CN210134073U - Comprehensive treatment device for blast furnace gas - Google Patents
Comprehensive treatment device for blast furnace gas Download PDFInfo
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- CN210134073U CN210134073U CN201920906466.6U CN201920906466U CN210134073U CN 210134073 U CN210134073 U CN 210134073U CN 201920906466 U CN201920906466 U CN 201920906466U CN 210134073 U CN210134073 U CN 210134073U
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- JJWKPURADFRFRB-UHFFFAOYSA-N carbonyl sulfide Chemical compound O=C=S JJWKPURADFRFRB-UHFFFAOYSA-N 0.000 claims abstract description 177
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 91
- 238000000926 separation method Methods 0.000 claims abstract description 83
- 238000001179 sorption measurement Methods 0.000 claims abstract description 66
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 48
- 239000012528 membrane Substances 0.000 claims abstract description 33
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 24
- 239000012466 permeate Substances 0.000 claims abstract description 22
- 238000003795 desorption Methods 0.000 claims abstract description 17
- 238000011084 recovery Methods 0.000 claims description 27
- 230000006835 compression Effects 0.000 claims description 22
- 238000007906 compression Methods 0.000 claims description 22
- 239000012535 impurity Substances 0.000 claims description 14
- RBORURQQJIQWBS-QVRNUERCSA-N (4ar,6r,7r,7as)-6-(6-amino-8-bromopurin-9-yl)-2-hydroxy-2-sulfanylidene-4a,6,7,7a-tetrahydro-4h-furo[3,2-d][1,3,2]dioxaphosphinin-7-ol Chemical compound C([C@H]1O2)OP(O)(=S)O[C@H]1[C@@H](O)[C@@H]2N1C(N=CN=C2N)=C2N=C1Br RBORURQQJIQWBS-QVRNUERCSA-N 0.000 claims description 12
- 239000007788 liquid Substances 0.000 claims description 9
- 239000007787 solid Substances 0.000 claims description 9
- 125000002915 carbonyl group Chemical group [*:2]C([*:1])=O 0.000 claims description 2
- 239000007789 gas Substances 0.000 abstract description 194
- 238000002485 combustion reaction Methods 0.000 abstract description 10
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 6
- 239000001257 hydrogen Substances 0.000 abstract description 6
- 125000004435 hydrogen atom Chemical class [H]* 0.000 abstract 1
- 238000000034 method Methods 0.000 description 29
- 238000007872 degassing Methods 0.000 description 19
- 239000003463 adsorbent Substances 0.000 description 12
- 239000003034 coal gas Substances 0.000 description 12
- 230000008569 process Effects 0.000 description 11
- 230000000694 effects Effects 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 5
- 230000009286 beneficial effect Effects 0.000 description 4
- 230000005540 biological transmission Effects 0.000 description 4
- 238000001914 filtration Methods 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 3
- 239000003546 flue gas Substances 0.000 description 3
- 239000002808 molecular sieve Substances 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 239000000741 silica gel Substances 0.000 description 3
- 229910002027 silica gel Inorganic materials 0.000 description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 3
- 229910000831 Steel Inorganic materials 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 239000012510 hollow fiber Substances 0.000 description 2
- 239000008258 liquid foam Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000010926 purge Methods 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 229920005597 polymer membrane Polymers 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- -1 this Chemical compound 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
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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
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
-
- 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
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
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- Separation Using Semi-Permeable Membranes (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
The utility model provides a comprehensive treatment device for blast furnace gas. The device comprises a first pressure swing adsorption separation unit and CO2A membrane separation unit and a second pressure swing adsorption separation unit, wherein the first pressure swing adsorption separation unit is provided with a blast furnace gas inlet, a first desorption gas outlet and a first CO2And a carbonyl sulfide rich gas outlet; CO 22The membrane separation unit is provided with a first CO2And carbonyl sulfide richA gas collection inlet, a non-permeate gas outlet, a carbon dioxide-enriched gas outlet, a first CO2And a carbonyl sulfide rich gas inlet and a first CO2Is connected with the carbonyl sulfide enriched gas outlet; the second pressure swing adsorption separation unit is provided with a non-permeable gas inlet, a second desorption gas outlet and second CO2And the carbonyl sulfide enriched gas outlet, the non-permeable gas inlet and the non-permeable gas outlet are connected. The utility model can effectively remove carbonyl sulfide and carbon dioxide in the gas, and effectively separate carbon dioxide and hydrogen, thereby obviously improving the combustion heat value of the blast furnace gas.
Description
Technical Field
The utility model relates to a flue gas treatment technical field particularly, relates to a comprehensive treatment device of blast furnace gas.
Background
Blast furnace gas is used as a byproduct tail gas in a plurality of industrial productions, has great emission and comprises the main components of CO and H2、CO2And N2And contains a small amount of carbonyl sulfide (COS). Wherein CO is2Has higher concentration, influences the combustion heat value of blast furnace gas, and is not beneficial to reducing CO2And (5) discharging. Based on increasing the heat value of blast furnace gas and reducing CO2For emission purposes, it is generally necessary to treat the CO in the blast furnace gas2Separation and collection are carried out. At the same time, COS can be converted into SO during the combustion of the blast furnace gas due to the existence of COS2SO that SO in the flue gas after combustion2The emission exceeds the atmospheric pollution control standard. Therefore, the separation and removal of COS in blast furnace gas are also required.
Common methods for carbonyl sulfide removal include hydrolysis, catalytic oxidation, and adsorption. Because the content of COS in the coal gas is low and CO with higher concentration exists2The application of these methods is significantly affected. CO capture in blast furnace gas2The method mainly adopts a membrane separation method at present, but the current membrane separation method cannot effectively separate CO in coal gas2And H2。
The above reasons cause the following defects in the current blast furnace gas treatment process: (1) carbonyl sulfide cannot be effectively removed; (2) in view of the poor effects of carbon dioxide separation and carbonyl sulfide removal, the combustion heat value of blast furnace gas is low, and practical application of the blast furnace gas is limited.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a comprehensive treatment device of blast furnace gas to carbonyl sulfur among the blast furnace gas of solving prior art can't effectively get rid of, the lower problem of the combustion calorific value of blast furnace gas.
In order to achieve the above object, according to one aspect of the present invention, there is provided an integrated processing apparatus for blast furnace gas, comprising: a first pressure swing adsorption separation unit provided with a blast furnace gas inlet, a first desorption gas outlet and a first CO2And a carbonyl sulfide-enriched gas outlet, the first pressure swing adsorption separation unit being used for separating high sulfur compoundsCO in the gas of the furnace2And carbonyl sulfide are subjected to pressure swing adsorption separation; CO 22A membrane separation unit provided with a first CO2And a carbonyl sulfide rich gas inlet, a non-permeate gas outlet, and a carbon dioxide rich gas outlet, a first CO2And a carbonyl sulfide rich gas inlet and a first CO2Is connected with the carbonyl sulfide enriched gas outlet; and a second pressure swing adsorption separation unit provided with a non-permeate gas inlet, a second stripping gas outlet and a second CO2A carbonyl sulfide enriched gas outlet, a non-permeable gas inlet and a non-permeable gas outlet, and a second pressure swing adsorption separation unit for adsorbing CO in the non-permeable gas discharged from the non-permeable gas outlet2And carbonyl sulfide is subjected to pressure swing adsorption separation.
Furthermore, the device also comprises a first compression unit which is arranged on the gas inlet pipeline where the blast furnace gas inlet is positioned and used for compressing the blast furnace gas.
Further, the device also comprises a second compression unit which is arranged at the first CO2And a carbonyl sulfide rich gas inlet and a first CO2On a line connected to the carbonyl sulfide rich gas outlet for the first CO2And CO discharged from the carbonyl sulfide-enriched gas outlet2And the enriched gas of carbonyl sulfide is compressed.
Further, the device also comprises a gas treatment unit which is arranged between the second compression unit and the first CO2And the pipeline connected with the carbonyl sulfide enriched gas inlet is used for removing solid impurities and liquid impurities in the compressed enriched gas.
Further, the gas treatment unit comprises a second cooler, a second demister and a second filter which are sequentially connected in series.
Further, the device also comprises a first pressure energy recovery device, and the first pressure energy recovery device is connected with the first desorption gas outlet through a first gas transmission pipeline.
Further, the second degassing outlet is connected with the first gas transmission pipeline through a second gas transmission pipeline.
Further, the device also comprises a second pressure energy recovery device, and the second pressure energy recovery device is arranged on the second gas transmission pipeline.
The utility model provides a comprehensive treatment device for blast furnace gas, which comprises a first pressure swing adsorption separation unit and a CO separation unit2A membrane separation unit and a second pressure swing adsorption separation unit, wherein the first pressure swing adsorption separation unit is provided with a blast furnace gas inlet, a first desorption gas outlet and a first CO2And a carbonyl sulfide enriched gas outlet, wherein the first pressure swing adsorption unit is used for treating CO in blast furnace gas2And carbonyl sulfide are subjected to pressure swing adsorption separation; CO 22The membrane separation unit is provided with a first CO2And a carbonyl sulfide rich gas inlet, a non-permeate gas outlet, and a carbon dioxide rich gas outlet, a first CO2And a carbonyl sulfide rich gas inlet and a first CO2Is connected with the carbonyl sulfide enriched gas outlet; the second pressure swing adsorption separation unit is provided with a non-permeable gas inlet, a second desorption gas outlet and second CO2A carbonyl sulfide enriched gas outlet, a non-permeable gas inlet and a non-permeable gas outlet, and a second pressure swing adsorption separation unit for adsorbing CO in the non-permeable gas discharged from the non-permeable gas outlet2And carbonyl sulfide is subjected to pressure swing adsorption separation.
Utilize the utility model provides a device handles blast furnace gas, carbonyl sulphur and carbon dioxide in the desorption coal gas more effectively, carbon dioxide and hydrogen also can effectively separate, and this correspondence can obviously improve blast furnace gas's heat value of burning.
Drawings
The accompanying drawings, which form a part of the present application, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention and not to limit the invention. In the drawings:
fig. 1 shows a schematic view of an integrated treatment plant for blast furnace gas according to an embodiment of the present invention.
Wherein the figures include the following reference numerals:
10. a first pressure swing adsorption separation unit; 20. CO 22A membrane separation unit; 30. a second pressure swing adsorption separation unit; 40. a first compression unit; 50. a second compression unit; 60. gas treatmentA unit; 70. a first pressure energy recovery device; 80. and the second pressure energy recovery device.
Detailed Description
It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict. The present invention will be described in detail below with reference to the accompanying drawings in conjunction with embodiments.
The present application is described in further detail below with reference to specific examples, which should not be construed as limiting the scope of the invention as claimed.
As described in the background section, the carbonyl sulfide in blast furnace gas in the prior art cannot be effectively removed, and the combustion calorific value of the blast furnace gas is low.
In order to solve the above problems, the present invention provides a comprehensive treatment device for blast furnace gas, as shown in fig. 1, comprising a first pressure swing adsorption separation unit 10, CO2A membrane separation unit 20 and a second pressure swing adsorption separation unit 30, the first pressure swing adsorption separation unit 10 is provided with a blast furnace gas inlet, a first desorption gas outlet and a first CO2And a carbonyl sulfide rich gas outlet, the first pressure swing adsorption separation unit 10 is used for treating CO in blast furnace gas2And carbonyl sulfide are subjected to pressure swing adsorption separation; CO 22The membrane separation unit 20 is provided with a first CO2And a carbonyl sulfide rich gas inlet, a non-permeate gas outlet, and a carbon dioxide rich gas outlet, a first CO2And a carbonyl sulfide rich gas inlet and a first CO2Is connected with the carbonyl sulfide enriched gas outlet; the second pressure swing adsorption separation unit 30 is provided with a non-permeate gas inlet, a second stripping gas outlet and a second CO2A carbonyl sulfide-enriched gas outlet, a non-permeate gas inlet and a non-permeate gas outlet, and a second pressure swing adsorption separation unit 30 for separating CO from the non-permeate gas discharged from the non-permeate gas outlet2And carbonyl sulfide is subjected to pressure swing adsorption separation.
Different from the traditional membrane separation method, the utility model adopts a device combining membrane separation and pressure swing adsorption separation to treat blast furnace gas. Specifically, the method comprises the following steps:
the first pressure swing adsorption separation unit 10 can be used for blast furnacesCO in coal gas2And carbonyl sulfide are separated by pressure swing adsorption due to H2So that CO can be adsorbed by the adsorbent2Carbonyl sulfide and H2And (4) effectively separating. CO 22Carbonyl sulfide and a small amount of N2Is separated by adsorption with CO by the first pressure swing adsorption separation unit 10 to form a COs enriched gas. H2And most of N2CO together constitute the first degassing gas. Due to CO2And H2So that H in the first degassing gas is removed2Higher in concentration and therefore has a higher combustion heat value. And CO is efficiently separated in the process2And H2And also overcomes the membrane separation of CO2And H2The requirements for the membrane material.
Second, the COs rich gas enters CO2The membrane separation unit 20 is subjected to further processing, in which process most of the CO is present2And COS, N2The CO is further separated to form CO with higher purity2And (5) producing gas. COS and N separated2CO and a little CO2The remaining components, which constitute the non-permeate gas, are passed to a second pressure swing adsorption separation unit 30 for further pressure swing adsorption. CO in the non-permeable gas can be removed in the high process2And further absorbing and removing COS to form a second removed gas containing N with higher concentration2And CO. The first strip gas and the second strip gas constitute a product gas a having a higher heat of combustion value.
Based on above reason, utilize the utility model discloses above-mentioned device handles blast furnace gas, carbon dioxide and carbonyl sulphur in the desorption coal gas more effectively, and can effectively separate carbon dioxide and hydrogen wherein, can enough enrich the carbon dioxide more effectively, can obviously improve the heat value of burning of blast furnace gas again. In addition to the above beneficial effects, the removal of carbon dioxide is also beneficial to reducing carbon emission, and since the non-permeate gas itself has higher pressure, the pressure can be directly utilized in the operation process of the second pressure swing adsorption separation unit 30, and the energy consumption is also reduced to a certain extent.
The second stripping gas separated by the second pressure swing adsorption separation unit 30 contains high-concentration CO2And COS, which can be sold directly to oil field companies, injected into deep underground portions of oil fields, and CO2And the pollutants are sealed and stored underground for a long time to realize pollutant emission reduction.
In a preferred embodiment, the first pressure swing adsorption separation unit 10 and the second pressure swing adsorption separation unit 30 each comprise a pressure swing adsorption unit for CO and a desorption unit2And carbonyl sulfide is subjected to pressure swing adsorption, and the desorption unit is used for desorbing the adsorbed adsorbent. The specific desorption method may be vacuum evacuation or the like.
In a preferred embodiment, CO2The membrane modules in the membrane separation unit 20 may be selected from hollow fiber membranes, spiral wound membranes or plate membranes. Specific membrane materials may be those commonly used in the art.
In a preferred embodiment, the apparatus further comprises a first compression unit 40, and the first compression unit 40 is disposed on the gas inlet pipeline where the blast furnace gas inlet is located and is used for compressing the blast furnace gas. CO that can be the first pressure swing adsorption separation unit 10 using the first compression unit 402And carbonyl sulfide pressure swing adsorption further provide pressure conditions. Preferably, the above apparatus further comprises a second compression unit 50, the second compression unit 50 being disposed at the first CO2And a carbonyl sulfide rich gas inlet and a first CO2On a line connected to the carbonyl sulfide rich gas outlet for the first CO2And CO discharged from the carbonyl sulfide-enriched gas outlet2And the enriched gas of carbonyl sulfide is compressed. CO can be produced by the second compression unit 502CO of the Membrane separation Unit 202Osmosis further provides pressure drive. And it should be noted that the present invention utilizes the second compression unit 50 to provide sufficient pressure differential to drive sufficient CO compared to the method of using vacuum or purge to reduce pressure on the permeate side2Permeation through membranes, especially polymeric separation membranes, to further increase CO2The collection and recovery rate of (1).
In a preferred embodiment, the apparatus further comprises a gas treatment unit 60, the gas treatment unit 60 being arranged between the second compression unit 50 and the first CO2And carbonyl sulfide rich gas feedThe pipeline connected with the port is used for removing the moisture in the compressed enriched gas. This is advantageous for further CO enhancement2Operational stability of the membrane separation unit 20. Preferably, the gas treatment unit 60 includes a second cooler, a second demister, and a second filter, which are sequentially arranged in series, or the gas treatment unit 60 is a dehydration device.
Preferably, the gas treatment unit 60 further comprises a heat exchanger provided with an inlet to be heated and an outlet to be heated, the inlet to be heated being connected to the outlet of the second filter, and the outlet to be heated being connected to the CO2The cos rich gas inlet of membrane separation unit 20 is connected.
After the pressure swing adsorption separation treatment, the first desorption gas has certain pressure energy, and in order to recover the pressure energy and save energy consumption, in a preferred embodiment, the device further comprises a first pressure energy recovery device 70, and the first pressure energy recovery device 70 is connected with the first desorption gas outlet through a first gas pipeline. In practical applications, the first pressure energy recovery device 70 may be an existing TRT energy recovery system of a steel plant or an expansion work principle-based device. Preferably, the second degassing outlet is connected to the first gas line via a second gas line. Thus, the first degassing gas and the second degassing gas can be recovered together by pressure energy.
In a preferred embodiment, the device further comprises a second pressure energy recovery device 80, the second pressure energy recovery device 80 being arranged on the second gas line. This allows the pressure energy recovery of the second stripping gas before the first stripping gas is mixed.
According to another aspect of the present invention, there is provided a method for comprehensive treatment of blast furnace gas, comprising the steps of: performing first pressure swing adsorption separation on the blast furnace gas to separate CO in the blast furnace gas2And carbonyl sulfide to obtain a first degassing gas and a first CO2And carbonyl sulfide enriched gas; introducing a first CO2CO with carbonyl sulfide rich gas2Membrane separation treatment to obtain non-permeate gas and carbon dioxide enriched gas; subjecting the non-permeate gas to a second pressure swing adsorption separation to separate CO from the non-permeate gas2And carbonyl sulfide to obtain a second degassing gas and a second CO2And a carbonyl sulfide enriched gas. Utilize the utility model discloses above-mentioned method to handle blast furnace gas, carbon dioxide and carbonyl sulfide in the desorption coal gas more effectively, especially carbon dioxide and hydrogen in the separation coal gas can enough more effectively desorption carbonyl sulfide, enrichment carbon dioxide like this, and can obviously improve the heat value of burning of blast furnace gas.
In order to further enhance the effect of the pressure swing adsorption separation of carbon dioxide and carbonyl sulfide, in a preferred embodiment, in the first pressure swing adsorption separation step, the process conditions are as follows: the treatment temperature is-10-180 ℃, the treatment pressure is 0.10-1.50 MPa (A), and the adsorbent is one or more of molecular sieve, silica gel and activated carbon; in the second pressure swing adsorption separation step, the process conditions are as follows: the treatment temperature is-10-100 ℃, the treatment pressure is 0.10-1.50 MPa (A), and the adsorbent is one or more of molecular sieve, silica gel, activated carbon and activated alumina.
Preferably, the step of first pressure swing adsorption separation comprises: performing first pressure swing adsorption on the blast furnace gas by using the adsorbent under the process conditions to obtain a first adsorbent for removing gas and adsorbing carbon dioxide and carbonyl sulfide; desorbing the adsorbent with carbon dioxide and carbonyl sulfide under vacuum condition to obtain first CO2And a carbonyl sulfide enriched gas.
Preferably, the step of second pressure swing adsorption separation comprises: carrying out second pressure swing adsorption on the non-permeable gas by using the adsorbent under the process condition to obtain a second adsorbent which is used for removing gas and adsorbing carbon dioxide and carbonyl sulfide; desorbing the adsorbent with carbon dioxide and carbonyl sulfide under vacuum condition to obtain second CO2And a carbonyl sulfide enriched gas.
In a preferred embodiment, the method further comprises, prior to the step of performing the first pressure swing adsorption separation, the step of performing a first compression of the blast furnace gas; preferably, in the first compression step, the gas pressure is 0.10 to 1.50MPa (A) absolute. Thus can be CO2And transformation of carbonyl sulfideAdsorption further provides pressure conditions. More preferably, CO is carried out2Before the step of membrane separation treatment, the method further comprises subjecting the first CO2And compressing the carbonyl sulfide rich gas; preferably, in the second compression step, the gas pressure is greater than 0.10mpa (a) absolute. This can be CO2Osmosis further provides pressure drive. And it should be noted that, compared with the method of using vacuum pumping or purging to reduce pressure, the present invention can provide enough pressure difference by using the second compression to drive enough CO2Permeation through membranes, especially polymeric separation membranes, to further increase CO2The collection and recovery rate of (1).
In a preferred embodiment, after the step of first compressing, the method further comprises the step of removing solid and liquid impurities from the compressed blast furnace gas; preferably, the step of removing solid and liquid impurities from the compressed blast furnace gas comprises: and cooling, demisting and filtering the compressed blast furnace gas in sequence. Condensable liquid foam, fog drops and possibly entrained solid particles which influence the adsorption effect in the coal gas can be removed through demisting. And then harmful impurities such as fine liquid and the like which can be entrained in the coal gas can be further removed through filtering treatment. In a word, the method can be used for more fully removing impurities such as liquid impurities, solid particles and the like in the coal gas, and the subsequent adsorption separation effect is improved.
In a preferred embodiment, after the step of second compressing, the method further comprises removing the compressed first CO2And a step of enriching solid impurities and liquid impurities in the gas with carbonyl sulfide; preferably, the compressed first CO is removed2And the steps of enriching the gas with carbonyl sulfide of solid impurities and liquid impurities comprise: sequentially aligning the compressed first CO2And cooling, demisting and filtering the carbonyl sulfide enriched gas. Condensable liquid foam, fog drops and possibly entrained solid particles which influence the adsorption effect in the coal gas can be removed through demisting. And then harmful impurities such as fine liquid and the like which can be entrained in the coal gas can be further removed through filtering treatment.
In a preferred embodiment, after the step of obtaining the first degassing gas, the method further comprises the step of recovering the pressure energy of the first degassing gas; preferably, the second stripping gas is subjected to pressure energy recovery together with the first stripping gas. In practice, the pressure energy in the first degassing gas (and optionally the second degassing gas) can be recovered by the TRT energy recovery system already existing in the steel plant or by a device based on the expansion work principle.
Preferably, before the step of performing pressure energy recovery on the second degassing gas together with the first degassing gas, the method further comprises the step of performing pressure energy recovery on the second degassing gas under reduced pressure or after pressure energy recovery, and then performing pressure energy recovery on the second degassing gas after pressure energy recovery under reduced pressure or after pressure energy recovery together with the first degassing gas.
The following examples further illustrate the beneficial effects of the present invention:
example 1
The device shown in the figure 1 of the utility model balances the low-concentration CO in blast furnace gas2The trapping of the process and the treatment effect of other gases such as carbonyl sulfide, hydrogen and the like.
Wherein, the carbon dioxide membrane separation units all adopt hollow fiber type polymer membranes; the process conditions of the first pressure swing adsorption separation device are as follows: the treatment temperature is 40 ℃, the treatment pressure is 0.30MPa, and the adsorbent is silica gel; the process conditions of the second pressure swing adsorption separation device are as follows: the treatment temperature is 30 ℃, the treatment pressure is 0.50MPa, and the adsorbent is a molecular sieve.
The mass balance results are shown in table 1:
TABLE 1
As can be seen from Table 1, when the flue gas flow rate was 16300.00Nm3/h，CO2The content is 23.10%CO content 21.86%, H2The content of COS is 3.20%, and the content of COS is 50mg/Nm3CO obtained by the process in this example2The flow rate of permeation gas (product gas) of the membrane separation unit is 699Nm3/h，CO2The content was 97.11%. The CO concentration is increased from 21.86% to 30.97%, the hydrogen concentration is increased from 3.20% to 4.20%, and the COS concentration is increased from 50mg/Nm3Reduction to 15.10mg/Nm in first degassing gas3And 10mg/Nm in the second degassing gas3Realizes the effective removal of carbonyl sulfide and the capture of CO2And improving the combustion heat value of the blast furnace gas.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (8)
1. An integrated processing apparatus for blast furnace gas, comprising:
a first pressure swing adsorption separation unit (10) provided with a blast furnace gas inlet, a first desorption gas outlet and a first CO2And a carbonyl sulfide rich gas outlet, the first pressure swing adsorption separation unit (10) is used for separating CO in blast furnace gas2And carbonyl sulfide are subjected to pressure swing adsorption separation;
CO2a membrane separation unit (20) provided with a first CO2And a carbonyl sulfide rich gas inlet, a non-permeate gas outlet, and a carbon dioxide rich gas outlet, the first CO2And a carbonyl sulfide rich gas inlet and the first CO2Is connected with the carbonyl sulfide enriched gas outlet; and
a second pressure swing adsorption separation unit (30) provided with a non-permeate gas inlet, a second stripping gas outlet and a second CO2And a carbonyl sulfide-enriched gas outlet, the non-permeate gas inlet being connected to the non-permeate gas outlet, the second pressure swing adsorption separation unit (30) being adapted to separate CO from the non-permeate gas discharged from the non-permeate gas outlet2Performing pressure swing adsorption with carbonyl sulfideAnd (5) separating.
2. The arrangement according to claim 1, characterized by a first compression unit (40), which first compression unit (40) is arranged on the gas inlet line where the blast furnace gas inlet is located, for compressing the blast furnace gas.
3. The plant according to claim 1 or 2, further comprising a second compression unit (50), said second compression unit (50) being arranged at said first CO2And a carbonyl sulfide rich gas inlet and the first CO2On a line connected to the COs rich gas outlet for the first CO2And CO discharged from the carbonyl sulfide-enriched gas outlet2And the enriched gas of carbonyl sulfide is compressed.
4. The apparatus according to claim 3, further comprising a gas treatment unit (60), the gas treatment unit (60) being arranged between the second compression unit (50) and the first CO2And the pipeline is connected with the carbonyl sulfide enriched gas inlet and is used for removing solid impurities and liquid impurities in the compressed enriched gas.
5. The apparatus according to claim 4, wherein the gas treatment unit (60) comprises a second cooler, a second demister and a second filter arranged in series in this order.
6. A device according to claim 1 or 2, further comprising a first pressure energy recovery device (70), the first pressure energy recovery device (70) being connected to the first stripping gas outlet via a first gas line.
7. The apparatus of claim 6 wherein the second stripping gas outlet is connected to the first gas line by a second gas line.
8. The device according to claim 7, characterized in that the device further comprises a second pressure energy recovery device (80), which second pressure energy recovery device (80) is arranged on the second gas line.
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| CN110157490A (en) * | 2019-06-14 | 2019-08-23 | 林千果 | The Integrated Processing Unit and method of blast furnace gas |
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| CN110157490A (en) * | 2019-06-14 | 2019-08-23 | 林千果 | The Integrated Processing Unit and method of blast furnace gas |
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Effective date of registration: 20240325 Address after: Unit 506, Building 22, Yunhe Jiayuan, Huaicheng Street, Huai'an District, Huai'an City, Jiangsu Province, 223200 Patentee after: Jiangsu Carbon Energy Safety and Environmental Technology Co.,Ltd. Country or region after: China Address before: 1401, 14th Floor, Building 5, Courtyard 5, North 4th Street, Gaojiaoyuan, Changping District, Beijing Patentee before: Lin Qianguo Country or region before: China |
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