WO1993021138A1 - Olefin production - Google Patents
Olefin production Download PDFInfo
- Publication number
- WO1993021138A1 WO1993021138A1 PCT/GB1993/000765 GB9300765W WO9321138A1 WO 1993021138 A1 WO1993021138 A1 WO 1993021138A1 GB 9300765 W GB9300765 W GB 9300765W WO 9321138 A1 WO9321138 A1 WO 9321138A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- isomerisation
- hydrogen
- stream
- transhydrogenation
- product
- Prior art date
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Classifications
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C11/00—Aliphatic unsaturated hydrocarbons
- C07C11/02—Alkenes
-
- 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
- C07C5/50—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with an organic compound as an acceptor
- C07C5/52—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with an organic compound as an acceptor with a hydrocarbon as an acceptor, e.g. hydrocarbon disproportionation, i.e. 2CnHp -> CnHp+q + CnHp-q
Definitions
- This invention relates to the production of olefins and in particular to the production of branched chain olefins, particularly 2-methyl propene (iso-butene, hereinafter i-butene).
- i-Butene is a valuable chemical intermediate and is in increasing demand as a reactant for the production of methyl t-butyl ether (MTBE) by reaction of i-butene with methanol.
- MTBE methyl t-butyl ether
- i-Butene and other branched chain olefins, are usually produced by subjecting a suitable paraffin stream containing straight chain paraffins, eg n-butane, to isomerisation by passage over a suitable catalyst, which is often a sodium aluminium silicate material such as Na-zeolite, to give branched chain paraffins, eg 2-methyl propane, (iso-butane, hereinafter i-butane). The resultant i-butane is then dehydrogenated to give i-butene.
- a suitable paraffin stream containing straight chain paraffins eg n-butane
- a suitable catalyst which is often a sodium aluminium silicate material such as Na-zeolite
- the dehydrogenation is effected by a procedure termed transhydrogenation.
- a hydrogen-donor such as a paraffin
- a hydrogen-acceptor such as an unsaturated compound
- the hydrogen-donor may be dehydrogenated further, to the corresponding diene, and/or that a mixture of the paraffin and the corresponding olefin may be dehydrogenated, by reaction with the hydrogen-acceptor olefin, to give a mixture of the olefin and diene corresponding to the paraffin.
- n-butane and butene-1 or butene-2 may be reacted with ethene as the hydrogen-acceptor olefin to give a mixture of butene-1, butene-2, and butadiene-1,3.
- transhydrogenation to produce i-butene is described in EP-A-474188 where n-butenes, eg butene-1, are transhydrogenated with i-butane to give-n-butane and i-butene. That reference discloses the separation of the i-butene by reaction with methanol to form MTBE and recycle of the n-butane to the transhydrogenation step via an isomerisation unit wherein the n-butane is converted to i-butane.
- a more highly unsaturated compound such as a diene or acetylene, is used as the hydrogen- acceptor in place of a mono-olefin hydrogen-acceptor. This results in net olefin production.
- a process for the production of a branched chain olefin comprises subjecting a hydrocarbon stream containing at least one straight chain paraffin having 4 or more carbon atoms to isomerisation and transhydrogenation with a stream containing at least one hydrogen-acceptor that is more highly unsaturated than a mono-olefin, thereby producing a stream containing at least one branched chain olefin product, separating said product to give a stream depleted of said product, and recycling at least part of the stream depleted of said product to before the isomerisation and transhydrogenation stages.
- the transhydrogenation may be effected before, at the same time as, or after, isomerisation.
- the paraffin stream may contain branched, as well as straight, chain compounds. Where the transhydrogenation is effected before isomerisation, the straight-chain paraffin, and any branched chain paraffin present, act as the hydrogen-donor. If the trans ⁇ hydrogenation is effected after isomerisation, the isomerisation products, ie branched chain paraffin, and any remaining straight chain paraffin, act as the hydrogen-donor.
- the amount of hydrogen-acceptor is preferably such that there are 0.5 to 20 moles of said hydrogen-donor for each mole of hydrogen-acceptor.
- the amount of said hydrogen-acceptor hydrocarbon hydrogenated is such that the heat of hydrogenation of said hydrogen-acceptor hydrocarbon provides at least 252 of the heat required for dehydrogenation of said hydrogen-donor hydrocarbon.
- dehydrogenation reactions In the absence of a hydrogen-acceptor compound, dehydrogenation reactions generally are endothermic and, to obtain a useful conversion, have to be effected at high temperatures. At such temperatures dehydrogenation is usually accompanied by thermal cracking with the formation of carbon deposits. Such carbon deposits tend to build up on the catalyst de-activating the latter: frequent regeneration of the catalyst is required wherein the deposited carbon is burnt off by subjecting the catalyst to a stream of a heated oxygen-containing gas such as air.
- transhydrogenation may be effected under reaction conditions, eg lower temperatures or in the presence of hydrogen, at which only little dehydrogenation of the hydrogen-donor would take place in the absence of the hydrogen-acceptor and, under such conditions, there may be less tendency to carbon deposition even though, in the absence of the hydrogen-donor, such hydrogen- acceptor compounds may exhibit a significant tendency to thermal cracking with carbon deposition.
- the heat required for the dehydrogenation of the hydrogen-donor is in effect provided by hydrogenation of the hydrogen-acceptor.
- at least 25Z, particularly at least 50Z, and more particularly at least 70Z, of the heat required for dehydrogenation of the hydrogen-donor is in effect provided by the exothermic hydrogenation of the hydrogen-acceptor.
- the reaction conditions may be adjusted such that the reaction is net endothermic, net exothermic, or thermally neutral: this simplifies and reduces the cost of the transhydrogenation reactor.
- the reaction can be effected in the presence of hydrogen and the reaction conditions may be such that there is a net production or net consumption of hydrogen.
- the ability to operate in the presence of hydrogen may be advantageous to decrease the tendency to coke formation.
- the hydrogen-acceptor stream may typically comprise at least one diene and/or acetylene alone or in admixture with at least one mono-olefin and./or at least one paraffin.
- suitable hydrogen-acceptor streams include propyne, propadiene, butadiene-1,2, butadiene-1,3, and mixtures thereof, eg propyne " plus propadiene; C streams such as a mixed C4 stream from a steam cracker; and C5 gasoline, and/or full range pygas, streams from a cracker.
- the feedstock stream contains one or more straight chain paraffins containing 4 or,more carbon atoms, eg n-butane; it may also contain a proportion of one or more branched chain paraffins such as i-butane.
- the hydrogen-acceptor and hydrogen-donor compounds may contain the same number of carbon atoms: in this way the olefin produced will also contain the same number of carbon atoms.
- the stream containing the straight chain paraffin may be a stream comprising n-butane and the hydrogen-acceptor stream is butadiene or a mixed C4 stream containing butadiene.
- the operating conditions eg temperatures and pressures, employed will depend on the choice of catalyst, the hydrogen partial pressure, and the nature of the hydrogen-donor and hydrogen-acceptor. Preferably the conditions are such that a total of at least 10Z by weight of the hydrogen-donor is dehydrogenated.
- the total pressure is preferably in the range 0.3 to 20, particularly 0.5 to 10, and more particularly in the range 1 to 5, bar abs.
- the partial pressure of hydrogen-donor plus hydrogen- acceptor is preferably in the range 0.1 to 20, particularly 0.1 to 5, bar abs.
- the temperature is preferably in the range 200 to 800°C, particularly 450 to 700°C.
- the amount of hydrogen-donor is from 0.5 to 20, particularly 1 to 10, and more particularly 2 to 10, moles for each mole of hydrogen-acceptor employed.
- the molar amount, if any, of hydrogen added is less than 10 times the total molar amount of hydrocarbon present.
- the reaction may be effected in the presence of a diluent such as steam which, in some cases, may suppress coke formation and/or may serve to activate the catalyst. Methane may alternatively or additionally be used as a diluent.
- the transhydrogenation process is effected in the presence of a dehydrogenation catalyst.
- dehydrogenation catalyst we mean a catalyst that exhibits activity for dehydrogenation of the hydrogen-donor under the conditions employed. The catalyst employed will depend on the nature of the hydrogen-acceptor and hydrogen-donor compounds.
- Suitable catalysts include noble metals, eg platinum and/or other platinum group metals such as palladium, on a support such as alumina; such catalysts modified with other species, eg Group IV elements such as tin; chromia, alone or in conjunction with a platinum group metal or iron oxide, on a support such as alumina, zirconia and/or alkaline earth oxides, especially those stabilised for use at high temperatures; platinum group metals supported on such supports. Sulphided versions of the above catalysts and/or molybdenum sulphide may also be used.
- platinum on alumina may not be suitable for some processes as some polyunsaturated compounds, eg butadiene, may be so strongly adsorbed that there is negligible reaction with the hydrogen-donor, eg paraffin.
- Chromia optionally in admixture with a platinum group metal, and preferably doped with alkali, on alumina is particularly suitable.
- Another particularly suitable catalyst is a mixture of platinum and tin, supported on alumina, again preferably doped with alkali. In alkali doped catalysts, the alkali is preferably potassium or cesium.
- the catalyst may be regenerated periodically by passing hot air, optionally mixed with an inert such as nitrogen, over the catalyst.
- Other regeneration processes known in the dehydrogenation art, using eg steam and/or hydrogen, m y be employed.
- a moving catalyst bed type of reactor may be employed. As indicated above the isomerisation reaction may be effected at the same time as transhydrogenation.
- transhydrogenation and isomerisation catalysts or to employ a catalyst that exhibits activity for both processes.
- a mixture of platinum and tin on alumina exhibits both trans ⁇ hydrogenation and isomerisation activity.
- Other catalysts that exhibit isomerisation activity are known in the art and are generally strongly acidic.
- suitable catalysts include noble metals such as platinum or palladium on supports such as alumina, alumino-silica es, boro-aluminates, zeolites, ordenite, and the like; activated alumina and acidic zeolitic materials; and halogen-containing derivatives of zirconia, alumina, and alkaline earth oxides.
- the transhydrogenation is preferably effected in the presence of hydrogen.
- the products from the transhydrogenation process will contain some hydrogen, and also other low molecular weight products such as methane, and/or hydrocarbons containing 2-3 carbon atoms. These may be separated before separation of the desired branched chain olefin product: where isomerisation follows transhydrogenation, these low molecular weight compounds may be separated before or after isomerisation.
- isomerisation is effected after transhydrogenation, and the isomerisation catalyst also exhibits activity for the hydrogenation of olefins, it is preferred to separate hydrogen from the trans ⁇ hydrogenation product before the isomerisation stage.
- the product of transhydrogenation and isomerisation will contain, in addition to the branched chain olefin product, some paraffin and/or straight chain olefin as a result of incomplete isomerisation and/or transhydrogenation.
- the desired branched chain olefin product is then separated. This separation may be by physical means, eg fractionation, or may be by a chemical route.
- the mixture of branched chain olefin and straight chain olefin and/or paraffin preferably after separation of the aforesaid low molecular weight compounds, may be fed to a reactor wherein a compound such as MTBE is synthesised from the branched chain olefin: that compound is then separated and the residual components recycled.
- At least part of these residual components are recycled to before the isomerisation and transhydrogenation stages.
- a feedstock stream of n-butane, or a mixture thereof with i-butane, fed via line 10 is mixed with a cracker C stream containing a mixture of butenes, butanes, and butadiene, fed via line 12.
- Butadiene-1,2 is often present as a small proportion of the total butadienes, and for simplicity hereinafter, except where the contrary is indicated, when reference is made to butadiene we mean a mixture of butadienes containing butadiene-1,3 and not more than 20Z by weight of butadiene-1,2.
- this isomerisation unit is operated under conditions effective to isomerise at least part of the n-butenes as well as n-butane.
- the resultant isomerisation product comprising i-butane, i-butene, in admixture with unconverted n-butane and n-butenes and butadiene, is then fed via line 20 to a reactor 22 wherein transhydrogenation is effected, giving a transhydrogenation product mixture comprising i-butene, i-butane, n-butane, n-butenes, light hydrocarbons, and hydrogen.
- This transhydrogenation product is fed via line 24 to a separator 26 wherein hydrogen and light hydrocarbons are separated as a light stream 28 and a stream 30 predominantly comprising C hydrocarbons.
- Stream 30 is then fed to a MTBE synthesis stage 32 wherein MTBE is synthesised from the i-butene in the stream 30 and methanol supplied via line 34.
- the MTBE and unreacted methanol are separated, by means not shown, to give a MTBE product stream 36, and a stream of unreacted C4 hydrocarbons which is recycled as the aforesaid stream 16.
- the light stream 28 is fed from the separator 26 to a hydrogen recovery unit 38 wherein the hydrogen is separated into a stream 40 enriched in hydrogen and a stream 42 comprising essentially low molecular weight hydrocarbons.
- the hydrogen is recycled to the isomerisation and transhydrogenation stages via line 14.
- make-up hydrogen is imported or the excess of hydrogen exported via line 44.
- make-up hydrogen is imported or the excess of hydrogen exported via line 44.
- the hydrogen stream 14 may be added to stream 20, instead of being mixed with the streams 10, 12 and 16 fed to the isomerisation unit.
- the recycle stream 16 may be subjected to a separation stage (not shown) to give a butenes stream which is added to stream 20 and a butanes stream which is recycled as shown to isomerisation stage 18.
- the cracker C stream 12 is desirably added to stream 20 rather than being fed to isomerisation unit 18. While this may give a larger recycle stream leaving the MTBE synthesis stage 32, the butenes recycled to stream 20 will undergo transhydrogenation in unit 22 with i-butane produced in isomerisation unit 18, and the butanes recycled to isomerisation unit 18 will be isomerised therein.
- heat exchangers (not shown) will be employed to modify the temperatures between the various stages.
- heat exchange can be effected between the transhydrogenation product and the feed thereto.
- the isomerisation stage follows transhydrogenation: in this case, the isomerisation and/or transhydrogenation stages preferably exhibit significant activity for the isomerisation of olefins: isomerisation and trans- hydrogenation stages exhibiting only paraffin isomerisation activity would necessitate a large recycle of paraffin in stream 16. Integration of the isomerisation and transhydrogenation stages into a single stage, eg by using a catalyst that exhibits both transhydrogenation and isomerisation activity, is advantageous in requiring fewer reaction vessels.
- the following examples illustrates the isomerisation activity of a transhydrogenation catalyst.
- Propane was catalytically transhydrogenated in the presence of hydrogen with a C stream typical of the product from steam cracking a hydrocarbon feedstock.
- the catalyst employed was platinum/tin on alumina (1Z of a Pt/Sn mixture having a Pt/Sn weight ratio of 1:1).
- hydrogen was passed over the catalyst at 550°C to ensure that the catalyst was fully reduced.
- a mixture of propane (about 40Z v/v), hydrogen (about 50Z v/v), and C4 stream (about 10Z v/v) was then passed at atmospheric pressure over the catalyst at 550°C at a weight hourly space velocity of 5.5 h -1 (ie 5.5 g of feed per g of catalyst per hour).
- the composition of the feed gas and the effluent gas is shown in Table 1.
- the calculated heat of hydrogenation of the butadiene exceeds the calculated heat of dehydrogenation of the propane.
- Example 2 In this example n-butane was catalytically trans- hydrogenated in the presence of hydrogen with a butadiene stream using a fresh sample of the catalyst employed in Example 1.
- Table 2 The composition of the feed gas and product at various times is shown in Table 2.
- the catalyst was then regenerated by passing air over the catalyst at 500°C to burn off the coke, and then the regenerated catalyst was fully reduced with hydrogen at 500°C and used for the transhydrogenation/isomerisation at 500°C of a different gas mixture containing about 7Z by volume butadiene, 56Z by volume n-butane, and 37Z by volume hydrogen.
- the composition of the feed gas and product at various times is shown in Table 3.
- Example 3 To illustrate the isomerisation activity of the catalyst in the absence of transhydrogenation, butene-1 was passed at 550°C over a fresh sample of the catalyst used in the previous examples and which had been fully reduced by passing hydrogen thereover at 550°C.
- the feed and product compositions are as shown in Table 4.
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US08/318,723 US5639926A (en) | 1992-04-14 | 1993-04-13 | Process for producing a branched chain olefin by isomerization and transhydrogenation |
DE69312481T DE69312481T2 (en) | 1992-04-14 | 1993-04-13 | METHOD FOR THE PRODUCTION OF OLEFINS |
EP93908032A EP0636114B1 (en) | 1992-04-14 | 1993-04-13 | Olefin production |
Applications Claiming Priority (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB919109691A GB9109691D0 (en) | 1991-05-03 | 1991-05-03 | Transhydrogenation |
GB919121732A GB9121732D0 (en) | 1991-10-14 | 1991-10-14 | Olefin production |
GB929208154A GB9208154D0 (en) | 1991-05-03 | 1992-04-14 | Transhydrogenation |
GB9208154.6 | 1992-04-14 | ||
GB929220958A GB9220958D0 (en) | 1992-04-14 | 1992-10-06 | Olefin production |
GB9220958.4 | 1992-10-06 |
Publications (1)
Publication Number | Publication Date |
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WO1993021138A1 true WO1993021138A1 (en) | 1993-10-28 |
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Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/GB1993/000765 WO1993021138A1 (en) | 1991-05-03 | 1993-04-13 | Olefin production |
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Country | Link |
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WO (1) | WO1993021138A1 (en) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5639926A (en) * | 1992-04-14 | 1997-06-17 | Institut Francais Du Petrole | Process for producing a branched chain olefin by isomerization and transhydrogenation |
US9051230B2 (en) | 2011-04-20 | 2015-06-09 | Uop Llc | Processes for producing propylene from paraffins |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3211635A (en) * | 1961-04-14 | 1965-10-12 | Phillips Petroleum Co | Production of olefins from paraffins and acetylenes |
US4546204A (en) * | 1983-11-07 | 1985-10-08 | Imperial Chemical Industries Australia Limited | Process for the manufacture of methyl t-butyl ether |
WO1992019575A1 (en) * | 1991-05-03 | 1992-11-12 | Imperial Chemical Industries Plc | Transhydrogenation |
-
1993
- 1993-04-13 WO PCT/GB1993/000765 patent/WO1993021138A1/en active IP Right Grant
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3211635A (en) * | 1961-04-14 | 1965-10-12 | Phillips Petroleum Co | Production of olefins from paraffins and acetylenes |
US4546204A (en) * | 1983-11-07 | 1985-10-08 | Imperial Chemical Industries Australia Limited | Process for the manufacture of methyl t-butyl ether |
WO1992019575A1 (en) * | 1991-05-03 | 1992-11-12 | Imperial Chemical Industries Plc | Transhydrogenation |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5639926A (en) * | 1992-04-14 | 1997-06-17 | Institut Francais Du Petrole | Process for producing a branched chain olefin by isomerization and transhydrogenation |
US9051230B2 (en) | 2011-04-20 | 2015-06-09 | Uop Llc | Processes for producing propylene from paraffins |
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