A method may include: oxidizing iso-butane with oxygen to produce t-butyl hydroperoxide and t-butyl alcohol; dehydrating at least a portion of the t-butyl alcohol to produce di-tert-butyl ether and isobutylene; epoxidizing at least a portion of the isobutylene with the t-butyl hydroperoxide to produce isobutylene oxide and t-butyl alcohol; and carbonylating at least a portion of the isobutylene oxide with carbon monoxide to produce pivalolactone.

A method may include: oxidizing iso-butane with oxygen to produce t-butyl hydroperoxide and t-butyl alcohol; dehydrating at least a portion of the t-butyl alcohol to produce di-tert-butyl ether and isobutylene; epoxidizing at least a portion of the isobutylene with the t-butyl hydroperoxide to produce isobutylene oxide and t-butyl alcohol; and carbonylating at least a portion of the isobutylene oxide with carbon monoxide to produce pivalolactone.

Disclosed herein is a method for converting an epoxide to a first C3 product, a second C3 product, and/or a first C4 product within an integrated system. The method includes converting the epoxide to a beta lactone to produce an outlet stream comprising beta lactone. The method includes converting the beta lactone of the outlet stream to a first C3 product in the first C3 reactor to produce an outlet stream comprising the first C3 product; converting the beta lactone to a second C3 product in the second C3 reactor to produce an outlet stream comprising the second C3 product, and/or converting the beta lactone to a first C4 product in the first C4 reactor to produce an outlet stream comprising the first C4 product.

Disclosed herein is a method for converting an epoxide to a first C3 product, a second C3 product, and/or a first C4 product within an integrated system. The method includes converting the epoxide to a beta lactone to produce an outlet stream comprising beta lactone. The method includes converting the beta lactone of the outlet stream to a first C3 product in the first C3 reactor to produce an outlet stream comprising the first C3 product; converting the beta lactone to a second C3 product in the second C3 reactor to produce an outlet stream comprising the second C3 product, and/or converting the beta lactone to a first C4 product in the first C4 reactor to produce an outlet stream comprising the first C4 product.

Provided herein are membrane separation systems and methods suitable for use in separating carbonylation catalyst from a beta-lactone product stream. Such membrane separation systems utilize a cross flow separation technique and employ a sweep stream.

Provided herein are membrane separation systems and methods suitable for use in separating carbonylation catalyst from a beta-lactone product stream. Such membrane separation systems utilize a cross flow separation technique and employ a sweep stream.

Provided herein are membrane separation systems and methods suitable for use in separating carbonylation catalyst from a beta-lactone product stream. Such membrane separation systems utilize a cross flow separation technique and employ a sweep stream.

Provided herein are membrane separation systems and methods suitable for use in separating carbonylation catalyst from a beta-lactone product stream. Such membrane separation systems utilize a cross flow separation technique and employ a sweep stream.

The integrated processes herein provide improved carbon efficiency for processes based on coal or biomass gasification or steam methane reforming. Provided are also ethylene oxide carbonylation products such as beta-propiolactone and succinic anhydride having a bio-based content between 0% and 100%, and methods for producing and analyzing the same.

The integrated processes herein provide improved carbon efficiency for processes based on coal or biomass gasification or steam methane reforming. Provided are also ethylene oxide carbonylation products such as beta-propiolactone and succinic anhydride having a bio-based content between 0% and 100%, and methods for producing and analyzing the same.