WO2009030777A1 - Procédé de production de gaz à l'aide de membranes de séparation de gaz - Google Patents

Procédé de production de gaz à l'aide de membranes de séparation de gaz Download PDF

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Publication number
WO2009030777A1
WO2009030777A1 PCT/EP2008/061870 EP2008061870W WO2009030777A1 WO 2009030777 A1 WO2009030777 A1 WO 2009030777A1 EP 2008061870 W EP2008061870 W EP 2008061870W WO 2009030777 A1 WO2009030777 A1 WO 2009030777A1
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Prior art keywords
gas
aforementioned
pressure
residual
gas separation
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PCT/EP2008/061870
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English (en)
Inventor
Kazuo Kitsukawa
Naohiko Yamashita
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L'air Liquide, Société Anonyme pour l'Étude et l'Exploitation des Procédés Georges Claude
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Publication of WO2009030777A1 publication Critical patent/WO2009030777A1/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
    • B01D53/225—Multiple stage diffusion
    • B01D53/226—Multiple stage diffusion in serial connexion
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
    • B01D53/225—Multiple stage diffusion
    • B01D53/227—Multiple stage diffusion in parallel connexion
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/10—Single element gases other than halogens
    • B01D2257/108—Hydrogen

Definitions

  • This invention pertains to a gas production method using gas separation membranes, and specifically to a gas production method using gas separation membranes with selective permeability to separate into permeable gas rich in highly-permeable and non-condensable components and a residual gas with reduced aforementioned components.
  • a cascade cycle as shown in figure 12 is effective.
  • two sets of gas separation membranes 201 (primary gas separation membrane 201 a and secondary gas separation membrane 201 b) are combined and used.
  • feed gas g1 merges with permeable gas g2aa of secondary gas separation membrane 201 b, and then is supplied to primary gas separation membrane 201 a after compression.
  • permeable gas g2a from primary gas separation membrane 201a is produced and its residual gas g2b is supplied as feed gas to secondary gas separation membrane 201 b. Residual gas is produced at this secondary gas separation membrane 201 b.
  • Permeable gas g2aa from this merges with the original feed gas and reused (see the Japanese patent application 2000-33222 for example).
  • figure 12 shows a composition of reusing permeable gas g2aa from secondary gas separation membrane 201 b, it is also possible to collect permeable gas g2a as the high- pressure product gas and permeable gas g2aa as the low-pressure product gas.
  • FIG 13 It is also possible to compose a system, as a parallel cycle, as shown in figure 13, that separates and collects enriched nitrogen gas from air.
  • two hollow-fiber separation membrane modules 312 and 313 are used in parallel, the supply gas is diverged and supplied after pretreatment to each of hollow-fiber separation membrane modules 312 and 313, and the enriched nitrogen gas obtained from each of hollow-fiber separation membrane modules 312 and 313 is merged and led to product gas outlet 324.
  • the air taken in from air inlet 301 is led to dust filter 302 to remove suspended particles in the air, and sent to compressor 303.
  • the pressurized air here is supplied from the gas supply port of hollow-fiber separation membrane modules 312 and 313 and sent to the supply side of the membranes.
  • the permeable gas permeated flows through the permeated side of the membranes, forms a permeable gas discharge flow via the permeable gas discharge port, and is discharged out of the system after its flow rate is reduced at flow rate adjustment valves 316 and 317 at the middle of the piping (see the Japanese patent application 2002-35530 for example).
  • figure 13 shows a system in which enriched nitrogen gas is collected as the product gas and since the permeable gas discharge flow is enriched oxygen gas, it is also possible to collect this as the product gas.
  • the permeable gas from one as the high-pressure product gas and collect the permeable gas from the other as the low-pressure product gas.
  • the purity and yield ratio of the product become the primary characteristics when using gas separation membranes to produce gas.
  • the desired purity is determined depending on the use of the product gas, and after investigation along the policy to secure the highest yield ratio within that purity range, the control method including the processes and volume reduction operations is determined.
  • yield ratio the desired component yield ratio of the permeable gas
  • the underpressure dew point of the gas at the residual gas outlet becomes important, and if the dew point is lower compared to the gas temperature at the gas separation membrane, liquefaction in the gas at the primary side of the gas separation membrane will not occur.
  • residual gas pressure the pressure immediately after the residual gas outlet of the gas separation membrane
  • residual gas dew point the dew point under residual gas pressure immediately after the residual gas outlet of the gas separation membrane
  • residual gas flow rate the flow rate of the residual gas of the gas separation membrane
  • permeable gas pressure the pressure and flow rate of the permeable gas
  • the objective of this invention is to provide a method of preventing liquefaction of the condensable components in the primary side gas of the gas separation membranes with a versatile and cost-efficient method when collecting the desired components from the feed gas that contains multiple components including poorly-permeable and condensable components, using the gas separation membranes with selective permeability, separating the feed gas into permeable gas rich in highly-permeable and non-condensable components and residual gas with reduced said components, and obtaining as high as possible yield ratio while securing the desired purity.
  • Its objective in particular is to gain even higher yield ratio when conducting the volume reduction operation. In this patent claim, simply
  • yield ratio means the ratio of the total volume of the flow rate of the desired components in the product gas to the flow rate of the desired components in the feed gas. Moreover, needless to say, this also includes cases in which the final residual gas or by-product liquid is used as the by-product product.
  • the inventors of this invention reached completion of this invention after accumulation of dedicated research to realize the aforementioned objective by the production method of permeable gas and by-product gas as described below.
  • the upstream side is referred to as the primary or first
  • the downstream side is referred to as the secondary or second.
  • This invention relates to a gas production method that separates a feed gas containing multiple components including at least a highly permeable and non- condensable component A and a poorly permeable and condensable component B into a gas rich in highly-permeable and non-condensable component A and a residual gas with a reduced concentration of the aforementioned component A, using gas separation membranes with selective permeability, said production method being characterized by:
  • component A highly permeable and non-condensable components
  • component B poorly permeable and condensable components
  • Component A consists of one or several highly permeable gases, such as, but not limited to, hydrogen, oxygen and/or nitrogen.
  • Component B consists of one or several less permeable, condensable gases, such as, but not limited to, water and/or organic compounds.
  • "Highly permeable”, “semi permeable” and “condensable” can have a relative meaning, in the sense that component A is more permeable than component B through the membranes that are considered and chosen for the purpose of the invention and component B is more easily condensed than component A in an industrial vapor-liquid separation.
  • a method of using a separation function with gas separation membranes with selective permeability, and a method of using a vapor-liquid separation function based on the difference in condensability of each component have been used.
  • This invention proposes a method of preventing liquefaction of component B in the primary side gas of the gas separation membrane when component B is contained in the feed gas with a versatile yet cost-efficient method, separating it into permeable gas rich in component A and residual gas with reduced component A, and obtaining as high as possible yield ratio while securing the desired purity.
  • residual gas dew point Z residual gas dew point
  • the yield ratio of the permeable gas also lowers, but at the same time, as the flow rate of the residual gas increases, the concentration of component A in the residual gas also increases. That is, by the synergistic effect of the increase in the concentration of component A as the pressure lowers, dew point Z of the residual gas lowers and it is possible to return it to below the reference value.
  • gas separation membrane is not limited to cases in which one membrane module is used with inlet ports and outlet ports of supply gas, permeable gas and residual gas, but also includes compositions using a necessary number of multiple membrane modules lined in parallel and each module having an integrated composition of inlet ports and outlet ports for each of the supply gas, permeable gas and residual gas.
  • condensable components refer to components with condensability to the condensation treatment, and are not limited to high or poor permeability to the gas separation membrane.
  • Highly permeable and non-condensable components refer to components with high permeability to the gas separation membrane and non-condensability to the condensation treatment, and more specifically refer, in the implementation example below, to hydrogen when, for example, hydrogen, methane, butane and pentane coexist in the feed gas.
  • “Poorly permeable and non-condensable components,” described later, refer to components with poor permeability to the gas separation membrane and non-condensability to the condensation treatment, and in the above example, refer to methane.
  • “Poorly permeable and condensable components” refer to components with poor permeability to the gas separation membrane and condensability to the condensation treatment, and in the above example, refer to butane and pentane.
  • this invention essentially has the same effect in cases where small amounts of permeable and condensable components (such, for example, as water in the feed gas in the implementation example below) are contained in the feed gas. Therefore, it is noted here that this invention also includes such cases.
  • Process value connected with the pressure refers to a process value that changes with the pressure change, and such values as the residual gas flow rate to the residual gas pressure and the permeable gas flow rate to the permeable gas pressure can be cited. The same applies to the following.
  • the permeability is higher as the temperature is higher, but there is also a tendency that the selectivity is higher as the temperature is lower (ratio of permeability between highly permeable components and poorly permeable components).
  • the alteration range of the dew point is determined corresponding to the alteration range of the gas supply temperature. It was found that the correlation function can be expanded to a form including residual gas dew point Z as a parameter, as stated later in the embodiment examples, by analyzing the correlation function between the residual gas pressure and the concentration of component A in the residual gas according to the method described above at several dew points.
  • monitoring while in operation, the status of the aforementioned dew point Z to be below the reference value Zb determined by the temperature of feed gas supplied to aforementioned gas separation membranes, said monitoring using the aforementioned correlation function and being based on the aforementioned mixing ratio obtained from the measured value of each feed gas flow rate and on the measured value of the aforementioned component A concentration in the residual gas, and
  • this invention found it possible to provide more accurate control by pre-analyzing the correlation function so that it includes the mixing ratio of the feed gases as a parameter in cases where the mixing ratio of the feed gases can be confirmed or estimated, and prevents liquefaction of the condensable components in the primary side gas of the gas separation membranes by setting reference value Za based on the feed gas supply temperature and controlling the residual gas pressure from the concentration of specific components (component A) in the residual gas using the aforementioned correlation function.
  • the above mentioned gas production methods are characterized by: - performing a pre-operation analysis of the aforementioned correlation function, before the step of supplying aforementioned feed gas to aforementioned gas separation membrane, including, as analysis parameter, the temperature of vapor-liquid separation process of step (U1 ) hereafter) in cases the following steps are included:
  • the vapor- liquid separation treatment is applied prior to the process of supplying the feed gas to the gas separation membranes, it is effective since the condensable components can be removed and the treatment efficiency at the gas separation membranes can be improved.
  • the composition of the feed gas is consistent, since only the by-product gas components generated by the vapor- liquid separation function is supplied to the gas separation membranes after heating, the gas composition supplied to the gas separation membranes varies due to the pressure and temperature of the vapor-liquid separation process.
  • the method described above can not be applied as is since the supply gas composition to the gas separation membranes is constant.
  • the cascade cycle is used to secure the desired product purity and yield ratio even with relatively small membrane area in such cases as producing multiple product gases with different purity, by using multiple stages of gas separation membranes and making the permeable gas from each membrane as the product gas.
  • this invention that pre-analyzes the correlation function of each layer and uses it for the operational control, it is possible to secure an even higher yield ratio while preventing liquefaction of component B in the primary side gas of each gas separation membrane layer.
  • the dew point can be kept lower, it is possible to prevent liquefaction even if component B is concentrated by controlling the primary pressure of each layer of the gas separation membrane sequentially lower as the gas is supplied sequentially to the gas separation membranes, and it is further possible to improve the yield ratio of the permeable gas.
  • the latter stages can be used at a higher temperature limitation and control it so that the temperature is sequentially higher towards the latter stages, it is preferable as liquefaction can be prevented even if component B is concentrated.
  • the gas production method pertaining to this invention it is possible to propose a versatile yet cost-efficient method of preventing liquefaction in the primary side gas of the gas separation membranes, separate the gas into permeable gas rich in highly-permeable and non- condensable component A and residual gas with reduced component A, and provide a gas component and condensable component production method that allows as high as possible yield ratio while securing the desired purity. It has become possible to realize an even higher yield ratio especially when conducting a volume reduction operation.
  • this composition is characterized by setting reference value Za of dew point Z and pre-operation analyzing the correlation function between the residual gas pressure and the concentration of the components A in the residual gas, based on the characteristics of the feed gas and the gas separation membranes, monitoring the dew point Z so that it is below the reference value Za from the measured value of the concentration of the components A in the residual gas using the correlation function during operation, and in case it exceeds the reference value Za, adjusting it with either the residual gas pressure, permeable gas pressure, or the process value that is connected with these values to maintain it below the reference value Za and prevent liquefaction in the primary side gas of the gas separation membranes.
  • FIG 1 shows compositional example 1 (this Process 1 ) of the gas production process pertaining to this invention (hereinafter referred to as "this Process").
  • feed gas flow path Uo is composed of feed gas flow path Uo, gas separation membranes S, permeable gas flow path T1 , residual gas flow path R1 , pressure control means PCrI (pressure control valve PCV1 and pressure controller PC1 ) installed in residual gas flow path R1 , and control section (not shown in figure).
  • feed gas analysis port APo permeable gas analysis port Apt, and residual gas analysis port Apr (used for batch analysis by such instruments as a gas chromatography mass spectrometer) are installed.
  • concentration measuring means is also possible to install concentration measuring means. Details will be discussed later.
  • This Process 1 is designed to obtain the desired purity and improve yield ratio of component A and component B while preventing liquefaction of the condensable component at the primary side of the membrane by (i) pre-setting reference value Za of dew point Z to prevent liquefaction of the condensable components, (ii) pre- operation analyzing the correlation function between residual gas pressure Pr and concentration X of component A in the residual gas, and optimally controlling the activation condition of gas separation membrane S using this correlation function during actual operation including volume reduction operation.
  • the specific control method will be discussed later, but a method of monitoring residual gas dew point so that it is below reference value Za from the measured value of concentration X of component A in the residual gas, and controlling residual gas pressure Pr of gas separation membrane S so that it is below reference value Za is taken.
  • the feed gas it is desirable to supply refined gas or refinement-treated crude gas, and specifically such gases as refined air, refined naphtha cracking gas, refined reformed gas, refined water gas, and refined natural gas can be considered.
  • the above gases are used generally at ambient temperature, and a flow rate of 1 ,000 ⁇ 100,000 [Nm 3 /h].
  • the pressure condition varies depending on the purpose of the permeable gas, but it should be pressurized to approximately 1 ⁇ 50 [bar (abs)].
  • gas separation membranes S those with the optimal material, capacity (surface area) and form shall be selected depending on the type of the feed gas or permeable gas.
  • gas separation membranes S such materials, for example, as polyethylene (PE), polypropylene (PP), silicone rubber, polysulfone, cellulose acetate, polyaramid (PA), and polyimide (Pl) can be considered.
  • PE polyethylene
  • PP polypropylene
  • silicone rubber silicone rubber
  • PA polysulfone
  • cellulose acetate cellulose acetate
  • PA polyaramid
  • Pl polyimide
  • heating section H heating section H
  • feed gas flow path Uo that supplies the feed gas to gas separation membranes S. It is desirable that gas separation is performed at an adequate temperature depending on the characteristics and purpose of the gas separation membranes, and it is necessary to heat the feed gas to a certain adequate temperature. If liquid mist is contained in the feed gas, there is a risk of causing deterioration of the gas separation membrane depending on its material.
  • the feed gas contains high-boiling point components
  • liquefaction may occur at ambient temperature
  • this high-boiling point component is poorly-permeable gas (component B)
  • component B there is a risk of concentration and liquefaction of component B in the gas at the primary side of gas separation membrane S. Therefore, it is possible to prevent the risk of generating liquid mist at gas separation membrane S by heating it using heating section H installed in feed gas flow path Uo.
  • feed supply temperature Ts pre-setting reference value Za of dew point Z determined by supply temperature Ta (hereinafter referred to as "feed supply temperature Ts") to gas separation membrane S to prevent liquefaction of the condensable components
  • pre-operation analyzing of the correlation function between residual gas pressure Pr and concentration X of component A in the residual gas as a parameter so that it includes residual gas dew point Z, and optimally controlling the operational condition of gas separation membrane S using this correlation function during actual operation it is possible to secure the desired purity and improve the yield ratio of component A and component B while preventing liquefaction of component B at the primary side of gas separation membrane S.
  • the gases sampled from analysis ports APo and AP1 are batch-analyzed using such devices as the gas chromatography, and can be used to monitor the stability of the feed gas composition and process performance from their regular periodic analysis results.
  • concentration measuring means it is desirable to use an analyzer that is highly selective to the desired components, that is the product gas components, and highly reliable for continuous analysis.
  • the component is hydrogen
  • such analyzers as the thermal conductivity type analyzer, or in case the component is methane
  • an infrared ray absorption type analyzer can be considered. It is also possible to adopt a method of combining the batch analysis and continuous analysis. It is possible to provide for judging fine adjustments while checking the deviation of the continuous analysis instrument from the results of the more reliable batch analysis.
  • FIG. 4 shows a modified example of this Process 1 (this Process 2). While the basic composition is the same as basic composition example 1 , the following items are added in feed gas flow path Uo, (a1 ) feed gas vapor-liquid separation section D, or cooling section C and vapor- liquid separation section D,
  • pressure control means PCro pressure control valve PCVo and pressure controller PCo
  • cooling section C installed in by-product gas flow path D.
  • Cooling section C, vapor-liquid separation section D, by-product gas flow path G, heating section H, by-product liquid flow path L, pressure control means PCro (pressure control valve PCVo and pressure controller PCo) and either liquid-surface detection section LC1 or control valve LCV1 are added so that primary treatment can be pre-applied to the feed gas.
  • This Process 2 is desirable for application in cases where the feed gas contains an even larger amount of component B to prevent generation of mist. It is possible to lower the concentration of the condensable components and, at the same time, increase the concentration of component A in the supply gas to gas separation membrane S, and reduce the burden of the selective separation treatment by gas separation membrane S, by the primary cooling treatment and primary vapor-liquid separation treatment of the feed gas. Moreover, it is possible to secure a higher yield ratio while preventing liquefaction in the primary side gas of gas separation membrane S by controlling residual gas pressure Pr from concentration X of component A in the residual gas using the pre-analyzed correlation function.
  • heating section H in by-product gas flow path G to gas separation membrane S. It is necessary to conduct gas separation at an adequate temperature to suit the characteristics and use of gas separation membrane S since if liquid mist is contained in the feed gas, there is a risk of causing deterioration of gas separation membrane S itself. Moreover, when condensable components are contained in the feed gas, there is a risk of liquefaction at ambient temperature, and if this condensable component is poorly- permeable gas (component B), there is a risk of component B in the primary side gas (non-permeable side) of gas separation membrane S to condense and liquefy as the gas separation proceeds.
  • component B poorly- permeable gas
  • Figure 5 shows compositional example 2 of gas production process pertaining to this invention. While the basic composition is the same as compositional example 1 , it uses multiple stages of gas separation membranes S1 , S2, — Sn, connects the residual gas flow path of the earlier stages of the gas separation membranes to the supply gas flow path of the latter stages of the gas separation membranes to form a cascade connection.
  • Figure 5 shows a composition in which two gas separation membranes are used, and is hereinafter referred to as "this Process 3.” That is, by connecting primary residual gas flow path R1 of primary gas separation membrane S1 to the supply gas flow path of secondary gas separation membrane S2, it is possible to collect the primary permeable gas from primary permeable gas flow path T1 and the secondary permeable gas from secondary permeable gas flow path T2.
  • Pressure control means PCrI pressure control valve PCV1 and pressure controller PC1
  • pressure control means PCr2 pressure control valve PCV2 and pressure controller PC2
  • PCrI pressure control valve PCV1 and pressure controller PC1
  • PCr2 pressure control valve PCV2 and pressure controller PC2
  • heating section H1 in feed gas flow path Uo to primary gas separation membrane S1 , and heating section H2 in primary residual gas flow path R1 to secondary gas separation membrane S2.
  • FIG. 7 A modified example of this Process 3 (this Process 4) is shown in figure 7. While the basic composition is the same as compositional example 2, in figure 7, cooling section C, vapor-liquid separation section D, by-product gas flow path G, heating section H, and by-product liquid flow path L are added between feed gas flow path Uo and primary gas separation membrane S1 , as well as pressure control means PCr (pressure control valve PCVo and pressure controller PCo) in by-product gas flow path G and liquid surface detection section LC1 and control valve LCV1 in by-product liquid flow path L so that a primary treatment of the feed gas can be pre-applied.
  • This Process 4 as with this Process 2, is desirable for application in cases the feed gas contains a large amount of poorly-permeable and condensable components.
  • the general control method depends on individual circumstance.
  • the following three viewpoints are described regarding the adjustment method pertaining to prevention of liquefaction in the primary side gas of the gas separation membrane.
  • Equation 1 The basic balance of a multicomponent type composed of n types of molecules is expressed by equation 1 below.
  • ⁇ i x yi x P Yi x xi x Pi° — (equation 1 )
  • P denotes pressure
  • ⁇ i denotes fugacity coefficient
  • vi denotes activation coefficient
  • Pi°de denotes vapor pressure of pure component
  • xi and yi represent molar fractions of liquid phase and gaseous phase respectively.
  • Equation 2 Equation 2
  • Equation 4-2 can be expressed from conditions of equation 4-1 below. [Equation 4] — (equation 4-1 )
  • equation 5 can be expressed.
  • Equation 6 yif • (1 - X) / (1 - Xo) — (equation 6) That is, it shows that every mole type except the first type is concentrated at multiplication of (1 - X) / (1 - Xo). Evaluating residual gas dew point Z at residual gas pressure Pr with the above approximate representation according to equation 3-2, equation 7 below can be expressed. [Equation 7]
  • the material of the gas separation membranes, both primary and secondary gas separation membranes, used in the analysis was polyamide.
  • the temperature of the feed gas at the entrance of the gas separation membrane was 90 0 C, unless otherwise noted.
  • the reference of residual gas dew point Z is set at 80 0 C (gas temperature -
  • the reference of the supply pressure to the primary gas separation membrane was set at 30.8bar (abs) unless otherwise noted, when the feed gas flow rate is maximum.
  • the yield ratio rose notably as the volume reduction progressed as shown in table 2. At this pressure level, condensation did not occur even when the feed gas was cooled to 40 0 C.
  • Pe represents residual gas pressure corresponding to concentration X of component A expected from the correlation function.
  • Residual gas pressure Pr was adjusted according to this equation and the analysis was made.
  • the verification results are shown in table 13.
  • the verification results of the primary layer were the same as table 2.
  • the hydrogen yield ratio rose notably in response to the degree of volume reduction.
  • FC1 Flow rate controllers
  • FCrI FCrI , FCr2 Flow rate control means
  • FCV1 FCV2 Flow rate control valves

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
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  • Hydrogen, Water And Hydrids (AREA)
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Abstract

L'invention porte sur un procédé de production de gaz qui sépare un gaz d'alimentation contenant de multiples composants comprenant au moins un composant A hautement perméable et non condensable, et un composant B faiblement perméable et condensable en un gaz riche en composant A hautement perméable et non condensable et un gaz résiduel ayant une concentration réduite des composants A mentionnés ci-dessus, à l'aide de membranes de séparation de gaz présentant une perméabilité sélective. Ce procédé de production est caractérisé par les opérations consistant à : régler une valeur de référence Za pour le point de rosée Z sous pression au niveau de la voie d'écoulement immédiatement après la sortie de gaz résiduel des membranes de séparation de gaz mentionnées ci-dessus, et analyser de façon pré-opérationnelle la fonction de corrélation entre la pression du gaz résiduel provenant des membranes de séparation de gaz mentionnées ci-dessus et la concentration du composant A mentionné ci-dessus dans le gaz résiduel, sur la base des caractéristiques du gaz d'alimentation et des membranes de séparation de gaz mentionnées ci-dessus, surveiller, lors du fonctionnement, l'état du point de rosée Z mentionné ci-dessus pour qu'il soit inférieur à la valeur de référence Za mentionnée ci-dessus à l'aide de la fonction de corrélation mentionnée ci-dessus, et de la valeur mesurée de la concentration du composant A mentionné ci-dessus dans le gaz résiduel, et dans le cas où le point de rosée Z mentionné ci-dessus dépasse la valeur de référence Za mentionnée ci-dessus, l'ajuster soit avec la pression de gaz résiduel des membranes de séparation de gaz mentionnées ci-dessus, la pression de gaz perméable, soit une valeur de traitement qui est reliée à ces valeurs pour la maintenir au-dessous de la valeur de référence Za mentionnée ci-dessus et empêcher une liquéfaction dans le gaz côté primaire des membranes de séparation de gaz mentionnées ci-dessus.
PCT/EP2008/061870 2007-09-07 2008-09-08 Procédé de production de gaz à l'aide de membranes de séparation de gaz WO2009030777A1 (fr)

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FR2227037A1 (en) * 1973-04-30 1974-11-22 Skarstrom Charles Selectively separating esp drying gas mixts - selected constituents permeate from higher side of membrane
FR2571270A1 (fr) * 1984-10-04 1986-04-11 Petroles Cie Francaise Circuit de permeation pour gaz contenant des hydrocarbures
DE4432482A1 (de) * 1994-09-13 1996-03-14 Akzo Nobel Nv Vorrichtung zur Trocknung gasförmiger Medien
EP0974389A2 (fr) * 1998-07-22 2000-01-26 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et dispositif pour la récupération d'un composant gazeux à partir d'un mélange de gaz
FR2781390A1 (fr) * 1998-07-22 2000-01-28 Air Liquide Procede et installation pour la purification d'un gaz contenant des impuretes lourdes
JP2002035530A (ja) * 2000-07-28 2002-02-05 Ube Ind Ltd ガス分離膜の運転方法
WO2007099242A2 (fr) * 2006-03-01 2007-09-07 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Controle du traitement d'un gaz hydrogene par voie membranaire

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Publication number Priority date Publication date Assignee Title
FR2227037A1 (en) * 1973-04-30 1974-11-22 Skarstrom Charles Selectively separating esp drying gas mixts - selected constituents permeate from higher side of membrane
FR2571270A1 (fr) * 1984-10-04 1986-04-11 Petroles Cie Francaise Circuit de permeation pour gaz contenant des hydrocarbures
DE4432482A1 (de) * 1994-09-13 1996-03-14 Akzo Nobel Nv Vorrichtung zur Trocknung gasförmiger Medien
EP0974389A2 (fr) * 1998-07-22 2000-01-26 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et dispositif pour la récupération d'un composant gazeux à partir d'un mélange de gaz
FR2781390A1 (fr) * 1998-07-22 2000-01-28 Air Liquide Procede et installation pour la purification d'un gaz contenant des impuretes lourdes
JP2002035530A (ja) * 2000-07-28 2002-02-05 Ube Ind Ltd ガス分離膜の運転方法
WO2007099242A2 (fr) * 2006-03-01 2007-09-07 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Controle du traitement d'un gaz hydrogene par voie membranaire

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