Integrated oxygenate conversion and olefin oligomerization

A method for forming a naphtha composition and a distillate composition, comprising:

• exposing a feed comprising oxygenates to a conversion catalyst at an average reaction temperature of about 440° C. to about 530° C. (or about 450° C. to about 500° C.), a total pressure of 100 psig (˜700 kPag) to 300 psig (˜2100 kPag), and a WHSV of 0.1 hr−1 to 10.0 hr−1 to form a converted effluent comprising at least 50 wt % of a naphtha boiling range fraction relative to a weight of hydrocarbons in the converted effluent, the naphtha boiling range fraction comprising at least 40 wt % aromatics, the converted effluent further comprising ethylene, propylene, or a combination thereof;
• separating at least a portion of the converted effluent to form at least a first effluent fraction comprising at least 50 wt % of the naphtha boiling range fraction and a second effluent fraction comprising at least 50 wt % of the ethylene, propylene, or a combination thereof, at least one of the first effluent fraction and the naphtha boiling range fraction having an octane rating of at least 95, the octane rating being defined as (RON+MON)/2;
• and
• exposing at least a portion of the second effluent fraction to an oligomerization catalyst at a temperature of 125° C. to 250° C. and a total pressure of 150 psig (˜1000 kPag) to 1000 psig (˜6900 kPag) to form an oligomerized effluent comprising, relative to a weight of hydrocarbons in the oligomerized effluent, at least 60 wt % of a distillate boiling range fraction, at least 10 wt % of a 371° C.+ fraction, and less than 20 wt % of a 177° C.− fraction, the distillate boiling range fraction having an aromatics content of about 1.0 wt % or less and a cetane rating of at least 40, the 371° C.+ fraction having a cetane rating of at least 50,
• wherein the conversion catalyst comprises a 10-member ring zeolite, the zeolite having a silicon to aluminum ratio of 10 to 200 and an Alpha value of at least 5, the conversion catalyst further comprising 0.1 wt % to 1.5 wt % Zn supported on the catalyst.

A method for forming a naphtha composition and a distillate composition, comprising:

• exposing a feed comprising methanol to a conversion catalyst in a fluidized bed or moving bed at an average reaction temperature of about 400° C. to about 530° C., a total pressure of 100 psig (˜700 kPag) to 300 psig (˜2100 kPag), and a WHSV of 0.1 hr−1 to 10.0 hr−1 to form a converted effluent comprising a naphtha boiling range fraction;
• separating at least a portion of the converted effluent to form at least a first effluent fraction comprising at least 50 wt % of the naphtha boiling range fraction and a second effluent fraction comprising ethylene, propylene, or a combination thereof;
• and
• exposing at least a portion of the second effluent fraction to an oligomerization catalyst at a temperature of 125° C. to 250° C. and a total pressure of 150 psig (˜1000 kPag) to 1000 psig (˜6900 kPag) to form an oligomerized effluent comprising, relative to a weight of hydrocarbons in the oligomerized effluent, at least 60 wt % of a distillate boiling range fraction, at least 10 wt % of a 371° C.+ fraction, and less than 20 wt % of a 177° C.− fraction, the distillate boiling range fraction having an aromatics content of about 1.0 wt % or less and a cetane rating of at least 40, the 371° C.+ fraction having a cetane rating of at least 50,
• wherein the conversion catalyst comprises a 10-member ring or 12-member ring zeolite, the zeolite having a framework structure different from an MFI or MEL framework structure, the zeolite having a silicon to aluminum ratio of 10 to 200 and an Alpha value of at least 5, the conversion catalyst further comprising 0.1 wt % to 1.5 wt % Zn supported on the catalyst, and
• wherein the conversion catalyst comprises an average catalyst exposure time of 25 grams to 200 grams of methanol per gram of catalyst.

A system for performing oxygenate conversion, comprising:

• a conversion reactor comprising a conversion reactor inlet and a conversion reactor outlet, the conversion reactor further comprising a conversion catalyst comprising a zeolite having an MFI or MEL framework structure, the zeolite structure having a silicon to aluminum ratio of 20 to 40 and an Alpha value of at least 5, the conversion catalyst further comprising 0.1 wt % to 1.5 wt % Zn supported on the catalyst;
• a separation stage comprising a separator inlet, a first separator outlet, a second separator product, and an aqueous phase outlet, the separator inlet being in direct fluid communication with the conversion reactor outlet, the direct fluid communication not passing through a compressor;
• and
• an oligomerization reactor comprising an oligomerization reactor inlet and an oligomerization reactor outlet, the oligomerization reactor further comprising an oligomerization catalyst, the oligomerization reactor inlet being in direct fluid communication with the first separator outlet, the direct fluid communication not passing through a compressor, the oligomerization reactor inlet being in indirect fluid communication with the conversion reactor outlet via the separation stage, the oligomerization catalyst comprising a 10-member ring zeolite, the zeolite having a silicon to aluminum ratio of 10 to 200 and an Alpha value of at least 5.