Integrated process for converting methanol to gasoline and distillates

An integrated process for converting an oxygenate feed to selectively produce gasoline range liquid hydrocarbons which consists essentially of the steps of

• splitting the oxygenate feed into two portions,
• contacting a first 60 to 40% portion of the oxygenate feed with a zeolite catalyst in a MTO first reactor at elevated temperature of 800.degree. to 950.degree. F. and moderate pressure of 10 to 80 psig to convert at least 80 wt. % of the oxygenate feed to C.sub.2 + olefin hydrocarbons and recovering an effluent comprising C.sub.2 + olefin hydrocarbons and by-product water,
• cooling the effluent from the MTO first reactor and separating a C.sub.2 to C.sub.9 hydrocarbon stream containing C.sub.5 -C.sub.9 aromatic hydrocarbons, and by-product water,
• contacting a second 40 to 60% portion of the oxygenate feed and the entire C.sub.2 to C.sub.9 hydrocarbon stream, including the C.sub.5 -C.sub.9 aromatic hydrocarbons, from the MTO first reactor in a MOI intermediate reactor with a zeolite catalyst at moderate temperature of 550.degree. to 700.degree. F. and a pressure of 100 to 250 psig to selectively convert at least 50% of the oxygenate feed and the C.sub.2 to C.sub.9 olefins to gasoline range liquid hydrocarbons comprising C.sub.2 - and C.sub.3 + olefins and by-product water,
• cooling the effluent from the MOI intermediate reactor and separating a C.sub.2 - olefin containing hydrocarbon stream, a C.sub.3 + olefin hydrocarbon stream containing a high concentration of gasoline range liquid hydrocarbons and by-product water.

An integrated process for converting an oxygenate feed comprising methanol, dimethyl ether or mixtures thereof to selectively produce distillate range liquid hydrocarbons which consists essentially of the steps of splitting the oxygenate feed into two portions,

• contacting a first 60 to 40% potion of the oxygenate feed with a zeolite catalyst in a MTO first reactor at elevated temperature of 800.degree. to 950.degree. F. and moderate pressure of 10 to 80 psig to convert at least 80 wt. % of the oxygenate feed to C.sub.2 + olefin hydrocarbons and by-product water,
• cooling the effluent from the MTO first reactor and separating a C.sub.2 to C.sub.9 hydrocarbon stream containing C.sub.5 -C.sub.9 aromatic hydrocarbons, and by-product water,
• removing the C.sub.5 -C.sub.9 aromatic hydrocarbons from the C.sub.2 to C.sub.9 hydrocarbon stream to obtain a C.sub.2 to C.sub.9 olefin hydrocarbon stream,
• contacting a second 40 to 60% portion of the oxygenate feed and the entire C.sub.2 to C.sub.9 olefin hydrocarbon stream from the MTO first reactor in a MOI intermediate reactor with a zeolite catalyst at moderate temperature of 550.degree. to 700.degree. F. and at a pressure of 100 to 250 psig to convert at least 50 wt. % of the oxygenate feed and the C.sub.2 to C.sub.9 olefins to heavier hydrocarbons comprising C.sub.2 - and C.sub.3 + olefins and by-product water,
• cooling the effluent from the MOI intermediate reactor and separating a C.sub.2 - olefin hydrocarbon stream, a C.sub.3 to C.sub.20 olefin hydrocarbon stream and by-product water,
• contacting the C.sub.3 to C.sub.20 hydrocarbon stream in a MOGD second reactor with an oligomerization zeolite catalyst at moderate temperature of 400.degree. to 650.degree. F. and increased pressure of 600 to 1500 psig under oligomerization reaction conditions to selectively convert the C.sub.3 to C.sub.20 hydrocarbons to distillate range liquid hydrocarbons.