CN218321195U - System for preparing methanol from coke oven gas - Google Patents
System for preparing methanol from coke oven gas Download PDFInfo
- Publication number
- CN218321195U CN218321195U CN202221555932.9U CN202221555932U CN218321195U CN 218321195 U CN218321195 U CN 218321195U CN 202221555932 U CN202221555932 U CN 202221555932U CN 218321195 U CN218321195 U CN 218321195U
- Authority
- CN
- China
- Prior art keywords
- gas
- methanol
- coke oven
- tower
- oven gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Abstract
The utility model discloses a system for preparing methanol from coke oven gas, which comprises a gas holder communicated with a gas pipeline of a coking plant, wherein the gas holder is communicated with a coke oven gas compressor; the coke-oven gas compressor is connected with a fine desulfurizing tower for desulfurizing the hydrogen sulfide to less than 0.1ppm, and the fine desulfurizing tower is connected with a converter; the reformer is connected with an oxygen pipeline, and the other end of the oxygen pipeline is an air distribution machine; the pressure difference between steam and oxygen in the converter is more than or equal to 0.13MPa, and the pressure difference between oxygen and a system is more than or equal to 0.13MPa; the converter is connected with a synthesis gas compressor for increasing the pressure to 5.9Mpa, and the synthesis gas compressor is connected with a gas-gas heat exchanger; the gas-gas heat exchanger is connected with a methanol synthesis tower, and the methanol synthesis tower is connected with a water cooler for cooling methanol; the water cooler is connected with a rectifying tower for purifying the crude methanol. The utility model has the advantages of high utilization rate of coke oven gas, simple structure, convenient maintenance and high safety performance.
Description
Technical Field
The utility model relates to a coke oven gas system methyl alcohol technical field, more specifically relates to a system for coke oven gas preparation methyl alcohol.
Background
Coke oven gas is a coking byproduct and comprises H as the main component 2 、CH 4 CO and CO 2 It is a good chemical raw material and high-calorific-value fuel. The coke oven gas generated in the coking process is fully utilized, so that not only can energy waste be avoided, but also the pollution to the environment can be reduced. In recent years, china develops a process for fully utilizing coke oven gas, namely, the coke oven gas is used for preparing methanol.
In the process of the method for preparing the methanol from the coke oven gas, the coke oven gas is sequentially subjected to compression treatment, pretreatment, hydrodesulfurization treatment, wet decarburization treatment, coke oven gas conversion treatment and methanol synthesis treatment to prepare a methanol product. However, the utilization rate of the coke oven gas by the process is low, and the safety and stability of the existing coke oven gas conversion treatment system are low.
SUMMERY OF THE UTILITY MODEL
The technical problem to be solved by the utility model is to provide a system for preparing methanol from coke oven gas, which solves the problems in the background technology.
In order to solve the technical problem, the utility model adopts the following technical proposal.
A system for preparing methanol from coke oven gas comprises a gas holder communicated with a gas pipeline of a coking plant, wherein the gas holder is communicated with a coke oven gas compressor used for increasing the pressure to 2.5 MPa; the coke oven gas compressor is connected with a fine desulfurization tower which is used for desulfurizing the hydrogen sulfide in the coke oven gas to less than 0.1ppm, and the fine desulfurization tower is connected with a converter; the reforming furnace is connected with an oxygen pipeline, and the other end of the oxygen pipeline is an air distribution machine; the pressure difference between steam and oxygen in the converter is more than or equal to 0.13MPa, and the pressure difference between oxygen and a system is more than or equal to 0.13MPa; the reformer is connected with a synthesis gas compressor for increasing the pressure to 5.9Mpa, and the synthesis gas compressor is connected with a gas-gas heat exchanger; the gas-gas heat exchanger is connected with a methanol synthesis tower, and the methanol synthesis tower is connected with a water cooler for cooling methanol; the water cooler is connected with a rectifying tower for purifying the crude methanol.
According to the further optimized technical scheme, the gas-gas heat exchanger and the methanol synthesis tower are respectively connected with a boiler device for recovering purge gas through pipelines, and are simultaneously connected with a converter to be used as fuel gas.
Further optimizing the technical scheme, a cooler and a precision filter are arranged between the fine desulfurization tower and the converter.
Further optimizing the technical scheme, the rectifying tower is connected with a residual liquid tank for storing the fusel.
Due to the adoption of the technical scheme, the utility model has the following technical progress.
The utility model provides a pair of system for coke oven gas preparation methyl alcohol has set up the factor of safety of reformer operation, and as long as one of them is less than 0.13MPa with the pressure differential of system, oxygen of steam and oxygen, the system can interlock and cut oxygen and park, ensures that the device does not appear the safety problem. The utility model has the advantages of high utilization rate of coke oven gas, simple structure, convenient maintenance and high safety performance.
Drawings
Fig. 1 is a schematic structural view of the present invention;
wherein: 1. the system comprises a gas holder, 2, a coke-oven gas compressor, 3, a fine desulfurization tower, 4, a converter, 5, an air separation machine, 6, a synthesis gas compressor, 7, a gas-gas heat exchanger, 8, a methanol synthesis tower, 9, a water cooler, 10, a rectification tower, 11 and a boiler device.
Detailed Description
The present invention will be described in further detail with reference to the drawings and specific embodiments.
A system for preparing methanol from coke oven gas is shown in a combined figure 1 and comprises a gas holder 1, a coke oven gas compressor 2, a fine desulfurization tower 3, a converter 4, an air separation machine 5, a synthesis gas compressor 6, a gas-gas heat exchanger 7, a methanol synthesis tower 8, a water cooler 9, a rectifying tower 10 and a boiler device 11.
The gas holder 1 is communicated with a gas outlet of a coking plant through a pipeline, the gas holder 1 is communicated with the coke-oven gas compressor 2, and the coke-oven gas compressor 2 raises the pressure to 2.5MPa. The coke oven gas compressor 2 is connected with the fine desulfurizing tower 3, and the fine desulfurizing tower 3 is used for desulfurizing the hydrogen sulfide in the coke oven gas to less than 0.1ppm so as to prevent subsequent conversion and synthetic catalyst poisoning.
The fine desulfurization tower 3 is connected with the converter 4, and a cooler and a fine filter are arranged between the fine desulfurization tower 3 and the converter 4. The gas is cooled to less than or equal to 40 ℃ by the cooler step by step, and then is further dechlorinated and desulfurized by a zinc oxide dechlorinating agent and a zinc oxide desulfurizing agent at normal temperature, and the gas is filtered by a precise filter.
The other air inlet of the reformer 4 is connected with an oxygen pipeline, and the other end of the oxygen pipeline is provided with an air distribution machine 5. The pressure difference between steam and oxygen in the reformer 4 is more than or equal to 0.13MPa, and the pressure difference between oxygen and a system is more than or equal to 0.13MPa. Through setting up the pressure differential of three, prevented that the material from falling the cluster, also ensure that oxygen can get into reformer 4 smoothly and participate in the reaction, and steam provides the guard action and participates in the reaction for whole reaction. The pressure difference is taken as the safety coefficient of the operation of the conversion device, and the system can be interlocked to cut off oxygen and stop when one of the pressure difference of steam and oxygen and the pressure difference of oxygen and the system is lower than 0.13MPa, so that the device is ensured not to have safety problems. In addition, the pressure difference between the steam and the oxygen and the pressure difference value between the oxygen and the system are displayed on a central control DCS interface, and central control staff do not need to calculate manually at fixed points, so that the labor intensity of operators is reduced.
The converter 4 is connected with a synthesis gas compressor 6, the synthesis gas compressor 6 raises the pressure to 5.9Mpa, and the synthesis gas compressor 6 is connected with a gas-gas heat exchanger 7. The gas-gas heat exchanger 7 is connected with a methanol synthesis tower 8, and the methanol synthesis tower 8 is connected with a water cooler 9 for cooling methanol. The gas-gas heat exchanger 7 and the methanol synthesis tower 8 are respectively connected with a boiler device 11 through pipelines and are simultaneously connected with the reformer 4, and the reformer 4 and the boiler device 11 are used for recovering purge gas which is reused as fuel gas.
The water cooler 9 is connected to a rectifying column 10 for purifying the crude methanol. The rectifying tower 10 is connected with a residual liquid tank for storing fusel, and the content of methanol in the residual liquid tank is less than or equal to 0.4%; fusel can also be pumped to coke quenching.
The utility model discloses when in actual use, come from the coke oven gas that the coke-oven plant produced, through buffering entering coke oven gas compressor 2 in gas holder 1 and carry the pressure to 2.5MPa and send the essence desulfurization. Mixing coke-oven gas obtained by fine desulfurization with self-produced steam of conversion waste heat boiler, preheating to 330 deg.C in preheater (shell pass), preheating to 660 deg.C in preheater, mixing in converter 4, introducing with oxygen from air separation into converter 4, performing oxidation combustion of pure oxygen steam at 950-1250 deg.C, subjecting high-temperature gas to methane steam conversion by catalyst bed layer, and controlling outlet gas CH 4 Less than or equal to 1.0 percent. Cooling to less than or equal to 40 deg.C by cooler, dechlorinating and desulfurizing with zinc oxide dechlorinating agent and zinc oxide desulfurizer at normal temperature, filtering gas with precise filter, and feeding to synthesis gas compressor 6; the fresh gas from the conversion is compressed to 5.9Mpa to synthesize methanol; the synthesis gas from synthesis gas compression enters a methanol synthesis tower 8 through a gas-gas heat exchanger 7, methanol synthesis reaction is carried out under the action of a catalyst, crude methanol cooled by a water cooler 9 after reaction is sent to rectification, and meanwhile, a small part of the system is used as purge gas and sent to a converter 4 and a boiler device 11 to be used as fuel gas. And (3) after the crude methanol is rectified by three rectifying towers, discharging residual liquid from the bottom of the normal pressure tower, analyzing that the content of the methanol in the residual liquid is less than or equal to 0.4%, pumping the residual liquid to coking coke quenching, simultaneously sending part of the extracted residual liquid to a residual liquid tank, and selling qualified refined methanol.
Claims (4)
1. A system for preparing methanol from coke oven gas is characterized in that: the coke oven gas pressure raising device comprises a gas holder (1) communicated with a gas pipeline of a coke oven plant, wherein the gas holder (1) is communicated with a coke oven gas compressor (2) used for raising the pressure to 2.5 MPa; the coke oven gas compressor (2) is connected with a fine desulfurization tower (3) for desulfurizing the hydrogen sulfide in the coke oven gas to less than 0.1ppm, and the fine desulfurization tower (3) is connected with a converter (4); the reformer (4) is connected with an oxygen pipeline, and the other end of the oxygen pipeline is provided with an air distribution machine (5); the reformer (4) is connected with a synthesis gas compressor (6) for increasing the pressure to 5.9Mpa, and the synthesis gas compressor (6) is connected with a gas-gas heat exchanger (7); the gas-gas heat exchanger (7) is connected with a methanol synthesis tower (8), and the methanol synthesis tower (8) is connected with a water cooler (9) for cooling methanol; the water cooler (9) is connected with a rectifying tower (10) for purifying the crude methanol.
2. The system for preparing the methanol from the coke oven gas as claimed in claim 1, wherein: the gas-gas heat exchanger (7) and the methanol synthesis tower (8) are respectively connected with a boiler device (11) for recovering purge gas through pipelines, and are simultaneously connected with the reformer (4) as fuel gas.
3. The system for preparing the methanol from the coke oven gas as claimed in claim 2, wherein: a cooler and a precision filter are arranged between the fine desulfurization tower (3) and the converter (4).
4. The system for preparing the methanol from the coke oven gas as claimed in claim 1, wherein: the rectifying tower (10) is connected with a residual liquid tank for storing fusel.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221555932.9U CN218321195U (en) | 2022-06-21 | 2022-06-21 | System for preparing methanol from coke oven gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221555932.9U CN218321195U (en) | 2022-06-21 | 2022-06-21 | System for preparing methanol from coke oven gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN218321195U true CN218321195U (en) | 2023-01-17 |
Family
ID=84868375
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202221555932.9U Active CN218321195U (en) | 2022-06-21 | 2022-06-21 | System for preparing methanol from coke oven gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN218321195U (en) |
-
2022
- 2022-06-21 CN CN202221555932.9U patent/CN218321195U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100526273C (en) | Method for integral production of liquid ammonia and methanol and/or dimethyl ether by using coke oven gas as raw material | |
| CN101434879A (en) | Method for preparing methyl alcohol synthesis gas and compressed natural gas from coke oven gas and coal | |
| CN101289620A (en) | Integration process of coke dry quenching co-production synthesis gas and downstream products thereof of methanol | |
| CN102050699B (en) | Process for co-producing methanol and ammonia by utilizing calcium carbide tail gas | |
| CN102531835B (en) | Method for synthesizing methanol through low-carbon technology | |
| CN103303863A (en) | Method for producing ammonia synthesis gas from coke-oven gas | |
| CN111320528A (en) | Method and system for preparing ethanol by comprehensively utilizing steel mill tail gas | |
| CN100579896C (en) | Method and system for preparing synthetic gas with appropriate hydrogen-carbon ratio from lurgi furnace outlet coal gas through non-catalytic partial oxidation by pure oxygen | |
| CN101148250B (en) | Joint production process of alcohol and ammonia | |
| CN101870479B (en) | Fischer-Tropsch synthesis cogeneration process for synthesizing ammonia | |
| CN204874343U (en) | Marsh gas and coke oven gas joint production methyl alcohol device | |
| CN105883851B (en) | A kind of Novel gasification and pyrolysis coupling coal gas multi-production process | |
| CN112023923B (en) | Copper-based catalyst activation method for hydrogen production by methanol pyrolysis | |
| CN101818087B (en) | Novel process for making synthetic natural gas by using coke-oven gas | |
| CN218321195U (en) | System for preparing methanol from coke oven gas | |
| CN209854029U (en) | Device for preparing methanol from synthesis gas without conversion system | |
| CN208292658U (en) | A kind of device for producing hydrogen | |
| CN100408530C (en) | Method for producing methanol by using coke oven gas as raw material | |
| CN103072945A (en) | Process for preparing ethanediol synthetic gas by non sulfur-tolerant shift of calcium carbide furnace gas | |
| CN103910330A (en) | Process for preparing synthesis gas through catalytic partial oxidation of natural gas and carbon dioxide mixed gas | |
| CN104058368A (en) | Process and system for producing hydrogen by converting hydrocarbon-containing tail gas | |
| CN112940797A (en) | Coke oven gas fine desulfurization system | |
| CN112980519A (en) | CO conversion processing device in coke oven gas and conversion processing method thereof | |
| CN215667144U (en) | Gas conversion and purification device for producing high-purity hydrogen by using methane | |
| CN201102901Y (en) | System for preparing synthetic gas or hydrogen gas from lurgi-furnace outlet coal gas by non-catalysis and partial oxidation |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |