CN210134072U

CN210134072U - Comprehensive treatment device for blast furnace gas

Info

Publication number: CN210134072U
Application number: CN201920906442.0U
Authority: CN
Inventors: 林千果
Original assignee: Individual
Current assignee: Individual
Priority date: 2019-06-14
Filing date: 2019-06-14
Publication date: 2020-03-10
Anticipated expiration: 2029-06-14

Abstract

The utility model provides a comprehensive treatment device for blast furnace gas. The apparatus comprises CO₂Membrane separation unit, carbonyl sulfide pressure swing adsorption separation unit and cryogenic rectification unit, CO₂The membrane separation unit is provided with a blast furnace gas inlet, a carbon dioxide enriched gas outlet and a non-permeation gas outlet(ii) a The carbonyl sulfide pressure swing adsorption separation unit is provided with a non-permeable gas inlet, a carbonyl sulfide enriched gas outlet and a first desorption gas outlet, the non-permeable gas inlet is connected with the non-permeable gas outlet, and the carbonyl sulfide pressure swing adsorption separation unit is used for carrying out pressure swing adsorption separation on carbonyl sulfide in non-permeable gas; the cryogenic rectification unit is provided with a carbon dioxide enriched gas inlet, a carbon dioxide product gas outlet, a carbonyl sulfide product gas outlet and a second desorption gas outlet, and the carbon dioxide enriched gas inlet is respectively connected with the carbon dioxide enriched gas outlet and the carbonyl sulfide enriched gas outlet. The utility model can effectively remove carbonyl sulfide in the gas, improve the enrichment degree of carbon dioxide and improve the combustion heat value of the blast furnace gas.

Description

Comprehensive treatment device for blast furnace gas

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 is mainly a membrane separation method at present, but the separation effect of the current membrane separation method is limited.

The above reasons cause the following defects in the current blast furnace gas treatment process: (1) carbonyl sulfide cannot be effectively removed; (2) the enrichment degree of carbon dioxide is low; (3) 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 discloses a main aim at provides a blast furnace gas's integrated processing device to the following problem that exists when handling blast furnace gas among the solution prior art: (1) carbonyl sulfide cannot be effectively removed; (2) the enrichment degree of carbon dioxide is low; (3) 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.

In order to achieve the above object, according to the present inventionIn one aspect, an integrated processing plant for blast furnace gas is provided, comprising: CO2₂The membrane separation unit is provided with a blast furnace gas inlet, a carbon dioxide enriched gas outlet and a non-permeation gas outlet; the carbonyl sulfide pressure swing adsorption separation unit is provided with a non-permeable gas inlet, a carbonyl sulfide enriched gas outlet and a first desorption gas outlet, the non-permeable gas inlet is connected with the non-permeable gas outlet, and the carbonyl sulfide pressure swing adsorption separation unit is used for carrying out pressure swing adsorption separation on carbonyl sulfide in non-permeable gas discharged from the non-permeable gas outlet; and the cryogenic rectification unit is provided with a carbon dioxide enriched gas inlet, a carbon dioxide product gas outlet, a carbonyl sulfide product gas outlet and a second desorption gas outlet, and the carbon dioxide enriched gas inlet is respectively connected with the carbon dioxide enriched gas outlet and the carbonyl sulfide enriched gas outlet.

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 gas treatment unit which is arranged on a pipeline connected with the first compression unit and the blast furnace gas inlet and is used for removing solid impurities and liquid impurities in the compressed blast furnace gas.

Further, the gas treatment unit comprises a filter, a cooler and a demister which are sequentially arranged in series.

Furthermore, the carbon dioxide enriched gas inlet is connected with the carbon dioxide enriched gas outlet through a carbon dioxide enriched gas conveying pipeline, and the carbonyl sulfide enriched gas outlet is connected with the carbon dioxide enriched gas conveying pipeline.

Further, the device also comprises a second compression unit which is arranged on the carbon dioxide enriched gas conveying pipeline, and the connection position of the carbonyl sulfide enriched gas outlet and the carbon dioxide enriched gas conveying pipeline is positioned at the upstream of the second compression unit.

Further, the device also comprises a pressure energy recovery unit, and the pressure energy recovery unit is connected with the first desorption gas outlet.

Further, the pressure energy recovery unit is connected with the first degassing outlet through a degassing conveying main pipe, and the second degassing outlet is connected with the degassing conveying main pipe through a degassing conveying branch pipe.

Further, the device also comprises a regulating unit which is arranged on the degassing conveying branch pipe and is used for regulating the pressure of the gas discharged from the second degassing outlet so as to reduce the pressure difference between the gas discharged from the first degassing outlet and the gas discharged from the second degassing outlet.

The utility model provides a comprehensive treatment device for blast furnace gas, which comprises CO₂Membrane separation unit, carbonyl sulfide pressure swing adsorption separation unit and cryogenic rectification unit, CO₂The membrane separation unit is provided with a blast furnace gas inlet, a carbon dioxide enriched gas outlet and a non-permeation gas outlet; the carbonyl sulfide pressure swing adsorption separation unit is provided with a non-permeable gas inlet, a carbonyl sulfide enriched gas outlet and a first desorption gas outlet, the non-permeable gas inlet is connected with the non-permeable gas outlet, and the carbonyl sulfide pressure swing adsorption separation unit is used for carrying out pressure swing adsorption separation on carbonyl sulfide in non-permeable gas discharged from the non-permeable gas outlet; the cryogenic rectification unit is provided with a carbon dioxide enriched gas inlet, a carbon dioxide product gas outlet, a carbonyl sulfide product gas outlet and a second desorption gas outlet, and the carbon dioxide enriched gas inlet is respectively connected with the carbon dioxide enriched gas outlet and the carbonyl sulfide enriched gas outlet.

Utilize the device provided by the utility model to handle blast furnace gas, carbonyl sulfur in the desorption coal gas more effectively to improve carbon dioxide's enrichment degree, also corresponding 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、CO₂a membrane separation unit; 20A carbonyl sulfide pressure swing adsorption separation unit; 30. a cryogenic rectification unit; 40. a first compression unit; 50. a gas processing unit; 60. a second compression unit; 70. a pressure energy recovery unit; 80. an adjustment 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, the following problems exist in the prior art when treating blast furnace gas: (1) carbonyl sulfide cannot be effectively removed; (2) the enrichment degree of carbon dioxide is low; (3) 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.

In order to solve the above problems, the present invention provides a comprehensive treatment device for blast furnace gas, as shown in fig. 1, which comprises CO₂ Membrane separation unit 10, carbonyl sulfide pressure swing adsorption separation unit 20 and cryogenic rectification unit 30, CO₂The membrane separation unit 10 is provided with a blast furnace gas inlet, a carbon dioxide enriched gas outlet and a non-permeate gas outlet; the carbonyl sulfide pressure swing adsorption separation unit 20 is provided with a non-permeable gas inlet, a carbonyl sulfide enriched gas outlet and a first desorption gas outlet, the non-permeable gas inlet is connected with the non-permeable gas outlet, and the carbonyl sulfide pressure swing adsorption separation unit 20 is used for carrying out pressure swing adsorption separation on carbonyl sulfide in non-permeable gas discharged from the non-permeable gas outlet; the cryogenic rectification unit 30 is provided with a carbon dioxide enriched gas inlet, a carbon dioxide product gas outlet, a carbonyl sulfide product gas outlet and a second stripping gas outlet, wherein the carbon dioxide enriched gas inlet is connected with the carbon dioxide enriched gas outlet and the carbonyl sulfide enriched gas outlet respectively.

Different from the traditional membrane separation method, the utility model adopts a device combining membrane separation, pressure swing adsorption separation and cryogenic rectification to treat blast furnace gas. Specifically, the method comprises the following steps:

by using CO₂The membrane separation unit 10 may first subject the blast furnace gas to CO₂The membrane separation treatment utilizes CO due to the large amount of flue gas required for carbon capture₂The membrane separation unit 10 advantageously reduces the footprint and simplifies the process. In CO₂Most of the CO in the flue gas is treated by the membrane separation unit 10₂And part of COS, H₂Forming carbon dioxide enriched gas through the separation membrane, discharging the carbon dioxide enriched gas from the carbon dioxide enriched gas outlet, wherein CO and N are₂The remainder of H₂A small amount of CO₂And COS form the non-permeating gas to be discharged.

The carbonyl sulfide in the non-permeable gas can be removed by performing pressure swing adsorption separation on the carbonyl sulfide in the carbonyl sulfide pressure swing adsorption separation unit 20. It should be noted that most of CO is used₂By CO₂CO of the first high pressure non-permeate gas, which has been separated after treatment in the membrane separation unit 10₂The concentration is remarkably reduced, which can effectively prevent high concentration CO₂The influence on the carbonyl sulfide pressure swing adsorption process enables carbonyl sulfide to be removed more fully. At the same time, due to H₂Is difficult to be adsorbed in the carbonyl sulfide pressure swing adsorption separation unit 20, so that CO is difficult to be adsorbed₂And H₂More sufficient separation is possible. In addition, lower concentrations of CO in the non-permeate gas₂Can also be adsorbed and separated together with carbonyl sulfide. In conclusion, after the processing of the carbonyl sulfide pressure swing adsorption separation unit 20, the carbonyl sulfide and the carbon dioxide in the non-permeable gas are sufficiently removed, and the first degassing gas contains higher concentrations of CO and N₂And H₂And has higher combustion heat value.

The carbon dioxide enriched gas is then processed by cryogenic rectification unit 30 to effectively separate carbon dioxide and carbonyl sulfide therein to form a carbon dioxide product gas, a carbonyl sulfide product gas, and a second degassing gas. The second degassing gas contains CO and N with higher concentration₂And H₂And the second degassing gas and the first degassing gas are used together as a product gas A with higher combustion heat value.

The reason is that the device of the utility model can more sufficiently separate and enrichCarbonyl sulfide and carbon dioxide in blast furnace gas, and corresponding reaction of H₂CO, these high calorific value gases and N₂Enriching to form product gas A with high combustion heat value. Besides the beneficial effects, the removal of the carbon dioxide is also beneficial to reducing the carbon emission, and the pressure swing adsorption separation and the low-temperature rectification are adopted, so that the carbon dioxide and carbonyl sulfide in the blast furnace gas can be more fully separated, and the carbon dioxide and the hydrogen can be fully separated, so that the CO can be fully separated₂The membrane separation unit 10 is not particularly limited to a membrane material. Meanwhile, the non-permeable gas has higher pressure, and the pressure can be directly utilized in the carbonyl sulfide pressure swing adsorption separation process, thereby reducing the energy consumption to a certain extent.

In a preferred embodiment, the cos PSA separation unit 20 comprises a cos PSA unit for pressure swing adsorption of cos and carbon dioxide and a cos desorption unit for desorption of 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 10 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, the first compression unit 40 being arranged on the gas inlet line where the blast furnace gas inlet is located for compressing the blast furnace gas. CO can be produced by means of 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).

Blast furnace gas contains CO and H₂、CO₂COS and N₂In addition, some solid impurities (particles) andliquid impurities (moisture) to reduce CO by these solid and liquid impurities₂The influence of the polymer separation membrane in the membrane separation unit 10, in a preferred embodiment, the apparatus further comprises a gas treatment unit 50, wherein the 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 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 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 gas treatment unit 50 includes a cooler, a demister, and a filter arranged in series in this order. The liquid in the blast furnace gas can be further condensed by using a cooler, then the condensable liquid foam, fog drops and possibly entrained solid particles in the blast furnace gas are removed by a demister, and finally harmful impurities such as possibly entrained fine liquid in the gas can be further removed by using a filter. Meanwhile, the arrangement of the cooler is also beneficial to controlling the temperature of the coal gas so as to further improve CO₂Operational stability of the membrane separation unit 10.

In a preferred embodiment, the carbon dioxide-rich gas inlet is connected to the carbon dioxide-rich gas outlet via a carbon dioxide-rich gas delivery line, and the cos-rich gas outlet is connected to the carbon dioxide-rich gas delivery line. Thus, the carbonyl sulfide-enriched gas (containing a part of CO) obtained by the carbonyl sulfide pressure swing adsorption separation unit 20 can be treated₂) The low-temperature rectification is carried out together with the carbon dioxide enriched gas, thereby further improving the separation and enrichment effects of the gas.

In a preferred embodiment, the apparatus further comprises a second compression unit 60, the second compression unit 60 being disposed on the carbon dioxide enriched gas delivery line and the connection of the cos enriched gas outlet to the carbon dioxide enriched gas delivery line being upstream of the second compression unit 60 for compressing the carbon dioxide enriched gas exiting the first carbon dioxide enriched gas outlet.

After the carbonyl sulfide pressure swing adsorption separation treatment, the first stripping gas has certain pressure energy, in order to recover the pressure energy and save energy consumption, in a preferred embodiment, the device further comprises a pressure energy recovery unit 70, and the pressure energy recovery unit 70 is connected with the first stripping gas outlet. In practice, the pressure energy recovery unit 70 may be implemented by an existing TRT energy recovery system of a steel plant or an expansion work principle-based device.

In order to further recover the pressure energy in the second stripping gas discharged from the second stripping gas outlet, in a preferred embodiment, the pressure energy recovery unit 70 is connected to the first stripping gas outlet via a stripping gas main conveyor pipe, and the second stripping gas outlet is connected to the stripping gas main conveyor pipe via a stripping gas branch conveyor pipe. Preferably, the apparatus further comprises a regulating unit 80, the regulating unit 80 being arranged in the stripping gas delivery manifold for regulating the pressure of the gas exiting the second stripping gas outlet in order to reduce the pressure difference between it and the gas exiting the first stripping gas outlet. This facilitates mixing of gases at different pressures.

According to another aspect of the present invention, there is provided a method for comprehensive treatment of blast furnace gas, comprising the steps of: subjecting blast furnace gas to CO₂Membrane separation treatment to obtain carbon dioxide enriched gas and non-permeate gas; carrying out carbonyl sulfide pressure swing adsorption separation on the non-permeate gas to obtain carbonyl sulfide enriched gas and first degassing gas; and (3) carrying out low-temperature rectification on the mixed gas of the carbon dioxide enriched gas and the carbonyl sulfide enriched gas to obtain a carbon dioxide product gas, a carbonyl sulfide product gas and a second degassing gas.

The method of the utility model can more fully separate and enrich carbonyl sulfide and carbon dioxide in blast furnace gas, and correspondingly make H₂CO, these high calorific value gases and N₂Enriching to form product gas A with high combustion heat value. Besides the beneficial effects, the removal of the carbon dioxide is also beneficial to reducing the carbon emission, and the pressure swing adsorption separation and the low-temperature rectification are adopted, so that the carbon dioxide and carbonyl sulfide in the blast furnace gas can be more fully separated, and the carbon dioxide and the hydrogen can be fully separatedIs separated so as to be specific to CO₂The membrane separation process is not particularly limited by the membrane material. Meanwhile, the non-permeable gas has higher pressure, and the pressure can be directly utilized in the carbonyl sulfide pressure swing adsorption separation process, thereby reducing the energy consumption to a certain extent.

In order to further enhance the effectiveness of the pressure swing adsorption separation of carbonyl sulfide, in a preferred embodiment, the process conditions employed in the step of performing the pressure swing adsorption separation of carbonyl sulfide are as follows: the treatment temperature is absolute pressure, the treatment pressure is 0.10-1.50 MPa (absolute pressure), and the adsorbent is one or more of molecular sieve, silica gel, activated carbon and modified adsorbent thereof. Preferably, the step of pressure swing adsorption separation of carbonyl sulfide comprises: carrying out carbonyl sulfide pressure swing adsorption on the non-permeable gas by using the adsorbent under the process condition to obtain carbonyl sulfide removal gas and the adsorbent adsorbed with carbonyl sulfide; and desorbing the adsorbent adsorbed with the carbonyl sulfide in a vacuumized state to obtain carbonyl sulfide enriched gas, wherein the carbonyl sulfide enriched gas contains carbon dioxide with higher concentration because low-concentration carbon dioxide can also be adsorbed along with the carbonyl sulfide.

In order to more fully separate CO in carbon dioxide enriched gas₂COS, in a preferred embodiment, the process conditions employed in the cryogenic rectification step described above are as follows: the treatment temperature is-70 to 0 ℃, and the treatment pressure is 1.5 to 10.0MPa (A).

In a preferred embodiment, the CO 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 greater than 0.10mpa (a). May be CO₂CO treated by membrane separation₂Osmosis further provides pressure drive. More preferably, the method further comprises the step of subjecting the mixed gas to a second compression before the step of performing cryogenic rectification; preferably, in the second compression step, the gas pressure is greater than 1.50mpa (a).

In a preferred embodiment, 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 sequentially filtering, cooling and demisting the compressed blast furnace gas. 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.

After the pressure swing adsorption separation treatment of carbonyl sulfide, the first degassing gas has certain pressure energy, and in order to recover the pressure energy and save energy consumption, 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. In practical application, the pressure energy in the first 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. Preferably, the second stripping gas is subjected to pressure energy recovery together with the first stripping gas.

In a preferred embodiment, the method further comprises the step of adjusting the pressure of the second degassing gas, preferably to reduce the pressure difference between the second degassing gas and the first degassing gas, before the step of subjecting the second degassing gas to pressure energy recovery together with the first degassing gas, which facilitates the mixing between the gases.

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 capture of COS, and the treatment effect of other gases such as hydrogen.

Wherein, the carbon dioxide membrane separation units all adopt polymer separation membranes. The polymer is Polyimide (PI); in the step of carbonyl sulfide pressure swing adsorption separation, the process conditions are as follows: the treatment temperature is 80 ℃, the adsorption pressure is 0.50MPa (A), and the adsorbent is silica gel; the process conditions for cryogenic rectification were as follows: the treatment temperature is-20 ℃, and the treatment pressure is 3.0MPa (A).

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 10000Nm³H, CO2 content 25.70%, CO content 21.86%, H₂The content of COS is 2.96 percent and the content of COS is 50mg/Nm³The cryogenic rectification of CO obtained in the process of this example₂At a flow rate of 102Nm³/h，CO₂The content was 99.5%. The CO concentration is increased from 21.86% to 26.95% after pressure swing adsorption and 35% after low-temperature rectification, the hydrogen concentration is increased from 2.96% to 15% after low-temperature rectification, and the COS concentration is increased from 50mg/Nm³³Reduced to 5mg/nm after pressure swing adsorption³And 5mg/Nm after cryogenic rectification³Realizes 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

1. An integrated processing apparatus for blast furnace gas, comprising:

CO₂a membrane separation unit (10) provided with a blast furnace gas inlet, a carbon dioxide enriched gas outlet and a non-permeable membraneA venting outlet;

the carbonyl sulfide pressure swing adsorption separation unit (20) is provided with a non-permeable gas inlet, a carbonyl sulfide enriched gas outlet and a first desorption gas outlet, the non-permeable gas inlet is connected with the non-permeable gas outlet, and the carbonyl sulfide pressure swing adsorption separation unit (20) is used for carrying out pressure swing adsorption separation on carbonyl sulfide in non-permeable gas discharged from the non-permeable gas outlet; and

the cryogenic rectification unit (30) is provided with a carbon dioxide enriched gas inlet, a carbon dioxide product gas outlet, a carbonyl sulfide product gas outlet and a second desorption gas outlet, wherein the carbon dioxide enriched gas inlet is respectively connected with the carbon dioxide enriched gas outlet and the carbonyl sulfide enriched gas outlet.

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 arrangement according to claim 2, characterized by further comprising a gas treatment unit (50), the gas treatment unit (50) being arranged on the line 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.

4. The apparatus according to claim 3, wherein the gas treatment unit (50) comprises a filter, a cooler and a demister arranged in series in the sequence.

5. The apparatus of any one of claims 1 to 4, wherein the carbon dioxide-rich gas inlet is connected to the carbon dioxide-rich gas outlet by a carbon dioxide-rich gas delivery line, and the cos-rich gas outlet is connected to the carbon dioxide-rich gas delivery line.

6. The apparatus according to claim 5, further comprising a second compression unit (60), the second compression unit (60) being disposed on the carbon dioxide enriched gas delivery line, and the connection of the cos enriched gas outlet to the carbon dioxide enriched gas delivery line being upstream of the second compression unit (60).

7. The apparatus according to any one of claims 1 to 4, further comprising a pressure energy recovery unit (70), the pressure energy recovery unit (70) being connected to the first stripping gas outlet.

8. The apparatus according to claim 7, wherein the pressure energy recovery unit (70) is connected to the first stripping gas outlet via a stripping gas transfer main and the second stripping gas outlet is connected to the stripping gas transfer main via a stripping gas transfer branch.

9. An apparatus according to claim 8, further comprising a regulating unit (80), said regulating unit (80) being arranged in said degassing gas transfer branch for regulating the pressure of the gas exiting said second degassing gas outlet in order to reduce the pressure difference between it and the gas exiting said first degassing gas outlet.