Classifications

• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
  • C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
  • C07C2/56—Addition to acyclic hydrocarbons
  • C07C2/58—Catalytic processes
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C2529/00—Catalysts comprising molecular sieves
  • C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays

Definitions

• the invention relates to a process for the catalytic conversion of at least one isoparaffin with 4 to 6 C atoms per molecule with at least one olefin with 2 to 6 C atoms per molecule in the liquid phase to an alkylate-containing product.
• the invention is based on the object of carrying out this process inexpensively with a high alkylate yield and a low proportion of by-products.
• This is achieved according to the invention in that an suspension containing isoparaffin and a granular zeolite catalyst is fed to the upper region of a reaction column, and an isoparaffin-olefin mixture is passed into the reaction column below the feed point of the catalyst-containing suspension, the temperatures in the reaction column in the range from 50 to 120 ° C., that an alkylate-containing product mixture is drawn off from the bottom region of the reaction column and alkylate product is obtained therefrom in a separation by distillation.
• the temperatures in the reaction column are preferably in the range from 60 to 100.degree. It is important for the process that the olefin is only present in the lowest possible concentration in the reaction column where it meets with isoparaffin and the catalyst in order to largely rule out that the olefin reacts with itself.
• the reaction column has several gas- and liquid-permeable trays and the mixture to be reacted runs downwards in the column over the trays. It is expedient to keep a liquid mixture on at least some of the trays, at the same time passing isoparaffin in vapor form through the mixture from below. Usually one works at a pressure in the reaction chamber of 5 to 20 bar.
• the method can e.g. serve to catalytically convert isobutane with butene to isooctane and thus produce an additive for gasoline.
• Zeolites of the type X, Y or LSX are suitable as catalysts, which are commercially available and e.g. manufactured by Südchemie, Kunststoff (DE).
• Fig. 1 is a flow diagram of the method
• Fig. 2 shows a vertical section through a bottom of the reaction column.
• reaction column (1) which has numerous horizontal trays (2), for example 5 to 20 trays.
• the floors (2) are gas and liquid permeable.
• a suspension containing isoparaffin and granular zeolite catalyst is introduced through line (3) into the upper region of column (1), fresh catalyst being metered in through line (4).
• a mixture of isoparaffin and olefin is introduced in line (5), which is distributed to the reactor (1) through several branch lines (5a), (5b) and (5c). It is expedient to ensure that the isoparaffin-olefin mixture entering the reactor (1) has a relatively low olefin content in the range from 1 to 50% by weight.
• a partial stream of the alkylate-containing product mixture passes through line (6) into a distillation column (13), from which the separated alkylate product is withdrawn through line (14).
• the distillation column (13) is provided with a bottom heater (15).
• Vapors containing isoparaffin are passed through line (16) to a condenser (17) and collect in a subsequent separator, from where a partial stream is fed back through line (18) to the top of column (13).
• the rest of the condensate, which contains isoparaffin in particular passes through line (19) to a pump (20) and is then combined with the partial fraction which is brought up in line (23). This fraction contains high boilers and catalyst, part of this fraction is removed from the process through line (22).
• the suspension containing isoparaffin and catalyst thus formed passes through line (3) back to the reaction column (1).
• Fig. 2 shows a section of the reaction column (1) with a tray (2) on which a liquid mixture (25) is held.
• the dotted liquid level (25a) is determined by the upper inlet of a passage channel (26), through which the liquid flows down to the next floor, not shown.
• an isoparaffin-olefin mixture is fed through the branch line (5c) and first reaches a distributor pipe (27), from where it exits to the bottom (2) through a number of line branches (28) and (29). In this way it is ensured that the olefin concentration in the liquid mixture (25) can only reach a low maximum locally.
• the bottom (2) of FIG. 2 has a cylindrical steam outlet (31) closed at the top and provided with a plurality of openings (30). In reality, several of these are Steam outlets (31) are provided on each floor. This makes it possible for steam containing isoparaffin, which rises from below, to pass through the openings (30) into the liquid mixture (25), where it is at least partially converted.
• the excess of isobutane should prevent the reaction of the butenes with themselves (for example by oligomerization or polymerization).
• the feed stream of line (5) was fed to the reaction column in 4 trays.
• the reaction column was operated at a pressure of 11 bar. Operating the reaction column under boiling conditions with steam flowing upward ensured thorough mixing of the reaction mixture with the catalyst suspension on the individual column trays.
• the amount of catalyst added at the top of the column was retained at the bottom of the column.
• the mixture of reaction product and catalyst drawn off at the bottom of the column can subsequently be fed to a distillation in order to separate the alkylate product from the unreacted isobutane and the catalyst.
• the isobutane / catalyst mixture obtained in this way can be returned to the reaction column through line (3), but this was not done in the laboratory tests.
• the laboratory tests should only examine the technical feasibility of the process in a single pass through the process steps described.

Landscapes

• Chemical & Material Sciences (AREA)
• Organic Chemistry (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
• Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
• Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)

Applications Claiming Priority (3)

Publications (1)

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ID=7685929

Family Applications (1)

Country Status (7)

Families Citing this family (4)

Family Cites Families (3)

• 2001
  • 2001-05-22 DE DE10125230.7A patent/DE10125230B4/de not_active Expired - Fee Related
• 2002
  • 2002-03-26 JP JP2002591422A patent/JP4011489B2/ja not_active Expired - Fee Related
  • 2002-03-26 EP EP02704767A patent/EP1395533A1/de not_active Withdrawn
  • 2002-03-26 CN CNB028093852A patent/CN1246268C/zh not_active Expired - Fee Related
  • 2002-03-26 WO PCT/EP2002/003360 patent/WO2002094747A1/de active Application Filing
  • 2002-03-26 BR BR0209868-7A patent/BR0209868A/pt not_active Application Discontinuation
  • 2002-03-26 US US10/477,773 patent/US7271309B2/en not_active Expired - Fee Related

Non-Patent Citations (1)

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