This is a national stage application filed under 35 U.S.C. §371 of international application PCT/EP2013/070731, filed under the authority of the Patent Cooperation Treaty on Oct. 4, 2013, published; which claims the benefit of Italian Patent Application No. MI2012A001673, filed on Oct. 5, 2012. The entire disclosures of all the aforementioned applications are expressly incorporated herein by reference for all purposes.
The present patent application relates to a process for the production of high-purity isobutene through the cracking of MTBE (methyl-tert butyl ether) or ETBE (ethyl-tert butyl ether) and an integrated process for the production of the relative ether (MTBE or ETBE).
The process for the production of isobutene is an endothermic cracking reaction typically of commercial MTBE, i.e. with a purity degree normally higher than 98% by weight (according to the sales specification).
The reaction takes place in the presence of an extremely selective catalyst without any problems of corrosion, which should have a relatively long life cycle, without creating problems of toxicity for the environment.
The catalyst must be acid and active: the activity guarantees a high conversion of MTBE per reaction step, whereas the acidity limits side-reactions and the formation of byproducts.
The cracking reaction takes place in vapour phase in a tubular reactor in which the catalyst is positioned at the tube side, with a conversion of MTBE higher than 80%, operating at a temperature ranging from 100 to 300° C., using vapour at a suitable pressure or diathermic oil, as heating means.
The production plant of isobutene from the cracking of oxygenated compounds is generally divided into three sections: a reaction section, a section for the recovery and purification of isobutene and a section for the recovery of methanol and its possible purification.
The isobutene is then used in plants for the production of rubber or for the production of chemicals.
The production scheme generally consists of reactor, fractionation and washing column in sequence.
From the production schemes of isobutene of the known art, it is difficult to effect:
It has now been found that the disadvantages of the known art indicated above can be eliminated or substantially reduced by means of a solution which comprises inverting the washing column with the fractionation column, consequently positioning the washing column before the fractionation column, thus avoiding having to operate in the presence of azeotropic mixtures which are difficult to separate.
All the methanol (or ethanol in the case of ETBE) and water are recovered during the washing thus facilitating the recovery of unconverted MTBE (or ETBE).
In particular, in the case of MTBE, in order to control the formation of by-products, above all DME, a side-stream present in the case of methanol Grade A or the water recovered from the condensates produced in the plant, is recycled to the reactor.
The process, object of the present invention, for the production of high-purity isobutene starting from a stream prevalently containing MTBE (Methyl-Tert Butyl Ether) or ETBE (Ethyl-Tert Butyl Ether) essentially comprises the following areas in sequence:
Said process for the production of isobutene starting from MTBE preferably comprises the following steps:
The stream at the bottom of the washing column containing methanol and water can be sent to a single fractionation column, separating a stream containing methanol and ethers at the head, and at the bottom, water recycled to the washing column or to a first fractionation column, separating high-octane mixtures (HOM) at the head, substantially consisting of alcohols and ethers, and a stream of water and methanol at the bottom, which is sent to a second fractionation column, separating a stream of high-purity methanol, Grade A, at the head, and the water recycled to the washing column at the bottom.
A stream, recycled to the cracking reactor(s), can also be removed laterally from the possible second fractionation column of the stream of water and methanol.
The stream at the bottom containing MTBE of the fractionation column for separating isobutene from MTBE may preferably be recycled to the fractionation column(s) for purifying MTBE.
The fractionation column for the purification of MTBE can operate at a pressure ranging from 1 to 12 barg, preferably from 4 to 8 barg.
The cracking reactor(s) can operate at a temperature ranging from 100 to 300° C., preferably from 150 to 240° C., and at a pressure ranging from 1 to 10 barg, preferably from 3 to 6 barg.
The cracking reactor(s) can operate with a wide variety of acid catalysts selected from ion exchange resins, suitably modified zeolites, catalysts based on silicified alumina, boralites, zeolites and silica suitably modified. Among these catalysts, the use of silica modified with the addition of alumina in a quantity ranging from 0.1 to 3% by weight (EP-524679) is preferred.
The washing column of the stream leaving the cracking reactor(s) can operate at a temperature ranging from 20 to 100° C., preferably from 30 to 50° C., and at a pressure ranging from 2 to 15 barg, preferably from 6 to 9 barg.
The fractionation column for the separation of isobutene from the MTBE can operate at a pressure at the head ranging from 2 to 10 barg, preferably from 4 to 6 barg.
The fractionation column for the purification of isobutene can operate at a pressure at the head ranging from 2 to 15 barg, preferably from 6 to 9 barg.
The fractionation column(s) of the stream prevalently containing methanol and water coming from the bottom of the washing column can operate at a pressure at the head ranging from atmospheric pressure to 10 barg, preferably from 0.1 to 5 barg.
A further object of the present invention relates to the integrated process for the production of MTBE or ETBE and high-purity isobutene.
The integrated process for the production of MTBE or ETBE and high-purity isobutene, starting from streams prevalently containing C4 hydrocarbons, essentially comprises the following areas, already described above for the production of isobutene:
In particular, the integrated process for the production of MTBE and high-purity isobutene, starting from streams prevalently containing C4 hydrocarbons, essentially comprises the following areas, already described above for the production of isobutene:
Said integrated process for the production of MTBE preferably essentially comprises the following steps already described above for the production of isobutene:
The purification step of MTBE, both in the case of one etherification area and in the case of two etherification areas, is preferably effected in a single fractionation column.
The etherification reactor(s) can operate with a wide variety of acid catalysts selected from mineral acids (e.g. sulfuric acid, BF3, supported phosphoric acid), zeolites suitably modified, heteropolyacids and sulfonated polymeric resins, for example Amberlyst 15, Amberlyst 35 , Amberlyst 36, etc. Among these catalysts, the use of macroreticular sulfonated resins, generally copolymers of styrene and divinylbenzene, is preferred. The characteristics of these resins are widely described in literature (see for example A. Mitschker, R. Wagner, P. M. Lange, “Heterogeneous Catalysis and fine Chemicals”, M. Guisnet ed, Elsevier, Amsterdam (1988)).
The reaction can be carried out in tubular or adiabatic reactors, either in vapour phase or liquid phase, liquid phase being preferred.
The preferred operating conditions for operating in liquid phase are: a temperature ranging from 20 to 150° C., preferably from 30 to 100° C., and a pressure lower than 50 barg, preferably from 2 to 25 barg.
The additional washing column of the stream containing C4 hydrocarbons and methanol can operate at a temperature ranging from 20 to 100° C., preferably from 30 to 50° C. and at a pressure ranging from 2 to 30 barg preferably from 10 to 15 barg.
The disclosures provided in the description for MTBE can also be easily applied to ETBE, for an expert in the field.
Some preferred embodiments of the invention are now provided with the help of the enclosed
A stream (1) prevalently containing MTBE is fed to a fractionation column (C-1) for the purification of the MTBE, from which a stream (2) containing MTBE and compounds lighter than MTBE is separated at the head, a stream (3) of MTBE having a purity higher than 98% by weight is separated laterally and a stream (4) containing MTBE and compounds heavier than MTBE is separated at the bottom.
The stream (3) of MTBE having a purity higher than 98% by weight is sent to a cracking reactor (R-1) from which a stream (5) containing the cracking products and non-reacted reagents exits, which is fed to a washing column (C-2) with water, from which a stream (6) containing isobutene, MTBE and light compounds is separated at the head and a stream (7) prevalently containing methanol and water at the bottom, which is sent to a fractionation column (C-3) for the separation of the methanol from the water, obtaining a stream (8) at the head, containing methanol, and a stream (9) at the bottom, containing water, which is sent to the washing column (C-2).
The stream (6) containing isobutene, MTBE and light compounds is sent to a fractionation column (C-4) for the separation of the isobutene from the MTBE, obtaining, at the head, a stream (10) containing isobutene and light compounds, which, in turn, is sent to a fractionation column (C-5) for purification of the isobutene, and at the bottom, a stream (11) containing non-converted MTBE.
From the fractionation column (C-5), a stream (12) containing light compounds is separated at the head, and a stream (13) of high-purity isobutene, at the bottom.
Stream (11) containing MTBE can be possibly recycled to the fractionation column (C-1).
Streams (2) and (4), containing MTBE and respectively compounds lighter than MTBE and compounds heavier than MTBE, among which di-isobutene, can be possibly joined (called HOM (High octane mixture)) and sent to a gasoline pool. The stream (8) containing methanol leaving the fractionation column (C-3) has a percentage of MTBE which is such as to allow it to be used for the production of MTBE.
The stream (8) containing methanol (Grade A) obtained, is at a higher purity than that obtained in
A stream (16) containing methanol, water and other oxygenated products in the cracking reaction can be possibly removed laterally from the fractionation column (C-3), which can be recycled to the cracking reactor (R-1) or joined with streams (2) and/or (4).
A stream (22) essentially consisting of methanol (20) and a C4 cut (21) , is sent to a first tubular etherification reactor (R-T1) and the outgoing product (23) to a second adiabatic etherification reactor (R-A1), obtaining a stream (1) prevalently containing MTBE, which is fed to the fractionation column (C-1), the same column (C-1) as the scheme of
The stream (3) removed laterally from said fractionation column (C-1), containing MTBE having a purity higher than 98% by weight, is sent to the cracking reactor (R-1) of the scheme of
The stream (2) removed at the head from said fractionation column (C-1), containing C4 hydrocarbons, among which non-converted isobutene and lighter compounds formed in the etherification reaction, is sent to a washing column (C-L) with water, separating, at the head, a stream (24) containing C4 hydrocarbons from a stream (25) containing, at the bottom, methanol and water, which is sent to the fractionation column (C-3), the same column (C-3) as the scheme of
The stream (4), taken at the bottom from said fractionation column (C-1), containing MTBE and compounds heavier than MTBE, is removed from the plant to be sent to a gasoline pool.
Number | Date | Country | Kind |
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MI2012A1673 | Oct 2012 | IT | national |
Filing Document | Filing Date | Country | Kind |
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PCT/EP2013/070731 | 10/4/2013 | WO | 00 |
Publishing Document | Publishing Date | Country | Kind |
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WO2014/053645 | 4/10/2014 | WO | A |
Number | Name | Date | Kind |
---|---|---|---|
6072095 | Marion | Jun 2000 | A |
6143936 | Marion | Nov 2000 | A |
6696612 | Yamase | Feb 2004 | B2 |
6852899 | Yamase | Feb 2005 | B2 |
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Number | Date | Country | |
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20150251968 A1 | Sep 2015 | US |