US20040000513A1 - Apparatus using solid perm-selective membranes in multiple groups for simultaneous recovery of specified products from a fluid mixture - Google Patents

Apparatus using solid perm-selective membranes in multiple groups for simultaneous recovery of specified products from a fluid mixture Download PDF

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US20040000513A1
US20040000513A1 US10/183,793 US18379302A US2004000513A1 US 20040000513 A1 US20040000513 A1 US 20040000513A1 US 18379302 A US18379302 A US 18379302A US 2004000513 A1 US2004000513 A1 US 2004000513A1
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modules
permeate
product
membrane
group
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Craig Colling
George Huff
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BP Corp North America Inc
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BP Corp North America Inc
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Priority to US10/185,825 priority Critical patent/US6830691B2/en
Priority to US10/183,793 priority patent/US20040000513A1/en
Assigned to BP CORPORATION NORTH AMERICA INC. reassignment BP CORPORATION NORTH AMERICA INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: COLLING, CRAIG W., HUFF JR., GEORGE A.
Priority to PCT/US2003/020182 priority patent/WO2004002609A2/en
Priority to ES03762078T priority patent/ES2388918T3/es
Priority to EP03762078A priority patent/EP1515790B1/en
Priority to AU2003247716A priority patent/AU2003247716B2/en
Publication of US20040000513A1 publication Critical patent/US20040000513A1/en
Priority to ZA200410341A priority patent/ZA200410341B/xx
Abandoned legal-status Critical Current

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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
    • 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
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/501—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by diffusion
    • C01B3/503—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by diffusion characterised by the membrane
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0405—Purification by membrane separation
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/048—Composition of the impurity the impurity being an organic compound
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency

Definitions

  • apparatus of the invention comprises modules using solid perm-selective membranes. More particularly, the invention relates to a plurality of membrane modules disposed in a first product group, a second product group, and optionally one or more intermediate groups. Apparatus of the invention with the membrane modules in multiple groups is beneficially useful for simultaneous recovery of a very pure permeate product and a desired non-permeate product from a mixture containing organic compounds.
  • Membranes useful for the separation of gaseous mixtures are of two very different types: one is microporous while the other is nonporous.
  • Discovery of the basic laws governing the selectivity for gases effusing through a microporous membrane is credited to T. Graham.
  • the permeate is enriched in the gas of the lower molecular weight.
  • Practical and theoretical enrichments achievable by this technique are very small because the molecular weight ratios of most gases are not very large and the concomitant selectivities are proportional to the square roots of these ratios.
  • Another aspect of the art is related to two-stage and/or multi-stage membrane separation processes and apparatus for removing a component from a fluid stream. Such systems may be considered when a desired separation cannot be completed using avaiable membrane materials in a single stage.
  • membrane permeator processes have been described, for example, S. Weller and W. Steiner published one of the first articles to address aspects of multi-stage membrane apparatus in “Engineering Aspects of Gases Fractional Permeation Through Membranes” in Chem. Eng. Prog. 46, 585-590 (1950).
  • U.S. Pat. Nos. 5,256,295 and 5,256,296 in the name of Richard W. Baker and Johannes G. Wijmans relate to membrane separation systems having an auxiliary membrane module installed across the pump that drives the main membrane unit, so that the permeate streams from the main and auxiliary membrane units are mixed and pass together through a common driving pump.
  • the concentration of the mixed permeate stream is said to build up by circulating the stream through the auxiliary unit, and where the concentration reaches a desired level, the mixed stream can be tapped and the product stream drawn off.
  • An auxiliary membrane module is also described as being installed across the second stage of the two-stage membrane separation system.
  • the driving force for the auxiliary module is provided by the pump or other driving unit for the first membrane stage.
  • the auxiliary module provides additional treatment of the residue stream from the second membrane stage, but is driven by the first stage driving unit.
  • Baker and Wijmans did not discover that the efficiency of this design can be dramatically improved by choosing a different feed position. Location of the feed position for multi-stage systems becomes critical to the recovery of two products.
  • U.S. Pat. Nos. 5,102,432 and 5,709,732 in the name of Ravi Prasad relate to three-stage membrane gas separation systems for air.
  • U.S. Pat. No. 5,102,432 is directed to production of very high purity nitrogen by separation of air in a three stage membrane system in which the permeate from the product stage is recycled to the intermediate second stage and permeate from this second stage is recycled to the feed stage with the membrane surface area being distributed between the stages to recovery a single purified product.
  • U.S. Pat. No. 5,709,732 is directed to production of purified oxygen gas (60-90% purity) from ambient air in systems of at least three permeator stages which together use less than one compressor per stage.
  • the permeate from the product stage is the purified oxygen gas
  • the non-permeate from the product stage is recycled to the intermediate stage (identified as stage 1)
  • non-permeate from this intermediate stage is recycled to the feed stage (identified as stage 2)
  • the non-permeate effluent of the feed stage is the oxygen depleted waste stream. Only a single purified product is recovered.
  • U.S. Pat. No. 5,873,928 in the name of Richard A. Callahan describes a membrane process for the production of a desired very high purity permeate gas by use of a two-stage membrane process.
  • a process feed gas mixture is provided to a primary unit comprising a membrane having a relatively high intrinsic permeability to provide an intermediate permeate gas and a retentate by-product, and the intermediate permeate gas is provided to a secondary membrane unit comprising a membrane having a relatively low intrinsic permeability to produce therefrom a very high purity permeate gas product.
  • the non-permeate from the secondary membrane unit is recycled with the feed gas mixture to the primary unit.
  • a further object of the invention is to provide inexpensive processes and apparatus for the efficient separation of chemical compounds from mixtures which are difficult to separate, e.g., separation of propane-propylene by fractional distillation.
  • Improved apparatus should provide for an integrated sequence, carried out with streams in gas and/or liquid state, using a suitable perm-selective membrane, preferably a solid perm-selective membrane which under a suitable differential of a driving force exhibits selective permeability of a desired product.
  • a suitable perm-selective membrane preferably a solid perm-selective membrane which under a suitable differential of a driving force exhibits selective permeability of a desired product.
  • apparatus using perm-selective membranes for simultaneous recovery of a very pure permeate product and a desired non-permeate product shall avoid or minimize formation of unwanted by-products, waste streams.
  • an improved separation apparatus shall efficiently employ perm-selective membranes having the same or different pre-selected permeabilities, and with optimum distribution between stages so as to efficiently produce very high purity product.
  • the present invention is directed to apparatus using solid perm-selective membranes for economical separation of fluid mixtures. More particularly, this invention relates to apparatus comprising a plurality of membrane modules disposed in a first product group, a second product group, and optionally one or more intermediate groups. Advantageously apparatus of the invention with the membrane modules in multiple groups is employed for simultaneous recovery of a very pure permeate product and a desired non-permeate product from a mixture containing organic compounds.
  • This invention contemplates the treatment of a fluid feedstock, e.g. various type organic materials, especially a fluid mixture of compounds of petroleum origin.
  • the fluid feedstock is a gaseous mixture comprising a more selectively permeable component and a less permeable component.
  • Apparatus of the invention are particularly useful in processes for treatment of a gaseous mixture comprised of a more selectively permeable alkene component and a corresponding alkane component, e.g. the separation of propylene from propane.
  • the invention provides apparatus using perm-selective membranes in multiple groups for simultaneous recovery of a very pure permeate product and a desired non-permeate product from a fluid mixture of compounds.
  • the apparatus comprises: a plurality of membrane modules disposed in a first product group, one or more intermediate groups, and a second product group, each module comprising a solid perm-selective membrane which under a suitable differential of a driving force exhibits a permeability of at least 0.1 Barrer, a channel having at least one inlet and one outlet for flow of fluid in contact with one side of a membrane, and contiguous with the opposite side thereof a permeate chamber having at least one outlet for flow of permeate; means for distribution of a fluid feedstock into the channel inlets of at least a portion of the intermediate group of modules; means for collection of permeate effluent from the chamber outlets of at least a portion of the intermediate group of modules and distribution of this intermediate permeate into the channel inlets of the first product group modules
  • the means for collection and distribution of permeate into the channel inlets of the first product group modules advantageously comprises a compressor and/or pump, preferably a compressor.
  • preferred embodiments of the invention further comprises means for distribution of another fluid feedstock into the channel inlets of the first and/or second product of modules.
  • the apparatus further comprises means for distribution of another feedstock into the channel inlets of the first product of modules.
  • the apparatus may further comprises means for distribution of a “sweep” stream into the permeate chambers of one or more of the modules.
  • this invention provides apparatus using perm-selective membranes in multiple groups for simultaneous recovery of a very pure permeate product and a desired non-permeate product from a fluid mixture of compounds in which the apparatus comprises: a plurality of membrane modules disposed in a first product group, one or more intermediate group, and a second product group, each module comprising a solid perm-selective membrane which under a suitable differential of a driving force exhibits a permeability of at least 0.1 Barrer, a channel having at least one inlet and one outlet for flow of fluid in contact with one side of a membrane, and contiguous with the opposite side thereof a permeate chamber having at least one outlet for flow of permeate; means for distribution of a first fluid feedstock into the channel inlets of at least a portion of the intermediate group of modules; means for collection of permeate effluent from the chamber outlets of at least a portion of the intermediate group of modules and distribution of this intermediate permeate into the channel inlets of the first product
  • preferred embodiments of the invention further comprises means for distribution of another fluid feedstock into the channel inlets of the second product of modules.
  • the means for collection and distribution of permeate into the channel inlets of the first product group modules comprises a compressor, and/or the means for collection and distribution of permeate into at least a portion the channel inlets of the intermediate group modules comprises a compressor.
  • the membrane modules in the second product group have membranes of lower selectivity than membranes in at least one of other group.
  • the membrane modules in the second product group have membranes of lower selectivity than membranes in the other groups.
  • the membrane modules in at least a portion of the intermediate group have membranes of higher selectivity than membranes in at least one of the other groups.
  • the membrane modules in the intermediate group have membranes of a selectivity which is about 35 percent or more higher than membranes another group, preferably at least about 50 percent higher, and more preferably at least about 100 percent higher.
  • the membrane modules in at least a portion of the intermediate group have membranes of higher selectivity than membranes in the other groups.
  • the membrane modules in the first product group have membranes of higher selectivity than membranes in at least one of the other groups. More preferably the membrane modules in the first product group have membranes of higher selectivity than membranes in the other groups.
  • This invention is particularly useful towards separations involving organic compounds, in particular compounds which are difficult to separate by conventional means such as fractional distillation.
  • organic compounds are chemically related as for example alkanes and alkenes of similar carbon number.
  • FIG. 1 is schematic drawing showing an embodiment of the present invention which includes three groups of perm-selective membrane modules, one feedstream location and a compressor.
  • FIG. 2 is schematic drawing showing an embodiment of the present invention which includes three groups of perm-selective membrane modules, one and/or two feedstream locations and two compressors.
  • Any solid perm-selective membrane which under a suitable differential of a driving force exhibits a permeability and other characteristics suitable for the desired separations may be used according to the invention.
  • Suitable membranes may take the form of a homogeneous membrane, a composite membrane or an asymmetric membrane which, for example may incorporate a gel, a solid, or a liquid layer.
  • Widely used polymers include silicone and natural rubbers, cellulose acetate, polysulfones and polyimides.
  • Preferred membranes for use in vapor separation embodiments of the invention are generally of two types.
  • the first is a composite membrane comprising a microporous support, onto which the perm-selective layer is deposited as an ultra-thin coating.
  • Composite membranes are preferred when a rubbery polymer is used as the perm-selective material.
  • the second is an asymmetric membrane in which the thin, dense skin of the asymmetric membrane is the perm-selective layer.
  • Both composite and asymmetric membranes are known in the art.
  • the form in which the membranes are used in the invention is not critical. They may be used, for example, as flat sheets or discs, coated hollow fibers, spiral-wound modules, or any other convenient form.
  • the driving forces for separation of vapor components by membrane permeation include, predominately their partial pressure difference between the first and second sides of the membrane.
  • the pressure drop across the membrane can be achieved by pressurizing the first zone, by evacuating the second zone, introducing a sweep stream, or any combination thereof.
  • the membranes used in each group of modules may be of the same type or different. Although both units may contain membranes selective to the desired component to be separated, the selectivities of the membranes may be different. For example, where intermediate modules process the bulk of the fluid feedstock, these modules may contain membranes of high flux and moderate selectivity. The module group which deals with smaller streams, may contain membranes of high selectivity but lower flux. Likewise the intermediate modules may contain one type of membrane, and product modules may contain another type, or all three groups may contain different types. Useful embodiments are also possible using membranes of unlike selectivities in the intermediate modules and product modules.
  • Suitable types of membrane modules include the hollow-fine fibers, capillary fibers, spiral-wound, plate-and-frame, and tubular types.
  • the choice of the most suitable membrane module type for a particular membrane separation must balance a number of factors.
  • the principal module design parameters that enter into the decision are limitation to specific types of membrane material, suitability for high-pressure operation, permeate-side pressure drop, concentration polarization fouling control, permeability of an otional sweep stream, and last but not least costs of manufacture.
  • Hollow-fiber membrane modules are used in two basic geometries.
  • One type is the shell-side feed design, which has been used in hydrogen separation systems and in reverse osmosis systems.
  • a loop or a closed bundle of fibers is contained in a pressure vessel.
  • the system is pressurized from the shell side; permeate passes through the fiber wall and exits through the open fiber ends.
  • This design is easy to make and allows very large membrane areas to be contained in an economical system.
  • the fiber wall must support considerable hydrostatic pressure, the fibers usually have small diameters and thick walls, e.g. 100 ⁇ m to 200 ⁇ m outer diameter, and typically an inner diameter of about one-half the outer diameter.
  • a second type of hollow-fiber module is the bore-side feed type.
  • the fibers in this type of unit are open at both ends, and the feed fluid is circulated through the bore of the fibers.
  • the diameters are usually larger than those of the fine fibers used in the shell-side feed system and are generally made by solution spinning. These so-called capillary fibers are used in ultra-filtration, pervaporation, and some low- to medium-pressure gas applications.
  • Concentration polarization is well controlled in bore-side feed modules.
  • the feed solution passes directly across the active surface of the membrane, and no stagnant dead spaces are produced. This is far from the case in shell-side feed modules in which flow channeling and stagnant areas between fibers, which cause significant concentration polarization problems, are difficult to avoid. Any suspended particulate matter in the feed solution is easily trapped in these stagnant areas, leading to irreversible fouling of the membrane.
  • Baffles to direct the feed flow have been tried, but are not widely used.
  • a more common method of minimizing concentration polarization is to direct the feed flow normal to the direction of the hollow fibers. This produces a cross-flow module with relatively good flow distribution across the fiber surface.
  • the fluid feedstock is a gaseous mixture comprising a more selectively permeable alkene component and a corresponding alkane component, for example propane and propene (propylene).
  • a more selectively permeable alkene component for example propane and propene (propylene).
  • propane and propene propane and propene (propylene).
  • Other examples of light hydrocarbon compounds which are difficult to separate by traditional separtion methods, such as fractional distillation, are shown in Table I.
  • the membrane staging configuration for a particular separation depends on many factors. These factors include (1) the concentration of the desired component in the feed stream; (2) the physical and chemical properties of the components being separated; (3) the required purity of the product streams; (4) the relative values of the products, which determines acceptable recovery; (5) the tradeoff between membrane capital cost and the cost of pumping or compression; and (6) how the membrane is integrated with other processing steps. In the separation of mixtures using membranes, the required product recoveries and product purity must be achieved at acceptable capital and operating costs. For multi-staged systems, the stage configuration and operating conditions of the individual stages must be balanced to meet the purity, recovery, and cost requirements.
  • membrane modules are disposed according to a preferred aspect of the invention in three groups represented in the drawing by modules 120 , 140 and 160 .
  • a feedstock from a source 112 is passed through conduit 114 , and, depending on the operating conditions employed in a particular application, an optional compressor or pump and vaporizer (not shown), into a first zone of intermediate membrane module 140 .
  • Permeate comprising the more selectively permeable component of the feedstock, e.g. alkene
  • a component of the feedstock e.g. alkene
  • compressor 150 is withdrawn from the second zone of membrane module 140 and transferred to compressor 150 through conduit 144 and manifold 146 .
  • Effluent from compressor 150 is transferred into the first zone of a first product module 160 through conduit 152 .
  • Very pure permeate product is recovered from the second zone of the first product module 160 through conduit 164 .
  • Non-permeate effluent comprising the less permeable component of the feedstock, e.g. alkane
  • Non-permeate effluent is withdrawn from the first zone of the first product module 160 is recycled through conduit 162 into the first zone of intermediate membrane module 140 .
  • Non-permeate effluent, comprising the less permeable component of the feedstock, e.g. alkane is withdrawn from the first zone of intermediate module 140 and transferred through conduit 142 into a first zone of second product module 120 .
  • a permeate gas is withdrawn from the second zone of second product module 120 and transferred to the suction side of compressor 150 through conduit 124 and manifold 146 .
  • Permeate from the second product module 120 and permeate from the intermediate module 140 are thereby mixed as they pass through the compressor, and a single stream is transferred into the first zone of a first product module 160 through 152 .
  • hydrocarbon compounds such as a gaseous mixture of light hydrocarbons having from 1 to about 4 carbon atoms
  • source 212 such as a steam-cracker, light-olefins upgrading unit or another refinery operation
  • Permeate comprising the more selectively permeable alkene component of the feedstock
  • Effluent from compressor 250 is transferred into the first zone of a first product module 260 through conduit 252 .
  • An additional feedstock which typically has a higher concentration of the alkene component than the first feedstock, from a source 266 is passed through conduit 268 and, depending on the operating conditions employed in a particular application, an optional compressor or pump and vaporizer (not shown), and into a first zone of the first product module 260 .
  • Very pure permeate product is recovered from the second zone of the first product module 260 through conduit 264 .
  • Non-permeate effluent comprising the less permeable alkane component of the feedstock
  • is withdrawn from the first zone of the first product module 260 is recycled through conduit 262 and manifold 234 into the first zone of intermediate membrane module 240 .
  • Non-permeate effluent, comprising the less permeable alkane component of the feedstock is withdrawn from the first zone of intermediate module 240 and transferred through conduit 242 into a first zone of second product module 220 .
  • a second product is withdrawn from the first zone of second module 220 through conduit 222 .
  • a permeate gas is withdrawn from the second zone of second product module 220 and transferred to the suction side of compressor 230 through conduit 224 and, depending on the operating conditions employed in a particular application, an optional heat exchanger (not shown).
  • Effluent from compressor 230 is transferred into the first zone of a intermediate module 240 through conduit 232 and manifold 234 .
  • another fluid feedstock which advantageously has a concentration of the alkene component of less than the first feedstock e.g. a steam-cracker, light-olefins upgrading unit or another refinery operation
  • a steam-cracker, light-olefins upgrading unit or another refinery operation is passed into the first zone of the second product module 220 thereby replacing or supplementing feedstock from source 212 and/or source 266 .
  • the permeability of gases through membranes is measured in “Barrer”, which is defined as 10 ⁇ 10 [cm 3 (STP) cm/(cm 2 ⁇ sec ⁇ cmHg)] and named after R. M. Barrer.
  • Membrane permeability is a measure of the ability of a membrane to permeate a gas.
  • membrane selectivity is defined as the ratio of the permeabilities of two gases and is a measure of the ability of a membrane to separate the two gases.
  • the feedstock compositions represent an industry average composition of catalytic or pyrolysis cracker effluents.
  • the liquid feed was pressurized with a pump to the operating level and vaporized before introduction into the apparatus.
  • the permeate from the non-permeate product and intermediate stages was compressed from the permeate pressure to the feed pressure before introduction to the next stage.
  • a cooler was used after each compressor to keep the feed to each membrane stage at 200° F.
  • the final non-permeate product was condensed with 100° F. water after exiting the process.
  • the final permeate product was compressed after exiting the process to a pressure where it could be condensed with 100° F. water (approximately 250 psia).
  • percent is defined liquid percent by volume.
  • This example documents an aspect of the preferred embodiment of the invention depicted in FIG. 1. Feed was supplied to modules 140 from source 112 . Membrane propylene selectivity of 35 and a propylene permeability of 1 Barrer in each of membrane modules were used for these calculations.
  • Membrane area for the non-permeate product modules and the permeate product modules were adjusted so that the final permeate product stream 164 met Polymer-Grade Propylene (PGP) specifications and, at the same time, the final non-permeate product steam 122 met Liquified Petroleum Gas (LPG) specifications. Also the membrane area for the intermediate modules 140 was adjusted to minimize the total required compression work, which is a major cost driver. The results of these calculations are shown in Table II. When the membrane selectivity dropped below about 25, the flow of material in stream 124 increased and the concentration of propylene in stream 152 decreased so much that it was no longer possible to make a final permeate product which met PGP specifications. At these lower membrane selectivities, an appratus similar to that shown in FIG.
  • This example documents an aspect of the preferred embodiment of the invention depicted in FIG. 2 where only the feed stream from source 212 was introduced into the apparatus, and the membrane modules had different membrane properties.
  • two propylene permeability-selectivity pairs were used in these calculations: propylene permeability of 2 Barrer with 15 propylene selectivity and propylene permeability of 1 Barrer with 35 propylene selectivity.
  • the membrane area for the permeate product module was adjusted so that the final permeate product met Polymer-Grade Propylene (PGP) specifications.
  • PPP Polymer-Grade Propylene
  • LPG Liquefied Petroleum Gas
  • the membrane area for the intermediate module was adjusted to minimize the total required compression work.
  • This example documents an aspect of the preferred embodiment of the invention depicted in FIG. 2 where different feed streams supplied from source 212 and source 266 were introduced into the apparatus at two different locations.
  • membranes with the same permeability-selectivity have been employed in each stage of the apparatus in this example: propylene permeability of 1 Barrer with a 35 propylene selectivity.
  • the same total feed rate 10,000 BPD
  • the membrane area for the permeate product and non-permeate product modules were adjusted so that the propylene and propane products met the PGP and LPG specifications, respectively, and the membrane area for the entermediate module was adjusted to minimize the total required compression work.
  • This example illustrates the effect of the composition of the streams from sources 212 and 266 on the total required compression work and membrane area needed to meet the PGP and LPG specifications.
  • the specific compositions used in this example were selected to keep the total amount of propylene constant (70 percent) and the same as that employed in previous examples.
  • Table IV shows the results of these calculations. Recall that in the previous example where a propylene permeability of 1 Barrer and 35 propylene selectivity was employed in each stage and feed with 70 percent propylene was introduced only from source 212 the total required compression work was 0.050 kWh/lb of propylene product and the total required membrane area was 675,000 ft 2 . Table V shows that the required work and membrane area increases when feed containing 70 percent propylene is introduced form sources 212 and 266 . However, Table V shows that the total work and membrane requirements are dependent on the propylene content of the streams from sources 212 and 266 .
  • This example is based upon the preferred embodiment of the invention depicted in FIG. 2, except that feed streams supplied from source 212 and source 266 were replaced with a single feed (not shown) which was introduced into the apparatus at a different location, i.e., into the first zone of the second product module 220 .
  • Membranes with the same permeability-selectivity have been employed in each stage of the apparatus in this example: propylene permeability of 1 Barrer with a 35 propylene selectivity.
  • the membrane area for the permeate and non-permeate modules were adjusted so that the propylene and propane products met the PGP and LPG specifications, respectively, and the membrane area for the intermediate module was adjusted to minimize the total required compression work.
  • Table V shows that the position where the feed is introduced greatly influences the compression and membrane area requirements needed to meet the PGP and LPG specifications.
  • TABLE IV SEPARATIONS USING TWO FEED LOCATIONS WITH MODULES DISPOSED INTO THREE GROUPS ⁇ PROPYLENE PROPYLENE CONTENT OF CONTENT OF MEMBRANE SOURCE212, SOURCE266, TOTAL AREA, percent percent COMPRESSION ⁇ ft 2 ⁇ 10 ⁇ 3 70 70 0.069 813 65 75 0.062 770 60 80 0.055 718 55 85 0.047 656 50 90 0.040 597
  • “predominantly” is defined as more than about fifty percent. “Substantially” is defined as occurring with sufficient frequency or being present in such proportions as to measurably affect macroscopic properties of an associated compound or system. Where the frequency or proportion for such impact is not clear, substantially is to be regarded as about twenty percent or more.
  • a feedstock consisting essentially of is defined as at least 95 percent of the feedstock by volume.
  • the term “essentially free of” is defined as absolutely except that small variations which have no more than a negligible effect on macroscopic qualities and final outcome are permitted, typically up to about one percent.
US10/183,793 2002-06-27 2002-06-27 Apparatus using solid perm-selective membranes in multiple groups for simultaneous recovery of specified products from a fluid mixture Abandoned US20040000513A1 (en)

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US10/185,825 US6830691B2 (en) 2002-06-27 2002-06-27 Processes using solid perm-selective membranes in multiple groups for simultaneous recovery of specified products from a fluid mixture
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PCT/US2003/020182 WO2004002609A2 (en) 2002-06-27 2003-06-26 Processes and apparatus using solid perm-selective membranes in multiple groups for simultaneous recovery of specified products from a fluid mixture
ES03762078T ES2388918T3 (es) 2002-06-27 2003-06-26 Procedimientos que utilizan membranas de permeabilidad selectiva de sólidos en múltiples grupos para la recuperación simultánea de productos específicos a partir de una mezcla de fluidos
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FR2926813A1 (fr) * 2008-01-28 2009-07-31 Inst Francais Du Petrole Procede de separation du propane et du propylene mettant en oeuvre une colonne a distiller et une unite de separation par membrane
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US20150336046A1 (en) * 2012-11-14 2015-11-26 Evonik Fibres Gmbh Control of gas composition of a gas separation system having membranes
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CN106000016A (zh) * 2015-03-30 2016-10-12 宇部兴产株式会社 气体分离系统及富化气体的制造方法
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US8083946B2 (en) 2006-08-08 2011-12-27 Exxonmobil Research And Engineering Company Chemically cross-linked polymeric membranes and method of use
US20080035566A1 (en) * 2006-08-08 2008-02-14 Sabottke Craig Y Chromatographic membrane separation
US20080035573A1 (en) * 2006-08-08 2008-02-14 Peiffer Dennis G Membrane for separating aromatic and aliphatic compounds
US7785471B2 (en) 2006-08-08 2010-08-31 Exxonmobil Research And Engineering Company Chromatographic membrane separation
US20080035571A1 (en) * 2006-08-08 2008-02-14 Exxonmobil Research And Engineering Company Integrally-layered polymeric membranes and method of use
US20080035574A1 (en) * 2006-08-08 2008-02-14 Sabottke Craig Y Membrane Barrier films and method of use
US7708151B2 (en) 2006-08-08 2010-05-04 Exxonmobil Research And Engineering Company Membrane for separating aromatic and aliphatic compounds
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US7875758B2 (en) 2007-01-08 2011-01-25 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes George Claude Systems and methods for the separation of propylene and propane
EP2357033A1 (en) 2007-01-08 2011-08-17 L'AIR LIQUIDE, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Systems and methods for the separation of propylene and propane
US20080210540A1 (en) * 2007-01-17 2008-09-04 Dieterle Rex A Separation and dewatering of organic solvents by integrating distillation and membrane separation operations
FR2926813A1 (fr) * 2008-01-28 2009-07-31 Inst Francais Du Petrole Procede de separation du propane et du propylene mettant en oeuvre une colonne a distiller et une unite de separation par membrane
US20110049051A1 (en) * 2008-01-28 2011-03-03 Ifp Process for separating propane and propylene using a distillation column and a membrane separation column
WO2009106706A1 (fr) * 2008-01-28 2009-09-03 Ifp Procede de separation du propane et du propylene mettant en oeuvre une colonne a distiller et une unite deseparation par membrane
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US20110077446A1 (en) * 2009-09-30 2011-03-31 American Air Liquide, Inc. Membrane Separation of a Mixture of Close Boiling Hydrocarbon Components
WO2011041179A1 (en) 2009-09-30 2011-04-07 L'air Liquide Societe Anonyme Pourl'etude Et L'exploitation Des Procedes Georges Claude Membrane separation of a mixture of close boiling hydrocarbon components
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CN104144951A (zh) * 2012-01-26 2014-11-12 道达尔研究技术弗吕公司 用于清除聚丙烯制造过程中的丙烷的方法
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US20170080381A1 (en) * 2015-09-21 2017-03-23 Fujifilm Manufacturing Europe B.V. Gas Separation Process
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AU2003247716A1 (en) 2004-01-19
EP1515790B1 (en) 2012-08-08
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