Highly integrated membrane tower coupling decarburization system

Abstract

The invention discloses a highly integrated membrane tower coupling decarburization system which comprises a cold box, a low-temperature separator, a throttle valve, a rectifying tower, a condenser, a condensing tank, a reboiler, a subcooler, a membrane inlet compressor, a gas membrane and a permeate gas compressor, and the condenser and the reboiler are respectively integrated at the tower top and the tower bottom of the rectifying tower. The energy-saving and efficient membrane tower coupling decarburization system is formed by coupling the membrane decarburization process and the rectification decarburization process, carbon dioxide and hydrocarbons in natural gas rich in carbon dioxide can be effectively separated, and high purification of carbon dioxide and purification of natural gas are achieved. Meanwhile, the highly integrated scheme greatly reduces the occupied space of the equipment, obviously reduces the energy consumption and the cost, improves the economical efficiency of the system, and has wide application prospects and obvious market competitiveness.

Description

Technical Field

[0001] This invention belongs to the field of oil and gas gathering and transportation and new energy technology, and more specifically, it relates to a highly integrated membrane tower coupled decarbonization system. Background Technology

[0002] As global efforts to exploit oil and gas resources continue to intensify, more and more natural gas is being found to contain high concentrations of carbon dioxide during the extraction process. This high carbon dioxide content in natural gas not only poses a severe challenge to natural gas gathering and transportation processes and pipeline corrosion prevention, but also, due to its complex composition, makes it difficult to utilize effectively and directly, greatly limiting the efficient development and utilization of natural gas resources.

[0003] To achieve efficient utilization of natural gas resources while addressing carbon dioxide emissions, various natural gas decarbonization technologies have been adopted in the industry. These technologies mainly include multi-tower distillation, membrane decarbonization, and amine decarbonization. While multi-tower distillation can achieve high carbon dioxide removal efficiency, it consumes a lot of energy and requires complex tower equipment and extensive cooling systems, resulting in large footprints and high costs. Membrane decarbonization offers some operational flexibility, but its membrane materials are expensive, and their performance gradually degrades under high carbon dioxide concentrations, requiring frequent replacements and increasing operating costs. Amine decarbonization technology suffers from high energy consumption during amine regeneration and the volatile and degradable nature of amines, further increasing system operating costs and maintenance complexity.

[0004] In confined spaces such as offshore oil and gas fields, the limitations of the aforementioned decarbonization technologies are even more pronounced. Offshore platforms have limited space, imposing strict restrictions on the footprint and weight of equipment, requirements that existing decarbonization technologies often struggle to meet. Therefore, current natural gas decarbonization technologies face pressing issues regarding energy consumption, cost, and equipment footprint, particularly in confined spaces like offshore environments, where the challenges are even greater. Summary of the Invention

[0005] This invention aims to address at least one of the technical problems existing in the prior art. To this end, this invention provides a highly integrated membrane tower coupled decarbonization system, designed to solve the problems of high energy consumption, high cost, and large equipment footprint of conventional decarbonization devices in related technologies.

[0006] To achieve the above objectives, the present invention adopts the following technical solution: a highly integrated membrane tower coupled decarbonization system, comprising a cold box, a cryogenic separator, a throttling valve, a distillation column, a condenser, a condenser tank, a reboiler, a subcooler, a membrane inlet compressor, a gas membrane, and a permeate compressor, wherein the condenser and reboiler are respectively integrated at the top and bottom of the distillation column; the cold box is connected to the feed gas inlet pipeline, and the carbon dioxide-containing feed gas from upstream enters the reboiler via the first pipeline after heat exchange in the cold box, serving as the heat source for the distillation column, and then returns to the cold box via the second pipeline for further heat exchange, and then enters the cryogenic separator via the third pipeline for gas-liquid separation; the gas phase of the cryogenic separator enters the cold box via the fourth pipeline for heat exchange, and then enters the gas membrane via the fifth pipeline; the liquid phase of the cryogenic separator is sent to the throttling valve via the sixth pipeline for further throttling and cooling, and then enters the distillation column via the seventh pipeline; the distillation column performs natural gas decarbonization and carbon dioxide purification on the incoming stream, and the distilled stream is low in carbon dioxide content. After being cooled by the condenser, the carbon dioxide gas is sent to the condenser tank via the eighth pipeline for gas-liquid separation. The gas phase from the condenser enters the subcooler via the ninth pipeline for heat exchange with the hot end stream, then enters the cold box via the tenth pipeline for heat exchange, then enters the membrane inlet compressor via the eleventh pipeline for pressurization, and then enters the gas membrane via the twelfth pipeline. The liquid phase from the condenser is returned to the distillation column via the thirteenth pipeline for further carbon dioxide purification. The high-concentration liquid carbon dioxide after distillation is sent to the subcooler via the fourteenth pipeline for heat exchange with the cold end stream, and then supplied to downstream users as a liquid carbon dioxide product via the fifteenth pipeline. The high-carbon dioxide gas from the permeate side of the gas membrane outlet enters the permeate compressor via the sixteenth pipeline for pressurization, then enters the cold box via the seventeenth pipeline for heat exchange, and then enters the distillation column via the eighteenth pipeline for natural gas decarbonization and carbon dioxide purification. The low-carbon dioxide gas from the residual permeate side of the gas membrane outlet is supplied to downstream users as a low-carbon dioxide natural gas product via the nineteenth pipeline.

[0007] Preferably, the cold box is connected to the first temperature refrigerant from the refrigeration system via the twentieth pipeline, and then connected to the first temperature refrigerant returning to the refrigeration system after heat exchange via the twenty-first pipeline.

[0008] Preferably, the cold box is connected to the second-temperature refrigerant from the refrigeration system via the twenty-second pipeline, and then connected to the second-temperature refrigerant returning to the refrigeration system after heat exchange via the twenty-third pipeline.

[0009] Preferably, the condenser is connected to the refrigerant at the third temperature position from the refrigeration system via the twenty-fourth pipeline, and then connected to the refrigerant at the third temperature position that returns to the refrigeration system after heat exchange via the twenty-fifth pipeline.

[0010] Preferably, a bypass branch is provided on the membrane inlet compressor, a first valve is provided on the bypass branch, a second valve is provided on the eleventh pipeline located inside the bypass branch, a third valve is provided on the twelfth pipeline located inside the bypass branch, and a pressure gauge is provided on the nineteenth pipeline, the pressure gauge being signal-connected to the first valve, the second valve and the third valve. When the gas pressure in the eleventh pipeline meets the pressure required by the downstream user of the nineteenth pipeline, the first valve is opened and the second and third valves are closed, bypassing the membrane inlet compressor without pressurization; when the gas pressure in the eleventh pipeline is lower than the pressure required by the downstream user of the nineteenth pipeline, the first valve is closed and the second and third valves are opened, using the membrane inlet compressor for pressurization.

[0011] Preferably, a first component monitor for monitoring the carbon dioxide concentration in the product natural gas is installed on the nineteenth pipeline, and the first component monitor is connected to the gas membrane signal. When the first component monitor detects that the carbon dioxide concentration in the product natural gas exceeds a set value, the first component monitor controls the gas membrane to open more membrane modules to enhance the separation effect.

[0012] Preferably, a second component monitor for monitoring the carbon dioxide concentration in the distillation column stream is installed on the fourteenth pipeline, and a regulating valve is installed on the twenty-fourth pipeline. The second component monitor is connected to the regulating valve. When the second component monitor detects that the carbon dioxide concentration in the liquid carbon dioxide product is lower than the set value, the second component monitor controls the regulating valve to increase the opening degree to enhance the carbon dioxide purification effect in the distillation column.

[0013] The present invention has the following advantages due to the adoption of the above technical solutions: 1. This invention achieves the dual objectives of carbon dioxide purification from high-carbon dioxide-content natural gas and recovery of natural gas hydrocarbon resources, significantly improving the efficient recovery and utilization rate of natural gas resources and the purification and resupply capacity of carbon dioxide resources, fully realizing the potential value of natural gas resources, and providing strong support for the sustainable use of energy.

[0014] 2. Compared with traditional single decarbonization methods, this invention exhibits significant advantages in several aspects: compared with multi-tower decarbonization processes, it significantly reduces the floor space required; compared with membrane decarbonization, it effectively reduces investment costs and hydrocarbon loss; and compared with amine decarbonization, it significantly reduces operating energy consumption. Through these optimizations, this invention achieves energy saving, cost reduction, and efficiency improvement in the decarbonization system, bringing greater economic benefits to users.

[0015] 3. This invention features a highly integrated system design. For example, the cooler is integrated into the top of the tower, the reboiler into the bottom of the tower, and the heat exchange process is integrated into a cold box. This integrated design significantly reduces the number of traditional equipment and the weight of system modules, making subsequent equipment hoisting and installation more convenient, thereby effectively reducing installation costs and improving the overall performance and reliability of the system.

[0016] 4. This invention optimizes system energy consumption by optimizing the heat exchange network. The use of a cold box significantly reduces the number of heat exchangers, fully utilizing the cooling capacity of the refrigerant and the heat of the natural gas to achieve thermal balance. Throughout the system operation, no external heat source (such as electric heating or hot oil heating) is required, thus minimizing system energy consumption, further improving the system's energy-saving effect, and reducing operating costs.

[0017] 5. The coupling process of this invention is not a simple upstream and downstream splicing (such as membrane + tower, tower + membrane), but rather, through ingenious coupling design, it minimizes system energy consumption and reduces the number of decarbonization membranes required. This coupling process not only improves decarbonization efficiency but also achieves the goal of cost reduction and energy saving, providing users with a more economical and efficient decarbonization solution.

[0018] In summary, the highly integrated membrane tower coupled decarbonization system provided by this invention can effectively separate carbon dioxide and hydrocarbons from carbon dioxide-rich natural gas, achieving efficient and energy-saving carbon dioxide purification and product gas purification functions. Simultaneously, the highly integrated solution significantly reduces the equipment's footprint, substantially lowers energy consumption and costs, and enhances the system's economics, demonstrating broad application prospects and significant market competitiveness. Attached Figure Description

[0019] Various other advantages and benefits will become apparent to those skilled in the art upon reading the following detailed description of preferred embodiments. The accompanying drawings are for illustrative purposes only and are not intended to limit the invention. Throughout the drawings, the same reference numerals denote the same parts. In the drawings: Figure 1 This is a schematic diagram of a highly integrated membrane tower coupled decarbonization system provided in an embodiment of the present invention. Detailed Implementation

[0020] To make the objectives, technical solutions, and advantages of the present invention clearer, specific embodiments of the present invention will be further described below with reference to the accompanying drawings. Although exemplary embodiments of the present invention are shown in the drawings, it should be understood that the present invention can be implemented in various forms and should not be limited to the embodiments set forth herein. Rather, these embodiments are provided to enable a more thorough understanding of the present invention and to fully convey the scope of the present invention to those skilled in the art.

[0021] In the description of this invention, it should be understood that the terms "center," "longitudinal," "lateral," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," "axial," "radial," and "circumferential" indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are used only for the convenience of describing this invention and simplifying the description, and are not intended to indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this invention.

[0022] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of this invention, "a plurality of" means two or more, unless otherwise explicitly specified.

[0023] In this invention, unless otherwise explicitly specified and limited, the terms "installation," "connection," "linking," and "fixing," etc., should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral part; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components. Those skilled in the art can understand the specific meaning of the above terms in this invention according to the specific circumstances.

[0024] In this invention, unless otherwise explicitly specified and limited, "above" or "below" the second feature can mean that the first feature is in direct contact with the second feature, or that the first feature is in indirect contact with the second feature through an intermediate medium. Furthermore, "above," "over," and "on top" of the second feature can mean that the first feature is directly above or diagonally above the second feature, or simply that the first feature is at a higher horizontal level than the second feature. "Below," "below," and "under" the second feature can mean that the first feature is directly below or diagonally below the second feature, or simply that the first feature is at a lower horizontal level than the second feature.

[0025] In the description of this specification, the references to terms such as "one embodiment," "some embodiments," "example," "specific example," or "some examples," etc., refer to specific features, structures, materials, or characteristics described in connection with that embodiment or example, which are included in at least one embodiment or example of the present invention. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments or examples. Moreover, without contradiction, those skilled in the art can combine and integrate the different embodiments or examples described in this specification, as well as the features of different embodiments or examples.

[0026] This invention provides a highly integrated membrane-coupling decarbonization system, comprising a cold box, a cryogenic separator, a throttling valve, a distillation column, a condenser, a condenser tank, a reboiler, a subcooler, a membrane inlet compressor, a gas membrane, and a permeate compressor. The condenser and reboiler are integrated at the top and bottom of the distillation column, respectively. This invention couples membrane decarbonization with distillation decarbonization processes to form an energy-efficient membrane-coupling decarbonization system capable of effectively separating carbon dioxide and hydrocarbons from carbon dioxide-rich natural gas, achieving high purification of carbon dioxide and purification of natural gas. Simultaneously, the highly integrated design significantly reduces the equipment's footprint, substantially lowers energy consumption and costs, and improves the system's economics, demonstrating broad application prospects and significant market competitiveness.

[0027] The highly integrated membrane tower coupled decarbonization system provided by the embodiments of the present invention will now be described in detail with reference to the accompanying drawings.

[0028] Please see Figure 1 This embodiment provides a highly integrated membrane tower coupled decarbonization system, including a cold box 111, a low-temperature separator 112, a throttling valve 113, a distillation column 114, a condenser 115, a condenser tank 116, a reboiler 117, a subcooler 118, a membrane inlet compressor 119, a gas membrane 122, and a permeate compressor 121, wherein the condenser 115 and the reboiler 117 are respectively integrated at the top and bottom of the distillation column 114.

[0029] The cold box 111 is connected to the raw gas inlet pipeline 11. The carbon dioxide-containing raw gas from the upstream enters the reboiler 117 via the first pipeline 12 after heat exchange in the cold box 111, serving as the heat source for the distillation column 114. Then, it returns to the cold box 111 via the second pipeline 13 for further heat exchange, and then enters the low-temperature separator 112 via the third pipeline 14 for gas-liquid separation.

[0030] The gas phase of the cryogenic separator 112 enters the cold box 111 for heat exchange via the fourth pipeline 28, and then enters the gas membrane 122 via the fifth pipeline 35; the liquid phase of the cryogenic separator 112 is sent to the throttling valve 113 via the sixth pipeline 15 for further throttling and cooling, and then enters the distillation column 114 via the seventh pipeline 16.

[0031] The natural gas undergoes decarbonization and carbon dioxide purification in the distillation column 114. The low-carbon dioxide gas after distillation is cooled by condenser 115 and then sent to condenser 116 via pipeline 17 for gas-liquid separation. The gas phase from condenser 116 enters subcooler 118 via pipeline 18 for heat exchange with the hot-end stream, then is sent to cold box 111 via pipeline 10 for heat exchange, then to membrane inlet compressor 119 via pipeline 111 for pressurization, and finally enters gas membrane 122 via pipeline 123. The liquid phase from condenser 116 is returned to distillation column 114 via pipeline 13 for further carbon dioxide purification. The high-concentration liquid carbon dioxide after distillation is sent to subcooler 118 via pipeline 140 for heat exchange with the cold-end stream, and then supplied to downstream users as liquid carbon dioxide product via pipeline 15.

[0032] High-carbon dioxide gas from the permeate side of the gas membrane 122 outlet enters the permeate compressor 121 via the sixteenth pipeline 25 for pressurization, then enters the cold box 111 via the seventeenth pipeline 26 for heat exchange, and then is sent to the distillation column 114 via the eighteenth pipeline 27 for natural gas decarbonization and carbon dioxide purification. Low-carbon dioxide gas from the residual permeate side of the gas membrane 122 outlet is supplied to downstream users as a low-carbon dioxide natural gas product via the nineteenth pipeline 24.

[0033] In the above embodiments, preferably, the cold box 111 is connected to the first temperature refrigerant from the refrigeration system via the twentieth pipeline 29, and then connected to the first temperature refrigerant returning to the refrigeration system after heat exchange via the twenty-first pipeline 30.

[0034] In the above embodiments, preferably, the cold box 111 is connected to the second-temperature refrigerant from the refrigeration system via the twenty-second pipeline 31, and then connected to the second-temperature refrigerant returning to the refrigeration system after heat exchange via the twenty-third pipeline 32.

[0035] In the above embodiments, preferably, the condenser 115 is connected to the refrigerant at the third temperature position from the refrigeration system via the twenty-fourth pipeline 33, and then connected to the refrigerant at the third temperature position that returns to the refrigeration system after heat exchange via the twenty-fifth pipeline 34.

[0036] In the above embodiments, preferably, a bypass branch is provided on the membrane inlet compressor 119, a first valve 120 is provided on the bypass branch, a second valve 130 is provided on the eleventh pipeline 22 located inside the bypass branch, a third valve 140 is provided on the twelfth pipeline 23 located inside the bypass branch, and a pressure gauge 124 is provided on the nineteenth pipeline 24. The pressure gauge is connected to the first valve 120, the second valve 130 and the third valve 140. When the gas pressure in the eleventh pipeline 22 meets the pressure required by the downstream user of the nineteenth pipeline 24 (not lower than the set value of pressure gauge 124), the first valve 120 is opened, the second valve 130 and the third valve 140 are closed, and the bypass membrane inlet compressor 119 does not pressurize; when the gas pressure in the eleventh pipeline 22 is lower than the pressure required by the downstream user of the nineteenth pipeline 24 (less than the set value of pressure gauge 124), the first valve 120 is closed, the second valve 130 and the third valve 140 are opened, and the membrane inlet compressor 119 is used for pressurization.

[0037] In the above embodiment, preferably, a first component monitor 221 for monitoring the carbon dioxide concentration in the product natural gas is provided on the nineteenth pipeline 24, and the first component monitor 221 is connected to the gas membrane 122 by signal. When the first component monitor 221 detects that the carbon dioxide concentration in the product natural gas exceeds the set value, the first component monitor 221 controls the gas membrane 122 to open more membrane modules to enhance the separation effect.

[0038] In the above embodiment, preferably, a second component monitor 222 for monitoring the carbon dioxide concentration in the stream of distillation column 114 is provided on the fourteenth pipeline 20, and a regulating valve 40 is provided on the twenty-fourth pipeline 33. The second component monitor 222 is connected to the regulating valve 40. When the second component monitor 222 detects that the carbon dioxide concentration in the liquid carbon dioxide product is lower than the set value, the second component monitor 222 controls the regulating valve 40 to increase the opening degree, so as to enhance the carbon dioxide purification effect in distillation column 114.

[0039] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of this application, and not to limit them. Although this application has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some or all of the technical features therein. These modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of this application, and they should all be covered within the scope of the claims and specification of this application. In particular, as long as there is no structural conflict, the various technical features mentioned in the embodiments can be combined in any way. This application is not limited to the specific embodiments disclosed herein, but includes all technical solutions falling within the scope of the claims.

Claims

1. A highly integrated membrane tower coupled decarbonization system, characterized in that, It includes a cold box, a cryogenic separator, a throttling valve, a distillation column, a condenser, a condenser tank, a reboiler, a subcooler, a membrane inlet compressor, a gas membrane, and a permeate compressor, wherein the condenser and the reboiler are respectively integrated at the top and bottom of the distillation column; The cold box is connected to the feed gas inlet pipeline. The carbon dioxide-containing feed gas from upstream is heat-exchanged in the cold box and then enters the reboiler through the first pipeline as the heat source of the distillation column. After returning to the cold box through the second pipeline for further heat exchange, it enters the low-temperature separator through the third pipeline for gas-liquid separation. The gas phase from the cryogenic separator enters the cold box for heat exchange via the fourth pipeline, and then enters the gas membrane via the fifth pipeline; the liquid phase from the cryogenic separator is sent to the throttling valve for further throttling and cooling via the sixth pipeline, and then enters the distillation column via the seventh pipeline. The distillation column performs natural gas decarbonization and carbon dioxide purification on the incoming stream. The low-carbon dioxide gas after distillation is cooled by the condenser and then sent to the condenser tank via the eighth pipeline for gas-liquid separation. The gas phase from the condenser enters the subcooler via the ninth pipeline to exchange heat with the hot end stream, then enters the cold box via the tenth pipeline for heat exchange, then enters the membrane inlet compressor via the eleventh pipeline for pressurization, and then enters the gas membrane via the twelfth pipeline. The liquid phase from the condenser is returned to the distillation column via the thirteenth pipeline for further carbon dioxide purification. The high-concentration liquid carbon dioxide after distillation is sent to the subcooler via the fourteenth pipeline to exchange heat with the cold end stream, and then supplied to downstream users as liquid carbon dioxide product via the fifteenth pipeline. The high-carbon dioxide gas from the permeate side of the gas membrane outlet enters the permeate gas compressor via the sixteenth pipeline, is then pressurized, enters the cold box for heat exchange via the seventeenth pipeline, and is then sent to the distillation tower via the eighteenth pipeline for natural gas decarbonization and carbon dioxide purification; the low-carbon dioxide gas from the residual permeate side of the gas membrane outlet is provided to downstream users as a low-carbon dioxide natural gas product via the nineteenth pipeline.

2. The membrane tower coupled decarbonization system according to claim 1, characterized in that, The cold box is connected to the first temperature refrigerant from the refrigeration system via the twentieth pipeline, and then connected to the first temperature refrigerant returning to the refrigeration system after heat exchange via the twenty-first pipeline.

3. The membrane tower coupled decarbonization system according to claim 2, characterized in that, The cold box is connected to the second-temperature refrigerant from the refrigeration system via the twenty-second pipeline, and then connected to the second-temperature refrigerant returning to the refrigeration system after heat exchange via the twenty-third pipeline.

4. The membrane tower coupled decarbonization system according to claim 3, characterized in that, The condenser is connected to the refrigerant at the third temperature position from the refrigeration system via the twenty-fourth pipeline, and then connected to the refrigerant at the third temperature position that returns to the refrigeration system after heat exchange via the twenty-fifth pipeline.

5. The membrane tower coupled decarbonization system according to claim 1, characterized in that, A bypass branch is provided on the membrane inlet compressor. A first valve is provided on the bypass branch. A second valve is provided on the eleventh pipeline located inside the bypass branch. A third valve is provided on the twelfth pipeline located inside the bypass branch. A pressure gauge is provided on the nineteenth pipeline. The pressure gauge is connected to the first valve, the second valve and the third valve. When the gas pressure in the eleventh pipeline meets the pressure required by the downstream user of the nineteenth pipeline, the first valve is opened and the second and third valves are closed, bypassing the membrane inlet compressor without pressurization; when the gas pressure in the eleventh pipeline is lower than the pressure required by the downstream user of the nineteenth pipeline, the first valve is closed and the second and third valves are opened, using the membrane inlet compressor for pressurization.

6. The membrane tower coupled decarbonization system according to any one of claims 1 to 5, characterized in that, A first component monitor is installed on the nineteenth pipeline to monitor the carbon dioxide concentration in the product natural gas. The first component monitor is connected to the gas membrane signal. When the first component monitor detects that the carbon dioxide concentration in the product natural gas exceeds a set value, the first component monitor controls the gas membrane to open more membrane modules to enhance the separation effect.

7. The membrane tower coupled decarbonization system according to any one of claims 1 to 5, characterized in that, A second component monitor is installed on the fourteenth pipeline to monitor the carbon dioxide concentration in the distillation column stream. A regulating valve is also installed on the fourteenth pipeline. The second component monitor is connected to the regulating valve. When the second component monitor detects that the carbon dioxide concentration in the liquid carbon dioxide product is lower than the set value, the second component monitor controls the regulating valve to increase the opening to enhance the carbon dioxide purification effect in the distillation column.

Images