PREPARATION OF A MOTOR SPIRIT BLENDING COMPONENT

Abstract: A motor spirit blending component is prepared by react­ ing a hydrocarbon feedstock containing isobutene and reac­ tive tertiary olefins of higher carbon number and having a final boiling point of at least 150°C with a lower aliphatic alcohol. The reaction is carried out in the presence of an etherification catalyst under a temperature in the range 30° to 200°C, a pressure in the range atmospheric to 100 bar, a liquid hourly space velocity in the range 0.1 to 20 vol/vol/hour and a molar ratio of alcohol to reactive C₄-C₇ tertiary olefins in the range 0.1:1 to 10:1. The product contains a mixture of tertiary ethers. Suitable feedstocks are cat cracker debutaniser and steam cracker depropaniser feed. The preferred alcohol is methanol.

Description: PREPARATION OF A MOTOR SPIRIT BLENDING COMPONENT This invention relates to a process for the preparation of a motor spirit blending component. Motor spirit is a blend of several components which can be selected, inter alia, from straight run distillate, catalytic reformate, isomerate, alkylate, catalytically cracked gasoline and steam cracked gasoline. Straight run distillates alone are inadequate both in quantity and quality for modern requirements and for many years it has been common practice to increase the yield of motor spirit component from crude oil by catalytically cracking heavier fractions. The catalytic cracking of heavier petroleum fractions, normally boiling in the range 3500 to 5500C, to lighter products, particularly to gasoline, conventionally uses a fluidised bed of catalyst in a riser, or riser and reactor, and a circulation system through which spent catalyst passes to a regenerator containing a fluidised bed of catalyst and back to the riser. Catalytic cracking produces a spectrum of products ranging from gases through light cat cracked gasoline and heavy cat cracked gasoline to decanted oil. These products are initially separated in a main fractionator and components with boiling points up to a value in the range 1500C to 3000C are taken in an overhead stream. This stream is then fed to an absorber stripper or similar system where most of the ethane and lighter components are removed as an overhead stream. The bottom stream containing propylene and higher boiling components is fed to a debutaniser where most of the butane and lighter components are taken overhead. The debutaniser bottom stream is either taken as a motor spirit component or is fed to a splitter to produce separate light and heavy gasoline and frequently also a gas oil stream as a bottom product. The debutaniser top stream is fed to a depropaniser where it is split into a C3 top stream and a C4 bottom stream. The C4 and lighter products are frequently separated into a C4 stream, a C3 stream and a light gas stream. The C4 stream contains significant quantities of isobutane, n-butane, isobutene and normal butenes and is useful as a source of alkylation feedstock for the production of motor spirit alkylate. One proposal to utilise the C4 stream involves etherification of the isobutene contained therein with a lower alcohol, e.g. methanol to produce methyl tertiary butyl ether (MTBE). MTBE, because of its high octane rating, good volatility characteristics and lack of chemical activity is a very desirable motor spirit component, particularly for blending with catalytic reformate which has a deficiency of high octane components in its lower boiling end (front end). The steam cracking of naphtha for the production of olefins is also a process of major importance. As with cat cracking, a spectrum of products is produced including ethylene, propylene, a C4 fraction and material boiling in the gasoline range. The latter after treatment to reduce its unsaturation which would otherwise lead to problems with gum formation is a suitable blending component for motor spirit. A complex product recovery system is necessary including a demethaniser for splitting between C1 and higher products, a de-ethaniser for splitting between C2 and higher products, a depropaniser for splitting between C3 and higher products and a debutaniser for splitting between C4 and raw gasoline. Reference is made to ModemPetroleum Technology, 4th Edition, edited by Hobson and Pohl and published by Applied Science Publishers Limited, Barking, Essex in 1973 on behalf of the Institute of Petroleum, at pages 449-453, for details of a steam cracking process and its product recovery system. The C4 stream is generally solvent extracted for butadiene recovery. After the latter has been removed the remaining C4 contains a higher proportion of isobutene than a cat cracked C4 stream. Processes have been disclosed in the Oil and Gas Journal, April 9th 1979, pages 149-152, and Hydrocarbon Proce-ing, I)c(mlor 1979, pa(lo:; 109-113, for the reaction of C4 streams with methanol to produce MTBE. In each case, however, the reaction product is fractionated to obtain MTBE as a relatively pure single compound, excess or unreacted methanol is recovered and recycled and unreacted material containing isobutene, isobutane and linear butenes and butanes is used for other purposes, e.g. alkylation or polymerisation. The MTBE is added to a motor spirit blend as a single compound. The Oil and Gas Journal, ibid, also discloses an analogous process for the production of methyl tertiary amyl ether. British Patent Specification No. 1249016 discloses a process for the production of gasoline by fractionating cracker reactor effluent to obtain a 15 two 1700F (-10 to 770C) cut containing C46 tertiary olefins and etherification of those olefins by reaction with a lower alcohol over an etherification catalyst followed by blending of the etherified cut with at least one other hydrocarbon stream. 1249016 warns against using a wider boiling range fraction. It states that if wider boiling ranges of materials are used, the improvement in octane rating is substantially decreased, rapidly approaching that of the whole untreated gasoline blend. Processes described in the prior art for the production of MTBE for use as a motor gasoline component, or for the etherification of a narrow cut containing isobutene together with higher iso-olefins, have suffered from the disadvantage that substantial amounts of energy are required before and after the etherification step (a) to separate the narrow cut for the etherification reaction and (b) to fractionate the product. We have discovered that an etherification stage can be inserted into the recovery section of a cat or steam cracker at the point, typically downstream of an absorber/stripper, where C2 hydrocarbons and lower boiling materials have been removed, leaving a mixture consisting substantially of C3, C4 and higher boiling hydrocarbons up to a final boiling point within the range 150 to 3000C. This enables the pre-reaction fractionation step to be omitted and reduces C4 removal requirements in the product fractionator (debutaniser) with consequent saving in capital and operating costs. Thus according to the present invention, there is provided a process for the production of a motor spirit blending component which process comprises reacting a hydrocarbon feedstock containing isobutene and reactive tertiary olefins of higher carbon number and having a final boiling point of at least 1500C, with a lower aliphatic alcohol in the presence of an etherification catalyst under a temperature in the range 30 to 2000C, a pressure in the range atmospheric to 100 bar, a liquid hourly space velocity in the range 0.1 to 20 vol/vol/hour and a molar ratio of alcohol to reactive C4-C7 tertiary olefins in the range 0.1:1 to 10:1 to produce a product containing tertiary ethers. The molar ratio of alcohol to olefins is defined with respect to C -C7 olefins for analytical reasons, although high tertiary olefins also react and the products will contain ethers derived from these materials. The process is particularly applicable to that fraction from a catalytic cracker product recovery system which would normally be fed to the debutaniser, i.e. C3 and higher hydrocarbons. The process is also applicable to that fraction from a steam cracker product recovery system which would normally be fed to the depropaniser, i.e., C3 and higher hydrocarbons. Preferably the feedstock has a final boiling point not greater than 300 C. By lower alcohol is meant an alcohol containing from 1 to 6 carbon atoms per molecule. The preferred alcohol is methanol. The catalysts are preferably relatively high molecular weight solid carbonaceous materials containing at least one -S03H group per molecule as the functional group. The most preferred are strongly acidic cation exchange resins consisting essentially of a sulphonated polystyrene resin, for instance a divinylbenzene cross-linked polystyrene matrix having 0.5 to 20% and preferably 4 to 16% of copolymerised divinylbenzene attached to which are ionisable or functional nuclear sulphonic acid groups. These resins are manufactured and sold commercially under various trade names. The temperature at which the etherification reaction is carried out is preferably in the range 500 to 800C. The pressure should be sufficient to maintain the reactants in the liquid phase. Pressures between 10 and 20 bar are preferred. Because of azeotrope formation between the alcohols, particu'arly methanol, and butenes and pentenes, it is desirable for the reaction product to have a relatively low alcohol content prior to fractionation. This is particularly so when methanol is employed as the alcohol and methanol is to be removed from the reaction products after fractionation. In certain circumstances methanol is an undesirable product in gasoline fractions because of the sensitivity of the Reid Vapour Pressure to relatively low concentrations of methanol. If, however, methanol is intended to form a significant component of the final blend of motor spirit, then the above consideration does not apply. It is therefore advisable from the former point of view to operate with a low alcohol content in the feedstock and therefore with a low molar ratio of alcohol to reactive tertiary olefins. The quantity of alcohol supplied may be less than the stoichiometric equivalent required for complete etherification of the reactive tertiary olefins. If this is the case then an alkyl tertiary butyl ether is formed preferentially because isobutene reacts more readily than higher boiling tertiary olefins. When progressively larger quantities of alcohol are added, progressively more of the reactive higher tertiary olefins are etherified but the conversion of alcohol decreases leaving a higher proportion of unreacted alcohol in the reaction product. Preferably the molar ratio of alcohol to reactive tertiary C4-C7 olefin is in the range 0.3:1 to 1.5:1. Alcohol addition is most limited when the objective is to achieve the optimum gain in octane number and the optimum increase in the production of gasoline for the least use of alcohol; larger additions of alcohol are used when it is desired to etherify more of the olefins. Increasing the ether content and reducing the olefin content results in a gasoline of reduced photochemical activity, reduced vapour pressure, reduced bromine number, increased octane number and increased density. Insofar as the liquid hourly space velocity (LHSV) of the feedstock is concerned, a compromise must be reached since decrf lsing the space velocity results in higher conversions and less unreacted alcohol whereas increasing the space velocity has the opposite effect. The preferred range lies between 0.5 and 5 vol/vol/hour. The MTBE and other ethers formed under the above conditions are retained in the gasoline produced by the later fractionation stages of a recovery section. The non-etherified C4 hydrocarbons, from which the isobutene has been substantially removed by etherification,may be recovered in the normal way by distillation without an additional step being necessary. Unreacted methanol, ethanol or propanol can be removed by washing the reaction product with water. Washing can be carried out before or after the fractionation of the product. However, because of azeotrope formation it is preferred to carry out this operation before. The invention is illustrated with reference to the accompanying drawing which is a simplified flow diagram. A stream 1 containing debutaniser feedstock from a fluidised cat cracking unit (not shown) is joined by a line 2 containing methanol and the combined stream is fed to an etherification reactor 3 containing a cation exchange resin in the hydrogen form. Line 4 takes the product from the reactor 3 to a washer 5 wherein it is scrubbed with water to remove unreacted methanol. The methanol-free product is then passed by line 6 to a debutaniser 7 which splits it into top and bottom products. The former is removed as LPG by line 8 after a conventional purification treatment (not shown). The bottom product which boils in the gasoline boiling range is passed by line 9 to a distillation column 10 which splits it into light and heavy cat cracked spirits. After conventional purification treatments, again not shown, these are removed by lines 11 and 12 respectively. Wash water containing recovered methanol is taken from washer S by line 13 and passed to a column 14 in which the water and methanol are separated by distillation. Water is returned to the washer by line 15 and methanol is recycled by line 16 to join the methanol feed line 2. The invention is iurther illustrated by the following Examples l - 7. EXAML'I,ES The feedstock was a simulated cat cracker debutaniser feed prepared by adding 12% by weight of a C4 cut to 88% by weight cat cracked stabiliser feed boiling in the range 290 to 2020C and derived from Forties vacuum distillate. The simulated debutaniser feedstock boiled in the range -70C to 202 C and had the following analysis. EMI7.1 <tb> <SEP> Concentration <tb> Material <SEP> X <SEP> wt <tb> lsobutene <SEP> 2.1 <tb> Reactive <SEP> tertiary <SEP> isopentenes <SEP> 3.7 <tb> Reactive <SEP> tertiary <SEP> isohexenes <SEP> 2.9 <tb> Reactive <SEP> tertiary <SEP> isoheptenes <SEP> 3.4 <tb> Relatively <SEP> inert <SEP> hydrocarbons <SEP> 87.9 <tb> ) 1.6 mol/Kg In each example, the catalyst was a sulphonated divinyl benzene cross-linked polystyrene cation exchange resin sold under the trade name Lewatit SPC 118 by Farbenfabriken Bayer AG. Methanol was the etherifying agent, the maximum reaction temperature was 740C and the pressure was 15 bar. Products were analysed by gas chromatography. Octane number measurements were made after the products had been washed with water to remove untreated methanol. Examples 1, 2 and 3 In Examples 1-3, methanol was supplied so that the molar ratio of methanol to reactive C4-C7 tertiary olefinswas0.72:1 andthe LHSVwas varied. The following results were obtained. EMI7.2 <tb> Example <SEP> LHSV <SEP> Isobu- <SEP> Selec- <SEP> Isopen- <SEP> Selec <tb> <SEP> tene <SEP> tivity <SEP> tene <SEP> tivity <tb> <SEP> Conver- <SEP> to <SEP> Conver- <SEP> to <tb> <SEP> sion <SEP> X <SEP> MTBE% <SEP> sion <SEP> % <SEP> MTAE% <SEP> <tb> <SEP> 1 <SEP> 1 <SEP> 91 <SEP> 94 <SEP> 51 <SEP> 100 <tb> <SEP> 2 <SEP> 2 <SEP> 91 <SEP> 94 <SEP> 44 <SEP> 100 <tb> <SEP> 3 <SEP> 3 <SEP> 90 <SEP> 95 <SEP> 36 <SEP> 100 <tb> EMI8.1 <tb> Example <SEP> LHSV <SEP> Isohex- <SEP> Selec- <SEP> Isohep- <SEP> Selec- <SEP> Metha <tb> <SEP> ene <SEP> tivity <SEP> tene <SEP> tivity <SEP> nol <tb> <SEP> Conver- <SEP> to <SEP> Conver- <SEP> to <SEP> Conver <tb> <SEP> sion <SEP> % <SEP> MTHEXE <SEP> X <SEP> sion <SEP> % <SEP> MTHEPE <SEP> % <SEP> sion <SEP> <RTI ID=8.2> X <SEP> <tb> <SEP> 1 <SEP> 1 <SEP> 30 <SEP> 100 <SEP> 17 <SEP> 100 <SEP> 74 <tb> <SEP> 2 <SEP> 2 <SEP> 21 <SEP> 100 <SEP> 14 <SEP> 100 <SEP> 67 <tb> <SEP> 3 <SEP> 3 <SEP> 14 <SEP> 100 <SEP> 12 <SEP> 100 <SEP> 61 <tb> MTBE = methyl tert-butyl ether MTAE = methyl tert-amyl ether MTHEXE = methyl tert-hexyl ether MTHEPE = methyl tert-heptyl ether Octane numbers were determined for Examples 1 to 3 on the feedstock, the products and the products with different quantities of TEL added. The results set out in the following Table I show the improvement of octane number obtained as a function of the LHSV. TABLE I EMI8.2 <tb> <SEP> original <tb> <SEP> ¯ <SEP> feed <SEP> <tb> RON <SEP> 96.8 <SEP> +0.4 <SEP> +0.4 <SEP> +0.4 <tb> +0.4 <SEP> g <SEP> TEL/1 <tb> MON <SEP> as <SEP> Pb <SEP> 85.2 <SEP> +0.4 <SEP> +0.4 <SEP> +0.4 <tb> RON <SEP> 95.1 <SEP> +0.3 <SEP> +0.3 <SEP> +0.3 <tb> 0.15 <SEP> g <SEP> TEL/l <SEP> <tb> <SEP> as <SEP> Pb <tb> MON <SEP> 83.7 <SEP> +0.5 <SEP> +0.5 <SEP> +0.5 <tb> RON <SEP> 91.5 <SEP> +0.3 <SEP> <SEP> +0.3 <SEP> +0.3 <SEP> <tb> clear <tb> MON <SEP> 80.6 <SEP> +0.4 <SEP> 1 <SEP> +0.4 <SEP> | <SEP> +0.4 <tb> Examples < , 5 and 6 In Examples 4 to 6, an LHSV of 1 was used throughout and the molar ratio of methanol to reactive C4-C7 tertiary olefin was varied. The following results were obtained, Example 1 being again included because it fits into the pattern. EMI9.1 <tb> Example <SEP> Molar <SEP> Isobu- <SEP> Selec- <SEP> Isopen- <SEP> Selec <tb> <SEP> Ratio <SEP> tene <SEP> tivity <SEP> tene <SEP> tivity <tb> <SEP> of <SEP> Met <SEP> Conver- <SEP> to <SEP> Conver- <SEP> to <tb> <SEP> anol <SEP> to <SEP> sion <SEP> MTBE <SEP> sion <SEP> MTAE <tb> <SEP> Olefins <SEP> % <SEP> % <SEP> X <SEP> % <tb> <SEP> 4 <SEP> 0.36:1 <SEP> 80 <SEP> 99 <SEP> 26 <SEP> 100 <tb> <SEP> 5 <SEP> 0.53:1 <SEP> 89 <SEP> 94 <SEP> 36 <SEP> 100 <tb> <SEP> 1 <SEP> 0.72:1 <SEP> 91 <SEP> 94 <SEP> 51 <SEP> 100 <tb> <SEP> 6 <SEP> 0.97: :1 <SEP> 92 <SEP> 94 <SEP> 60 <SEP> 100 <tb> EMI9.2 <tb> Example <SEP> Molar <SEP> Iso- <SEP> Selec- <SEP> Isohep- <SEP> Selec- <SEP> Metha <tb> <SEP> Ratio <SEP> hexene <SEP> tivity <SEP> tene <SEP> tivity <SEP> nol <tb> <SEP> ofMeth- <SEP> Conver- <SEP> to <SEP> Conver- <SEP> to <SEP> Conver <tb> <SEP> anol <SEP> to <SEP> sion <SEP> MTHEXE <SEP> sion <SEP> MTHEPE <SEP> sion <tb> <SEP> Olefins <SEP> % <SEP> % <tb> <SEP> 4 <SEP> 0.36:1 <SEP> 12 <SEP> 100 <SEP> 8 <SEP> 100 <SEP> j <SEP> 98 <tb> <SEP> 5 <SEP> 0.53:1 <SEP> 30 <SEP> 100 <SEP> 17 <SEP> 100 <SEP> 74 <tb> <SEP> 1 <SEP> 0.72:1 <SEP> 30 <SEP> 100 <SEP> 17 <SEP> 100 <SEP> 74 <tb> <SEP> 6 <SEP> 0.97:1 <SEP> 35 <SEP> 100 <SEP> 18 <SEP> 100 <SEP> 58 <tb> Octane numbers were determined for Examples 4 to 6 on the feedstock, the products and the products with different quantities of TEL added. The results set out in the following Table II show the improvement in octane number obtained as a function of the mole ratio of methanol to reactive C4-C7 tertiary olefins. TABLE II EMI10.1 <tb> <SEP> original <SEP> <tb> <SEP> feed <SEP> <SEP> Example <SEP> 41 <SEP> Example <SEP> 5 <SEP> Example <SEP> 1 <SEP> Example <SEP> 6 <SEP> <tb> RON <SEP> 96.8 <SEP> +0.5 <SEP> +0.4 <SEP> +0.4 <SEP> +0.5 <tb> +0,4 <SEP> g <SEP> TEL/1 <tb> <SEP> as <SEP> Pb <tb> MON <SEP> 85.2 <SEP> +0.3 <SEP> +0.3 <SEP> +0.4 <SEP> +0.6 <tb> NON <SEP> 83.7 <SEP> +0.4 <SEP> +0.4 <SEP> +0.5 <SEP> +0.8 <tb> RON <SEP> 91.5 <SEP> +0.3 <SEP> +0.3 <SEP> +0.3 <SEP> +0.5 <tb> clear <SEP> l <SEP> <tb> MON <SEP> 80.6 <SEP> +0.4 <SEP> +0.4 <SEP> +0.4 <SEP> +0.7 <tb> Example 7 A similar feedstock to that used in the previous Examples but containing twice as much isobutene and a total of 1.9 mole/Kg of reactive tertiary C4-C7 olefins was etherified with methanol. Etherification conditions were as follows: Catalyst ) Temperature ) as before Pressure ) LHSV 1 Molar ratio of methanol to reactive tertiary C4C7 olefins 1.52:1 Octane numbers were determined for the feedstock, the product, and the product with different quantities of TEL added. The following results were obtained. EMI11.1 <tb> Substance <SEP> Increase <SEP> in <SEP> Octane <SEP> No. <tb> <SEP> MON <SEP> RON <tb> Product <SEP> g/l <SEP> TEL <SEP> as <SEP> Pb <SEP> 1.6 <SEP> 1.3 <tb> Product <SEP> + <SEP> 0.15%gt1 <SEP> TEL <SEP> 1.4 <SEP> 0.8 <tb> <SEP> as <SEP> Pb <tb> Product <SEP> + <SEP> 0.4X <SEP> g/l <SEP> TEL <SEP> 1.5 <SEP> 0.8 <tb> <SEP> as <SEP> Pb <tb> TEL = Tetra ethyl lead MON = Motor Octane No. RON = Research Octane No. Examples 8 to 11 A similar feedstock to that used in the previous Examples but containing 3.15% wt isobutene, 4.7% wt isopentenes, 3.1% wt isohexenes and 3.4% wt isoheptenes and a total of 1.9 mole /Kg of reactive C4-C7 tertiary olefins was etherified with methanol. The catalyst and pressure were as before. The molar ratio of methanol to reactive tertiary C4-C7 olefins was 0.93 and the LHSV was 1. The following results were obtained. EMI11.2 <tb> <SEP> Isobu- <SEP> Selec Example <SEP> Temper- <SEP> Isobu- <SEP> Selec- <SEP> Isopen- <SEP> Selec <tb> <SEP> ature <SEP> tene <SEP> tivity <SEP> tene <SEP> tivity <tb> <SEP> C <SEP> Conver- <SEP> to <SEP> Conver- <SEP> to <tb> <SEP> sion <SEP> % <SEP> MTBE <SEP> % <SEP> sion <SEP> % <SEP> MTAE <SEP> X <SEP> <tb> <SEP> 8 <SEP> 74 <SEP> 93 <SEP> 98 <SEP> 61 <SEP> 100 <tb> <SEP> 9 <SEP> 70 <SEP> 93 <SEP> 100 <SEP> 56 <SEP> 100 <tb> <SEP> 10 <SEP> 66 <SEP> 93 <SEP> 100 <SEP> 51 <SEP> 100 <tb> <SEP> 11 <SEP> 62 <SEP> 92 <SEP> 100 <SEP> 46 <SEP> 100 <tb> EMI11.3 <tb> Example <SEP> Temper- <SEP> Iso- <SEP> Selec- <SEP> Isohep- <SEP> Selec- <SEP> Metha <tb> <SEP> ature <SEP> hexene <SEP> tivity <SEP> tene <SEP> tivity <SEP> nol <tb> <SEP> OC <SEP> Conver- <SEP> to <SEP> Conver- <SEP> to <SEP> Conver <tb> <SEP> sion <SEP> X <SEP> MTHEXEX <SEP> sion <SEP> % <SEP> MTHEPE% <SEP> sion <SEP> % <tb> <SEP> 8 <SEP> 74 <SEP> 35 <SEP> 100 <SEP> 20 <SEP> 100 <SEP> 64 <tb> <SEP> 9 <SEP> 70 <SEP> 29 <SEP> 100 <SEP> 17 <SEP> 100 <SEP> 62 <tb> <SEP> 10 <SEP> 66 <SEP> 24 <SEP> 100 <SEP> 15 <SEP> 100 <SEP> 60 <tb> <SEP> 11 <SEP> 62 <SEP> 20 <SEP> 100 <SEP> 15 <SEP> 100 <SEP> 54 <tb> Octane numbers were determined for Examples 8-10 on the feedstock, the products, and the products with TEL added. The results set out in the following Table III show the improvement in octane number obtained as a function of the temperature. TABLE III EMI12.1 <tb> <SEP> original <SEP> Example <SEP> 8 <SEP> Example <SEP> 9 <SEP> Example <SEP> 10 <tb> <SEP> feed <SEP> <tb> RON <SEP> 96.5 <SEP> +0.7 <SEP> +0.6 <SEP> +0.6 <tb> + <SEP> 0,15 <SEP> g <SEP> TEL/l <tb> <SEP> as <SEP> Pb <tb> MON <SEP> 85.0 <SEP> +1.1 <SEP> +1.1 <SEP> +1.1 <tb> RON <SEP> 92.9 <SEP> +0.5 <SEP> +0.6 <SEP> +0.6 <tb> MON <SEP> 81.8 <SEP> +0.8 <SEP> +1.0 <SEP> +1.0 <tb>

Claims: Claims: 1. A process for the production of a motor spirit blending component which process comprises reacting a hydrocarbon feedstock containing isobutene and reactive tertiary olefins of higher carbon number and having a final boiling point of at least 150 C with a lower aliphatic alcohol in the presence of an etherification catalyst under a temperature in the range 300 to 2000C, a pressure in the range atmospheric to 100 bar, a liquid hourly space velocity in the range 0.1 to 20 vol/vol/hour and a molar ratio of alcohol to reactive Cg-C7 tertiary olefins in the range 0.1:1 to 10:1 to produce a product containing tertiary ethers. 2. A process according to claim 1 wherein the feedstock is debutaniser feedstock from a catalytic cracker. 3. A process according to claim 1 wherein the feedstock is depropaniser feedstock from a steam cracker. 4. A process according to any of the preceding claims wherein the feedstock has a final boiling point not greater than 3000C. 5. A process according to any of the preceding claims wherein the alcohol is methanol. 6. A process according to any of the preceding claims wherein the catalyst is a sulphonated cation exchange resin in the hydrogen form. 7. A process according to any of the preceding claims wherein the etherification reaction is carried out at a temperature in the range 500 to 800C. 8. A process according to any of the preceding claims wherein the etherification reaction is carried out under a pressure in the range 10 to 20 bar. 9. A process according to any of the preceding claims wherein the molar ratio of alcohol to reactive tertiary olefin is in the range 0.3:1 to 1.5:1. 10. A process according to any of the preceding claims wherein the liquid hourly space velocity of the feedstock lies in the range 0.5 to @ vol/vol/hour.

Inventors: HAELSIG, CLAUS-PETER, HOENIG, HELMAR, PETZNY, WILFRIED, RAYMOND, DAVID WILLIAM
Applicants: THE BRITISH PETROLEUM COMPANY P.L.C.
Application year: 1981
Main classification: C10L1
IPC codes: C07C41, C10L1