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    • 专利摘要:
    The invention comprises an apparatus for separation, purification and concentration of gas mixtures, using the interconnection of separation modules with at least four stages (2,3,8,9), with a very low slip of product gas in the offgas stream. Using at least one energy recovery machine (7) on the product gas flow side (4), the use of at least one energy recovery machine (10, 11) instead of the throttle control valves (10, 11) on the rent charge gas side from the separation modules (7, 8, 17, 18), The energy consumption can be further reduced. In order to further reduce the energy expenditure for the separation of gas mixtures, the invention also includes the interconnection of separation modules (2, 3, 8, 9, 17, 18), wherein the permeate gas stream (5) is further concentrated via the separation modules (17, 18) is recycled, and the highly enriched with product gas Rententatgastrom on the suction side of the compressor (1). The invention also includes the interconnection of the separation modules (2,3,8,9,17,18) and the compression of the Rententatgaströme from the separation modules (8,17) on the feed gas stream before the separation module (2) and the feed to the feed gas stream from Separation module (2), and the Rententatgaströme from the separation modules (9,18) on the feed gas flow upstream of the separation module (3) and the feed into the feed gas flow to the separation module (3).
    公开号:AT515137A1
    申请号:T922/2013
    申请日:2013-12-02
    公开日:2015-06-15
    发明作者:Johann Gruber-Schmidt
    申请人:Johann Gruber-Schmidt；
    IPC主号:
    专利说明:

    Process for the separation, purification and concentration of gas mixtures
    The invention relates to a special device, in particular a combination of separation modules and energy harvesting machines, for energetically favorable separation, purification and concentration of gas mixtures in several fractions of high purity.
    The separation of gas mixtures that occur in the context of a chemical process, is a task that occurs in many production processes. Examples of applications include the removal of CO 2 from power plant effluent streams, the removal of CO 2 from biogas for the purification of biogas, the removal of CO 2 from waste gas during the production of dimethyl ether.
    For separating gas mixtures, a separation module (2,3) is used, which consists of three gas streams. The gas stream which leads into the separation module, which is also called feed gas stream (1), which carries with it the gas mixture to be separated. The gas stream leading from the separation module, which carries with it the component-enriched gas flow, also called the Rententatgasstrom (4), which thus includes the product gas. The third gas stream which is also called the off-gas stream, also referred to below as permeate gas stream (6), which carries the enriched residual gas with it. The sum of the incoming masses and the outgoing masses equals zero, which means that none of the mass flows are lost in the separation module. The separation module is therefore a gas-tight system. In terms of energy, in addition to the conservation of mass flows, the conservation of energy flows is also important. Energy is the mechanical energy in the form of pressure and temperature, the thermal energy in the form of temperature, and the chemical energy in the form of the reaction products, as they can arise in the chemical bond. The chemical energy leads to heat of reaction, resulting from absorption, adsorption or reaction. The heat released or absorbed into the environment completes the conservation of the energy set. For the separation of gas mixtures there are various methods, such as the mechanical separation process over membranes, where the pressure difference is used as a driving force, the chemical process, where the chemical absorptive binding of one or more gas components to a liquid carrier in direct or indirect contact is applied , the physical process where one or more gas components are adsorbed to a solid support.
    Each of the above methods requires energy to separate gas mixtures, which must be provided in the form of heat and / or mechanical power. From a thermodynamic point of view, the separation of gas mixtures is always an irreversible process that takes place with the application of mechanical, electrical and / or chemical power. In addition, the process of separation is always lossy, which always leads to a loss of electrical, mechanical or chemical energy in the form of heat. From a thermodynamic point of view, it has been established as a consequence of the second law of thermodynamics that the separation of gas mixtures never occurs by itself. Since energy must be expended, the question is to ask for the cheapest and least amount of energy for the separation process.
    The invention therefore also encompasses a device for separating gas mixtures with less energy consumption. This makes it possible to separate large gas volume flows energetically cheaper into individual gas fractions.
    The separation processes, mechanically, chemically or physically, also have other disadvantageous properties in addition to the energy input for the separation of gas mixtures into individual gas components. The mechanical separation process is based on the generation of a high pressure difference, which is the driving force of the separation. This pressure difference is in connection with a diaphragm, the mechanical separation system. The pressure difference is achieved by a high pressure on the feed gas stream side, on the
    Permeate gas flow side is given a low pressure. Located between the feed gas stream and the permeate gas stream are the membrane.
    The membrane shape and membrane type characterize the separation modules. Today, the following membrane forms are known, the hollow fiber, the wound membrane, the flat membranes. In the mechanical separation of gas mixtures in addition to the pressure difference also the area play a role. The higher the pressure difference, the smaller the necessary area for separation of the gas mixtures and vice versa.
    If the volume and pressure of the gas component is known, then the temperature is fixed.
    The advantage of the mechanical separation process over the chemical and physical separation process is the fact that there are no chemical changes and / or no contamination in the gas components. The membrane is a solid with a material selected in this way, which does not react with the individual gas components of the gas mixture.
    The separation across the membrane is accomplished by utilizing the process of diffusion of the gas through the membrane and the flow of the gas across the membrane. Although the membrane is said to be dense to a liquid, the membrane is not dense to a gas. Through the pores and pore channels in the microscopic area, ie in the range of molecular diameter and atomic diameter, one or the other gas component can flow and / or diffuse. The mechanical separation system is that method to which this invention relates.
    The chemical separation of gas mixtures is based on the property that certain gases are bound to liquids. This process is known as Absoprtion and is used in gas scrubber systems. It is known that the liquid can evaporate and can be taken up to the saturation limit of the gas mixture. This separation method has the disadvantage that it comes to contamination of the gas mixture.
    The physical separation of gas mixtures is based on the property that a specific gas can be bound to the surface of solids with pressure and temperature. This process is known as pressure swing adsorption. The disadvantage of this method is the solid used for binding a gas, itself. To bind a large amount of gas molecules is a large surface of the
    Solid body necessary. The solids are porous so as to have a large surface area. The porosity causes a low mechanical stability to pressure changes. Over time, the surfaces of the solid break and are transferred as particles in the gas mixture, whereby the disadvantage of contamination of the gas mixture is given.
    The invention described herein solves the problem and takes advantage of the mechanical separation process because it does not lead to contamination of the gas streams. Contamination means the loading of the product gas with substances in the form of a vapor or particles resulting from the chemical process or from the physical process and their application. From an energetic point of view, there is a further disadvantage of the chemical and physical separation processes, since as a result complicated technical purification processes are necessary in order to achieve a corresponding gas quality and gas purity.
    The method described in patent WO2012 / 00727 A1 also includes the mechanical separation process performed with hollow fiber modules or flat modules. The disadvantage of this described in the patent process is the high energy expenditure in the form of compression (1) of the feed gas stream, ie that gas volume flow of the separation module (2,3) is supplied. Although the material of the membrane modules described in the patent WO2012 / 00727 A1 is more resistant to higher temperatures and therefore more stable in structure, it results in higher pressures for the gas separation as a consequence. The materials cited in the patent WO2012 / 00727 A1 lead in the practical implementation to pressures on the feed gas side of from 16 bar to 20 bar, if a good separation behavior with a sensible surface is to be obtained.
    Figure 1 shows this procedure. By the return of the permeate stream (5) to the suction side of the compressor (1), the proportion of the gas volume flow, which is to be compressed, by at least ~ 50% higher. This requires a further increase in the energy expenditure for compaction (1).
    Furthermore, it can be seen from the process in FIG. 1 that the permeate stream (6) contains a high proportion of the product gas. This is on the order of ~ 10 vol% and higher. The use of the separation modules (2,3) in Figure 1 describe a two-stage process, wherein the product gas (4) is enriched in the concentration. The high proportion of product gas in the permeate gas stream (6), also referred to as slip, is a disadvantage because it represents a further energy loss. In addition, the yield of the product gas (4) is reduced by this slip.
    The energy consumption in the application of the mechanical separation process is an essential parameter that makes it possible to decide on the technical and economic suitability of this process in process engineering applications. Energy consumption is the sum of the electrical energy (kW) that must be expended for the compression and recooling of the compressed gas stream. The energy consumed (kW) is related to the biogas flow (Nm3 / h). So this gives a reference value of dimension kW / (Nm3 / h).
    The electrical power is composed of the electric power for the compressor Pv, the electric power for the cooling system Pk is reduced by the electric power from the recovery Pr from the
    Energy recovery equipment. VGM denotes the supplied gas mixture volume flow on the suction side to the compressor, without the gas streams Vrez returned from the separation of the separation modules to the suction side of the compressor. From the above simple formula for the compaction performance, it can be seen that the recirculated gas volume flow Vrez has a significant influence on the electric power. In addition, it can be seen from the above simple formula that the enthalpy h is a function of pressure and temperature.
    The usual methods today are at a value of e = 0.35 kW / (Nm3 / h). The method described in patent WO2012 / 00727 A1 also has a magnitude of specific energy consumption of this order of magnitude.
    The invention solves the problem of lower energy consumption with very low slip on the order of 0.2% by volume of product gas in the offgas stream (12) by using the separation modules (8) and (9). The lower energy consumption results from the reduced Rentenatgaströmen from the separation modules (8) and (9). In this on the suction side of the compressor (1) returned
    Rententatsgasströmen is a very high concentration of product gas (4) included. This is synonymous with a high separation of the off-gas (12) from the gas mixture.
    The invention solves the problem of a lower energy consumption by also the from the separation module (3) permeate gas stream (5) is not returned directly, as shown in Figure 1, but on the separation modules (17) and in the further consequence on the separation module (18) to be led.
    The Rententatsgaströme the separation modules (17) and (18) are recycled with a high product gas concentration to the suction side of the compressor (1). The sum of these gas volume flows is less than the permeate gas flow (5).
    Another advantage of this invention is based not only on the lower recirculated gas volume flow on the suction side of the compressor (1), but also the associated higher concentration of product gas on the feed gas flow side before the separation module (2). This results in a smaller separation area and a smaller pressure difference in order to obtain the same separation behavior of the separation module (2) as shown in the interconnection in Figure 1.
    With the interconnections of the separation modules on which this invention is based and the interconnection shown in FIG. 4, it is possible to achieve and realize a specific energy consumption of e = 0.25 kW / (Nm.sup.3 / h).
    Another advantage of the invention is the use of the separation modules (8,9) and (17,18) whereby very small slip of product gas can be produced in the permeate stream (12) or (12) and (20), respectively. The low slip means very low losses of product gases. With this invention, a very high yield of product gas can be achieved and a slip of up to 0.2% by volume of product gas in offgas (12) and or (20) can be achieved.
    The invention solves the problem of low energy consumption with the use of an energy recovery machine (7) on the product gas stream (4) after the separation module (3). Here, the different pressure level from the mechanical separation process and the feed pressure in the gas network is utilized.
    The invention solves the problem of lower energy consumption in the application of the mechanical separation process by replacing the throttle control valves (10,11)
    Energy recovery machines (15,16) are used. In combination with the energy recovery from the product gas (4) via the energy recovery machine (7) one can achieve a specific energy consumption of e = 0.15 kW / (Nm3 / h). Such interconnections according to the invention are shown in Figures 6 and 7.
    Figures 8 and 9 show a further development of the interconnections from Figure 7. Instead of returning the Rententatgasströme on the suction side of the compressor (21) (1) are the Rententatsgaströme the
    Separation modules (7) and, or (17) via a compressor (22) brought to the pressure of the feed gas stream upstream of the separation module (2) and fed, the Rententatsgaströme the separation modules (8) and, or (18) via a compressor to the pressure the Feedgasstromes brought before the separation module (3) and fed. The compressors (21) and, or (22) can also be driven as shown in Figure 9 by the energy recovery machine (7). Through this interconnection, the energy consumption is reduced to that energy of the compressor (1), which is necessary to reach the pressure of the feed gas stream before the separation module (2).
    The invention also solves the problem of lower slip of product gas in the offgas (12,20). The mechanical separation process is based on the utilization of the flow of a gas through micropores and microchannels, as well as the diffusion through the membrane. Depending on the membrane homogeneity and membrane type, either the separation by means of flow or the gas separation with diffusion predominates. The micropores exploit the property of the different molecular diameters, whereby the temperature also influences the vibrational activity of the molecule. Depending on the type of gas, different molecular diameters and different vibration activities result. This means that, depending on the membrane material, there is an optimum pressure and temperature at which the separation behavior with respect to a gas type reaches its optimum. Nevertheless, there is always a slip. The slippage means that even an undesired Gastype is mitabgetrennt. This means that if you want to achieve a very low slip in the permeate gas stream (12,20), a multi-stage separation process is necessary, as shown in the interconnections of Figures 6,7,8,9 according to the invention.
    In addition to the flow but also occurs on the diffusion. Diffusion of a gas through the membrane is understood to mean that the molecule travels between the long chain polymer molecules of the membrane. This means the need for a higher pressure and a higher temperature. Also associated with diffusion is the solubility of a gas in the membrane. Diffusion, solubility and flow of the gas through the membrane are also called selectivity. High selectivity with respect to a gas type makes it possible to separate this gas type from the gas mixture with a low energy input with the mechanical separation process via membrane modules.
    The underlying invention has a great variety of applications. Low slip of product gas in the off-gas, low energy input in the separation of gas mixtures, high yield of product gases, is critical for applications in environmental technology, power plant applications, and industrial process applications.
    In environmental technology in the concentration of biogases, the separation according to the invention of CO 2 (carbon dioxide) from the gas mixture CH 4 (methane) and CO 2 (carbon dioxide) is applicable. With the low energy consumption according to the invention for the separation of the gas mixture biogas to methane of high concentration to natural gas quality and to carbon dioxide of high concentration with low slip very attractive. The separation of carbon dioxide makes it possible to further utilize the offgas as a usable gas, since the slip at Merthan is very low.
    In power plant technology, the separation of carbon dioxide from the exhaust gas is of interest. Carbon dioxide of high technical purity (99%) can be separated with this invention and used as usable gas for further processes. The advantage of the application of this invention lies in the low energy consumption and in the high product gas yield.
    Naturally, combustion processes take place in commerce and industry. Therefore, the separation of carbon dioxide from the exhaust gas is of interest. Carbon dioxide of high technical purity (99%) can be separated with this invention and used as usable gas for further processes. The advantage of the application of this invention lies in the low energy consumption and in the high Produktgasaubeute.
    List of designations 1 Compressor 1 2 Separation module 1 3 Separation module 2 4 Enriched gas, Rententat, product gas 5 Permeate of separation module 2, Offgas with slip 6 Permeate of separation module 1, Offgas with slip 7 Recovery machine 1 8 Separation module 3 9 Separation module 4 10 Throttle control 3 11 Throttling control 4 12 Permeate line of separation module 4, Offgas with slip 13 Permeate line of separation module 3, Offgas with slip 14 Vacuum blower 1 15 Recovery machine 2 16 Recovery machine 3 17 Separation module 5 18 Separation module 6 19 Permeate line of separation module 5, Offgas with slip 20 Permeatleitung of the separation module 6, offgas with slip 21 compressor 2 22 compressor 3
    List of symbols F Force (N) A Area (m2) Δρ Pressure difference (N / m2)
    Ah enthalpy difference (kJ / kg) p Density (kg / m3) VGm Volume flow (Nm3 / h)
    Vrez flow rate (Nm3 / h)
    Peie electrical power (kW)
    Pv electric power of compressor (kW) PK electric power of recooling (kW) PR electric power of energy recovery machines (kW)
    List of pictures
    Fig. 1: Two-stage process with separation modules and gas recirculation to the suction side of the compressor
    Fig. 2: Representation of the pressure curve in gas enrichment
    Fig. 3: Two-stage process with separation modules and energy recovery on the product gas side
    Fig. 4: Four-stage process with separation modules and the recirculation of the enriched product gas streams
    Fig. 5: Four-stage process with separation modules and the recirculation of the enriched product gas streams and use of a vacuum blower in the fourth separation module on the permeate side
    Fig. 6: Four-stage process with separation modules and the use of energy recovery
    Figure 7: Extended four-step process with separation modules and the use of energy recovery
    Figure 8: Extended four-stage process with separation modules and the use of individual back compressors
    Figure 9: Extended four-stage process with separation modules and the use of coupled back compressors and energy recovery machine
    Description of the pictures:
    Figure 1: The interconnection shown in Figure 1 was used. The interconnection consists of a compressor (1) whose compressed gas stream is fed as feed gas stream into the separation module (2). From the separation module (2), the permeate stream (6) is derived. The Rententatgasstrom from the separation module (2) is passed into the separation module (3). From the separation module (3) the Rententatgasstrom, which is also referred to as product stream (4) derived. The permeate stream (5) from the separation module (3) is returned to the suction side of the compressor (1).
    Figure 2: The interconnection shown in Figure 2 was used. The figure shows the pressure curve. The gas mixture is compressed via the compressor to the pressure of the feed gas stream upstream of the separation module (2), after which the pressure loss through the flow of the product gas (4) through the separation module (2) and (3). This pressure is higher than the gas network pressure also referred to as feed pressure.
    Fig. 3: The interconnection shown in Figure 3 was used. The interconnection consists of a compressor (1) whose compressed gas stream is passed as feed gas stream into the separation module (2). From the separation module (2) of the permeate gas stream (6) is derived. The Rententatgasstrom is passed into the separation module (3). From the separation module (3) the Rententatgasstrom, which is also referred to as product gas stream (4) derived. The permeate gas stream (5) from the separation module (3) is returned to the suction side of the compressor (1). The pressure energy contained in the product gas stream (4) is converted into electrical energy via the recovery machine (7).
    Figure 4: The interconnection shown in Figure 4 was used. The interconnection consists of a compressor (1) whose compressed gas stream is passed as feed gas stream into the separation module (2). From the separation module (2), the permeate stream (6) is discharged into the separation module (8). The Rententatgasstrom from the separation module (2) is passed into the separation module (3). From the separation module (3) is the Rententatgasstrom, which is also referred to as product gas stream (4) obtained. The permeate gas stream (5) from the separation module (3) is returned to the suction side of the compressor (1). The product gas stream obtained from the separation module (8) is expanded as Rententatgasstrom via the throttle controller (10) to the suction pressure of the compressor (1) and fed to the suction side of the compressor (1). The permeate gas stream (13) derived from the separation module (8) is fed to the separation module (9). The Rententatgasstrom obtained from the separation module (9) is expanded via the throttle controller (11) to the suction pressure of the compressor (1) and fed to the gas flow on the suction side of the compressor (1). The permeate gas stream (12) from the separation module (9) is discharged as offgas (12).
    Fig. 5: The interconnection shown in Figure 2 was used. The interconnection consists of a compressor (1) whose compressed gas stream is fed as feed gas stream into the separation module (2). From the separation module (2), the permeate gas stream (6) is discharged into the separation module (8). The Rententatgasstrom from the separation module (2) is passed into the separation module (3). From the separation module (3) is the Rententatgasstrom, which is also referred to as product gas stream (4) obtained. The permeate gas stream (5) from the separation module (3) is returned to the suction side of the compressor (1). The product gas stream obtained from the separation module (8) is expanded as Rententatgasstrom via the throttle controller (10) to the suction pressure of the compressor (1) and fed to the suction side of the compressor (1). The permeate gas stream (13) derived from the separation module (8) is fed to the separation module (9). The Rententatgasstrom obtained from the separation module (9) is relaxed via the throttle controller (11) to the suction pressure of the compressor (1) and thus returned. The permeate gas stream (12) from the separation module (9) is discharged as offgas (12). In order to improve the separation effect of the permeate gas stream (12) is sucked by a vacuum blower (14) and forwarded.
    Fig. 6: The interconnection shown in Figure 2 was used. The interconnection consists of a compressor (1) whose compressed gas stream is passed as feed gas stream into the separation module (2). From the separation module (2), the permeate gas stream (6) is discharged into the separation module (8). The Rententatgasstrom from the separation module (2) is passed into the separation module (3). The rententate gas stream, also referred to as product stream (4), is recovered from the separation module (3). The energy contained in the product gas stream (4) is recovered via an energy recovery machine (7). The permeate gas stream (5) from the separation module (3) is returned to the suction side of the compressor (1). The product gas stream obtained from the separation module (8) is released as a rentate via a recovery machine (14) to the suction pressure of the compressor (1) and fed to the suction side of the compressor (1). The permeate gas stream (13) derived from the separation module (8) is fed to the separation module (9). The Rententatgasstrom obtained from the separation module (9) is relaxed by a recovery machine (15) to the suction pressure of the compressor (1) and fed. The permeate gas stream (12) from the separation module (9) is discharged as offgas (12). In order to improve the separation effect of the permeate gas stream (12) is sucked by a vacuum blower (14) and forwarded.
    Figure 7: The interconnection shown in Figure 2 was used. The interconnection consists of a compressor (1) whose compressed gas stream is passed as feed gas stream into the separation module (2). From the separation module (2), the permeate stream (6) is discharged into the separation module (8). The Rententatgasstrom from the separation module (2) is passed into the separation module (3). From the separation module (3) the Rententatgasstrom, which is also referred to as product gas stream (4), won.Die contained in the product gas stream (4) energy is recovered via an energy recovery machine (7). The permeate gas stream (5) from the separation module (3) is returned to the suction side of the compressor (1). The product gas stream obtained from the separation module (8) is released as a rent by a recovery machine (15) to the suction pressure and returned to the suction side of the compressor (1). The permeate gas stream (13) derived from the separation module (8) is fed to the separation module (9). The Rententatgasstrom obtained from the separation module (9) is relaxed via a recovery machine (16) to the suction pressure of the compressor (1) and thus returned. The permeate gas stream (12) from the separation module (9) is discharged as offgas (12). In order to improve the separation effect of the permeate gas stream (12) is sucked by a vacuum blower (14) and forwarded. The Permeatgaststrom (19) derived from the separation module (17) is fed to the separation module (18). The Rententatgasstrom obtained from the separation module (18) via a recovery machine (16) to the suction pressure of
    Compressor (1) relaxed and so returned. The permeate gas stream (20) from the separation module (18) is discharged as offgas (20). In order to improve the separation effect of the permeate gas stream (20) is sucked by a vacuum blower (14) and forwarded.
    Figure 8: The interconnection shown in Figure 2 was used. The interconnection consists of a compressor (1) whose compressed Gastro is passed as feed gas stream in the separation module (2). From the separation module (2), the permeate gas stream (6) is discharged into the separation module (8). The Rententatgasstrom from the separation module (2) is passed into the separation module (3). From the separation module (3) the Rententatgasstrom, which is also referred to as product gas stream (4) won. The energy contained in the Produktgastrom (4) energy is recovered via an energy recovery machine (7). The permeate gas stream derived from the separation module (2) is fed to the separation module (8) as feed gas stream. The product gas stream (5) obtained from the separation module (8) is compressed as a rentate via a compaction machine (21) to the feed gas pressure of the separation module (2). The permeate gas stream (13) derived from the separation module (8) is fed to the separation module (9). The Rententatgasstrom obtained from the separation module (9) is compressed via a compacting machine (21) to the feed gas pressure of the separation module (3) and fed to the feed gas stream upstream of the separation module (2). The permeate gas stream (12) from the separation module (9) is discharged as offgas (12). In order to improve the separation effect of the permeate gas stream (12) is sucked by a vacuum blower (14) and forwarded. The Permeatgaststrom (19) derived from the separation module (17) is fed to the separation module (18). The Rententatgasstrom obtained from the separation module (18) is compressed via a compacting machine (22) to the feed gas pressure before the separation module (3) and fed to the feed gas stream to the separation module (3). The permeate gas stream (20) from the separation module (18) is discharged as offgas (20). In order to improve the separation effect of the permeate gas stream (20) is sucked by a vacuum blower (14) and forwarded.
    Figure 9: The interconnection shown in Figure 2 was used. The interconnection consists of a compressor (1) whose compressed gas stream is passed as feed gas stream into the separation module (2). From the separation module (2) is the
    Permeate gas stream (6) in the separation module (8) derived. The Rententatgasstrom from the separation module (2) is passed into the separation module (3). From the separation module (3) the Rententatgasstrom, which is also referred to as product gas stream (4) won. The energy contained in the Produktgastrom (4) energy is recovered via an energy recovery machine (7). The permeate gas stream derived from the separation module (2) is fed to the separation module (8) as feed gas stream. The product gas stream (5) obtained from the separation module (8) is compressed as Rententatgasstrom via a compression machine (21) to the feed gas pressure of the separation module (2) and fed to the feed gas stream before the separation module (2). The permeate gas stream (13) derived from the separation module (8) is fed to the separation module (9). The Rententatgasstrom obtained from the separation module (9) is compressed via a compacting machine (22) to the feed gas pressure of the separation module (3) and thus returned. The permeate gas stream (12) from the separation module (9) is discharged as offgas (12). In order to improve the separation effect of the permeate gas stream (12) is sucked by a vacuum blower (14) and forwarded. The Permeatgaststrom (19) derived from the separation module (17) is fed to the separation module (18). The Rententatgasstrom obtained from the separation module (18) is compressed via a compression machine (22) to the feed gas pressure upstream of the separation module (3) and thus returned. The permeate gas stream (20) from the separation module (18) is discharged as offgas (20). In order to improve the separation efficiency, the permeate gas stream (20) is sucked by a vacuum blower (14) and passed on. The compacting machines (21) and (22) are directly driven by the energy recovery machine (7)
    权利要求:
    Claims (8)
    [1]
    The device for separation, cleaning and concentration of gas mixtures comprises at least the separation modules (2,3,8,9), at least one compressor (1) and, or at least one vacuum compressor (14), at least two throttle control valves (10,11 ), at least one energy recovery machine (7) is present, wherein the gas mixture in the feed gas flow to the separation module consists of at least two gases, the feed gas stream is separated via the separation module in a Permeatgasstrom and in a Rententagasstrom, the feed gas stream from the compressor (1) on the Is supplied to the separation module (2), the Rententatsgasstrom from the separation module (2) as feed gas stream the separation module (3) zuegführt, the Rententatsgasstrom (4) from the separation module (3) of the energy recovery machine (7) is supplied, the permeate gas stream (6 ) is fed from the separation module (2) as feed gas stream to the separation module (8), the Rententatsgasstrom from the separation module (8) the throttle control 10), the permeate gas stream (13) from the separation module (8) as feed gas stream (13) is supplied to the separation module (9), the Rententatgasstrom from the separation module (9) is fed to the throttle control valve (11), the Permeatgasstrom ( 12) from the separation module (9) is obtained as offgas (12), the Rententatgastrom is relaxed with the throttle control valve (10) to the suction pressure of the compressor (1), and the suction gas stream of the compressor (1) is supplied, the Rententatgasstrom with the Throttling control valve (11) to the suction pressure of the compressor (1) is relaxed, and the suction gas flow of the compressor (1) is supplied, characterized in that - the permeate gas stream from the separation module (2) is supplied to the separation module (8) - the Rententatgasstrom from the Separation module (8) to the suction pressure of the compressor (1) is relaxed - the Rententatgastrom from the separation module (9) to the suction pressure of the compressor (1) is relaxed - the product gas concentration after the compressor (1) as a feed gas stream is at least 60% - the offgas concentration (12) is at least preferably 98.5% and particularly preferably 99.8% and preferably 98.5% to 99.8% and the slip of the product gas is preferably 1.5% by volume and more preferably 0 , 2% and preferably 1.5% to 0.2% - the product gas concentration (4) is at least preferably 95% and more preferably 99% and preferably 95% to 99%
    [2]
    2. The device according to claim 1, characterized in that instead of the throttle control valves (10,11) energy recovery machines (15,16) are used.
    [3]
    3. The apparatus according to claim 1, characterized in that instead of the return of the permeate gas stream (5) from the separation module (3) to the suction side of the compressor, the permeate gas stream (5) is supplied to the separation module (17), the Rententatgastrom from the separation module ( 17) is supplied to the energy recovery machine (15), the permeate gas stream (19) is supplied to the separation module (18), the Rententatgasstrom from the separation module (18) of the energy recovery machine (16) is supplied, and the Permeatgasstrom (20) from the separation module (18 ) is supplied as offgas to the vacuum compressor (14).
    [4]
    4. The device according to claim 1, characterized in that instead of the return of the permeate gas stream (5) from the separation module (3) to the suction side of the compressor, the permeate gas stream (5) is fed to the separation module (17), the Rententatgasstrom from the separation module ( 17) is supplied to the throttle control valve (10), the permeate gas stream (19) is supplied to the separation module (18), the Rententatgasstrom from the separation module (18) is fed to the throttle control valve (11), and the Permeatgasstrom (20) from the separation module (18 ) is supplied as offgas to the vacuum compressor (14).
    [5]
    5. The device according to claim 1, characterized in that instead of the return of Rententatgasstromes from the separation module (7) and the relaxation of the pressure of the suction side of the compressor (1) the Rententatgasstrom from the separation module (7) with a compacting machine (21) the pressure of the feed gas stream of the separation module (2) is brought and the feed gas stream of the separation module (2) is supplied.
    [6]
    6. The device according to claim 1, characterized in that instead of returning the Rententatgasstromes from the separation module (8) and the relaxation on the pressure of the suction side of the compressor (1) the Rententatsgasstrom from the separation module (8) with a compacting machine (22) the pressure of the feed gas stream of the separation module (3) is brought and the feed gas stream of the separation module (3) is supplied.
    [7]
    7. The device according to claim 6, characterized in that the compressor (22) from the energy recovery machine (7) is driven directly.
    7. The device according to claim 1, characterized in that instead of the return of the Permeatgastromes (5) from the separation module (3) to the suction side of the compressor, the Permeatgasstrom (5) is supplied to the separation module (17), the Rententatgastrom from the separation module ( 17) is fed to a compressor (21), the so compressed Rententatgasstrom is fed to the feed gas flow side of the separation module (2), the Permeatgasstrom (19) is fed to the separation module (18), the Rententatgasstrom from the separation module (18) the compressor (22 ) is fed, the so-compressed Rententatgasstrom on the feed gas stream side of the separation module (3) is fed and the permeate gas stream (20) from the separation module (18) is supplied as offgas to the vacuum compressor (14). 6. The device according to claim 5, characterized in that the compressor (21) from the energy recovery machine (7) is driven directly.
    [8]
    8. The device according to claim 7, characterized in that the compressors (21,22) are driven by the energy recovery machine (7).
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    同族专利:
    公开号 | 公开日
    AT515137B1|2016-01-15|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US6168649B1|1998-12-09|2001-01-02|Mg Generon, Inc.|Membrane for separation of xenon from oxygen and nitrogen and method of using same|
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    WO2012000727A1|2010-07-01|2012-01-05|Evonik Fibres Gmbh|Process for separation of gases|EP3369473A1|2017-03-02|2018-09-05|L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude|Facility and method for treatment of a feed gas stream comprising methane and carbon dioxide by membrane permeation|
    FR3089821B1|2018-12-14|2021-06-18|Air Liquide|Installation and method of treatment by membrane permeation of a gas stream with adjustment of the suction pressure of the third permeate|
    法律状态:
    2019-08-15| MM01| Lapse because of not paying annual fees|Effective date: 20181202 |
    优先权:
    申请号 | 申请日 | 专利标题
    ATA922/2013A|AT515137B1|2013-12-02|2013-12-02|Process for the separation, purification and concentration of gas mixtures|ATA922/2013A| AT515137B1|2013-12-02|2013-12-02|Process for the separation, purification and concentration of gas mixtures|
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