol water washing tower (2) is communicated with the liquid inlet of the methanol flash tank (3).
2. The system for preparing methanol by hydrogenating carbon dioxide according to claim 1, wherein a liquid inlet of the methanol water washing tower (2) is communicated with a desalted water supply device.
3. The system for preparing methanol by hydrogenating carbon dioxide as claimed in claim 2, wherein the gas outlet of the methanol water washing tower (2) is communicated with a hydrogen recovery device.
4. The system for preparing methanol by hydrogenating carbon dioxide as claimed in claim 3, wherein the liquid outlet of the methanol flash drum (3) is communicated with a methanol rectification system.
5. The system for preparing methanol by hydrogenating carbon dioxide according to claim 3 is characterized by comprising three to eight methanol preparation units (1) connected in series.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114907186A (en) * | 2022-04-24 | 2022-08-16 | 中国成达工程有限公司 | Method for directly preparing methanol from carbon dioxide and hydrogen |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114907186A (en) * | 2022-04-24 | 2022-08-16 | 中国成达工程有限公司 | Method for directly preparing methanol from carbon dioxide and hydrogen |
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