US20010003949A1 - Permeation installation - Google Patents
Permeation installation Download PDFInfo
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- US20010003949A1 US20010003949A1 US09/734,213 US73421300A US2001003949A1 US 20010003949 A1 US20010003949 A1 US 20010003949A1 US 73421300 A US73421300 A US 73421300A US 2001003949 A1 US2001003949 A1 US 2001003949A1
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- permeation
- gaseous mixture
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
- B01D63/02—Hollow fibre modules
- B01D63/04—Hollow fibre modules comprising multiple hollow fibre assemblies
- B01D63/043—Hollow fibre modules comprising multiple hollow fibre assemblies with separate tube sheets
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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
- B01D53/225—Multiple stage diffusion
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2313/00—Details relating to membrane modules or apparatus
- B01D2313/23—Specific membrane protectors, e.g. sleeves or screens
Definitions
- the present invention relates to permeation installations.
- the technique or process of permeation permits the separation of a gas from a mixture of gases in gaseous phase with the help of porous walls.
- This technique consists in applying under a relatively high pressure of the order of several tens of bars, the gaseous mixture in the environment of a bundle of hollow fibers produced from polymer of a particular type. Under the influence of the pressure and because of the nature of the material, the molecules of a gas will be adsorbed selectively by the material constituting the hollow fibers, passing through the pores of these porous fibers and will be recovered by desorption within the channel of very small size existing in these fibers. On the other hand, the gas or gases corresponding to the other molecules will not pass or will very little pass through the porous wall and will remain outside the bundle of hollow porous fibers.
- a so-called sweeping gas flow of a different composition than the permeate, is introduced within the fibers, from the side opposite that for recovery of the permeate.
- This injection has for its object to increase the yield by recuperation of the gas preferentially passing through the fibers.
- FIG. 1 there is schematically shown a permeator. It comprises an external chamber 10 resistant to pressure, within which is mounted a bundle 12 of hollow porous fibers.
- the gaseous mixture is introduced by the nozzle 14 disposed at the lower end of the chamber 10 .
- the gas under pressure surrounds the bundle of hollow fibers.
- the fraction of the gas which passes through the hollow wall penetrates the channels of the fibers and is recovered at one end of these latter in a chamber 16 , the latter being connected to an outlet conduit 18 for the fraction of the gaseous mixture having passed through the wall of the fibers and which will ultimately be called permeate and indicated by the letter P.
- the fraction of the gaseous mixture which did not pass through the wall of the fibers is recovered, preferably with a tube provided with perforations 20 which extends axially along the bundle of fibers 12 .
- This fraction of the gaseous mixture leaves the chamber 10 by the nozzle 22 connected to the perforated tube 20 .
- the fraction of the gaseous mixture that did not pass through the wall of the hollow fibers will ultimately be called non-permeate and indicated by the letter R.
- the gaseous mixture is introduced via the central tube 22 and the non-permeate is recovered in the chamber 20 .
- the pressure of the gaseous mixture is relatively high, typically in the order of several tens of bars. It is thus necessary that the external chamber 10 with resistance to pressure have a relatively great wall thickness and the different nozzles such as 18 and 22 passing through this wall must also be made precisely to maintain the resistance to pressure of the chamber 10 .
- each permeation module be supplied by a predetermined gaseous flow rate, departing from this flow rate gives rise to a very great decrease in the output of the installation.
- An object of the present invention is to provide a permeation chamber in which several permeator or several permeation modules are disposed one beside the other within a single pressure resistant chamber whose dimension is reduced whilst permitting an overall higher output from this installation.
- the permeation installation comprises:
- each module being constituted by at least one permeator formed of hollow fibers with a porous wall and being disposed within an envelope provided with perforations placing in communication the external portion of each module and the common gaseous circuit,
- [0016] means to recover the fraction of the gaseous mixture that has passed through the wall of said fibers
- [0017] means to recover the fraction of the gaseous mixture that has not passed through the wall of said fibers.
- the modules are supplied with substantially equal flow rates for the different modules and with a good distribution of the flows for each module, thereby permitting the optimum operation of each permeation module and accordingly the optimum operation of the unit.
- the perforated envelopes are disposed at the interface of two gaseous media whose pressures are not very different. These envelopes can therefore have a relatively simple mechanical construction.
- the perforators are interposed in the supply circuit of the gaseous mixture to the permeation modules.
- the perforations are interposed in the recovery circuit of the fraction of the gaseous mixture that has not passed through the walls of the fibers of the permeators (non-permeate).
- each permeation module has a generally cylindrical shape
- each envelope has a cylindrical shape surrounding said permeation module over all its axial length and said cylindrical envelope is perforated in its lateral portion and is closed at each of its ends by a closed wall.
- each permeation module has a generally cylindrical shape, each permeation module is surrounded over all its length by an imperforate cylindrical wall and an imperforate plate closes one end of the imperforate cylindrical wall, another end plate having said perforations.
- the pressure drop created by said perforations is comprised between 10 and 90% of the total pressure drop between the inlet of the installation and the outlet for the fraction of the gaseous mixture that has not passed through the wall of the fibers, and preferably between 15 and 60%.
- FIG. 1 already described, shows schematically a permeator of the prior art
- FIG. 1A shows in simplified fashion a permeator that can be used with several permeation modules disposed side by side;
- FIG. 2 is a simplified view of a first embodiment of a permeation installation according to the invention.
- FIG. 3 shows in simplified manner a second embodiment of the permeation installation
- FIG. 4 shows in simplified manner a third embodiment of the permeation installation
- FIG. 5 shows in simplified manner a fourth embodiment of the permeation installation
- FIG. 6 shows in vertical cross-section a detailed example of embodiment of the permeation installation according to the embodiments of FIG. 3;
- FIG. 6A is a cross-sectional view on the line A-A of FIG. 6;
- FIG. 7 is a fragmentary view of FIG. 6 showing the recovery of the permeate and of the non-permeate in a permeation module.
- FIG. 7A is a cross-sectional view on the line A-A of FIG. 7.
- FIG. 2 there will be described a first embodiment of the permeation installation.
- the pressure resistant chamber 30 provided with its nozzle 32 for the introduction of the gaseous mixture F.
- two permeators 34 and 36 which could also be permeation modules constituted by several permeators mounted one above the other.
- Each permeation module 34 , 36 is disposed within an envelope constituted by a cylindrical wall 38 which extends over all the height of the permeation module and which is closed at its ends by two plates 40 and 42 .
- the sidewall 38 is perforated, with perforations of calibrated diameters, whilst the plates 40 and 42 are imperforate.
- tubing 44 for the recovery of the non-permeate R and the tubing 46 for recovery of the permeate P recovered within the hollow fibers constituting the permeators 34 , 36 .
- FIG. 3 shows in a simplified manner a second embodiment of the permeation installation.
- the latter again comprises the external pressure chamber 30 with its nozzle 32 for introduction of the gaseous mixture to be treated under pressure.
- the permeators or permeation modules 34 and 36 are disposed in individual envelopes constituted by a cylindrical wall 50 extending over all the height of the permeation module, this wall 50 being imperforate.
- a first end of the lateral 50 is closed by an imperforate plate 52 , whilst its second end is closed by a plate 54 provided with perforations of calibrated dimensions. The same is true for all the permeators or permeation modules contained within the chamber.
- the perforated plates 54 divided the entering flow and impose pressure drops which can be adjusted with high precision to obtain for each permeation module a same flow rate corresponding to the optimum operation of the permeation module.
- the envelopes 50 , 52 , 54 can be made with a relatively less thickness, because the pressure on their two surfaces is substantially the same.
- the non-permeate R is recovered by the tubes 44 and leaves the chamber 30 by the nozzle 55 .
- the installation has the same structure as that of FIG. 2. The difference resides in the circulation of the different gas flows.
- the gaseous mixture F to be treated is introduced into the permeators through the interior tubes 44 , whilst the non-permeate R is recovered through the outlet nozzle 32 of envelope 30 .
- the perforated envelope ( 38 , 40 , 42 ) is disposed in the flow R of non-permeate leaving the permeators.
- the installation has the same structure as that of FIG. 3. Only the circulation of the different gas flows is modified.
- the gaseous mixture F to be treated is introduced into the chamber 30 through the nozzle 55 and the non-permeate R is recovered through the nozzle 32 after having passed through the perforations of the plates 54 .
- each perforated envelope interposed between the introduction nozzle for the mixture into the chamber and each permeation module, or between each permeator and the recovery nozzle of the non-permeate permits defining very precisely the circulatory flow rate through each permeation module. It will also be understood that this pressure drop can be defined in such a manner as to be very much greater than the pressure drop resulting from the normal circulation of the gaseous mixture within the pressure resistant chamber and at the exterior of the envelope surrounding each permeation module. There can also be a certain number of permeation modules beside each other in a pressure resistant chamber of reduced dimensions. It will also be understood that the pressure on opposite sides of the perforated plates is relatively identical and that the plates can therefore be made of sheet metal of a thickness that is also relatively reduced.
- the pressure drop created by the perforated envelopes is comprised between 10 and 90% of the total pressure drop between the inlet of the installation and the non-permeate outlet. Preferably, this pressure drop is comprised between 15 and 60%.
- the total surface of the perforations represents from 0.1 to 3 times the cross-section of the supply nozzle for gaseous mixture (FIGS. 2 and 3) or this same proportion of the cross-section of the outlet nozzle for the non-permeate (FIGS. 4 and 5). Again preferably, these ranges are comprised between 0.5 and 2 times the cross-sectional area of the nozzle.
- the perforations can also be predetermined by the perforation that their total surface represents relative to the total surface of the perforated envelope. This proportion is preferably below 10% and again preferably below 1%.
- FIGS. 6 and 7 there will be described in greater detail a preferred embodiment of the permeation installation according to the principle shown in FIG. 3.
- FIG. 6 there is shown the external pressure resistant chamber 70 of the permeation installation which is constituted by a cylindrical sidewall 72 , by a bolted cover 74 and by a semispherical end cap 76 .
- Each permeation module is surrounded over all its length by a cylindrical envelope 94 whose upper end is closed by a plate 96 and whose lower end is closed by a lower perforated plate 98 which is connected in sealed fashion to the plate 80 or which is integral with it.
- the perforations such as 100 in the perforated plates 98 open directly into the supply chamber 81 and thereby permit creating a pressure drop between the introduction nozzle 78 and each permeation module 82 , 86 and 88 .
- the perforations are preferably disposed on a same circle relative to the longitudinal axis of the permeation modules, thereby permitting providing a homogeneous circulation over all the periphery of the module.
- FIGS. 7 and 7A The recovery of the permeate P and of the non-permeate R will be better understood with reference to FIGS. 7 and 7A, in which there is shown a portion of a permeation module. More precisely, in FIG. 7, there is shown for example the permeator 90 and the permeator 92 of the permeation module 82 . There is also shown the envelope 94 . At the upper end of the bundle of hollow fibers constituting the permeator 90 , is seen an annular chamber 102 for recovery of the permeate within the hollow fibers. The recovery of the non-permeate is carried out through a perforated tube 104 which is disposed in an axial passage 106 of each permeator.
- the permeation installations according to the invention can have numerous applications, particularly the purification of hydrogen.
- the permeate is thus the hydrogen of which it is desired that the purity be above 80% in total moles of permeate, preferably greater than 85%.
- the installation operates at a temperature comprised between 40 and 120° C.
- Another installation consists in obtaining a mixture of predetermined composition, of hydrogen and a gas selected from CO, N 2 , Ar, CO 2 and He.
- the mixture is the non-permeate R.
- the installation operates at a temperature comprised between 60 and 90° C.
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- Chemical Kinetics & Catalysis (AREA)
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
- The present invention relates to permeation installations.
- The technique or process of permeation permits the separation of a gas from a mixture of gases in gaseous phase with the help of porous walls. This technique consists in applying under a relatively high pressure of the order of several tens of bars, the gaseous mixture in the environment of a bundle of hollow fibers produced from polymer of a particular type. Under the influence of the pressure and because of the nature of the material, the molecules of a gas will be adsorbed selectively by the material constituting the hollow fibers, passing through the pores of these porous fibers and will be recovered by desorption within the channel of very small size existing in these fibers. On the other hand, the gas or gases corresponding to the other molecules will not pass or will very little pass through the porous wall and will remain outside the bundle of hollow porous fibers.
- In certain embodiments, a so-called sweeping gas flow, of a different composition than the permeate, is introduced within the fibers, from the side opposite that for recovery of the permeate. This injection has for its object to increase the yield by recuperation of the gas preferentially passing through the fibers.
- This embodiment somewhat complicates the technique of permeators and is not described in what follows. The invention can also be applied to this type of embodiment.
- In the accompanying FIG. 1, there is schematically shown a permeator. It comprises an
external chamber 10 resistant to pressure, within which is mounted abundle 12 of hollow porous fibers. The gaseous mixture is introduced by thenozzle 14 disposed at the lower end of thechamber 10. The gas under pressure surrounds the bundle of hollow fibers. The fraction of the gas which passes through the hollow wall penetrates the channels of the fibers and is recovered at one end of these latter in achamber 16, the latter being connected to an outlet conduit 18 for the fraction of the gaseous mixture having passed through the wall of the fibers and which will ultimately be called permeate and indicated by the letter P. On the other hand, the fraction of the gaseous mixture which did not pass through the wall of the fibers is recovered, preferably with a tube provided withperforations 20 which extends axially along the bundle offibers 12. This fraction of the gaseous mixture leaves thechamber 10 by thenozzle 22 connected to theperforated tube 20. The fraction of the gaseous mixture that did not pass through the wall of the hollow fibers will ultimately be called non-permeate and indicated by the letter R. - In another embodiment, the gaseous mixture is introduced via the
central tube 22 and the non-permeate is recovered in thechamber 20. - As already indicated, the pressure of the gaseous mixture is relatively high, typically in the order of several tens of bars. It is thus necessary that the
external chamber 10 with resistance to pressure have a relatively great wall thickness and the different nozzles such as 18 and 22 passing through this wall must also be made precisely to maintain the resistance to pressure of thechamber 10. - It will be understood that it is thus interesting to have
several permeator 12 within the same pressureresistant chamber 10. This has already been proposed, particularly in U.S. Pat. No. 4,874,405, which discloses a permeation module consisting of several individual permeators disposed one above the other, these permeators being disposed in a same pressure resistant chamber. - However, it appears that, for reasons both technical and economical, it is difficult to have more than three permeators one above the other within a same chamber. However, there exists a certain number of situations in which it is desired to be able to process volumes of gaseous mixture with relatively high flow rates which are not compatible with the use of three permeators disposed one above the other.
- To solve this problem, it could be envisaged to arrange within a same pressure chamber (shown at24 in the accompanying FIG. 1A), several permeations ensembles, such as 26, disposed one beside the others. In FIG. 1A, there is also shown the
inlet nozzle 28 for the gaseous mixture to be treated in thepressure chamber 24. However, it is important in such an installation that each permeation module be supplied by a predetermined gaseous flow rate, departing from this flow rate gives rise to a very great decrease in the output of the installation. To solve this problem, there can be envisaged provision ofdifferent permeation modules 26 in a pressureresistant chamber 24 of large dimension, such that the flow rates for each permeation module will be substantially the same. It will be understood, however, that such a solution is unacceptable because it leads to a very great increase in the cost of the installation because of the large dimensions of the pressureresistant chamber 24 and hence in particular the increase of the wall thickness of this chamber. - An object of the present invention is to provide a permeation chamber in which several permeator or several permeation modules are disposed one beside the other within a single pressure resistant chamber whose dimension is reduced whilst permitting an overall higher output from this installation.
- To achieve this object, according to the invention, the permeation installation comprises:
- a single pressure resistant chamber,
- at least two permeation modules disposed within said chamber, each module being constituted by at least one permeator formed of hollow fibers with a porous wall and being disposed within an envelope provided with perforations placing in communication the external portion of each module and the common gaseous circuit,
- means to supply said installation with a gaseous mixture to be processed,
- means to recover the fraction of the gaseous mixture that has passed through the wall of said fibers;
- means to recover the fraction of the gaseous mixture that has not passed through the wall of said fibers.
- It will be understood that, thanks to the interposition of the perforated envelopes constituting pressure drops in the common gaseous circuit, the modules are supplied with substantially equal flow rates for the different modules and with a good distribution of the flows for each module, thereby permitting the optimum operation of each permeation module and accordingly the optimum operation of the unit. It will be moreover understood that the perforated envelopes are disposed at the interface of two gaseous media whose pressures are not very different. These envelopes can therefore have a relatively simple mechanical construction.
- According to a first embodiment, the perforators are interposed in the supply circuit of the gaseous mixture to the permeation modules. According to a second embodiment, the perforations are interposed in the recovery circuit of the fraction of the gaseous mixture that has not passed through the walls of the fibers of the permeators (non-permeate).
- It will be understood that, in these two cases, the pressure drop which results permits substantially equalizing the gaseous flow rate in all the permeation modules.
- According to a first embodiment of the installation, each permeation module has a generally cylindrical shape, each envelope has a cylindrical shape surrounding said permeation module over all its axial length and said cylindrical envelope is perforated in its lateral portion and is closed at each of its ends by a closed wall.
- According to a second embodiment of the invention, each permeation module has a generally cylindrical shape, each permeation module is surrounded over all its length by an imperforate cylindrical wall and an imperforate plate closes one end of the imperforate cylindrical wall, another end plate having said perforations.
- Preferably, the pressure drop created by said perforations is comprised between 10 and 90% of the total pressure drop between the inlet of the installation and the outlet for the fraction of the gaseous mixture that has not passed through the wall of the fibers, and preferably between 15 and 60%.
- Another characteristics and advantages of the invention will become better apparent from a reading of the description which follows, of several embodiments of the invention, given by way of non-limiting example. The description refers to the accompanying figures, in which:
- FIG. 1, already described, shows schematically a permeator of the prior art;
- FIG. 1A, already described, shows in simplified fashion a permeator that can be used with several permeation modules disposed side by side;
- FIG. 2 is a simplified view of a first embodiment of a permeation installation according to the invention;
- FIG. 3 shows in simplified manner a second embodiment of the permeation installation;
- FIG. 4 shows in simplified manner a third embodiment of the permeation installation;
- FIG. 5 shows in simplified manner a fourth embodiment of the permeation installation;
- FIG. 6 shows in vertical cross-section a detailed example of embodiment of the permeation installation according to the embodiments of FIG. 3;
- FIG. 6A is a cross-sectional view on the line A-A of FIG. 6;
- FIG. 7 is a fragmentary view of FIG. 6 showing the recovery of the permeate and of the non-permeate in a permeation module; and
- FIG. 7A is a cross-sectional view on the line A-A of FIG. 7.
- A permeation installation according to the invention can belong to four different types, on the one hand, according to whether the envelope is perforated in its lateral portion (FIGS. 2 and 4) or at one of its ends (FIGS. 3 and 5) and on the other hand, according to the position of the perforated envelopes relative to the different gas flows, the perforated envelope being interposed within the gaseous mixture to be treated (FIGS. 2 and 3) or in the flow of non-permeate (FIGS. 4 and 5).
- Referring first to FIG. 2, there will be described a first embodiment of the permeation installation. In this simplified figure, there is shown the pressure
resistant chamber 30 provided with itsnozzle 32 for the introduction of the gaseous mixture F. In each figure, there is also shown twopermeators permeation module cylindrical wall 38 which extends over all the height of the permeation module and which is closed at its ends by twoplates sidewall 38 is perforated, with perforations of calibrated diameters, whilst theplates tubing 44 for the recovery of the non-permeate R and thetubing 46 for recovery of the permeate P recovered within the hollow fibers constituting thepermeators - It will be understood that thanks to the pressure drop resulting from the
perforations 38, the different permeators orpermeation modules gaseous mixture 32 to thepermeators lateral walls 38 and theend plates chamber 30 within theenvelopes 38. Theseenvelopes 38 can thus have a reduced thickness and very much less than the thickness of theexternal chamber 30. - FIG. 3 shows in a simplified manner a second embodiment of the permeation installation. The latter again comprises the
external pressure chamber 30 with itsnozzle 32 for introduction of the gaseous mixture to be treated under pressure. There are seen the permeators orpermeation modules cylindrical wall 50 extending over all the height of the permeation module, thiswall 50 being imperforate. A first end of the lateral 50 is closed by an imperforate plate 52, whilst its second end is closed by aplate 54 provided with perforations of calibrated dimensions. The same is true for all the permeators or permeation modules contained within the chamber. It will be understood that, as in the first embodiment, theperforated plates 54 divided the entering flow and impose pressure drops which can be adjusted with high precision to obtain for each permeation module a same flow rate corresponding to the optimum operation of the permeation module. As in the case of the first embodiment, theenvelopes tubes 44 and leaves thechamber 30 by thenozzle 55. - In the embodiment shown in FIG. 4, the installation has the same structure as that of FIG. 2. The difference resides in the circulation of the different gas flows. The gaseous mixture F to be treated is introduced into the permeators through the
interior tubes 44, whilst the non-permeate R is recovered through theoutlet nozzle 32 ofenvelope 30. The perforated envelope (38, 40, 42) is disposed in the flow R of non-permeate leaving the permeators. - According to the embodiment of FIG. 5, the installation has the same structure as that of FIG. 3. Only the circulation of the different gas flows is modified. The gaseous mixture F to be treated is introduced into the
chamber 30 through thenozzle 55 and the non-permeate R is recovered through thenozzle 32 after having passed through the perforations of theplates 54. - It follows that the number of permeators or of permeation modules is typically greater than 2, as is shown in simplified manner in FIGS.2 to 5. This number can be equal to 3, 5 or 7, which permits optimum filling of the interior of the
chamber 30. - It will be understood that no matter what the embodiment in question, the pressure drop created by each perforated envelope interposed between the introduction nozzle for the mixture into the chamber and each permeation module, or between each permeator and the recovery nozzle of the non-permeate, permits defining very precisely the circulatory flow rate through each permeation module. It will also be understood that this pressure drop can be defined in such a manner as to be very much greater than the pressure drop resulting from the normal circulation of the gaseous mixture within the pressure resistant chamber and at the exterior of the envelope surrounding each permeation module. There can also be a certain number of permeation modules beside each other in a pressure resistant chamber of reduced dimensions. It will also be understood that the pressure on opposite sides of the perforated plates is relatively identical and that the plates can therefore be made of sheet metal of a thickness that is also relatively reduced.
- Preferably, the pressure drop created by the perforated envelopes is comprised between 10 and 90% of the total pressure drop between the inlet of the installation and the non-permeate outlet. Preferably, this pressure drop is comprised between 15 and 60%.
- It can also be indicated that, preferably, the total surface of the perforations represents from 0.1 to 3 times the cross-section of the supply nozzle for gaseous mixture (FIGS. 2 and 3) or this same proportion of the cross-section of the outlet nozzle for the non-permeate (FIGS. 4 and 5). Again preferably, these ranges are comprised between 0.5 and 2 times the cross-sectional area of the nozzle.
- The perforations can also be predetermined by the perforation that their total surface represents relative to the total surface of the perforated envelope. This proportion is preferably below 10% and again preferably below 1%.
- Referring now to FIGS. 6 and 7, there will be described in greater detail a preferred embodiment of the permeation installation according to the principle shown in FIG. 3.
- In FIG. 6, there is shown the external pressure
resistant chamber 70 of the permeation installation which is constituted by acylindrical sidewall 72, by a boltedcover 74 and by a semispherical end cap 76. - The bottom76 of the pressure chamber is provided with a
nozzle 78 for the introduction of the gaseous mixture to be processed. The lower portion of the chamber is separated from the rest of the latter by aplate 80 which thereby defines, at the lower end of the chamber, asingle supply chamber 81. In this figure, there are also shown twopermeation modules third permeation module 86. Each permeation module comprises three unitary permeators generally indicated at 88, 90 and 92, disposed in series one above the other. Each permeation module is surrounded over all its length by acylindrical envelope 94 whose upper end is closed by aplate 96 and whose lower end is closed by a lowerperforated plate 98 which is connected in sealed fashion to theplate 80 or which is integral with it. Thus, the perforations such as 100 in theperforated plates 98 open directly into thesupply chamber 81 and thereby permit creating a pressure drop between theintroduction nozzle 78 and eachpermeation module - The recovery of the permeate P and of the non-permeate R will be better understood with reference to FIGS. 7 and 7A, in which there is shown a portion of a permeation module. More precisely, in FIG. 7, there is shown for example the
permeator 90 and thepermeator 92 of thepermeation module 82. There is also shown theenvelope 94. At the upper end of the bundle of hollow fibers constituting thepermeator 90, is seen anannular chamber 102 for recovery of the permeate within the hollow fibers. The recovery of the non-permeate is carried out through aperforated tube 104 which is disposed in anaxial passage 106 of each permeator. The perforated tube thus permits recovering the non-permeate which arrives at theupper end 108 of theperforated tube 104 above theplates 96 closing theenvelopes 94 surrounding each permeation module. The non-permeate thus arrives in theupper space 110 of the external chamber and redescends into the vertical spaces limited on the one hand by thecylindrical sidewall 72 of the external chamber, and on the other hand by theenvelopes 94 of the permeation modules. The non-permeate R is recovered through theoutlet nozzle 112 disposed at the lower end of thecylindrical sidewall 72 above theplate 80. - It will be understood that thanks to this arrangement, the assembly of the permeation modules is surrounded by a circulation of gas corresponding to the non-permeate which is also located along the external wall of the permeation installation. This circulation permits maintaining a very homogeneous temperature during operation of the modules by preventing any contact between the gas to be treated and the external medium, generally at a substantially lower temperature, thereby to obtain optimum performance.
- Returning to FIG. 7, it will be seen that the recovery of the permeate is carried out through an
axial tube 114 introduced into theperforated tube 104. At the level of eachchamber 102 for recovery of the permeate,tubing 116 connects thetube 114 to thechambers 102. The upper end of thetube 114 is closed whilst its lower end passes through the bulbous portion 76 of the external envelope to be connected tonozzles 118. - The permeation installations according to the invention can have numerous applications, particularly the purification of hydrogen.
- The permeate is thus the hydrogen of which it is desired that the purity be above 80% in total moles of permeate, preferably greater than 85%. The installation operates at a temperature comprised between 40 and 120° C.
- Another installation consists in obtaining a mixture of predetermined composition, of hydrogen and a gas selected from CO, N2, Ar, CO2 and He. In this case, the mixture is the non-permeate R. The installation operates at a temperature comprised between 60 and 90° C.
Claims (15)
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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FR9915755 | 1999-12-14 | ||
FR9915755A FR2802115B1 (en) | 1999-12-14 | 1999-12-14 | PERMEATION INSTALLATION |
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US20010003949A1 true US20010003949A1 (en) | 2001-06-21 |
US6451090B2 US6451090B2 (en) | 2002-09-17 |
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US09/734,213 Expired - Fee Related US6451090B2 (en) | 1999-12-14 | 2000-12-12 | Permeation installation |
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US (1) | US6451090B2 (en) |
EP (1) | EP1108459A1 (en) |
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US20050211097A1 (en) * | 2004-03-26 | 2005-09-29 | Thomas Eckman | Apparatus for permeate side sweep of fiber membrane permeators |
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US4352736A (en) * | 1980-12-08 | 1982-10-05 | Toyo Boseki Kabushiki Kaisha | Wound flattened hollow fiber assembly having plural spaced core sections |
JPS57102202A (en) * | 1980-12-18 | 1982-06-25 | Toyobo Co Ltd | Fluid separator |
US4670145A (en) * | 1986-07-08 | 1987-06-02 | E. I. Du Pont De Nemours And Company | Multiple bundle fluid separation apparatus |
DE8802771U1 (en) * | 1988-03-02 | 1989-07-06 | Akzo Patente GmbH, 5600 Wuppertal | Material and/or heat exchanger |
US4874405A (en) * | 1989-02-14 | 1989-10-17 | W. R. Grace & Co.-Conn. | Coupling fluid separation membrane elements |
US5071552A (en) * | 1990-12-20 | 1991-12-10 | Union Carbide Industrial Gases Technology Corporation | Multiple bundle fluid separation apparatus |
AU4279493A (en) * | 1992-05-18 | 1993-12-13 | Minntech Corporation | Hollow fiber filter cartridge and method of manufacture |
US5536405A (en) * | 1994-05-11 | 1996-07-16 | Uop | Stacked membrane disk assemblies for fluid separations |
US5470469A (en) * | 1994-09-16 | 1995-11-28 | E. I. Du Pont De Nemours And Company | Hollow fiber cartridge |
US5851267A (en) * | 1997-01-28 | 1998-12-22 | Uop Llc | Seal arrangement for rapid interconnection or axially arranged separation elements |
-
1999
- 1999-12-14 FR FR9915755A patent/FR2802115B1/en not_active Expired - Fee Related
-
2000
- 2000-11-24 EP EP00403299A patent/EP1108459A1/en not_active Withdrawn
- 2000-12-12 US US09/734,213 patent/US6451090B2/en not_active Expired - Fee Related
Cited By (5)
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US20100252501A1 (en) * | 2009-04-02 | 2010-10-07 | Greene William A | Quick connect modular water purification system |
US8333892B2 (en) * | 2009-04-02 | 2012-12-18 | Spintek Filtration, Inc. | Quick connect modular water purification system |
US20110146491A1 (en) * | 2009-12-02 | 2011-06-23 | Aisan Kogyo Kabushiki Kaisha | Separation membrane module and fuel vapor processing apparatus equipped with the same |
US8523982B2 (en) * | 2009-12-02 | 2013-09-03 | Aisan Kogyo Kabushiki Kaisha | Separation membrane module and fuel vapor processing apparatus equipped with the same |
CN114894691A (en) * | 2022-04-18 | 2022-08-12 | 中国电建集团西北勘测设计研究院有限公司 | Test system and method for determining permeability coefficient of homogeneous dam material |
Also Published As
Publication number | Publication date |
---|---|
FR2802115A1 (en) | 2001-06-15 |
US6451090B2 (en) | 2002-09-17 |
EP1108459A1 (en) | 2001-06-20 |
FR2802115B1 (en) | 2002-03-01 |
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