CN114456848A - Device and method for deoxidizing and desulfurizing converter gas - Google Patents
Device and method for deoxidizing and desulfurizing converter gas Download PDFInfo
- Publication number
- CN114456848A CN114456848A CN202210167503.2A CN202210167503A CN114456848A CN 114456848 A CN114456848 A CN 114456848A CN 202210167503 A CN202210167503 A CN 202210167503A CN 114456848 A CN114456848 A CN 114456848A
- Authority
- CN
- China
- Prior art keywords
- gas
- converter gas
- deoxidation
- reactor
- converter
- 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.)
- Pending
Links
- 238000000034 method Methods 0.000 title claims abstract description 25
- 230000003009 desulfurizing effect Effects 0.000 title claims description 11
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 67
- 230000023556 desulfurization Effects 0.000 claims abstract description 67
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 30
- 239000003054 catalyst Substances 0.000 claims abstract description 22
- 230000035939 shock Effects 0.000 claims abstract description 13
- 239000007789 gas Substances 0.000 claims description 183
- 230000007062 hydrolysis Effects 0.000 claims description 42
- 238000006460 hydrolysis reaction Methods 0.000 claims description 42
- 230000001105 regulatory effect Effects 0.000 claims description 23
- 238000006392 deoxygenation reaction Methods 0.000 claims description 22
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 17
- 229910052760 oxygen Inorganic materials 0.000 claims description 17
- 239000001301 oxygen Substances 0.000 claims description 17
- 238000010791 quenching Methods 0.000 claims description 13
- WQOXQRCZOLPYPM-UHFFFAOYSA-N dimethyl disulfide Chemical compound CSSC WQOXQRCZOLPYPM-UHFFFAOYSA-N 0.000 claims description 8
- 125000001741 organic sulfur group Chemical group 0.000 claims description 8
- 230000009471 action Effects 0.000 claims description 6
- 230000008569 process Effects 0.000 claims description 6
- 238000000746 purification Methods 0.000 claims description 6
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 claims description 4
- 239000002131 composite material Substances 0.000 claims description 4
- 238000007789 sealing Methods 0.000 claims description 4
- 230000004913 activation Effects 0.000 claims description 3
- 150000003568 thioethers Chemical class 0.000 claims description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 2
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 2
- 239000003034 coal gas Substances 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 abstract description 10
- 238000005265 energy consumption Methods 0.000 abstract description 4
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 8
- 230000000171 quenching effect Effects 0.000 description 5
- QMMFVYPAHWMCMS-UHFFFAOYSA-N Dimethyl sulfide Chemical compound CSC QMMFVYPAHWMCMS-UHFFFAOYSA-N 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 2
- 230000001588 bifunctional effect Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/004—Sulfur containing contaminants, e.g. hydrogen sulfide
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/34—Purifying combustible gases containing carbon monoxide by catalytic conversion of impurities to more readily removable materials
Abstract
The invention belongs to the technical field of deoxidation and desulfurization, and discloses a device and a method for deoxidation and desulfurization of converter gas. The invention adds a cold shock pipeline to enable gas to enter from the top and the bottom of the deoxidation reactor respectively, and simultaneously adjusts the flow rate of converter gas entering the bottom and the top by controlling the opening of a valve, thereby realizing that the top temperature is controlled at 70 ℃, the hot spot temperature of a catalyst bed layer of the deoxidation reactor is not more than 190 ℃ and the temperature equalization is not more than 150 ℃. The treatment capacity of the deoxidation reactor is improved. A shell-and-tube heat exchanger with a deflecting rod is used to replace the original inlet baffle and baffle plate type purified gas water cooler, so that the resistance drop of the water cooler of the purifier is reduced by 30KPa, and the integral pressure difference of the system is lower than 150 KPa. The deoxidized gas after passing through the device of the invention does not need to be partially recycled by entering a converter gas circulating compressor, the compressor is stopped, the resistance of the deoxidizer is reduced by 30KPa, the energy consumption is reduced, and the production cost of the device is also reduced.
Description
Technical Field
The invention belongs to the technical field of deoxidation and desulfurization, and particularly relates to a device and a method for deoxidation and desulfurization of converter gas.
Background
At present, when converter gas and coke oven gas are used as raw materials to produce glycol, 58000Nm of converter gas is consumed per hour3The content of CO in the converter gas is 45-50%, the oxygen content is less than or equal to 1%, and the content of organic sulfur such as COS, dimethyl sulfur and the like is less than or equal to 15mg/Nm3. To meet the production requirements of ethylene glycol, the production method needs to be implementedThe oxygen content in the converter gas is reduced to be below 30ppm, the total sulfur content is less than 0.1ppm, the converter gas deoxidation and fine desulfurization process adopts the technological route of COS hydrolysis, primary desulfurization, deoxidation and fine desulfurization, the overall resistance drop of the system is designed to be less than or equal to 150kpa, the deoxygenation reactor adopts an internal heat exchange type temperature-equalizing reactor, the hot point temperature of a catalyst bed is less than or equal to 180 ℃, and the temperature equalization of the bed is less than or equal to 150 ℃.
The existing deoxidation and desulfurization process mainly comprises the following steps: the converter gas is subjected to heat exchange with the deoxidized converter gas through a converter gas heat exchanger, the temperature is raised to 60 ℃, and then the converter gas enters a hydrolysis desulfurization tower for desulfurization. And mixing the gas from the top of the hydrolysis desulfurization tower with the deoxygenation circulating gas through a start-up heater, and then entering a deoxygenation reactor from the bottom to remove oxygen in the converter gas. And the deoxidized gas is divided into two parts, one part is used as deoxidized circulating gas, is pressurized by a converter gas circulating compressor and then is recycled, the other part is subjected to heat exchange with raw material gas by a converter gas heat exchanger to reduce the temperature, is cooled to 40 ℃ by a purified gas water cooler and then enters a fine desulfurization tower from the bottom of the tower to remove residual mercaptan and dimethyl disulfide in the gas.
In the actual operation process of the process, when the oxygen content of the inlet gas of the deoxygenation reactor exceeds 0.5 percent, the temperature of the hot spot of the catalyst bed layer of the deoxygenation reactor reaches more than 190 ℃ at most, and the temperature of the catalyst bed layer is equal to more than 160 ℃; the overall resistance of the system is reduced to 200kpa to far exceed the requirement of design indexes, and the system can only operate in a mode of reducing production load to ensure the safe operation of the device. Therefore, there are certain limitations, mainly expressed in the following points.
1. The treatment capacity of the existing deoxidation reactor has higher requirement on the index of oxygen content in the imported converter gas, and can not be higher than 0.5 percent. In order to control the oxygen content at the inlet, a converter gas circulating compressor needs to be operated to increase the circulating amount, so that the oxygen content is diluted, the space velocity of a reactor bed layer is increased, and the reaction heat is taken away. The rated power of the compressor is 420KW, the operation energy consumption is high, and the production cost is increased; and the overall pressure difference of the system is increased.
2. The reaction heat of the catalyst bed layer of the deoxidation reactor can be taken away only by increasing the circulation quantity through the circulation compressor, the adjustment means is single and the energy consumption is high, when the oxygen content at the inlet of the deoxidation reactor exceeds 0.5 percent, the temperature of the hot spot of the catalyst bed layer is ultrahigh, the production load operation can be reduced only, and the integral production capacity of the device is influenced.
3. The deoxidation catalyst is filled in the shell pass of the reactor, converter gas enters from the tube pass at the bottom of the reactor and exchanges heat with hot converter gas which has undergone deoxidation reaction in the shell pass, the heat exchange effect cannot be effectively controlled, the temperature is ultrahigh when the converter gas enters the shell pass and begins to react, and the temperature of a hot spot of a catalyst bed is ultrahigh.
4. The design structure of the purified gas water cooler has problems, and the original design adopts an inlet baffle plate and a baffle plate, so that the resistance of the purified gas water cooler is greatly reduced, which exceeds 40kpa, and the integral resistance of the system is greatly reduced.
Therefore, the novel device and the method for deoxidizing and desulfurizing the converter gas are provided, and the device and the method are of great significance for reducing the bed temperature and the system resistance of the deoxidation reactor, prolonging the service life of the deoxidation catalyst and improving the operation load of the converter gas deoxidation and desulfurization device.
Disclosure of Invention
The invention provides a device and a method for deoxidizing and desulfurizing converter gas. The device and the method can reduce the bed temperature and the system resistance of the deoxidation reactor in the prior method, prolong the service life of the deoxidation catalyst and improve the operation load of the converter gas deoxidation and desulfurization device.
In order to achieve the purpose, the invention adopts the following technical scheme:
the invention provides a device for deoxidizing and desulfurizing converter gas, which mainly comprises: the system comprises a deoxidation reactor, a quench pipeline, a deoxidation reactor inlet pipeline, a quench pipeline regulating valve, a deoxidation reactor inlet pipeline regulating valve, a purification water cooler, a converter gas heat exchanger, a hydrolysis desulfurization start-up heater, a hydrolysis desulfurization tower, a start-up heater and a fine desulfurization tower;
the converter gas heat exchanger comprises a converter gas heat exchanger, a converter gas heat exchanger gas outlet, a hydrolysis desulfurization start-up heater gas inlet, a hydrolysis desulfurization start-up heater gas outlet, a hydrolysis desulfurization tower gas outlet, a start-up heater gas inlet, a start-up heater gas outlet, a quenching pipeline, a deoxidation reactor gas inlet pipeline, a quenching pipeline regulating valve and a deoxidation reactor gas inlet pipeline regulating valve, wherein the converter gas heat exchanger gas inlet is connected with the converter gas, the converter gas heat exchanger gas outlet is connected with the hydrolysis desulfurization start-up heater gas inlet, the hydrolysis desulfurization start-up heater gas outlet is connected with the hydrolysis desulfurization tower gas inlet, the start-up heater gas outlet is divided into two branches, one branch is connected with the top gas inlet of the deoxidation reactor through a quenching pipeline, the other branch is connected with the gas inlet at the bottom of the deoxidation reactor through a deoxidation reactor gas inlet pipeline, and the quenching pipeline regulating valves and the deoxidation reactor gas inlet pipelines are respectively arranged on the quenching pipeline and the deoxidation reactor gas inlet pipeline and are respectively used for regulating the converter gas flow entering the top and the bottom of the deoxidation reactor; the gas outlet at the bottom of the deoxidation reactor is connected with the shell pass inlet of the converter gas heat exchanger, the shell pass outlet of the converter gas heat exchanger is connected with the shell pass inlet of the purified gas water cooler, and the shell pass outlet of the purified gas water cooler is connected with the gas inlet at the bottom of the fine desulfurization tower.
Further, the converter gas can be directly connected with the gas inlet of the hydrolysis desulfurization start-up heater without passing through a converter gas heat exchanger; the gas outlet at the bottom of the deoxidation reactor can also be directly connected with the shell pass inlet of the purified gas water cooler without passing through the converter gas heat exchanger.
Furthermore, the cold shock pipeline regulating valve and the deoxygenation reactor inlet pipeline regulating valve are DN600 triple eccentric flange type composite sealing butterfly valves.
Furthermore, the purification water cooler is a baffling rod shell-and-tube heat exchanger.
The invention also provides a converter gas deoxidation and desulfurization method, which comprises the following steps:
step 1: after the converter gas is subjected to heat exchange with the deoxidized converter gas through the converter gas heat exchanger and the temperature is raised to a set temperature, the converter gas enters a hydrolysis desulfurization tower from the bottom of the hydrolysis desulfurization tower through a hydrolysis desulfurization start heater, organic sulfur in the converter gas is hydrolyzed and converted into hydrogen sulfide under the action of a lower organic sulfur hydrolysis catalyst, and then H in the gas is removed under the action of an upper bifunctional fine desulfurizer2S and other sulfides;
step 2: after passing through a start-up heater, gas from the top of the hydrolysis desulfurization tower enters a deoxygenation reactor from the top and the bottom of the deoxygenation reactor respectively to remove oxygen in converter gas;
and step 3: the gas deoxidized by the deoxidation reactor exchanges heat with the original converter gas through a converter gas heat exchanger to be cooled, then is cooled to a set temperature through a purified gas water cooler, and then enters a fine desulfurization tower from the bottom of the fine desulfurization tower to remove residual mercaptan and dimethyl disulfide in the gas, and purified gas from the top of the fine desulfurization tower is led to the next process.
Further, the purifier water cooler in the step 3 is a baffling rod shell-and-tube heat exchanger.
Further, the gas flow entering the deoxygenation reactor from the top and the bottom of the deoxygenation reactor in the step 2 is respectively controlled by a cold shock pipeline regulating valve and a deoxygenation reactor inlet pipeline regulating valve, and the specific requirement is that the top temperature of the deoxygenation reactor is controlled at the catalyst activation temperature; when the oxygen content in the converter gas is not more than 1.0 percent, the temperature of the hot spot of the catalyst bed layer of the deoxidation reactor is not more than 190 ℃ and the temperature equalization is not more than 150 ℃.
Compared with the prior art, the invention has the following advantages:
1. the invention adds a cold shock pipeline to enable gas to enter the deoxidation reactor from the top and the bottom respectively, and simultaneously adjusts the flow of converter gas entering the bottom and the top by controlling the opening of a valve to realize that the temperature at the top is controlled at 70 ℃. When the oxygen content in the converter gas is not more than 1.0 percent, the hot spot temperature of the catalyst bed layer of the deoxidation reactor is not more than 190 ℃ and the temperature uniformity is not more than 150 ℃.
2. The deoxidized gas after passing through the device of the invention does not need to be partially recycled in a converter gas circulating compressor, the compressor is stopped, the resistance drop of the deoxidizer is reduced by 30KPa, and the deoxidized gas completely enters a purified gas water cooler.
3. The purifier water cooler of the invention adopts a baffling rod shell-and-tube heat exchanger to replace the original inlet baffle and baffle type purified gas water cooler, so that the resistance drop of the purifier water cooler is reduced by 30KPa, and the integral pressure difference of the system is lower than 150 KPa.
Comprehensively, the device and the method can improve the treatment capacity of the deoxygenation reactor, reduce the energy consumption and the production cost of the device, reduce the resistance drop of a system and improve the integral production load of the device.
Drawings
FIG. 1 is a schematic view of the apparatus for deoxidizing and desulfurizing converter gas according to the present invention.
Detailed Description
The technical solution of the present invention will be specifically and specifically described below with reference to the embodiments of the present invention and the accompanying drawings. It should be noted that variations and modifications can be made by those skilled in the art without departing from the principle of the present invention, and these should also be construed as falling within the scope of the present invention.
Example 1
A device for deoxidizing and desulfurizing converter gas, as shown in fig. 1, mainly comprising: the system comprises a deoxidation reactor 1, a quench pipeline 2, a deoxidation reactor inlet pipeline 3, a quench pipeline regulating valve 4, a deoxidation reactor inlet pipeline regulating valve 5, a purification water cooler 6, a converter gas heat exchanger 7, a hydrolysis desulfurization start-up heater 8, a hydrolysis desulfurization tower 9, a start-up heater 10 and a fine desulfurization tower 11.
Converter gas is connected with a gas inlet of a converter gas heat exchanger 7, a gas outlet of the converter gas heat exchanger 7 is connected with a gas inlet of a hydrolysis desulfurization start-up heater 8, a gas outlet of the hydrolysis desulfurization start-up heater 8 is connected with a gas inlet at the bottom of a hydrolysis desulfurization tower 9, a gas outlet at the top of the hydrolysis desulfurization tower 9 is connected with a gas inlet of a start-up heater 10, a gas outlet of the start-up heater 10 is respectively connected with a gas inlet at the top and a gas inlet at the bottom of a deoxidation reactor 1 through two branches of a cold shock pipeline 2 and a deoxidation reactor inlet pipeline 3, and the cold shock pipeline adjusting valve 4 and the deoxidation reactor inlet pipeline adjusting valve 5 are respectively arranged on the cold shock pipeline 2 and the deoxidation reactor inlet pipeline 3 and are respectively used for adjusting the flow of the converter gas entering the top and the bottom of the deoxidation reactor 1; the gas outlet at the bottom of the deoxidation reactor 1 is connected with the shell pass inlet of the converter gas heat exchanger 7, the shell pass outlet of the converter gas heat exchanger 7 is connected with the shell pass inlet of the purified gas water cooler 6, the shell pass outlet of the purified gas water cooler 6 is connected with the gas inlet at the bottom of the fine desulfurization tower 11, and the gas outlet at the top of the fine desulfurization tower 11 leads to the outside of the battery limits for the post-process.
The converter gas can also be directly connected with the gas inlet of the hydrolysis desulfurization start-up heater 8 without passing through the converter gas heat exchanger 7; the air outlet at the bottom of the deoxidation reactor 1 can also be directly connected with the shell pass inlet of the purified gas water cooler 6 without passing through the converter gas heat exchanger 7.
The cold shock pipeline regulating valve 4 and the deoxidation reactor inlet pipeline regulating valve 5 are DN600 triple eccentric flange type composite sealing butterfly valves.
The purification water cooler 6 is a baffling rod shell-and-tube heat exchanger.
Example 2
A method for deoxidizing and desulfurizing converter gas mainly comprises the following steps:
And 3, exchanging heat between the deoxidized gas and a feed gas (converter gas) through a converter gas heat exchanger 7 to reduce the temperature, reducing the temperature to 40 ℃ through a purified gas water cooler (namely a deflection rod shell-and-tube heat exchanger), then feeding the deoxidized gas into a fine desulfurization tower 11 from the bottom of the fine desulfurization tower 11 to remove residual mercaptan and dimethyl disulfide in the gas, and removing the purified gas from the top of the fine desulfurization tower, wherein the oxygen content is less than or equal to 30ppm, the total sulfur content is less than 0.1ppm, the pressure is more than or equal to 0.75MPa, and the post-process is carried out.
The method ensures that the hot spot temperature of the catalyst bed layer of the deoxygenation reactor is not more than 190 ℃ and the temperature uniformity is not more than 150 ℃. The resistance of the deoxygenation reactor is reduced by 30KPa, the resistance of the purifier water cooler is reduced by 30KPa, and the overall pressure difference of the system is lower than 150 KPa. The oxygen content of the finally obtained converter gas is less than or equal to 30ppm, the total sulfur content is less than 0.1ppm, the pressure is more than or equal to 0.75MPa, and the production process of the ethylene glycol is met.
Claims (7)
1. A device for deoxidizing and desulfurizing converter gas is characterized by comprising the following components: the system comprises a deoxidation reactor (1), a quench pipeline (2), a deoxidation reactor inlet pipeline (3), a quench pipeline regulating valve (4), a deoxidation reactor inlet pipeline regulating valve (5), a purification water cooler (6), a converter gas heat exchanger (7), a hydrolysis desulfurization start-up heater (8), a hydrolysis desulfurization tower (9), a start-up heater (10) and a fine desulfurization tower (11);
wherein, the air inlet of the converter gas heat exchanger (7) is connected with the converter gas, the air outlet of the converter gas heat exchanger (7) is connected with the air inlet of the hydrolysis desulfurization start-up heater (8), the air outlet of the hydrolysis desulfurization start-up heater (8) is connected with the air inlet at the bottom of the hydrolysis desulfurization tower (9), the air outlet at the top of the hydrolysis desulfurization tower (9) is connected with the air inlet of the start-up heater (10), the air outlet of the start-up heater (10) is divided into two branches, one branch is connected with the top air inlet of the deoxidation reactor (1) through a cold shock pipeline (2), the other branch is connected with the air inlet at the bottom of the deoxidation reactor (1) through a deoxidation reactor inlet pipeline (3), a cold shock pipeline regulating valve (4) and a deoxidation reactor inlet pipeline regulating valve (5) are respectively arranged on the cold shock pipeline (2) and the deoxidation reactor inlet pipeline (3) and are respectively used for regulating the flow of converter coal gas entering the top and the bottom of the deoxidation reactor (1); an air outlet at the bottom of the deoxidation reactor (1) is connected with a shell pass inlet of the converter gas heat exchanger (7), a shell pass outlet of the converter gas heat exchanger (7) is connected with a shell pass inlet of the purified gas water cooler (6), and a shell pass outlet of the purified gas water cooler (6) is connected with an air inlet at the bottom of the fine desulfurization tower (11).
2. The apparatus for deoxidation and desulphurisation of converter gas according to claim 1, characterized in that: the converter gas can also be directly connected with the gas inlet of the hydrolysis desulfurization start-up heater (8) without passing through the converter gas heat exchanger (7); the air outlet at the bottom of the deoxidation reactor (1) can also be directly connected with the shell pass inlet of the purified gas water cooler (6) without passing through the converter gas heat exchanger (7).
3. The apparatus for deoxidation and desulphurisation of converter gas according to claim 1, characterized in that: the cold shock pipeline regulating valve (4) and the deoxygenation reactor inlet pipeline regulating valve (5) are DN600 triple eccentric flange type composite sealing butterfly valves.
4. The apparatus for deoxidation and desulphurisation of converter gas according to claim 1, characterized in that: the purification water cooler (6) is a baffling rod shell-and-tube heat exchanger.
5. A method for deoxidizing and desulfurizing converter gas is characterized by comprising the following steps: the method comprises the following steps:
step 1: after the converter gas is subjected to heat exchange with the deoxidized converter gas through the converter gas heat exchanger (7) and the temperature is raised to a set temperature, the converter gas enters the hydrolysis desulfurization tower (9) from the bottom of the hydrolysis desulfurization tower (9) through the hydrolysis desulfurization start-up heater (8), organic sulfur in the converter gas is hydrolyzed and converted into hydrogen sulfide under the action of the organic sulfur hydrolysis catalyst at the lower layer, and then H in the gas is removed under the action of the dual-functional fine desulfurizer at the upper layer2S and other sulfides;
step 2: gas from the top of the hydrolysis desulfurization tower (9) passes through a start-up heater (10) and then enters a deoxygenation reactor (1) from the top and the bottom of the deoxygenation reactor (1) respectively to remove oxygen in converter gas;
and step 3: the gas deoxidized by the deoxidation reactor (1) exchanges heat with the original converter gas through the converter gas heat exchanger (7) to be cooled, then is cooled to a set temperature through the purified gas water cooler (6), and enters the fine desulfurization tower (11) from the bottom of the fine desulfurization tower (11) to remove residual mercaptan and dimethyl disulfide in the gas, and the purified gas coming out from the top of the fine desulfurization tower (11) is led to the next process.
6. The method for deoxidation and desulphurization of converter gas according to claim 5, characterized in that: and the purifier water cooler (6) in the step 3 is a baffling rod shell-and-tube heat exchanger.
7. The method for deoxidation and desulphurization of converter gas according to claim 5, characterized in that: in the step 2, the gas flow entering the deoxygenation reactor (1) from the top and the bottom of the deoxygenation reactor (1) is respectively controlled by a cold shock pipeline regulating valve (4) and a deoxygenation reactor inlet pipeline regulating valve (5), and the specific requirement is that the top temperature of the deoxygenation reactor (1) is controlled at the catalyst activation temperature; when the oxygen content in the converter gas is not more than 1.0 percent, the hot spot temperature of the catalyst bed layer of the deoxidation reactor (1) is not more than 190 ℃ and the temperature is not more than 150 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210167503.2A CN114456848A (en) | 2022-02-23 | 2022-02-23 | Device and method for deoxidizing and desulfurizing converter gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210167503.2A CN114456848A (en) | 2022-02-23 | 2022-02-23 | Device and method for deoxidizing and desulfurizing converter gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN114456848A true CN114456848A (en) | 2022-05-10 |
Family
ID=81415944
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210167503.2A Pending CN114456848A (en) | 2022-02-23 | 2022-02-23 | Device and method for deoxidizing and desulfurizing converter gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114456848A (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203359975U (en) * | 2013-05-31 | 2013-12-25 | 河北云山化工集团有限公司 | Self-heat-exchange deaerator |
| CN208748034U (en) * | 2018-07-25 | 2019-04-16 | 戴乐亭 | A kind of converter and/or blast furnace gas deoxygenation fine de-sulfur device |
| US20200370824A1 (en) * | 2019-05-23 | 2020-11-26 | Fluor Technologies Corporation | Integrated heavy hydrocarbon and btex removal in lng liquefaction for lean gases |
-
2022
- 2022-02-23 CN CN202210167503.2A patent/CN114456848A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203359975U (en) * | 2013-05-31 | 2013-12-25 | 河北云山化工集团有限公司 | Self-heat-exchange deaerator |
| CN208748034U (en) * | 2018-07-25 | 2019-04-16 | 戴乐亭 | A kind of converter and/or blast furnace gas deoxygenation fine de-sulfur device |
| US20200370824A1 (en) * | 2019-05-23 | 2020-11-26 | Fluor Technologies Corporation | Integrated heavy hydrocarbon and btex removal in lng liquefaction for lean gases |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101871031B (en) | Method and equipment for preparing reducing gas from coke oven gas to produce sponge iron | |
| CN101289620A (en) | Integration process of coke dry quenching co-production synthesis gas and downstream products thereof of methanol | |
| JP5781368B2 (en) | CO shift reactor and coal gasification combined cycle power generation system equipped with the same | |
| CN103446861A (en) | Circulating treatment method for regenerated waste gas produced in temperature swing adsorption desulfurization | |
| CN103508418B (en) | Go into operation gas heating system and heating means in water vapour process for making hydrogen | |
| CN114456848A (en) | Device and method for deoxidizing and desulfurizing converter gas | |
| CN101818087B (en) | Novel process for making synthetic natural gas by using coke-oven gas | |
| CN109264667A (en) | It is a kind of using coke-stove gas as the method and apparatus of waste synthesis gas | |
| CN208292658U (en) | A kind of device for producing hydrogen | |
| CN102219185B (en) | Process for activating catalyst during starting of natural gas steam transforming hydrogen production device | |
| CN1075740A (en) | Oil refinery dry gas and the charging of petroleum naphtha mixed phase are produced hydrogen, methane, carbon monoxide, the method for carbonic acid gas from hydrofining | |
| CN105236645A (en) | Hydrogenation acid water hydrogen sulfide recycling process and system thereof | |
| CN213590141U (en) | Chlor-alkali tail gas hydrogen extraction device | |
| CN210885331U (en) | Device for producing synthetic ammonia by utilizing sodium cyanide tail gas | |
| CN106564861A (en) | Process for efficiently recovering reforming gas energy in hydrocarbon steam reforming hydrogen production process | |
| CN213231512U (en) | Natural gas hydrogen production medium temperature shift system | |
| CN104946316B (en) | Gas cleaning plant and its operating method | |
| CN112940797A (en) | Coke oven gas fine desulfurization system | |
| CN213708250U (en) | Energy-saving production device for purifying, deoxidizing and fine desulfurizing coke oven gas | |
| CN110801797A (en) | Nitrogen circulating temperature rise and fall system of methanol preparation device and application method thereof | |
| CN219297443U (en) | Refined desulfurization, heating and vulcanization gas recovery device for preparing methanol from coke oven gas | |
| CN110763027A (en) | System for accelerating temperature reduction of shift converter and operation method | |
| CN217450092U (en) | Circulating gas return deoxidation system for high-oxygen-content gas | |
| CN215440342U (en) | Coke oven gas fine desulfurization system | |
| CN216296265U (en) | Methanol synthesis loop |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |