CN210134071U - Device for increasing combustion heat value of blast furnace gas - Google Patents
Device for increasing combustion heat value of blast furnace gas Download PDFInfo
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- CN210134071U CN210134071U CN201920906441.6U CN201920906441U CN210134071U CN 210134071 U CN210134071 U CN 210134071U CN 201920906441 U CN201920906441 U CN 201920906441U CN 210134071 U CN210134071 U CN 210134071U
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- 238000002485 combustion reaction Methods 0.000 title claims abstract description 20
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 298
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 253
- 238000000926 separation method Methods 0.000 claims abstract description 157
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 149
- 239000012528 membrane Substances 0.000 claims abstract description 120
- 238000001179 sorption measurement Methods 0.000 claims abstract description 45
- 239000012466 permeate Substances 0.000 claims abstract description 37
- 229920000642 polymer Polymers 0.000 claims abstract description 28
- 238000003795 desorption Methods 0.000 claims abstract description 10
- 230000006835 compression Effects 0.000 claims description 27
- 238000007906 compression Methods 0.000 claims description 27
- 239000012535 impurity Substances 0.000 claims description 19
- 239000007787 solid Substances 0.000 claims description 12
- 239000007788 liquid Substances 0.000 claims description 11
- 238000011084 recovery Methods 0.000 claims description 11
- 239000000047 product Substances 0.000 claims description 8
- 230000018044 dehydration Effects 0.000 claims description 4
- 238000006297 dehydration reaction Methods 0.000 claims description 4
- 238000011144 upstream manufacturing Methods 0.000 claims description 3
- 238000011278 co-treatment Methods 0.000 claims description 2
- 239000007789 gas Substances 0.000 abstract description 223
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 15
- 239000001257 hydrogen Substances 0.000 abstract description 14
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 11
- 239000003034 coal gas Substances 0.000 abstract description 8
- 238000000034 method Methods 0.000 description 19
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 10
- 239000003546 flue gas Substances 0.000 description 10
- 239000003463 adsorbent Substances 0.000 description 9
- 238000007872 degassing Methods 0.000 description 7
- 230000000694 effects Effects 0.000 description 7
- 239000002245 particle Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 239000004642 Polyimide Substances 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 4
- 150000002431 hydrogen Chemical class 0.000 description 4
- 229920001721 polyimide Polymers 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 229910000831 Steel Inorganic materials 0.000 description 3
- 125000003277 amino group Chemical group 0.000 description 3
- 238000001914 filtration Methods 0.000 description 3
- 239000010959 steel Substances 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 239000008258 liquid foam Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000000741 silica gel Substances 0.000 description 2
- 229910002027 silica gel Inorganic materials 0.000 description 2
- 239000004952 Polyamide Substances 0.000 description 1
- 229920002614 Polyether block amide Polymers 0.000 description 1
- 239000004721 Polyphenylene oxide Substances 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000012510 hollow fiber Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 229920002647 polyamide Polymers 0.000 description 1
- 229920000570 polyether Polymers 0.000 description 1
- 239000002861 polymer material Substances 0.000 description 1
- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 229920002554 vinyl polymer Polymers 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 device for improving the combustion heat value of blast furnace gas. The apparatus comprises a first CO2Membrane separation unit and CO2Pressure swing adsorption separation Unit, first CO2The membrane separation unit is provided with a blast furnace gas inlet, a first carbon dioxide enriched gas outlet, a first non-permeation gas outlet and a first CO2The membrane separation unit is provided with a first CO2Selective separation membraneAnd first CO2The selective separation membrane is a first polymer separation membrane; CO 22The pressure swing adsorption separation unit is provided with a first non-permeable gas inlet, a second carbon dioxide enriched gas outlet and a carbon dioxide desorption gas outlet, the first non-permeable gas inlet is connected with the first non-permeable gas outlet, and the CO is adsorbed by the first non-permeable gas inlet2The pressure swing adsorption separation unit is used for carrying out CO on non-permeate gas2Pressure swing adsorption separation. The utility model discloses can effectively separate the carbon dioxide in the coal gas, especially separate carbon dioxide and hydrogen wherein, can effectively enrich the carbon dioxide, can obviously improve the heat value of burning of blast furnace gas again.
Description
Technical Field
The utility model relates to a flue gas treatment technical field particularly, relates to an improve device of blast furnace gas heat value of burning.
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 N2. 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.
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 blast furnace flue gas2And hydrogen gas. Especially when the hydrogen concentration in the gas is high and CO is high2When the concentration is low, the problem of low hydrogen enrichment degree exists, so that the combustion heat value of blast furnace gas is low, and the practical application of the blast furnace gas is limited.
SUMMERY OF THE UTILITY MODEL
The main object of the utility model is to provide a device for improving the combustion heat value of blast furnace gas, which is used for solving the problem of CO in blast furnace gas in the prior art2And the problem that the combustion heat value of the coal gas is difficult to improve and the enrichment degree of carbon dioxide is low due to difficult separation of the coal gas and the hydrogen.
In order to achieve the above object, according to an aspect of the present invention, there is provided an apparatus for increasing a combustion heat value of blast furnace gas, comprising: first CO2A membrane separation unit provided with a blast furnace gas inlet, a first carbon dioxide enriched gas outlet, a first non-permeate gas outlet, a first CO2The membrane separation unit is provided with a first CO2A selective separation membrane and first CO2The selective separation membrane is a first polymer separation membrane; CO 22The pressure swing adsorption separation unit is provided with a first non-permeable gas inlet, a second carbon dioxide enriched gas outlet and a carbon dioxide desorption gas outlet, the first non-permeable gas inlet is connected with the first non-permeable gas outlet, and CO is adsorbed on the first non-permeable gas outlet2The pressure swing adsorption separation unit is used for carrying out CO on the non-permeable gas discharged from the first non-permeable gas outlet2Pressure swing adsorption separation.
Further, the apparatus further comprises a second CO2Membrane separation unit, second CO2The membrane separation unit is provided with a first carbon dioxide enriched gas inlet and CO2A product gas outlet, a first carbon dioxide enriched gas inlet connected to the first carbon dioxide enriched gas outlet, and a second CO2The membrane separation unit is provided with a second CO2A selective separation membrane, and a second CO2The selective separation membrane is a second polymer separation membrane.
Further, the first polymer separation membrane and the second polymer separation membrane respectively carry polar groups thereon.
Further, the first non-permeate gas inlet is connected with the first non-permeate gas outlet through a non-permeate gas conveying pipeline, and the second CO is2The membrane separation unit is also provided with a second non-permeate gas outlet which is connected with a non-permeate gas conveying pipeline.
Further, the first carbon dioxide enriched gas inlet is connected with the first carbon dioxide enriched gas outlet through a carbon dioxide enriched gas conveying pipeline, and the second carbon dioxide enriched gas outlet is connected with the carbon dioxide enriched gas conveying pipeline.
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.
Furthermore, the device also comprises a first gas treatment unit which is arranged on a pipeline connected with the blast furnace gas inlet of the first compression unit and used for removing solid impurities and liquid impurities in the compressed blast furnace gas.
Further, the first gas treatment unit comprises a first cooler, a first demister and a first filter which are sequentially connected in series.
Further, the device also comprises a second compression unit which is arranged on the carbon dioxide enriched gas conveying pipeline and is used for compressing the carbon dioxide enriched gas discharged from the first carbon dioxide enriched gas outlet.
Further, a second carbon dioxide enriched gas outlet is connected to the carbon dioxide enriched gas delivery line upstream of the second compression unit.
Furthermore, the device also comprises a second gas treatment unit, wherein the second gas treatment unit is arranged on the carbon dioxide enriched gas conveying pipeline between the second compression unit and the first carbon dioxide enriched gas inlet and is used for removing moisture in the compressed carbon dioxide enriched gas.
Further, the second gas treatment unit comprises a second cooler, a second demister and a second filter which are sequentially connected in series, or the second gas treatment unit is a dehydration device.
Further, the device also comprises a pressure energy recovery unit, wherein the pressure energy recovery unit is connected with the carbon dioxide removing gas outlet and is used for recovering the pressure energy of the gas discharged from the carbon dioxide removing gas outlet.
The utility model provides a device for improving combustion heat value of blast furnace gas, which comprises a first CO2Membrane separation unit and CO2Pressure swing adsorption separation Unit, first CO2The membrane separation unit is provided with a blast furnace gas inlet, a first carbon dioxide enriched gas outlet, a first non-permeation gas outlet and a first CO2The membrane separation unit is provided with a first CO2A selective separation membrane and first CO2The selective separation membrane is a first polymer separation membrane; CO 22The pressure swing adsorption separation unit is provided with a first non-permeable gas inlet, a second carbon dioxide enriched gas outlet and a carbon dioxide desorption gas outlet, the first non-permeable gas inlet is connected with the first non-permeable gas outlet, and the CO is adsorbed by the first non-permeable gas inlet2The pressure swing adsorption separation unit is used for carrying out CO on the non-permeable gas discharged from the first non-permeable gas outlet2Pressure swing adsorption separation.
Utilize the utility model discloses above-mentioned device handles blast furnace gas, can separate the carbon dioxide in the coal gas more effectively, especially 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.
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 apparatus for increasing the combustion heat value of blast furnace gas according to an embodiment of the present invention.
Wherein the figures include the following reference numerals:
10. first CO2A membrane separation unit; 20. CO 22A pressure swing adsorption separation unit; 30. second CO2A membrane separation unit; 40. a first compression unit; 50. a first gas treatment unit; 60. a second compression unit; 70. a second gas treatment unit; 80. a pressure energy recovery unit.
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, CO in blast furnace gas in the prior art2And the separation of the carbon dioxide and the hydrogen is difficult, so that the combustion heat value of the coal gas is difficult to improve, and the enrichment degree of the carbon dioxide is low.
In order to solve the above problems, the present invention provides a device for increasing the combustion heat value of blast furnace gas, as shown in fig. 1, which comprises a first CO2 Membrane separation unit 10 and CO2Pressure swing adsorption separation Unit 20, first CO2The membrane separation unit 10 is provided with a blast furnace gas inlet, a first carbon dioxide enriched gas outlet and a first non-permeate gas outlet, a first CO2The membrane separation unit 10 is provided with a first CO2A selective separation membrane and first CO2The selective separation membrane is a first polymer separation membrane; CO 22The pressure swing adsorption separation unit 20 is provided with a first non-permeate gas inlet, a second carbon dioxide enriched gas outlet and a carbon dioxide desorbed gas outlet, the first non-permeate gas inletThe gas-permeable inlet is connected to the first non-permeate gas outlet, and CO is introduced into the gas-permeable inlet2The pressure swing adsorption separation unit 20 is used for carrying out CO treatment on the non-permeate gas discharged from the first non-permeate gas outlet2Pressure 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:
using a first CO2The membrane separation unit 10 may first subject the blast furnace gas to CO2The first CO is utilized because of the huge amount of flue gas required for carbon capture in the membrane separation treatment2The membrane separation unit 10 advantageously reduces the footprint and simplifies the process. Due to CO2Is much higher than H2Result in CO2Is more condensable than H2Based on the principle, the utility model provides a first CO2The membrane separation unit 10 employs a first polymer separation membrane, CO2Solubility in polymeric separation membranes is greater than that of H2. In the first CO2Most of the CO in the flue gas is treated by the membrane separation unit 102Forming a first carbon dioxide enriched gas through the separation membrane, discharging CO, H from the first carbon dioxide enriched gas outlet2、N2And a small amount of CO2A first high pressure non-permeate gas is composed to be discharged.
Secondly, the utilization of CO2The pressure swing adsorption separation unit 20 may perform pressure swing adsorption separation on the carbon dioxide in the first high pressure non-permeate gas to further separate the CO therein2And H2。CO2The pressure swing adsorption separation unit 20 is based on the principle of equilibrium adsorption, i.e., relying on adsorbents for CO under pressure swing conditions2The adsorption strength of the CO and the hydrogen, the CO and the nitrogen can achieve the purpose of separating the CO2The purpose of (1). And undergoes the first CO2The membrane separation unit 10 is used for separating most of the carbon dioxide in the flue gas, and the concentration of the carbon dioxide in the first high-pressure non-permeable gas is obviously reduced, which is beneficial to reducing CO2The amount of adsorbent in the pressure swing adsorption separation unit 20 is used to further improve the adsorption separation effect of carbon dioxide and obtain a second carbon dioxide enriched gas. At the same time, H in the gas2Further enrichment of CO with N2Together, make up a product gas having a higher heat of combustion value (i.e., carbon dioxide degassing gas a shown in fig. 1).
In a word, utilize the utility model discloses above-mentioned device to handle blast furnace gas, can separate the carbon dioxide in the coal gas more effectively, especially 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 a preferred embodiment, CO2The pressure swing adsorption separation unit 20 includes CO2Pressure swing adsorption unit and CO2Desorption unit, CO2The pressure swing adsorption unit is used for treating CO2Performing pressure swing adsorption of CO2The desorption unit is used for desorbing the adsorbent after adsorbing the carbon dioxide. The specific desorption method may be vacuum evacuation or the like.
In order to further enrich the carbon dioxide, in a preferred embodiment, the above apparatus further comprises a second CO2 Membrane separation unit 30, second CO2The membrane separation unit 30 is provided with a first carbon dioxide enriched gas inlet and CO2A product gas outlet, a first carbon dioxide enriched gas inlet connected to the first carbon dioxide enriched gas outlet, and a second CO2The membrane separation unit 30 is provided with a second CO2A selective separation membrane, and a second CO2The selective separation membrane is a second polymer separation membrane. Thus, from the first CO2The first carbon dioxide enriched gas separated and enriched in the membrane separation unit 10 enters the second CO again2The membrane separation unit 30 performs separation and enrichment, and under the separation action of the second polymer separation membrane, carbon dioxide, a small amount of hydrogen, carbon monoxide, nitrogen and the like in the gas are further separated to form carbon dioxide product gas with higher purity.
In a preferred embodiment, the first polymer separation membrane and the second polymer separation membrane respectively carry polar groups thereon, and the polymer may be a polymer material such as Polyimide (PI), polyvinyl amine (PVam), polyether block polyamide (Pebax), and the like. CO 22Is much more polar than H2By carrying polar groups (e.g. amino groups, etc.)Polar groups) exist in the polymer separation membrane, and the polar groups further enhance the separation membrane to CO according to the principle of' similar compatibility2The solubility of (c). Except for CO2In addition to the improvement of solubility, the presence of polar groups can promote CO2Reversibly reacting with polar groups in the carrier of the polymer separation membrane, and H2Difficult to react with polar groups. Based on the reasons of the two aspects, the utility model discloses CO has further been improved2Is favorable for further improving CO2And the separation effect of hydrogen, thereby improving the enrichment degree of carbon dioxide and the combustion heat value of blast furnace gas.
In a preferred embodiment, the first CO2 Membrane separation unit 10 and secondary CO2The membrane modules in the membrane separation unit 30 are each independently selected from hollow fiber membranes, spiral wound membranes or plate membranes. Here, "independently selected from" means that the first CO is2 Membrane separation unit 10 and secondary CO2The membrane modules in the membrane separation unit 30 are each selected from one of the three membrane modules, and the three membrane modules may be identical to or different from each other.
In a preferred embodiment, as shown in FIG. 1, the first non-permeate gas inlet is connected to the first non-permeate gas outlet by a non-permeate gas transfer line and the second CO is connected to the first CO transfer line2The membrane separation unit 30 is further provided with a second non-permeate outlet which is connected to a non-permeate transfer line. Thus, the second CO2The non-permeate gas separated by the membrane separation unit 30 can be mixed with the first CO2The non-permeate gas separated by the membrane separation unit 10 enters a pressure swing adsorption link together, so that the enrichment degree of carbon dioxide in blast furnace gas can be further improved, and the combustion heat value of the blast furnace gas is correspondingly improved.
Quilt CO2The pressure swing adsorption separation unit 20 adsorbs separated CO2The purity of the carbon dioxide is relatively high, and the carbon dioxide can be directly used as carbon dioxide product gas. In a preferred embodiment, as shown in FIG. 1, the first carbon dioxide-enriched gas inlet is connected to the first carbon dioxide-enriched gas outlet by a carbon dioxide-enriched gas delivery line, and the second carbon dioxide is connected to the first carbon dioxide-enriched gas outlet by a carbon dioxide-enriched gas delivery lineThe carbon dioxide enriched gas outlet is connected with a carbon dioxide enriched gas conveying pipeline. This can further increase the degree of carbon dioxide enrichment.
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. Can be a first CO using the first compression unit 402CO of the Membrane separation Unit 102Osmosis further provides pressure drive. And it should be noted that the present invention utilizes the first compression unit 40 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). Likewise, it is preferable that the above apparatus further comprises a second compression unit 60, and the second compression unit 60 is disposed on the carbon dioxide-enriched gas delivery line for compressing the carbon dioxide-enriched gas discharged from the first carbon dioxide-enriched gas outlet.
Blast furnace gas contains CO and H2、CO2And N2Besides, some solid impurities (particles) and liquid impurities (moisture) are carried, and the first CO is reduced by the solid impurities and the liquid impurities2The influence of the polymer separation membrane in the membrane separation unit 10, in a preferred embodiment, the apparatus further comprises a first gas treatment unit 50, wherein the first gas treatment unit 50 is arranged on a pipeline of the first compression unit 40 connected with the blast furnace gas inlet and is used for removing solid impurities and liquid impurities in the compressed blast furnace gas. The polymer separation membrane is easily polluted by solid impurities such as particles and the like, has higher requirements on humidity and temperature, and can reduce the influences as much as possible by utilizing the first gas treatment unit 50, thereby further improving the treatment effect of the blast furnace gas.
In one embodiment, solid and liquid impurities in the flue gas may be removed using a filter. More preferably, the first gas treatment unit 50 includes a first cooler, a first demister, and a first filter arranged in series in this order. The height can be adjusted by the first coolerLiquid in the furnace gas is further condensed out, then condensable liquid foam, fog drops and possibly entrained solid particles are removed through the first demister, and finally harmful impurities such as possibly entrained fine liquid in the flue gas can be further removed through the first filter. Meanwhile, the arrangement of the first cooler is also beneficial to controlling the temperature of the flue gas so as to further improve the first CO2Operational stability of the membrane separation unit 10.
In a preferred embodiment, the first gas treatment unit 50 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 first filter and the outlet to be heated being connected to the blast furnace gas inlet. Thus, the blast furnace gas after removing the impurities can be heated by heat exchange in the heat exchanger, so that the operating temperature of the system is kept constant and is far away from the dew point.
Preferably, the second carbon dioxide enriched gas outlet is connected to the carbon dioxide enriched gas delivery line upstream of the second compression unit 60.
In a preferred embodiment, the apparatus further comprises a second gas treatment unit 70, the second gas treatment unit 70 being arranged in the carbon dioxide enriched gas transfer line between the second compression unit 60 and the first carbon dioxide enriched gas inlet for removing moisture from the compressed carbon dioxide enriched gas. This is advantageous for further enhancement of the secondary CO2Operational stability of the membrane separation unit 30. Preferably, the second gas treatment unit 70 includes a second cooler, a second demister, and a second filter, which are sequentially arranged in series, or the second gas treatment unit 70 is a dehydration device. The second cooler, second demister, and second filter function similarly to the first cooler, first demister, and first filter described above. A dehydration unit may also be utilized to remove moisture from the carbon dioxide enriched gas.
Similarly, it is preferable that the second gas treatment unit 70 further includes a heat exchanger provided with an inlet to be heated and an outlet to be heated, the inlet to be heated is connected to the outlet of the second filter, and the outlet to be heated is connected to the second CO2The first carbon dioxide-enriched gas inlet of the membrane separation unit 30 is connected.
By CO2After the pressure swing adsorption separation treatment, the carbon dioxide 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 pressure energy recovery unit 80, and the pressure energy recovery unit 80 is connected with a carbon dioxide desorption gas outlet and is used for recovering the pressure energy of the gas discharged from the carbon dioxide desorption gas outlet. In practice, the pressure energy recovery unit 80 may be an existing TRT energy recovery system of a steel plant or an expansion work principle-based device.
According to another aspect of the present invention, there is provided a method for increasing the combustion heat value of blast furnace gas, comprising the steps of: subjecting blast furnace gas to first CO2Membrane separation treatment to obtain a first carbon dioxide enriched gas and a first non-permeate gas; wherein CO is first2First CO used in membrane separation process2The selective separation membrane is a first polymer separation membrane; and carrying out carbon dioxide pressure swing adsorption separation on the first non-permeate gas to obtain a second carbon dioxide enriched gas and a carbon dioxide degassing gas. The method for treating blast furnace gas can effectively separate carbon dioxide in the gas, particularly carbon dioxide and hydrogen in the gas, can effectively enrich carbon dioxide, and can obviously improve the combustion heat value of the blast furnace gas.
To further increase the degree of carbon dioxide enrichment, in a preferred embodiment, after the step of obtaining the first carbon dioxide-enriched gas, the method further comprises subjecting the first carbon dioxide-enriched gas to a second CO2Step of membrane separation treatment, and second CO2Secondary CO used in membrane separation process2The selective separation membrane is a second polymer separation membrane.
Preferably, the first polymer separation membrane and the second polymer separation membrane each carry a polar group, and more preferably, the polar group is an amino group. CO 22Is much more polar than H2The polar groups are similar to each other by using a polymer separation membrane carrying polar groups (such as amino groups)The polar group further enhances the separation membrane to CO2The solubility of (c). Except for CO2In addition to the improvement of solubility, the presence of polar groups can promote CO2Reversibly reacting with polar groups in the carrier of the polymer separation membrane, and H2Difficult to react with polar groups. Based on the reasons of the two aspects, the utility model discloses CO has further been improved2Is favorable for further improving CO2And the separation effect of hydrogen, thereby improving the enrichment degree of carbon dioxide and the combustion heat value of blast furnace gas.
By CO2CO obtained by pressure swing adsorption separation2The purity of the carbon dioxide is relatively high, and the carbon dioxide can be directly used as carbon dioxide product gas. In a preferred embodiment, the first carbon dioxide-enriched gas is subjected to a second CO2In the step of membrane separation treatment, the carbon dioxide-enriched gas formed by mixing the second carbon dioxide-enriched gas and the first carbon dioxide-enriched gas is subjected to secondary CO2And (5) membrane separation treatment. This contributes to further increase of the purity of the carbon dioxide.
In order to enrich the carbon dioxide more fully and to increase the calorific value of the blast furnace gas, in a preferred embodiment, the second CO2And in the step of carbon dioxide pressure swing adsorption separation, the second non-permeable gas and the first non-permeable gas are subjected to carbon dioxide pressure swing adsorption separation together.
In order to further enhance the effect of the carbon dioxide pressure swing adsorption separation, in a preferred embodiment, in the step of carbon dioxide pressure swing adsorption separation, the process conditions are as follows: the treatment temperature is-10 to 160 ℃, the adsorption pressure is 0.10 to 1.50MPa (absolute pressure), and the adsorbent is one or more of molecular sieve, silica gel, activated carbon and modified adsorbent thereof. Preferably, the step of carbon dioxide pressure swing adsorption separation comprises: performing carbon dioxide pressure swing adsorption on the first high-pressure non-permeate gas (and optionally the second high-pressure non-permeate gas) by using the adsorbent under the process conditions to obtain carbon dioxide degassing gas and the adsorbent adsorbed with carbon dioxide; and desorbing the adsorbent adsorbed with the carbon dioxide in a vacuum state to obtain a second carbon dioxide enriched gas.
In a preferred embodiment, the first CO pass is carried out2Before the step of membrane separation treatment, the method also comprises the step of first compressing the blast furnace gas; preferably, in the first compression step, the gas pressure is made greater than 0.10mpa (a). Thus may be first CO2CO treated by membrane separation2Osmosis further provides pressure drive. Likewise, preferably, the second CO is performed2Before the step of membrane separation treatment, the method further comprises the step of performing secondary compression on the carbon dioxide enriched gas; preferably, in the second compression step, the gas pressure is greater than 0.10mpa (a).
In carrying out the second CO2Prior to the step of membrane separation treatment, the method further comprises the step of second compressing the first carbon dioxide enriched gas; preferably, in the second compression step, the gas pressure is greater than 0.10MP (A). After the step of first compressing, the method further comprises the step of removing solid impurities and liquid impurities in 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 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 short, the above method can remove impurities such as liquid impurities and solid particles in the gas more sufficiently, thereby further improving the carbon dioxide capture effect. Meanwhile, the gas is cooled, so that the temperature of the flue gas can be effectively controlled, and the operation stability of the polymer separation membrane is further improved.
More preferably, after the step of second compressing, the method further comprises the step of removing moisture from the compressed carbon dioxide-enriched gas; preferably, the step of removing moisture from the compressed carbon dioxide-enriched gas comprises: and sequentially cooling, demisting and filtering the compressed carbon dioxide enriched gas, or dehydrating the compressed carbon dioxide enriched gas.
By CO2After the pressure swing adsorption separation treatment, the carbon dioxide degassing gas has certain pressure energy, and in order to recover the pressure energy and save energy consumption, in a preferred embodiment, after the carbon dioxide degassing gas is obtained, the method further comprises the step of recovering the pressure energy in the carbon dioxide degassing gas. In practical application, the pressure energy in the carbon dioxide degassing gas can be recovered through the existing TRT energy recovery system of the steel plant or a device based on the expansion work-doing principle.
The following examples further illustrate the beneficial effects of the present invention:
example 1
The blast furnace gas of a certain steel plant is tested, the utility model balances the low concentration CO in the blast furnace gas by the device shown in the figure 12Trapping of (b), and treatment effects of other gases such as hydrogen.
Wherein, the carbon dioxide membrane separation units all adopt polymer separation membranes carrying amino polar groups. The polymer is Polyimide (PI); in the step of carbon dioxide pressure swing adsorption separation, the process conditions are as follows: the treatment temperature is 30 ℃, the treatment pressure is 0.50MPa (A), and the adsorbent is silica gel.
The mass balance results are shown in table 1:
TABLE 1
As can be seen from Table 1, when the blast furnace flue gas flow rate to be treated was 10000Nm3/h，CO225.70% of CO, 21.86% of H2At a content of 2.96%, in the treatment process in this example, the second stage CO2The 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 28.97%, and the hydrogen concentration is increased from 2.96% to 6.70%. Realizes the capture of CO2And simultaneously, the combustion heat value of the blast furnace gas is obviously improved.
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 (13)
1. An apparatus for increasing the combustion heat value of blast furnace gas, comprising:
first CO2A membrane separation unit (10) provided with a blast furnace gas inlet, a first carbon dioxide enriched gas outlet and a first non-permeate gas outlet, the first CO2The membrane separation unit (10) is provided with a first CO2A selective separation membrane, and the first CO2The selective separation membrane is a first polymer separation membrane;
CO2a pressure swing adsorption separation unit (20) provided with a first non-permeate gas inlet, a second carbon dioxide enriched gas outlet and a carbon dioxide desorption gas outlet, wherein the first non-permeate gas inlet is connected with the first non-permeate gas outlet, and the CO is discharged from the first non-permeate gas outlet2The pressure swing adsorption separation unit (20) is used for carrying out CO treatment on the non-permeable gas discharged from the first non-permeable gas outlet2Pressure swing adsorption separation.
2. The apparatus of claim 1, further comprising a second CO2A membrane separation unit (30), the second CO2The membrane separation unit (30) is provided with a first carbon dioxide enriched gas inlet and a CO2A product gas outlet, the first carbon dioxide enriched gas inlet connected to the first carbon dioxide enriched gas outlet, the second CO2The membrane separation unit (30) is provided with a second CO2A selective separation membrane, and the second CO2The selective separation membrane is a second polymer separation membrane.
3. The device of claim 2, wherein the first polymeric separation membrane and the second polymeric separation membrane each carry polar groups thereon.
4. The apparatus of claim 2, wherein the first non-permeate gas inlet is connected to the first non-permeate gas outlet by a non-permeate gas transfer line, and the second CO is connected to the first CO outlet by a second CO transfer line2The membrane separation unit (30) is further provided with a second non-permeate gas outlet, which is connected to the non-permeate gas transfer line.
5. The apparatus of claim 4, wherein the first carbon dioxide-enriched gas inlet and the first carbon dioxide-enriched gas outlet are connected by a carbon dioxide-enriched gas delivery line, and the second carbon dioxide-enriched gas outlet is connected to the carbon dioxide-enriched gas delivery line.
6. The arrangement according to any of the claims 1 to 5, 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.
7. The apparatus according to claim 6, characterized in that the apparatus further comprises a first gas treatment unit (50), the first gas treatment unit (50) being arranged on a conduit of the first compression unit (40) connected to the blast furnace gas inlet for removing solid and liquid impurities from the compressed blast furnace gas.
8. The apparatus according to claim 7, wherein the first gas treatment unit (50) comprises a first cooler, a first demister and a first filter arranged in series in this order.
9. The apparatus of claim 5, further comprising a second compression unit (60), the second compression unit (60) being disposed on the carbon dioxide enriched gas delivery line for compressing the carbon dioxide enriched gas discharged from the first carbon dioxide enriched gas outlet.
10. The arrangement according to claim 9, wherein the second carbon dioxide-rich gas outlet is connected to the carbon dioxide-rich gas delivery line upstream of the second compression unit (60).
11. The apparatus of claim 9, further comprising a second gas treatment unit (70), the second gas treatment unit (70) being arranged on the carbon dioxide enriched gas transfer line between the second compression unit (60) and the first carbon dioxide enriched gas inlet for removing moisture from the compressed carbon dioxide enriched gas.
12. The apparatus according to claim 11, wherein the second gas treatment unit (70) comprises a second cooler, a second demister and a second filter arranged in series in this order, or wherein the second gas treatment unit (70) is a dehydration device.
13. The apparatus according to any one of claims 1 to 5, further comprising a pressure energy recovery unit (80), the pressure energy recovery unit (80) being connected to the carbon dioxide stripping gas outlet for recovering pressure energy of the gas discharged from the carbon dioxide stripping gas outlet.
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