WO1998011038A1 - Verfahren und katalysator für die katalytische oxidative dehydrierung von alkylaromaten und paraffinen - Google Patents
Verfahren und katalysator für die katalytische oxidative dehydrierung von alkylaromaten und paraffinen Download PDFInfo
- Publication number
- WO1998011038A1 WO1998011038A1 PCT/EP1997/004546 EP9704546W WO9811038A1 WO 1998011038 A1 WO1998011038 A1 WO 1998011038A1 EP 9704546 W EP9704546 W EP 9704546W WO 9811038 A1 WO9811038 A1 WO 9811038A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- catalyst
- bismuthate
- oxygen
- dehydrogenation
- carrier
- Prior art date
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/42—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/02—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of the alkali- or alkaline earth metals or beryllium
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/02—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of the alkali- or alkaline earth metals or beryllium
- C07C2523/04—Alkali metals
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- C07C2523/18—Arsenic, antimony or bismuth
Definitions
- the invention relates to a process for the catalytic oxidative dehydrogenation of alkyl aromatics and paraffin hydrocarbons to the corresponding alkenyl aromatics and olefins, preferably dehydrogenation of ethylbenzene to styrene, water being formed and the dehydrogenation in the absence of free (ie continuously added to the educt stream) oxidizing agent such as molecular Oxygen or gases containing oxygen takes place and a bismuth oxide-containing redox catalyst acts as the sole oxygen source
- Oxygen storage or transfer takes over.
- the catalyst is reduced during the dehydrogenation and regenerated in a second step using an oxidizing agent, preferably an oxygen-containing gas or N 2 O.
- an oxidizing agent preferably an oxygen-containing gas or N 2 O.
- the bismuth compound to be used according to the invention can be applied to a carrier.
- Olefins and alkenylbenzenes are important monomers for engineering plastics and are produced in large quantities.
- Styrene is predominantly produced by non-oxidative dehydrogenation of ethylbenzene over a modified iron oxide catalyst, whereby one mole of hydrogen is produced per mole of styrene.
- it is an equilibrium reaction which is carried out at high temperatures of typically 600 to 700 ° C and with a conversion of about 60% with a styrene selectivity of about 90%.
- the catalyst oxygen carrier at the same time
- the catalyst is gradually consumed and regenerated in a second step, which restores the initial activity.
- a second step which restores the initial activity.
- dehydration with elemental oxygen hardly any side reactions (so-called total combustion) are observed.
- coke deposits are burned off.
- the regeneration is highly exothermic, so that the waste heat released is e.g. can be used for the production of steam.
- the reaction proceeds through the fixed catalyst bed in the form of a reaction front.
- the local heat release is determined solely by the local concentration of reactive oxygen in the catalyst.
- the dehydrogenation is only slightly endothermic, but the oxidation is strongly exothermic.
- the local storage capacity for active oxygen i.e. Oxygen that is consumed during dehydration can be used to control the local heat release.
- this can be achieved by appropriately diluting the catalytically active material with low or inactive metal oxides, by applying the active material to a carrier or by mixing active catalyst-oxygen storage material with inert material.
- the local temperature rise can thus be determined in advance and the thermal load on the catalytic converter can thus be set to an acceptable level.
- Dehydrogenation zone after separation of the reaction products formed, are conveyed to a separate regeneration reactor in which the reoxidation takes place.
- the regenerated catalyst is returned to the dehydrogenation zone.
- the catalytic converter is exposed to high mechanical loads and must therefore have sufficient hardness.
- the regeneration gas is periodically switched between the educt supply and, if necessary, after a winding phase.
- reducible metal oxides selected from the group V, Cr, Mn, Fe, Co, Pb, Bi, Mo, U and Sn, applied to supports made of clays, zeolites and oxides of Ti, Zr, Zn, Th, Mg, Ca, Ba, Si, AI. Catalysts that contain vanadium on magnesium oxide and those that contain bismuth on titanium dioxide are specifically emphasized.
- the catalyst for the dehydrogenation reaction should be in the highest possible oxidation state. For example, when using vanadium you will submit V0 5 .
- the invention solves the problem of finding an oxygen-transferring catalyst which enables higher conversions than the non-oxidative dehydrogenation and at the same time largely avoids side reactions of the oxidative dehydrogenation in the initial phase, so that the selectivity is increased and additional procedural steps, e.g. a partial pre-reduction of the oxygen carrier can be saved.
- Another object of the invention is to produce a particularly hard catalyst which can withstand the mechanical stress in industrial reactors without disintegrating.
- inexpensive and available carriers with a high surface area and a high pore volume should be able to be used.
- Catalysts suitable according to the invention consist of one or more reducible bismuth (5) mixed oxide phases which can be applied to a basic or neutral support and can be regarded as bismuthates (5).
- Bismutates of Na, K, Cs, Sr, Ba, and La are particularly preferred.
- K-bismuthates (5) of the general formula KBi y O z are particularly preferred, where y can have a value between 0.5 and 2 and z a value between 1.25 and 5.5, so that Bi is at least partially in the high range Oxidation level +5 is present and therefore the catalyst has a high oxide ion potential.
- Also preferred active phases are Na and Ba bismuthates (5) of the general formula NaBi s O c and Ba (Bi s O t ) 2 where s has a value between 0.25 and 3 and t has a value between 1.625 and 5.5 can accept.
- a preferred production process for the bismuthates according to the invention is the wet-chemical preparation by oxidation of Bi 2 0 3 in alkaline solution with bromine, since it can be calcined at low temperature (in comparison to solid-body reactions) and thus maintain the high surface area and the pore volume of the support stay.
- the bi-mixed oxide active phases are preferably applied to a support, for mechanical reasons
- Basic carriers suitable according to the invention are selected from the group consisting of alkali / alkaline earth / SE / Zn-titanates, alkali / alkaline earth / SE / Zn-Al spinels, alkali / alkaline earth / SE / Zn-silicates, MgO, CaO, hydrotalcites, pyroaurites or alkalized supports such as KF / AI 2 O3, LiP ⁇ 4 / Al 2 ⁇ 3 with a basic surface finish or neutral supports selected from the group Sie, Sij 4 . MgO, Al spinel, SiC are particularly preferred. Such carriers are advantageously inexpensive, easy to manufacture, have large surfaces and good hardness.
- the bismuth (5) mixed oxide support catalysts according to the invention can be prepared by known methods, such as dry mixing, precipitation, conspicuity, co-precipitation, spray drying, impregnation, drinking, spray impregnation, hicoating, washcoating, etc.
- the dehydrogenation is carried out at 200 to 800 ° C, preferably 350 to 550 ° C, and preferably in the range of atmospheric pressure.
- the pressure 100 mbar to 10 bar, preferably 500 mbar to 2 bar.
- the space-time yield (LHSV; liquid hourly space velocity) is 0.01 to 20 h- 1 , preferably 0.1 to 5 h- 1 .
- diluents such as CO 2 , N 2 , an inert gas or water vapor can be present in the feed stream.
- the regeneration of the reduced catalyst is carried out in the range 300 to 900, preferably 400 to 800 ° C. with a free oxidizing agent, preferably air, lean air, oxygen or NO. Diluents may be present in the reactor feed.
- the regeneration can be carried out at subatmospheric negative pressure, atmospheric or superatmospheric pressure. Pressures in the range from 500 mbar to 10 bar are preferred.
- the catalytic-oxidative dehydrogenation of ethylbenzene to styrene is investigated in a so-called pulse reactor at 500 ° C. 0.3 to 0.6 g of catalyst in a microfixed bed are "pulsating", ie alternately, for 90 seconds with pure ethylbenzene (without carrier gas) and helium as a substitute and the resulting reaction products are quantitatively recorded for each pulse by gas chromatography.
- the flow rate of the gases is 21.5 ml / min.
- a single pulse contains approx. 380 ⁇ g ethylbenzene. In this way, the time behavior of the catalyst can be tracked from the beginning with a high time resolution without dead times.
- the catalyst is highly active, so that almost quantitative conversion of ethylbenzene is observed.
- the selectivity to styrene steadily improves to an end value.
- the catalyst is deactivated more and more as its oxygen content is consumed, so that the conversion decreases.
- regeneration takes place after 90 to 200 pulses.
- the styrene yield as a product of selectivity and conversion generally goes through a flat maximum. The yields determined are listed in the table in part (1st-4th-7th-11th-21st-31st pulse).
- the suspension is stirred for 8 hours at room temperature, filtered off, with distilled water. Washed water and dried over P 4 O 10 .
- Catalyst preparation 7 g of Bi 2 O 3 and 21 g of SiC are added to 130 ml of 50% KOH solution and the rest of the procedure is as described above.
- a catalyst is produced according to the specification of EP-Al-0482 276. 336.3 g of ammonium metavanadate and 900 g of magnesium oxide are stirred into 8 l of water and then stirred vigorously for 1 hour. It is then sprayed on the spray dryer. The spray powder obtained is treated in a kneader for 2 hours, with little water and extractive agents being kneaded into the kneading compound. The modeling clay is then shaped into 3 mm full strands using an extruder. The strands are dried at 120 ° C. for 16 hours and then calcined at 600 ° C. for 4 hours. A uniformly yellow-colored strand with very low hardness is obtained. A 0.05 to 0.1 mm grit fraction is sieved out for the experiments. The catalyst contains 22.5% by weight of V 2 O and 77.7% by weight of MgO. Table: Sales results in the pulse reactor at 500 ° C
- Example 1 1.9 0.7 0.5 0.5 0.3 0.3
- Example 2 6 0.5 0.3 0.2 0.1 0.1
- Example 5 10.4 1.5 0.9 0.7 0.6 0.3
- the comparative catalyst is very active and allows a high maximum styrene yield.
- the decisive disadvantage is the strong initial gasification, which leads to enormous losses of ethylbenzene and is at the expense of the oxygen reservoir of the catalyst.
- the first ethylbenzene pulses are completely burned (100% gasification to worthless carbon dioxide), so that the calculated initial selectivity for styrene over the first pulses is zero.
- the systems according to the invention are characterized by significantly lower gasification with likewise very high activity.
- the catalyst according to the invention produces slightly increased amounts of benzene and toluene in the initial phase, these then decrease rapidly as the reaction time progresses.
- the formation of benzene and toluene is unproblematic compared to
- the catalyst according to the invention is therefore also superior to the prior art in this regard, regardless of the fact that the mean styrene yield, i.e. the total yield of styrene recorded over a whole measuring cycle and related to one cycle is higher than the yield achievable with the known catalysts.
- Initial gasification i.e. the overall performance of the catalyst is made possible by better selectivity for styrene at the beginning of a cycle.
- the catalyst according to the invention also has significantly better mechanical strength than the comparison catalyst and is particularly resistant to abrasion.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
Description
Claims
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP97942868A EP0931040A1 (de) | 1996-09-11 | 1997-08-21 | Verfahren und katalysator für die katalytische oxidative dehydrierung von alkylaromaten und paraffinen |
JP10513189A JP2001500137A (ja) | 1996-09-11 | 1997-08-21 | アルキル芳香族およびパラフィン化合物の接触的酸化脱水素方法およびこの目的用の触媒 |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE1996136884 DE19636884A1 (de) | 1996-09-11 | 1996-09-11 | Verfahren und Katalysator für die katalytische oxidative Dehydrierung von Alkylaromaten und Paraffinen |
DE19636884.7 | 1996-09-11 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO1998011038A1 true WO1998011038A1 (de) | 1998-03-19 |
Family
ID=7805241
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP1997/004546 WO1998011038A1 (de) | 1996-09-11 | 1997-08-21 | Verfahren und katalysator für die katalytische oxidative dehydrierung von alkylaromaten und paraffinen |
Country Status (4)
Country | Link |
---|---|
EP (1) | EP0931040A1 (de) |
JP (1) | JP2001500137A (de) |
DE (1) | DE19636884A1 (de) |
WO (1) | WO1998011038A1 (de) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN102533391A (zh) * | 2012-02-16 | 2012-07-04 | 华北电力大学 | 新型夹层核壳结构铁基载氧体及其制备方法 |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
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KR20070086361A (ko) * | 2004-11-18 | 2007-08-27 | 셀 인터나쵸나아레 레사아치 마아츠샤피 비이부이 | 티타늄 농도가 낮은 고도 활성 및 고도 안정성 산화철계탈수소화 촉매, 이의 제조방법 및 용도 |
CN114561195A (zh) * | 2022-04-28 | 2022-05-31 | 河北钢研德凯科技有限公司 | 用于镁合金熔模铸造的冷却元件材料及其制备方法和应用 |
Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE4436385A1 (de) * | 1994-10-12 | 1996-04-18 | Basf Ag | Verfahren zur katalytischen oxidativen Dehydrierung von Alkylaromaten und Paraffinen |
DE4437252A1 (de) * | 1994-10-18 | 1996-04-25 | Basf Ag | Katalysator und Verfahren für die katalytische oxidative Dehydrierung von Alkylaromaten und Paraffinen |
-
1996
- 1996-09-11 DE DE1996136884 patent/DE19636884A1/de not_active Withdrawn
-
1997
- 1997-08-21 WO PCT/EP1997/004546 patent/WO1998011038A1/de not_active Application Discontinuation
- 1997-08-21 EP EP97942868A patent/EP0931040A1/de not_active Ceased
- 1997-08-21 JP JP10513189A patent/JP2001500137A/ja active Pending
Patent Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE4436385A1 (de) * | 1994-10-12 | 1996-04-18 | Basf Ag | Verfahren zur katalytischen oxidativen Dehydrierung von Alkylaromaten und Paraffinen |
DE4437252A1 (de) * | 1994-10-18 | 1996-04-25 | Basf Ag | Katalysator und Verfahren für die katalytische oxidative Dehydrierung von Alkylaromaten und Paraffinen |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN102533391A (zh) * | 2012-02-16 | 2012-07-04 | 华北电力大学 | 新型夹层核壳结构铁基载氧体及其制备方法 |
CN102533391B (zh) * | 2012-02-16 | 2014-06-25 | 华北电力大学 | 新型夹层核壳结构铁基载氧体及其制备方法 |
Also Published As
Publication number | Publication date |
---|---|
DE19636884A1 (de) | 1998-03-12 |
JP2001500137A (ja) | 2001-01-09 |
EP0931040A1 (de) | 1999-07-28 |
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