CN220454075U - System for separating and preparing CO2 and COS of blast furnace gas analysis gas - Google Patents
System for separating and preparing CO2 and COS of blast furnace gas analysis gas Download PDFInfo
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- CN220454075U CN220454075U CN202321491606.0U CN202321491606U CN220454075U CN 220454075 U CN220454075 U CN 220454075U CN 202321491606 U CN202321491606 U CN 202321491606U CN 220454075 U CN220454075 U CN 220454075U
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- gas
- cos
- blast furnace
- furnace gas
- outlet
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- 238000004868 gas analysis Methods 0.000 title claims abstract description 23
- 238000000926 separation method Methods 0.000 claims abstract description 45
- 239000007788 liquid Substances 0.000 claims abstract description 18
- 238000004821 distillation Methods 0.000 claims abstract description 15
- 238000009835 boiling Methods 0.000 claims abstract description 7
- 230000018044 dehydration Effects 0.000 claims abstract description 4
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 4
- 238000004064 recycling Methods 0.000 claims abstract description 4
- 238000001816 cooling Methods 0.000 claims description 9
- 239000000498 cooling water Substances 0.000 claims description 9
- 239000003507 refrigerant Substances 0.000 claims description 3
- 238000005292 vacuum distillation Methods 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- 238000005057 refrigeration Methods 0.000 claims description 2
- 238000003795 desorption Methods 0.000 abstract description 6
- 238000002360 preparation method Methods 0.000 abstract description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 2
- 229910052799 carbon Inorganic materials 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 60
- 238000000034 method Methods 0.000 description 9
- 238000006477 desulfuration reaction Methods 0.000 description 5
- 230000023556 desulfurization Effects 0.000 description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 229910052717 sulfur Inorganic materials 0.000 description 4
- 239000011593 sulfur Substances 0.000 description 4
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000005245 sintering Methods 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Abstract
The utility model discloses a blast furnace gas analysis gas CO 2 And COS separation and preparation system, relates to the technical field of blast furnace gas analysis gas recycling, and aims to solve the problem that the prior art is not specially used for blast furnace gas analysis gas CO 2 And a problem with the COS separation device; the blast furnace gas resolving gas pipeline is connected to the air inlet of the condenser and is used for resolvingThe gas outlet of the cyclone dehydrator is connected to the air inlet end of the cyclone dehydrator for dehydration, and the air outlet end of the cyclone dehydrator is connected to the air inlet pipe of the primary cryogenic system for CO 2 And COS liquefaction, the air outlet pipe of the primary cryogenic system is connected to a gas-liquid separation device for separating liquefied CO 2 And COS, the liquid outlet of which is connected to the cryogenic distillation separation system for separating CO by utilizing the difference in boiling points 2 And COS; the utility model has simple and reasonable structure and can prepare CO 2 COS, high heat value gas is recovered, the additional utilization value of the blast furnace gas desorption gas can be improved, and carbon emission is reduced.
Description
Technical Field
The utility model relates to the technical field of recycling of blast furnace gas analysis gas, in particular to blast furnace gas analysis gas CO 2 And a COS separation and production system.
Background
SO after combustion of blast furnace gas as byproduct for iron and steel enterprises 2 The problem of exceeding standard is that part of enterprises begin to adopt blast furnace gas source fine desulfurization methods, and the specific desulfurization methods mainly comprise two major types of dry desulfurization and wet desulfurization. The blast furnace gas is desulfurized by a dry method, sulfur in the gas is mainly adsorbed by an adsorbent, and after the adsorption material is adsorbed and saturated, the regenerated desorption gas can adopt hot gas to desorb adsorbed sulfide, so that the regeneration of the adsorption material is completed, and the requirement of repeated use for multiple times is met.
In a certain blast furnace gas dry desulfurization project, H in blast furnace gas analysis gas is obtained through field actual measurement 2 O accounts for 1%, N 2 Duty ratio of 58%, O 2 1% by weight, 18% by weight of CO, and CO 2 20% and 2% of COS. The temperature was about 220 ℃.
Aiming at desorbed blast furnace gas analysis gas, one treatment method is that the gas is conveyed to a sintering user for combustion through a pipeline, and the existing treatment device of sintering flue gas is utilized to meet the requirements of standard emission; the second treatment method is to set sulfur melting kettle and other devices to prepare sulfur, but the purity of the prepared sulfur is not high; both treatment methods can not effectively improve the additional utilization value of the blast furnace gas analysis gas, and if the additional utilization value of the blast furnace gas analysis gas can be improved, the industrial gas CO with high additional value in the blast furnace gas analysis gas can be obtained 2 And COS are separated, utilized or sold, so that the method is a multi-purpose method, but the prior art is not specially used for resolving gas CO of blast furnace gas 2 And COS separation, there is therefore a need for a blast furnace gas stripping gas CO 2 And a COS separation and production system.
Disclosure of Invention
The utility model aims to provide a blast furnace gas analysis gas CO 2 And COS separation and preparation system to solve the problem that the prior art is not specially used for blast furnace gas analysis gas CO 2 And a COS separation device.
In order to achieve the above purpose, the present utility model provides the following technical solutions: blast furnace gas analysis gas CO 2 The COS separation and preparation system comprises a blast furnace gas analysis gas pipeline, a condenser, a cyclone dehydrator, a primary cryogenic system, a gas-liquid separation device and a low-temperature distillation separation system; the blast furnace gas resolving gas pipeline is connected to the gas inlet of the condenser for cooling resolving gas, the gas outlet is connected to the gas inlet end of the cyclone dehydrator for dehydration, the gas outlet end of the cyclone dehydrator is connected to the gas inlet pipe of the primary cryogenic system for cooling CO 2 And COS liquefaction, the air outlet pipe of the primary cryogenic system is connected to a gas-liquid separation device for separating liquefied CO 2 And COS, the liquid outlet of which is connected to the cryogenic distillation separation system for separating CO by utilizing the difference in boiling points 2 And COS.
Preferably, the condenser adopts cooling water for indirect heat exchange, and the temperature of the air outlet is 70 ℃.
Preferably, the lower end of the cyclone dehydrator is provided with a water outlet for collecting cooling water.
Preferably, the primary cryogenic system is refrigerated by a refrigerant, the internal pressure of the primary cryogenic system is higher than 1atm, and the cooling temperature is between-50 ℃ and-85 ℃.
Preferably, the gas outlet of the gas-liquid separation device is connected back to the gas system for recycling.
Preferably, the cryogenic distillation separation system is reduced pressure distillation.
Compared with the prior art, the utility model has the beneficial effects that:
the blast furnace gas is resolved into gas CO 2 And COS separation and preparation system, simple and reasonable structure, and can complete preparation and separation of CO from blast furnace gas analysis gas by only connecting a plurality of common devices in series in sequence 2 And COS processes; can improve the additional utilization value of the blast furnace gas analysis gas, and in addition, due to the addition of CO 2 And COS, the gas outlet of the gas-liquid separation device can be connected back to the gas system, CO and the like can be used as high-heat-value gas, so that reduction of carbon emission can be realized incidentally; although liquefaction and distillation are carried out in the aspect of energy consumption, the recovered high-heating-value gas can improve the utilization rate of resources and separate CO 2 And COS brings about other benefits.
Drawings
Fig. 1 is a schematic structural view of the present utility model.
In the figure: 1. a condenser; 2. a spin-flow dehydrator; 3. a primary cryogenic system; 4. a gas-liquid separation device; 5. cryogenic distillation separation system.
Detailed Description
As shown in fig. 1, a blast furnace gas resolving gas CO 2 The COS separation and preparation system comprises a blast furnace gas analysis gas pipeline, and further comprises a condenser 1, a cyclone dehydrator 2, a primary cryogenic system 3, a gas-liquid separation device 4 and a low-temperature distillation separation system 5; the blast furnace gas desorption gas pipeline is connected to the air inlet of the condenser 1 and used for cooling desorption gas, the condenser 1 can adopt cooling water to carry out indirect heat exchange, cooling water is adopted to cool the blast furnace gas desorption gas, and the temperature of the blast furnace gas desorption gas is reduced from 220 ℃ to 70 ℃ by controlling the cooling water quantity and the inlet and outlet temperatures of the cooling water; the air outlet of the condenser 1 is connected to the air inlet end of the cyclone dehydrator 2 to dehydrate the cooled blast furnace gas analysis gas, and in addition, the lower end of the cyclone dehydrator 2 is also provided with a water outlet for collecting cooling water, and parameters such as the diameter, the height and the like of a cylinder of the cyclone dehydrator 2 can be determined according to the requirements of the blast furnace gas analysis gas amount, the dehydration rate and the like; the air outlet end of the cyclone dehydrator 2 is connected to an air inlet pipe of the primary cryogenic system 3 for introducing CO 2 And COS liquefaction, the exit gas from primary cryogenic system 3The pipe is connected to a gas-liquid separation device 4 for separating out liquefied CO 2 And COS, the liquid outlet of which is connected to the cryogenic distillation separation system 5 for separating CO using the difference in boiling points 2 And COS.
The primary cryogenic system 3 uses a refrigerant for refrigeration, and needs to be cooled to-80 to-85 ℃ under normal atmospheric pressure, and CO is cooled at the temperature 2 And COS will liquefy, but CO, N 2 And O 2 The device is still gas, gas-liquid separation can be carried out, and the commercially available cryogenic liquefaction device usually has a pressurizing function, so that the liquefaction separation is more time-saving and energy-saving compared with the pure cooling, and the liquefaction separation is realized through the control of pressure and temperature, when the common device is further adopted, the internal pressure of the primary cryogenic system 3 is optionally higher than 1atm, the cooling temperature is between minus 50 ℃ and minus 85 ℃, and the CO is realized only 2 And COS liquefaction;
in a preferred embodiment, the gas outlet of the gas-liquid separation device 4 is connected back to the gas system, wherein CO and N are contained 2 And O 2 And the like, can be recycled as high-heat-value gas.
The cryogenic distillation separation system 5 preferably employs reduced pressure distillation using CO by controlling pressure and temperature in the distillation column 2 Different from COS in boiling point (CO at normal pressure) 2 Boiling point of-78.5 ℃ and COS boiling point of-50 ℃ for CO 2 Separation from COS, see FIG. 1, CO 2 Collecting the gasified COS from the upper part of the distillation tower, wherein COS is still in a liquid state, and collecting the COS from the bottom of the distillation tower; after separation, CO with higher purity can be obtained 2 And COS, for storage utilization or for export.
The above is only a preferred embodiment of the present utility model, but the scope of the present utility model is not limited thereto, and any changes or substitutions easily contemplated by those skilled in the art within the technical scope of the present utility model should be covered by the present utility model. Therefore, the protection scope of the present utility model should be defined by the claims.
The present utility model is not described in detail in the present application, and is well known to those skilled in the art.
Claims (6)
1. Blast furnace gas analysis gas CO 2 And COS separation system of preparing, including blast furnace gas analysis gas pipeline, its characterized in that: the system also comprises a condenser (1), a cyclone dehydrator (2), a primary cryogenic system (3), a gas-liquid separation device (4) and a low-temperature distillation separation system (5); the blast furnace gas resolving gas pipeline is connected to the gas inlet of the condenser (1) for cooling resolving gas, the gas outlet is connected to the gas inlet end of the cyclone dehydrator (2) for dehydration, the gas outlet end of the cyclone dehydrator (2) is connected to the gas inlet pipe of the primary cryogenic system (3) for cooling CO 2 And COS liquefaction, the gas outlet pipe of the primary cryogenic system (3) is connected with a gas-liquid separation device (4) for separating liquefied CO 2 And COS, the liquid outlet of which is connected to a cryogenic distillation separation system (5) for separating CO using differences in boiling points 2 And COS.
2. A blast furnace gas resolving gas CO according to claim 1 2 And COS separation system of making, its characterized in that: the condenser (1) adopts cooling water to carry out indirect heat exchange, and the temperature of an air outlet is 70 ℃.
3. A blast furnace gas resolving gas CO according to claim 1 2 And COS separation system of making, its characterized in that: the lower end of the cyclone dehydrator (2) is provided with a water outlet for collecting cooling water.
4. A blast furnace gas resolving gas CO according to claim 1 2 And COS separation system of making, its characterized in that: the primary cryogenic system (3) adopts a refrigerant for refrigeration, the internal pressure is higher than 1atm, and the cooling temperature is between minus 50 ℃ and minus 85 ℃.
5. A blast furnace gas resolving gas CO according to claim 1 2 And COS separation system of making, its characterized in that: the gas outlet of the gas-liquid separation device (4) is connected with a gas return system for recycling.
6. A blast furnace gas resolving gas CO according to claim 1 2 And COS separation system of making, its characterized in that: the cryogenic distillation separation system (5) is a reduced pressure distillation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321491606.0U CN220454075U (en) | 2023-06-13 | 2023-06-13 | System for separating and preparing CO2 and COS of blast furnace gas analysis gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321491606.0U CN220454075U (en) | 2023-06-13 | 2023-06-13 | System for separating and preparing CO2 and COS of blast furnace gas analysis gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220454075U true CN220454075U (en) | 2024-02-06 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321491606.0U Active CN220454075U (en) | 2023-06-13 | 2023-06-13 | System for separating and preparing CO2 and COS of blast furnace gas analysis gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220454075U (en) |
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2023
- 2023-06-13 CN CN202321491606.0U patent/CN220454075U/en active Active
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