US20090166258A1 - Method for Producing a Hydrogen-Enriched Gas Stream from Hydrogenated Gas Streams Comprising Hydrocarbons - Google Patents

Method for Producing a Hydrogen-Enriched Gas Stream from Hydrogenated Gas Streams Comprising Hydrocarbons Download PDF

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Publication number
US20090166258A1
US20090166258A1 US12/067,322 US6732206A US2009166258A1 US 20090166258 A1 US20090166258 A1 US 20090166258A1 US 6732206 A US6732206 A US 6732206A US 2009166258 A1 US2009166258 A1 US 2009166258A1
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United States
Prior art keywords
hydrogen
gas
hydrocarbons
gas stream
pressure
Prior art date
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Abandoned
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US12/067,322
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English (en)
Inventor
Francois-Xavier Haulle
Sylvain Gerard
Bruno Alban
Vincent Pudys
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Application filed by LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Assigned to L'AIR LIQUIDE, SOCIETE ANONYME POUR L'ETUDE ET L'EXPLOITATION DES PROCEDES GEORGES CLAUDE reassignment L'AIR LIQUIDE, SOCIETE ANONYME POUR L'ETUDE ET L'EXPLOITATION DES PROCEDES GEORGES CLAUDE ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: GERARD, SYLVAIN, PUDYS, VINCENT, ALBAN, BRUNO, HAULLE, FRANCOIS-XAVIER
Publication of US20090166258A1 publication Critical patent/US20090166258A1/en
Abandoned legal-status Critical Current

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    • 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
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • 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
    • B01D53/002—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 condensation
    • 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
    • B01D53/02—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 adsorption, e.g. preparative gas chromatography
    • B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
    • 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
    • C01B3/506—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification at low temperatures
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/12—Liquefied petroleum gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/30—Physical properties of adsorbents
    • B01D2253/302—Dimensions
    • B01D2253/306—Surface area, e.g. BET-specific surface
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/30—Physical properties of adsorbents
    • B01D2253/302—Dimensions
    • B01D2253/308—Pore size
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/16—Hydrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B01D2257/702—Hydrocarbons
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/40077—Direction of flow
    • B01D2259/40081—Counter-current
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/414—Further details for adsorption processes and devices using different types of adsorbents
    • B01D2259/4141—Further details for adsorption processes and devices using different types of adsorbents within a single bed
    • B01D2259/4143—Further details for adsorption processes and devices using different types of adsorbents within a single bed arranged as a mixture
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/414—Further details for adsorption processes and devices using different types of adsorbents
    • B01D2259/4141—Further details for adsorption processes and devices using different types of adsorbents within a single bed
    • B01D2259/4145—Further details for adsorption processes and devices using different types of adsorbents within a single bed arranged in series
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/416—Further details for adsorption processes and devices involving cryogenic temperature treatment
    • 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
    • C01B2203/042—Purification by adsorption on solids
    • C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
    • 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
    • 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
    • C01B2203/14—Details of the flowsheet
    • C01B2203/146—At least two purification steps in series

Definitions

  • the present invention relates to a process for enhancing various streams based on hydrogen and on hydrocarbons so as to produce a high-purity hydrogen stream.
  • the objective of the present invention is to propose a process for enhancing various streams based on hydrogen and hydrocarbons so as to produce a high-purity hydrogen stream, a liquefied petroleum gas and a waste gas, the investment cost of which is reduced by increasing the high-purity hydrogen production yield.
  • Another objective of the present invention is to propose a process for enhancing various streams based on hydrogen and hydrocarbons so as to produce a high-purity hydrogen stream, a liquefied petroleum gas and a waste gas, of which the energy consumption is optimized.
  • the invention relates to a process for producing a hydrogen-enriched gas stream and a liquefied petroleum gas from at least one gas stream mainly comprising hydrogen at pressure P and a gas stream comprising hydrogen and hydrocarbons, in which the following steps are carried out:
  • the process according to the invention allows the treatment of two gas streams comprising hydrogen at various concentrations so as to produce a hydrogen-enriched gas stream, a liquefied petroleum gas (or LPG) and a waste gas.
  • the first gas stream treated is a gas stream that mainly comprises hydrogen, that is to say having a hydrogen concentration between 50 and 99 vol %. This stream also comprises hydrocarbons having from 1 to 8 carbon atoms and compounds such as CO, CO 2 , H 2 S, etc.
  • the second stream treated is a gas stream comprising hydrogen and hydrocarbons having a hydrogen concentration at least 10% lower, preferably at least 15% lower and more preferably still 15 to 50% lower, relative to the value of the hydrogen concentration of the gas stream mainly comprising hydrogen.
  • This second stream also comprises hydrocarbons having 1 to 8 carbon atoms, and also compounds such as H 2 O, H 2 S, etc.
  • this second gas stream has a hydrocarbon concentration between 10 and 50 vol %.
  • the pressure of this second gas stream comprising hydrogen and hydrocarbons is adjusted so that it is close to 2, either by compression, or by pressure drop depending on the origin of this stream. It is also possible that this stream already has a pressure P, in this case it is used as is without a pressure adjustment.
  • These various streams may be derived from the purge of the gas loop of a hydrotreatment unit such as a hydrodesulfurization or hydrocracking unit of a refinery, or else such as a hydrodealkylation or isomerization unit of a petrochemical site.
  • the first and second gas streams treated in the present invention may be derived from mixtures of various purges of such units. These mixtures may make it possible to attain the pressure P desired by combining the streams having a pressure below P with streams having a pressure above P.
  • the invention makes it possible to enrich the gas stream mainly comprising hydrogen.
  • This enrichment is obtained by hydrogen depletion of the second gas stream comprising hydrogen and hydrocarbons.
  • the unit thus produces the hydrogen-enriched gas stream generally having a hydrogen purity greater than 99 vol %, and the unit also produces a waste stream of low hydrogen purity and of low pressure which may be conveyed to the fuel gas network.
  • the pressure and hydrogen concentration of the waste stream are respectively below the pressure and hydrogen concentration values of all the effluents going into the unit (U).
  • This waste stream also comprises hydrocarbons (C 1 to C 8 ) and compounds such as H 2 O, H 2 S, CO, CO 2 , etc.
  • the gas separation unit (U) is a pressure swing adsorption (PSA) unit combined with an integrated compressor, in which, for each adsorber of the unit, a pressure swing cycle is carried out comprising a succession of phases which define the phases of adsorption, decompression, purge and pressure rise, such that:
  • PSA pressure swing adsorption
  • the adsorbent of the PSA beds should, in particular, allow the adsorption and desorption of impurities.
  • the adsorbent bed is generally composed of a mixture of several adsorbents, said mixture comprising, for example, at least two adsorbents chosen from: activated carbons, silica gels, aluminas or molecular sieves.
  • the silica gels should have a pore volume between 0.4 and 0.8 cm 3 /g and a specific surface area greater than 600 m 2 /g.
  • the aluminas have a pore volume greater than 0.2 cm 3 /g and a specific surface area greater than 220 m 2 /g.
  • each PSA adsorbent bed is composed of at least three layers of adsorbents of different natures.
  • Each PSA adsorbent bed may comprise: in the bottom part, a protective layer composed of alumina and/or silica gel surmounted by a layer of activated carbon and/or of carbon-based molecular sieve and optionally in the upper part a molecular sieve layer.
  • the proportions vary as a function of the nature of the gas mixture to be treated (especially as a function of its percentages of CH 4 and of C 3+ hydrocarbons).
  • a water-free gas mixture comprising 75 mol % of H 2 , 5% of C 3+ and 20% of light (C 1 -C 2 ) hydrocarbons, CO and N 2 may be treated by an adsorption unit whose beds comprise at least 10 vol % of alumina and 15 vol % of silica gel in the bottom bed, the remainder being obtained from activated carbon.
  • the waste gas is produced.
  • This production of the waste gas may be obtained by countercurrent decompression initiated at a pressure below P.
  • This waste gas comprises impurities and has a hydrogen content lower than all the streams introduced into the PSA unit.
  • This waste gas may be discharged from the process and burnt or reused as a recycle gas in the PSA unit as indicated previously.
  • a purge phase is carried out to finalize the regeneration of the adsorber.
  • a gas is introduced countercurrently into the adsorber and a purge gas is produced.
  • the gas introduced countercurrently into the adsorber during the purge phase is a gas stream derived from one of the steps of the decompression phase.
  • the purge gas is generally used as a recycle gas after recompression.
  • the pressure of the adsorber is increased by countercurrent introduction of a gas stream comprising hydrogen such as the gas produced during the various steps of the decompression phase.
  • the temperature of the gas stream comprising hydrogen and hydrocarbons is lowered so as to condense the hydrocarbons, preferably to less than 0° C., more preferably still to less than ⁇ 20° C.
  • this temperature drop is carried out by means of a cryogenic device, such as cryogenic (compression/expansion) loops using liquid ammonia or propane.
  • FIG. 1 illustrates the process according to the invention.
  • the stream 2 comprising hydrogen and hydrocarbons is compressed by the compressor 3 to have a pressure P equal to that of the stream 1 that mainly comprises hydrogen.
  • the stream 21 comprising hydrogen and hydrocarbons and that is compressed is then treated by a device 4 that makes it possible to lower its temperature and to condense the hydrocarbons.
  • the device 4 produces:
  • This stream 22 and the stream 1 are treated by the gas separation unit 5 so as to produce: a hydrogen-enriched stream 6 , a waste gas 7 and a purge gas 8 which is mixed with the stream 2 comprising hydrogen and hydrocarbons before compression of the latter.
  • the process also makes it possible to treat another stream 9 comprising hydrogen and hydrocarbons that is equivalent to the stream 2 but originates from another purge.
  • This stream 9 already has a pressure P or a pressure that is slightly greater than P; it is therefore directly treated by the device 4 with the mixture 21 resulting from the compressor.
  • the process additionally makes it possible to produce, at the outlet of the temperature-lowering device, a liquefied petroleum gas, which may be a stream of high added value, that can be recovered as a fuel.
  • the process of the invention also has the advantage of allowing a natural energy integration between the cryogenic device enabling the temperature to be reduced and the compressor of the pressure swing adsorption unit.
  • the stream of liquefied hydrocarbons may be recovered as a commercial product within the plant.
  • the liquefied petroleum gas resulting from the cryogenic device is a product of high added value which compensates for the additional energy used by the cryogenic device of the process according to the invention relative to the process of the prior art.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Separation Of Gases By Adsorption (AREA)
US12/067,322 2005-09-30 2006-09-21 Method for Producing a Hydrogen-Enriched Gas Stream from Hydrogenated Gas Streams Comprising Hydrocarbons Abandoned US20090166258A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR0552972 2005-09-30
FR0552972A FR2891538B1 (fr) 2005-09-30 2005-09-30 Procede de production d'un flux gazeux enrichi en hydrogene a partir de flux gazeux hydrogenes comprenant des hydrocarbures
PCT/FR2006/050921 WO2007036660A2 (fr) 2005-09-30 2006-09-21 Procede de production d’un flux gazeux enrichi en hydrogene a partir de flux gazeux hydrogenes comprenant des hydrocarbures

Publications (1)

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US20090166258A1 true US20090166258A1 (en) 2009-07-02

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US12/067,322 Abandoned US20090166258A1 (en) 2005-09-30 2006-09-21 Method for Producing a Hydrogen-Enriched Gas Stream from Hydrogenated Gas Streams Comprising Hydrocarbons

Country Status (8)

Country Link
US (1) US20090166258A1 (fr)
EP (1) EP1934136B1 (fr)
CN (1) CN101277898A (fr)
AT (1) ATE423078T1 (fr)
CA (1) CA2623298A1 (fr)
DE (1) DE602006005259D1 (fr)
FR (1) FR2891538B1 (fr)
WO (1) WO2007036660A2 (fr)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20100037655A1 (en) * 2008-08-13 2010-02-18 Air Liquide Process And Construction Inc. Hydrogen Recovery From A Mixture Of Hydrogen and Hydrocarbons At Low Pressure And Of Low Hydrogen Content
US20100170296A1 (en) * 2009-01-08 2010-07-08 Stefan Wolf Separation of volatile components from a gas flow
US20150175907A1 (en) * 2013-12-20 2015-06-25 Phillips 66 Company Converting ethane to liquid fuels and chemicals
US20160168491A1 (en) * 2013-06-05 2016-06-16 Jianhua Yao Converting ethane to liquid fuels and chemicals
CN111467925A (zh) * 2020-06-05 2020-07-31 上海优华系统集成技术股份有限公司 一种浅冷和psa耦合装置及其使用方法

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2011144198A1 (fr) * 2010-05-17 2011-11-24 Karl-Werner Dietrich Transport et stockage d'hydrogène

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4547205A (en) * 1984-10-11 1985-10-15 Uop Inc. Dehydrocyclodimerization process
US6592749B1 (en) * 1999-03-19 2003-07-15 Membrane Technology And Research, Inc. Hydrogen/hydrocarbon separation process, including PSA and membranes
US20080244972A1 (en) * 2003-10-31 2008-10-09 Pascal Tromeur Method for Converting Hyrogenous Gaseous Flows Arising From Chemical Reactor Units Using Hydrogen

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA2469153C (fr) * 2001-12-18 2008-03-04 Fluor Corporation Extraction combinee d'hydrocarbure et d'hydrogene liquides dans des gaz contenant de l'hydrogene

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4547205A (en) * 1984-10-11 1985-10-15 Uop Inc. Dehydrocyclodimerization process
US6592749B1 (en) * 1999-03-19 2003-07-15 Membrane Technology And Research, Inc. Hydrogen/hydrocarbon separation process, including PSA and membranes
US20080244972A1 (en) * 2003-10-31 2008-10-09 Pascal Tromeur Method for Converting Hyrogenous Gaseous Flows Arising From Chemical Reactor Units Using Hydrogen

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20100037655A1 (en) * 2008-08-13 2010-02-18 Air Liquide Process And Construction Inc. Hydrogen Recovery From A Mixture Of Hydrogen and Hydrocarbons At Low Pressure And Of Low Hydrogen Content
US20100170296A1 (en) * 2009-01-08 2010-07-08 Stefan Wolf Separation of volatile components from a gas flow
US20160168491A1 (en) * 2013-06-05 2016-06-16 Jianhua Yao Converting ethane to liquid fuels and chemicals
US10087380B2 (en) * 2013-06-05 2018-10-02 Phillips 66 Company Converting ethane to liquid fuels and chemicals
US20150175907A1 (en) * 2013-12-20 2015-06-25 Phillips 66 Company Converting ethane to liquid fuels and chemicals
US20150175908A1 (en) * 2013-12-20 2015-06-25 Phillips 66 Company Ethane and ethanol to liquid transportation fuels
US9731270B2 (en) * 2013-12-20 2017-08-15 Phillips 66 Company Converting ethane to liquid fuels and chemicals
US10173195B2 (en) * 2013-12-20 2019-01-08 Phillips 66 Company Ethane and ethanol to liquid transportation fuels
CN111467925A (zh) * 2020-06-05 2020-07-31 上海优华系统集成技术股份有限公司 一种浅冷和psa耦合装置及其使用方法

Also Published As

Publication number Publication date
DE602006005259D1 (de) 2009-04-02
EP1934136B1 (fr) 2009-02-18
EP1934136A2 (fr) 2008-06-25
ATE423078T1 (de) 2009-03-15
FR2891538A1 (fr) 2007-04-06
FR2891538B1 (fr) 2007-11-16
WO2007036660A2 (fr) 2007-04-05
CN101277898A (zh) 2008-10-01
CA2623298A1 (fr) 2007-04-05
WO2007036660A3 (fr) 2007-06-21

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