WO2015173018A1 - Procédé de production de peroxyde d'hydrogene - Google Patents

Procédé de production de peroxyde d'hydrogene Download PDF

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Publication number
WO2015173018A1
WO2015173018A1 PCT/EP2015/059284 EP2015059284W WO2015173018A1 WO 2015173018 A1 WO2015173018 A1 WO 2015173018A1 EP 2015059284 W EP2015059284 W EP 2015059284W WO 2015173018 A1 WO2015173018 A1 WO 2015173018A1
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WO
WIPO (PCT)
Prior art keywords
fixed bed
reactor
reaction medium
hydrogen
catalyst
Prior art date
Application number
PCT/EP2015/059284
Other languages
German (de)
English (en)
Inventor
Thomas Haas
Original Assignee
Evonik Degussa Gmbh
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Evonik Degussa Gmbh filed Critical Evonik Degussa Gmbh
Priority to CN201580024705.XA priority Critical patent/CN106458584A/zh
Publication of WO2015173018A1 publication Critical patent/WO2015173018A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B15/00—Peroxides; Peroxyhydrates; Peroxyacids or salts thereof; Superoxides; Ozonides
    • C01B15/01—Hydrogen peroxide
    • C01B15/029—Preparation from hydrogen and oxygen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
    • B01J8/025—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical in a cylindrical shaped bed
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0278—Feeding reactive fluids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0285—Heating or cooling the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0292—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds with stationary packing material in the bed, e.g. bricks, wire rings, baffles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
    • B01J8/0449—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds
    • B01J8/0453—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds the beds being superimposed one above the other
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0492—Feeding reactive fluids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0496—Heating or cooling the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
    • B01J8/067—Heating or cooling the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
    • B01J2208/0015—Plates; Cylinders
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00212—Plates; Jackets; Cylinders
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00884—Means for supporting the bed of particles, e.g. grids, bars, perforated plates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00938—Flow distribution elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00761—Details of the reactor

Definitions

  • the invention is directed to a method for
  • the noble metal catalyst can be used both as a suspension catalyst and as
  • Precious metal supported catalyst can be used in a fixed bed.
  • reaction in a fixed bed has the advantage that no separation of reaction product and catalyst must be carried out.
  • the implementation can be done in one as
  • Reactions are for example from EP 0 049 806 and
  • WO 2004/096701 known. From WO 2005/108285 it is also known that with such a mode of operation with a suitable design of the reactor, the corrosion of the reactor material can be avoided.
  • the productivity can be achieved in a reaction on a fixed bed catalyst and improve the selectivity of the reaction by using a high cross-sectional loading of the packed bed with liquid of at least 0.3 m / h.
  • the object of the invention was therefore, a
  • the invention therefore relates to a process for the preparation of hydrogen peroxide, comprising the reaction of hydrogen and oxygen in the presence of a liquid reaction medium and a particulate noble metal supported catalyst in a fixed bed reactor, wherein in
  • Oxygen-containing gas phase is flown, which is characterized in that the fixed bed in the reactor is arranged so that the fixed bed expands in the operating state by 1 to 10% in volume compared to a resting state without influx of the fixed bed.
  • hydrogen and oxygen are reacted in the presence of a liquid reaction medium and a supported noble metal catalyst.
  • the reaction is preferably with a hydrogen and
  • Oxygen-containing gas mixture carried out the composition is chosen so that the gas mixture is not explosive. Preference is given to a gas mixture
  • the gas mixture in addition to hydrogen and oxygen also contains one or more inert gases, preferably nitrogen.
  • the hydrogen content in the gas mixture is preferably limited to a maximum of 6% by volume, particularly preferably at most 5% by volume. In particular, is the
  • the oxygen content in the gas mixture is preferably
  • Oxygen is preferably separated from the reactor
  • Oxygen can be in pure form as well as in the form of air or oxygen
  • the liquid reaction medium an aqueous, aqueous-organic or organic reaction medium can be used.
  • the liquid reaction medium consists essentially of an alcohol or a mixture of alcohol and water, preferably methanol or a mixture of methanol and water.
  • the liquid reaction medium preferably also contains a halide dissolved in an amount effective to inhibit the decomposition of hydrogen peroxide on the noble metal catalyst during the direct synthesis.
  • the halides used are preferably bromide and / or iodide and more preferably bromide.
  • the liquid reaction medium contains the halide preferably in a concentration ranging from 10 "6 to 10" 2 mol / 1, particularly preferably in the range from 10 "5 to 10" 3 mol / 1, and particularly in the range from 10 "5 to 5 ' 10 ⁇ 4 mol / l If the halide concentration is above the preferred range, then the stability of the halide preferably in a concentration ranging from 10 "6 to 10" 2 mol / 1, particularly preferably in the range from 10 "5 to 10" 3 mol / 1, and particularly in the range from 10 "5 to 5 ' 10 ⁇ 4 mol / l If the halide concentration is above the preferred range, then the stability of the halide preferably in a concentration ranging from 10 "6 to 10" 2 mol / 1, particularly preferably in the range from 10 "5 to 10" 3 mol / 1, and particularly in the range from 10 "5 to 5 ' 10 ⁇ 4 mol / l If the halide concentration is above the preferred range, then the stability of
  • the halide may be added to the reaction medium in the form of an alkali metal or
  • Alkaline earth metal salt may be added, preferably as NaBr or Nal.
  • the halide can also be in the form of
  • Hydrohalic acid for example as HBr or HI be added.
  • the liquid reaction medium may optionally additionally contain a strong acid.
  • Strong acids in the context of the invention are all acids which have a pK a value of less than 3 and preferably a pK a value of less than 2.
  • Particularly suitable are mineral acids such as sulfuric acid, phosphoric acid and nitric acid.
  • Also usable in the medium are soluble sulfonic acids and phosphonic acids.
  • the acid concentration is preferably in the range of 0.0001 to 0.5 mol / l, and more preferably in the range of 0.001 to 0.1 mol / l. Is that lying
  • the reaction takes place in the presence of a particulate noble metal supported catalyst.
  • Particulate noble metal supported catalysts in the context of the invention are
  • Carrier material containing one or more precious metals in pure form or in the form of alloys is preferred.
  • Precious metals are the platinum metals, especially palladium, as well as gold.
  • elements from the series Rh, Ru, Ir, Cu and Ag can be present. Especially preferred
  • Catalysts contain as catalytically active metals at least 80 wt .-% palladium and 0 to 20 wt .-% platinum, and 0 to 20 wt .-% gold and / or 0 to 5 wt .-% silver in alloyed or unalloyed form. Most preferred are catalysts containing palladium and platinum.
  • the support materials are:
  • particulate materials such as powders, extrudates,
  • Granules or other molded body formed from a powdery material.
  • oxidic, silicate or nitridic carrier materials are used, in particular aluminum oxide, silica, titanium dioxide,
  • Zirconia and zeolites Zirconia and zeolites.
  • carbon-based supports such as activated carbon supports can also be used.
  • the supported noble metal catalyst can be prepared by mixing the catalytically active component present in very finely divided form with a pulverulent carrier material, plastifying and deforming the mixture, and solidifying the shaped articles by calcination. According to an alternative, it is also possible to use an already prefabricated shaped support with a
  • catalytically active material to or in the carrier material can also be carried out by known binders, such as waterglass, calcium oxalate, boric acid and other glass-forming compositions.
  • binders such as waterglass, calcium oxalate, boric acid and other glass-forming compositions.
  • a calcining step at 300 to 600 ° C.
  • the catalytically active supported catalysts can also be obtained by impregnation of the support with a solution containing a compound of the catalytically active metals and subsequent hydrogenation, calcining and washing steps.
  • the size of the particles of the supported noble metal catalyst can be in wide ranges, preferably in the range of 0.1 to 10 mm. A small particle size leads to a higher pressure drop; if the particle size is too large, the catalytically active surface decreases. Particular preference is given to using a supported catalyst which consists of spherical particles with a mean particle diameter dpso in the range from 0.5 to 5 mm.
  • the supported noble metal catalyst is used in the following
  • a fixed bed according to the invention is a random bed of particles of the noble metal supported catalyst. Such a fill can
  • the fixed bed is flown from below both from the liquid reaction medium and from the hydrogen and oxygen-containing gas phase, i. the liquid reaction medium and the gas phase enter from below into the fixed bed,
  • the fixed bed in the reactor on a gas and
  • liquid-permeable bottom through which the liquid reaction medium and the gas phase over the entire cross-section of the fixed bed can enter into the fixed bed.
  • a gas distributor is arranged in the reactor below such a bottom in order to ensure a uniform gas distribution over the cross section of the fixed bed
  • the fixed bed is in the operating state of the gas phase with a superficial velocity of 50 to 500 m / h, particularly preferably from 50 to 200 m / h, flowed.
  • Reaction medium is preferably carried out with a
  • An essential feature of the method according to the invention is the arrangement of the fixed bed in the reactor, so that the fixed bed expands in the operating state by 1 to 10% in volume compared to a resting state without influx of the fixed bed.
  • This feature is preferably realized in that a gas- and liquid-permeable cover is arranged above the fixed bed, which limits an expansion of the fixed bed and thus an extension of more than the
  • Such a cover may for example take the form of a fixed
  • liquid-permeable cover a non-woven fabric arranged on the fixed bed, fabric, mesh or sieve whose movement is limited by the cover.
  • the fixed bed reactor comprises at least one cooling device, which is designed so that in the fixed bed, the distance between the supported catalyst and a
  • the fixed bed reactor can be carried out as a tube bundle reactor in which tubes filled with the noble metal-supported catalyst are cooled via a common cooling jacket.
  • the fixed bed reactor can also be designed as a plate-bundle reactor in which the fixed bed is arranged in each case in layers between plates aligned in parallel and through which a coolant flows.
  • each fixed bed is arranged so that it expands in the operating state by 1 to 10% in volume compared to the resting state.
  • Such an arrangement makes it possible to additionally feed hydrogen and / or oxygen between the fixed beds and between the fixed beds
  • Reactor can prevent it during the course of
  • the reaction was carried out in a bubble column reactor with a cooling jacket with an inner diameter of 16 mm and a length of 200 cm.
  • a cooling jacket with an inner diameter of 16 mm and a length of 200 cm.
  • a fixed catalyst bed with a
  • Catalyst was a palladium-supported catalyst with
  • the reactor was from below as a liquid reaction medium, a mixture of 98 parts by weight of methanol and
  • Liquid reaction medium and gas mixture flowed through the fixed catalyst bed in a cocurrent from bottom to top. From the flow rates of liquid and gas and the reactor cross section resulted in a
  • the hydrogen conversion was 24% and the withdrawn hydrogen peroxide solution contained 1.9% by weight of hydrogen peroxide.
  • the selectivity of the conversion to hydrogen peroxide was 71% based on reacted hydrogen.
  • the pressure difference over the fixed catalyst bed was 1.2 bar. After 37 hours of operation, the pressure difference rose to within a few minutes
  • Example 1 was repeated, but the space between the sieves was not complete but only 80% with
  • Example 2 was repeated, but instead of the upper sieve a layer of about 12 ml of PTFE wool (PTFE sealing wool from Semadeni) and above one
  • the Raschig rings formed a solid, non-mobile under the reaction conditions packing in the reactor, so that the fixed catalyst bed during the reaction could only expand by about 3% of its volume by compressing the PTFE wool.
  • the hydrogen conversion was 22% and the withdrawn hydrogen peroxide solution contained 1.8 wt .-% hydrogen peroxide.
  • the selectivity of the conversion to hydrogen peroxide was 72% based on reacted hydrogen.
  • the pressure difference over the fixed catalyst bed was 215 mbar. After 3000 hours of operation, the pressure difference remained unchanged at 215 mbar.
  • Hydrogen peroxide solution contained 1.7% by weight
  • Catalyst fixed bed 20% in the operating state however, it came to a wear of the catalyst, which leads to a clogging of the grease bed and an increase in the

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Inorganic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • Catalysts (AREA)

Abstract

L'invention concerne un procédé de production de peroxyde d'hydrogène, par la mise en réaction d'hydrogène et d'oxygène en présence d'un milieu réactionnel liquide et d'un catalyseur supporté à base de métal noble particulaire dans un réacteur à lit fixe. Selon ce procédé, le lit fixe afflue par le bas dans le milieu réactionnel liquide et une phase gazeuse contenant de l'hydrogène et de l'oxygène, le lit fixe étant disposé dans le réacteur de manière telle qu'en mode de fonctionnement, il se dilate de 1 à 10 % en volume par rapport à un mode de repos sans afflux de lit fixe. La dilatation selon l'invention du lit fixe permet de prévenir toute obstruction du lit fixe par l'abrasion du catalyseur.
PCT/EP2015/059284 2014-05-14 2015-04-29 Procédé de production de peroxyde d'hydrogene WO2015173018A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201580024705.XA CN106458584A (zh) 2014-05-14 2015-04-29 制备过氧化氢的方法

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102014209114.4 2014-05-14
DE102014209114.4A DE102014209114A1 (de) 2014-05-14 2014-05-14 Verfahren zur Herstellung von Wasserstoffperoxid

Publications (1)

Publication Number Publication Date
WO2015173018A1 true WO2015173018A1 (fr) 2015-11-19

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Country Link
CN (1) CN106458584A (fr)
DE (1) DE102014209114A1 (fr)
TW (1) TW201609524A (fr)
WO (1) WO2015173018A1 (fr)

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2019025967A1 (fr) * 2017-07-31 2019-02-07 Sabic Global Technologies B.V. Système et procédé de déshydrogénation d'isobutane en isobutylène
DE102020208801A1 (de) 2020-07-15 2022-01-20 Mahle International Gmbh Ionentauscher für ein Brennstoffzellensystem

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0049806A1 (fr) 1980-10-10 1982-04-21 Air Products And Chemicals, Inc. Synthèse de peroxyde d'hydrogène
WO1998016463A1 (fr) 1996-10-16 1998-04-23 Basf Aktiengesellschaft Procede de production de peroxyde d'hydrogene
EP1308416A1 (fr) 2001-10-30 2003-05-07 Degussa AG Synthèse directe de péroxyde d'hydrogène et sa intégration dans des procédés d'oxidation
WO2004096701A1 (fr) 2003-03-28 2004-11-11 Hydrocarbon Technologies, Inc. Production de peroxyde d'hydrogene utilisant l'addition d'hydrogene par etage
WO2005108285A1 (fr) 2004-05-11 2005-11-17 Degussa Ag Procede destine a la synthese directe de peroxyde d'hydrogene
DE102005016877A1 (de) * 2005-04-13 2006-10-19 Degussa Ag Verfahren zur Herstellung von Wasserstoffperoxid

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0049806A1 (fr) 1980-10-10 1982-04-21 Air Products And Chemicals, Inc. Synthèse de peroxyde d'hydrogène
WO1998016463A1 (fr) 1996-10-16 1998-04-23 Basf Aktiengesellschaft Procede de production de peroxyde d'hydrogene
EP1308416A1 (fr) 2001-10-30 2003-05-07 Degussa AG Synthèse directe de péroxyde d'hydrogène et sa intégration dans des procédés d'oxidation
WO2004096701A1 (fr) 2003-03-28 2004-11-11 Hydrocarbon Technologies, Inc. Production de peroxyde d'hydrogene utilisant l'addition d'hydrogene par etage
WO2005108285A1 (fr) 2004-05-11 2005-11-17 Degussa Ag Procede destine a la synthese directe de peroxyde d'hydrogene
DE102005016877A1 (de) * 2005-04-13 2006-10-19 Degussa Ag Verfahren zur Herstellung von Wasserstoffperoxid

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Publication number Publication date
CN106458584A (zh) 2017-02-22
TW201609524A (zh) 2016-03-16
DE102014209114A1 (de) 2015-11-19

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