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The invention relates to a process for the preparation of an olefinic product comprising ethylene and/or propylene from an oxygenate comprising: a) an oxygenate conversion step wherein a gaseous effluent comprising olefins is obtained; b) separation of water from the effluent; c) compression of the

The invention relates to a process for the preparation of an olefinic product comprising ethylene and/or propylene from an oxygenate comprising: a) an oxygenate conversion step wherein a gaseous effluent comprising olefins is obtained; b) separation of water from the effluent; c) compression of the effluent; d) acid gas removal from the effluent wherein the water-depleted compressed gaseous effluent is treated with a caustic solution in a caustic tower and a non-aqueous liquid stream comprising one or more aromatic C7+ hydrocarbons is added to the caustic solution to control the formation of red oil; and e) separating the olefinic product from the gaseous effluent treated in step d).

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1. A process for the preparation of an olefinic product comprising ethylene and/or propylene from an oxygenate, the process comprising the following steps: a) contacting the oxygenate in an oxygenate conversion reaction zone with a molecular sieve-comprising catalyst at a temperature in the range of

1. A process for the preparation of an olefinic product comprising ethylene and/or propylene from an oxygenate, the process comprising the following steps: a) contacting the oxygenate in an oxygenate conversion reaction zone with a molecular sieve-comprising catalyst at a temperature in the range of from 350 to 1000° C. to produce an oxygenate conversion effluent comprising olefins, water, carbon dioxide and carbonyl compounds including C2+ aldehyde and/or ketone;b) separating water from the oxygenate conversion effluent to obtain a water-depleted gaseous oxygenate conversion effluent comprising olefins, carbon dioxide and C2+ aldehyde and/or ketone;c) compressing the water-depleted gaseous effluent with the optional removal of any condensed phase to obtain a compressed gaseous stream comprising olefins, carbon dioxide and C2+ aldehyde and/or ketone;d) separating carbon dioxide from the compressed gaseous stream by subjecting the compressed gaseous stream to a caustic wash treatment in a caustic tower wherein the gaseous stream is countercurrently contacted with a caustic solution to obtain a washed gaseous stream comprising olefins; ande) subjecting the washed gaseous stream to one or more separation steps such that at least an olefin product stream comprising ethylene and/or propylene is obtained,wherein in step d) a non-aqueous liquid stream comprising one or more aromatic C7+ hydrocarbons is added to the caustic solution prior to contacting the caustic solution with the gaseous stream and wherein a liquid phase comprising spent caustic solution and the one or more aromatic C7+ hydrocarbons is discharged from the caustic tower and wherein the non-aqueous liquid stream comprises less than 0.1 wt % of olefinic hydrocarbons and at least part of the non-aqueous liquid stream comprising one or more aromatic C7+ hydrocarbons is recovered from the oxygenate conversion effluent in step b), step c), and/or step e). 2. A process according to claim 1, wherein in step d) the compressed gaseous stream is countercurrently contacted with a caustic solution in at least two stages in series before being countercurrently contacted with the water stream, wherein the gaseous stream is contacted in each stage of the at least two stages with a caustic solution having a concentration of caustic, wherein the concentration of caustic in a next stage is higher than the concentration of caustic in the stage directly preceding said next stage, wherein the non-aqueous liquid stream is added to the caustic solution of at least one stage and wherein the liquid phase comprising spent caustic solution and the one or more aromatic hydrocarbons is discharged from the first stage. 3. A process according to claim 2, where the non-aqueous liquid stream is added to the caustic solution in the first stage. 4. A process according to claim 3, wherein the non-aqueous liquid stream is added to the caustic solution in all of the at least two stages. 5. A process according to claim 1, wherein the non-aqueous liquid stream consists essentially of C7-C10 hydrocarbons. 6. A process according to claim 5, wherein the non-aqueous liquid stream essentially consists of C8-C10 hydrocarbons. 7. A process according to claim 1, wherein the non-aqueous liquid stream comprises xylene. 8. A process according to claim 1, wherein in step e) a stream comprising C7+ hydrocarbons is obtained and wherein the non-aqueous liquid stream comprises at least part of the stream comprising C7+ hydrocarbons. 9. A process according to claim 8, wherein in step e) a stream comprising C8-C10 hydrocarbons is obtained, and wherein the non-aqueous liquid stream comprises at least part of the stream comprising C8-C10 hydrocarbons. 10. A process according to claim 1, wherein the temperature of the compressed gaseous stream that is contacted with the caustic solution is at most 40° C. 11. A process according to claim 1, wherein the caustic wash treatment is operated at a temperature of at most 50° C. 12. A process according to claim 1, wherein the colour of the liquid phase discharged from the caustic tower or of a non-aqueous phase separated from the liquid phase is determined, and wherein the amount of non-aqueous liquid stream added to the caustic solution is controlled in accordance with the determined colour. 13. A process according to claim 12, wherein the colour is determined by inspection through a sight glass located in a conduit for recycling or withdrawal of the liquid phase and/or a conduit for withdrawal of a non-aqueous phase separated from the liquid phase. 14. A process according to claim 1, wherein the compressed gaseous stream obtained in step c) is heated to a temperature in the range of from 2 to 5° C. above its dew point prior to subjecting the compressed gaseous stream to the caustic wash treatment in step d).