CN215946777U - Co-production system of ammonia, methanol and acetic acid - Google Patents

Co-production system of ammonia, methanol and acetic acid Download PDF

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Publication number
CN215946777U
CN215946777U CN202122405336.4U CN202122405336U CN215946777U CN 215946777 U CN215946777 U CN 215946777U CN 202122405336 U CN202122405336 U CN 202122405336U CN 215946777 U CN215946777 U CN 215946777U
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gas
methanol
ammonia
distribution station
acetic acid
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张蒙恩
孟雪
朱止阳
尚卫平
耍芬芬
李庆华
张路明
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Henan Xinlianxin Chemicals Group Co Ltd
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Henan Xinlianxin Chemicals Group Co Ltd
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    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
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    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals

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Abstract

The utility model relates to a CO-production system of ammonia, methanol and acetic acid, which comprises a gasification furnace, an ammonia product storage tank, a methanol product storage tank and an acetic acid product storage tank, wherein a raw material gas pipeline of the gasification furnace is connected with a raw material gas distribution station, the raw material gas distribution station is respectively connected with an unconverted gas heat recovery system and a CO full conversion device, the CO full conversion device is connected with a fully converted gas methanol washing device through the fully converted gas heat recovery device, and a product gas outlet of the fully converted gas methanol washing device is connected with the ammonia product storage tank through a liquid nitrogen washing device and an ammonia synthesis device; have simple structure, reasonable in design, realize carrying out effective distribution to relevant equipment through setting up various gas distribution stations, not only can realize gaseous temporary storage and accurate distribution to can satisfy the different demands of each chemical product to carbon monoxide, hydrogen and carbon dioxide, realize the advantage of coproduction ammonia, methyl alcohol, acetic acid through the simple flow that easily controls under the prerequisite that reduces investment cost and use less equipment with reaching.

Description

Co-production system of ammonia, methanol and acetic acid
Technical Field
The utility model relates to the technical field of coal chemical industry and cost, in particular to a co-production system of ammonia, methanol and acetic acid.
Background
The coal chemical production process generally uses coal as raw materials, raw material gases such as carbon monoxide, hydrogen and carbon dioxide are obtained in a gasification furnace or a gasification reactor and are used for producing downstream chemical products such as synthetic ammonia, methanol and acetic acid, wherein the synthetic ammonia needs hydrogen as the raw material gas, the methanol needs hydrogen, carbon monoxide and the like as the raw material gas, the acetic acid needs carbon monoxide and methanol as the raw material gas, different devices required by the production of different downstream products are different due to different requirements of the raw material gas, the raw material gas purification flows are different, generally one chemical product needs to be matched with one set of carbon monoxide conversion device and even more than two sets of methanol washing purification devices, the number of devices is large, the flow is complex, and the production regulation is difficult.
SUMMERY OF THE UTILITY MODEL
Aiming at the defects of the prior art, the utility model provides the ammonia, methanol and acetic acid co-production system which has a simple structure and reasonable design, realizes effective gas distribution of relevant equipment by arranging various gas distribution stations, can realize temporary storage and accurate distribution of gas, and can simultaneously produce ammonia, methanol and acetic acid on the premise of reducing equipment investment and facilitating process control.
In order to achieve the purpose, the utility model adopts the technical scheme that:
the utility model provides a coproduction system of ammonia, methyl alcohol and acetic acid, includes gasifier, ammonia product storage tank, methyl alcohol product storage tank and acetic acid product storage tank, the feed gas pipeline of gasifier links to each other with feed gas distributor station, feed gas distributor station respectively with do not transform gas heat recovery system and CO full conversion equipment, CO full conversion equipment passes through full conversion gas heat recovery unit and links to each other with full conversion gas methyl alcohol washing device, and the product gas export of full conversion gas methyl alcohol washing device passes through liquid nitrogen washing device and ammonia synthesis device and links to each other with ammonia product storage tank.
Preferably, the unconverted gas heat recovery system is connected with the unconverted gas methanol washing device, a synthesis gas outlet of the unconverted gas methanol washing device is connected with the acetic acid production device through a CO purification device, and an outlet of the acetic acid production device is connected with a methanol product storage tank; the raw material inlet of the acetic acid production device is connected with the outlet of the methanol synthesis device.
Preferably, the carbon dioxide gas outlet of the total shift gas methanol washing device and the carbon dioxide gas outlet of the unshifted gas methanol washing device are respectively connected with CO2Distribution station connected, CO2Outlets of the distribution station being connected to the CO respectively2Pipe network and CO2Compressor units connected to each other, CO2The outlet of the compression device is connected with the raw material inlet of the methanol synthesis device.
Preferably, a hydrogen distribution station is arranged between the product gas outlet of the full-conversion gas methanol washing device and the liquid nitrogen washing device, and the product gas outlet of the hydrogen distribution station is respectively connected with the inlet of the liquid nitrogen washing device and the raw material inlet of the methanol synthesis device.
Preferably, the tail gas outlet of the CO purification device is connected with a hydrogen-rich gas distribution station through a hydrogen-rich gas compression device, and the gas outlet of the hydrogen-rich gas distribution station is connected with the raw material inlet of the methanol synthesis device.
Preferably, the gas outlet of the hydrogen-rich gas distribution station is further connected to a tee provided between the feed gas distribution station and the CO total shift unit.
Preferably, the synthesis gas outlet of the unshifted gas methanol washing device and the CO purification device are connected with a CO distribution station, and the gas outlet of the CO distribution station is respectively connected with the inlet of the CO purification device and the raw material inlet of the methanol synthesis device.
The utility model has the advantages of simple structure and reasonable design, realizes effective gas distribution on related equipment by arranging various gas distribution stations, can realize temporary storage and accurate distribution of gas, and can meet different requirements of various chemical products on carbon monoxide, hydrogen and carbon dioxide, thereby achieving the purpose of realizing co-production of ammonia, methanol and acetic acid by simple and easily controlled flow on the premise of reducing investment cost and using less equipment.
Drawings
FIG. 1 is a schematic structural diagram of the present invention.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Referring to fig. 1: the utility model relates to a CO-production system of ammonia, methanol and acetic acid, which comprises a gasification furnace 1, an ammonia product storage tank 18, a methanol product storage tank 19 and an acetic acid product storage tank 21, wherein a raw material gas pipeline of the gasification furnace 1 is connected with a raw material gas distribution station 2, the raw material gas distribution station 2 is respectively connected with an unconverted gas heat recovery system 3 and a CO full conversion device 6, the CO full conversion device 6 is connected with a fully converted gas methanol washing device 8 through a full converted gas heat recovery device 7, and a product gas outlet of the fully converted gas methanol washing device 8 is connected with a liquid nitrogen washing device 16 and an ammonia synthesis device through a liquid nitrogen washing device 16And the device 17 is connected with an ammonia product storage tank 18. The unconverted gas heat recovery system 3 is connected with the unconverted gas methanol washing device 4, a synthetic gas outlet of the unconverted gas methanol washing device 4 is connected with an acetic acid production device 20 through a CO purification device 5, and an outlet of the acetic acid production device 20 is connected with a methanol product storage tank 19; the raw material inlet of the acetic acid production device 20 is connected with the outlet of the methanol synthesis device 12. The carbon dioxide gas outlets of the full-conversion gas methanol washing device 8 and the unconverted gas methanol washing device 4 are respectively connected with CO2Distribution station 14 connected to, CO2Outlets of the distribution station 14 are connected to the CO respectively2Pipe network 13 and CO2A compressor 15 connected to the CO2The outlet of the compression device 15 is connected with the raw material inlet of the methanol synthesis device 12. A hydrogen distribution station 9 is arranged between a product gas outlet of the full conversion gas methanol washing device 8 and the liquid nitrogen washing device 16, and a product gas outlet of the hydrogen distribution station 9 is respectively connected with an inlet of the liquid nitrogen washing device 16 and a raw material inlet of the methanol synthesis device 12. And a tail gas outlet of the CO purification device 5 is connected with a hydrogen-rich gas distribution station 11 through a hydrogen-rich gas compression device 10, and a gas outlet of the hydrogen-rich gas distribution station 11 is connected with a raw material inlet of a methanol synthesis device 12. The gas outlet of the hydrogen-rich gas distribution station 11 is also connected with a tee joint arranged between the raw gas distribution station 2 and the CO full-shift device 6. The synthetic gas outlet of the unshifted gas methanol washing device 4 and the CO purification device 5 are connected with a CO distribution station 22, and the gas outlet of the CO distribution station 22 is respectively connected with the inlet of the CO purification device 5 and the raw material inlet of the methanol synthesis device 12.
The working principle of the utility model is as follows: the gasification furnace 1 obtains raw material gas such as carbon monoxide, hydrogen, carbon dioxide and the like, and the raw material gas is divided into two parts at a raw material gas distribution station 2 and respectively supplied to an unconverted gas heat recovery system 3 and a CO full conversion device 6. The raw material gas is subjected to heat recovery in an unshifted gas heat recovery device 3, the recovered heat enters an unshifted gas methanol washing device 4 to remove acid gases such as carbon dioxide in the unshifted gas methanol washing device 4, and the carbon dioxide obtained by the unshifted gas methanol washing device 4 enters CO2A distribution station 14, and the purified gas of the unshifted gas methanol washing device 4 enters a CO distribution station 22. The CO distribution station 22 is connected to the CO purification device 5 and the methanol synthesis device respectivelyThe forming device 12 supplies air. And the product gas of the CO purification device 5 is CO, and enters an acetic acid production device 20, and the acetic acid product obtained by the acetic acid production device 20 enters an acetic acid product storage tank 21. And tail gas of the CO purification device 5 is pressurized by a hydrogen-rich gas compression device 10 and enters a hydrogen-rich gas distribution station 11, the hydrogen-rich gas distribution station 11 supplies gas to a CO full-conversion device 6 and a methanol synthesis device 12 respectively, and a product of the methanol synthesis device 12 enters a methanol product storage tank 19. The raw material gas completely reacts CO in a CO full conversion device 6 to convert into hydrogen and carbon dioxide, the hydrogen and carbon dioxide enter a full conversion gas methanol washing device 8 after heat is recovered in a full conversion gas heat recovery device 7, and the carbon dioxide analyzed by the full conversion gas methanol washing device 8 enters CO2Distribution station 14, the CO2Carbon dioxide passing through CO in the distribution station 142The compressor 15 supplies the methanol synthesis unit 12 with the CO2The distribution station 14 feeds the remaining carbon dioxide to the CO2The pipe network 13 is used by other products or users. The pure gas of the full conversion gas methanol washing device 8 enters a hydrogen distribution station 9, the hydrogen distribution station 9 supplies gas to a methanol synthesis device 12 and a liquid nitrogen washing device 16 respectively, the liquid nitrogen washing device 16 gives vent to anger and enters an ammonia synthesis device 17, and products in the ammonia synthesis device 17 enter an ammonia product storage tank 18.
Specifically, the co-production process of the co-production system of ammonia, methanol and acetic acid comprises the following steps: the method comprises the following steps: the gasification furnace 1 obtains raw material gas such as carbon monoxide, hydrogen, carbon dioxide and the like, and the raw material gas is divided into two parts at a raw material gas distribution station 2 and respectively supplied to an unconverted gas heat recovery system 3 and a CO total conversion device 6. The gasification furnace 1 obtains the feed gas with 43-55% of dry-based CO content. The gasification furnace 1 may include various gasification reactors including a coal water slurry gasification furnace and a pulverized coal furnace. The operating pressure of the gasification furnace 1 is 2.5MPa-8.7 MPa. Step two: the raw gas is cooled to 20-40 ℃ in the unconverted gas heat recovery system 3 and then enters the unconverted gas methanol washing device 4 to remove acid gases such as carbon dioxide and the like in the raw gas. The unconverted gas heat recovery system 3 comprises equipment and devices such as a waste boiler, a gas-liquid separation tank, a water cooler, an ammonia washing tower and the like. The carbon dioxide obtained by the unconverted gas methanol washing device 4 entersCO2Within the distribution station 14, the unshifted gas methanol scrubbing unit 4 cleans the gas into a CO distribution station 22. And the purity of the carbon dioxide obtained in the unconverted gas methanol washing device 4 is 98-99.9%. The unconverted gas methanol washing device 4 is a low-temperature methanol washing process system and comprises equipment and devices such as a methanol washing tower, a carbon dioxide analysis tower, a methanol thermal regeneration tower and the like. Step three: the CO distribution station 22 supplies gas to the CO purification apparatus 5 and the methanol synthesis apparatus 12, respectively. And the purity of the product gas CO in the CO purification device 5 is 96.5-99.5%, the product gas CO enters an acetic acid production device 20, and an acetic acid product obtained by the acetic acid production device 20 enters an acetic acid product storage tank 21. The CO purification device 5 comprises relevant equipment used in a purification process, and the purification process comprises the processes of membrane separation of CO, cryogenic separation of CO, pressure swing adsorption and the like. Step four: tail gas of the CO purification device 5 is pressurized to enter a hydrogen-rich gas distribution station 11 through a hydrogen-rich gas compression device 10; the CO content in the hydrogen-rich gas is 20-40%; the hydrogen-rich gas compression device 10 includes centrifugal compressors, reciprocating compressors, intercoolers, and the like. The hydrogen-rich gas distribution station 11 supplies gas to the CO full-shift device 6 and the methanol synthesis device 12 respectively, and the product of the methanol synthesis device 12 enters a methanol product storage tank 19. Step five: the raw material gas completely reacts and converts CO into hydrogen and carbon dioxide in a CO full-conversion device 6, and the hydrogen and carbon dioxide enter a full-conversion methanol washing device 8 after heat is recovered in a full-conversion gas heat recovery device 7. The CO dry-based molar content in the process gas at the outlet of the CO full-conversion device 6 is 0.2-0.6%. The temperature of the process gas at the outlet of the full shift gas heat recovery device 7 is as follows: 20-40 ℃, and the full conversion gas heat recovery device 7 comprises equipment and devices such as a conversion furnace, a waste boiler, a gas-liquid separation tank, a water cooler, an ammonia washing tower and the like. Step six: the carbon dioxide resolved in the total shift gas methanol washing device 8 enters CO2Within the dispensing station 14. The purity of the carbon dioxide obtained by the full conversion gas methanol washing device 8 is 98-99.9%. The CO is2Carbon dioxide passing through CO in the distribution station 142The compressor 15 supplies gas to the methanol synthesis 12 unit. The molar concentration of carbon dioxide at the inlet of the methanol synthesis device 12 is 2-4%. The CO is2 Distribution station 14 remaining carbon dioxide into CO2The pipe network 13 is used by other products or users. Step seven: the full shift gas methanol scrubber 8 purges the gas into a hydrogen distribution station 9. The hydrogen distribution station 9 supplies gas to the methanol synthesis 12 device and the liquid nitrogen washing device 16, respectively. The CO content of the gas discharged from the liquid nitrogen washing device 16 is less than 2ppm, the gas enters an ammonia synthesis device 17 to synthesize ammonia, and finally the ammonia enters an ammonia product storage tank 18.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art through specific situations.
The above examples are only intended to illustrate the technical solution of the present invention, but not to limit it; although the present invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; and such modifications or substitutions do not depart from the spirit and scope of the corresponding technical solutions of the embodiments of the present invention.

Claims (7)

1. The utility model provides a coproduction system of ammonia, methyl alcohol and acetic acid, includes gasifier (1), ammonia product storage tank (18), methyl alcohol product storage tank (19) and acetic acid product storage tank (21), its characterized in that: a raw material gas pipeline of the gasification furnace (1) is connected with a raw material gas distribution station (2), the raw material gas distribution station (2) is respectively connected with an unconverted gas heat recovery system (3) and a CO full conversion device (6), the CO full conversion device (6) is connected with a full conversion gas methanol washing device (8) through a full conversion gas heat recovery device (7), and a product gas outlet of the full conversion gas methanol washing device (8) is connected with an ammonia product storage tank (18) through a liquid nitrogen washing device (16) and an ammonia synthesis device (17).
2. The system of claim 1, wherein the system comprises: the unconverted gas heat recovery system (3) is connected with the unconverted gas methanol washing device (4), a synthesis gas outlet of the unconverted gas methanol washing device (4) is connected with an acetic acid production device (20) through a CO purification device (5), and an outlet of the acetic acid production device (20) is connected with a methanol product storage tank (19);
the raw material inlet of the acetic acid production device (20) is connected with the outlet of the methanol synthesis device (12).
3. The system of claim 2, wherein the ammonia, methanol and acetic acid co-production system comprises: the carbon dioxide gas outlets of the full-conversion gas methanol washing device (8) and the unconverted gas methanol washing device (4) are respectively connected with CO2A distribution station (14) connected to the CO2The outlets of the distribution station (14) are connected to the CO respectively2Pipe network (13) and CO2A compression device (15) connected to the CO2The outlet of the compression device (15) is connected with the raw material inlet of the methanol synthesis device (12).
4. The system of claim 1, wherein the system comprises: and a hydrogen distribution station (9) is arranged between a product gas outlet of the full-conversion gas methanol washing device (8) and the liquid nitrogen washing device (16), and a product gas outlet of the hydrogen distribution station (9) is respectively connected with an inlet of the liquid nitrogen washing device (16) and a raw material inlet of the methanol synthesis device (12).
5. The system of claim 2, wherein the ammonia, methanol and acetic acid co-production system comprises: and a tail gas outlet of the CO purification device (5) is connected with a hydrogen-rich gas distribution station (11) through a hydrogen-rich gas compression device (10), and a gas outlet of the hydrogen-rich gas distribution station (11) is connected with a raw material inlet of a methanol synthesis device (12).
6. The system of claim 5, wherein the ammonia, methanol and acetic acid co-production system comprises: and the gas outlet of the hydrogen-rich gas distribution station (11) is also connected with a tee joint arranged between the raw material gas distribution station (2) and the CO full conversion device (6).
7. The system of claim 2, wherein the ammonia, methanol and acetic acid co-production system comprises: the synthesis gas outlet of the unconverted gas methanol washing device (4) and the CO purification device (5) are connected with a CO distribution station (22), and the gas outlet of the CO distribution station (22) is respectively connected with the inlet of the CO purification device (5) and the raw material inlet of the methanol synthesis device (12).
CN202122405336.4U 2021-09-30 2021-09-30 Co-production system of ammonia, methanol and acetic acid Active CN215946777U (en)

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CN202122405336.4U CN215946777U (en) 2021-09-30 2021-09-30 Co-production system of ammonia, methanol and acetic acid

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CN202122405336.4U CN215946777U (en) 2021-09-30 2021-09-30 Co-production system of ammonia, methanol and acetic acid

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CN215946777U true CN215946777U (en) 2022-03-04

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