A process is presented for the production of light olefins. The process utilizes a SAPO-18 catalyst and is operated at an elevated pressure. The process generates higher concentrations of heavier olefins which can then be processed to generate light olefins. The processing of the heavier olefins can include metathesis reactions and olefin cracking processes.

A process is presented for generating light olefins with the methanol to olefins process from a combination of catalysts. The process controls the product distribution for ethylene, propylene and butylenes, to enable shifting of the product distribution. The process includes passing a second catalyst to a reactor while the process is on-going.

A process is presented for generating light olefins with the methanol to olefins process from a combination of catalysts. The process controls the product distribution for ethylene, propylene and butylenes, to enable shifting of the product distribution. The process includes passing a second catalyst to a reactor while the process is on-going.

A process is presented for generating light olefins with the methanol to olefins process from a combination of catalysts. The process controls the product distribution for ethylene, propylene and butylenes, to enable shifting of the product distribution. The process includes passing a second catalyst to a reactor while the process is on-going.

The present disclosure provides natural gas and petrochemical processing systems, including oxidative coupling of methane reactor systems that may integrate process inputs and outputs to cooperatively utilize different inputs and outputs in the production of higher hydrocarbons from natural gas and other hydrocarbon feedstocks. The present disclosure also provides apparatuses and methods for heat exchange, such as an apparatus that can perform boiling and steam super-heating in separate chambers in order to reach a target outlet temperature that is relatively constant as the apparatus becomes fouled. A system of the present disclosure may include an oxidative coupling of methane (OCM) subsystem that generates a product stream comprising compounds with two or more carbon atoms, and a dual compartment heat exchanger downstream of, and fluidically coupled to, the OCM subsystem.

The present disclosure provides natural gas and petrochemical processing systems, including oxidative coupling of methane reactor systems that may integrate process inputs and outputs to cooperatively utilize different inputs and outputs in the production of higher hydrocarbons from natural gas and other hydrocarbon feedstocks. The present disclosure also provides apparatuses and methods for heat exchange, such as an apparatus that can perform boiling and steam super-heating in separate chambers in order to reach a target outlet temperature that is relatively constant as the apparatus becomes fouled. A system of the present disclosure may include an oxidative coupling of methane (OCM) subsystem that generates a product stream comprising compounds with two or more carbon atoms, and a dual compartment heat exchanger downstream of, and fluidically coupled to, the OCM subsystem.

The present disclosure provides natural gas and petrochemical processing systems, including oxidative coupling of methane reactor systems that may integrate process inputs and outputs to cooperatively utilize different inputs and outputs in the production of higher hydrocarbons from natural gas and other hydrocarbon feedstocks. The present disclosure also provides apparatuses and methods for heat exchange, such as an apparatus that can perform boiling and steam super-heating in separate chambers in order to reach a target outlet temperature that is relatively constant as the apparatus becomes fouled. A system of the present disclosure may include an oxidative coupling of methane (OCM) subsystem that generates a product stream comprising compounds with two or more carbon atoms, and a dual compartment heat exchanger downstream of, and fluidically coupled to, the OCM subsystem.

Mixed pentenes may be converted to propylene by feeding an alcohol, linear pentenes, and isopentenes to an etherification reactor. The alcohol and isopentenes may be reacted in the etherification reactor to convert isopentenes to tertiary amyl alkyl ether, which may be separated from the linear pentenes, recovered as a linear pentene fraction. The tertiary amyl alkyl ether may be fed to a decomposition reactor to convert at least a portion of the tertiary amyl alkyl ether to alcohol and isopentenes. The alcohol and isopentenes may then be separated to recover an isopentene fraction and an alcohol fraction. The isopentene fraction is then fed to a skeletal isomerization reactor to convert at least a portion of the isopentenes to linear pentenes, the effluent from which may be recycled to the etherification reactor. Ethylene and the linear pentene fraction may then be fed to a metathesis reactor to produce propylene.

Mixed pentenes may be converted to propylene by feeding an alcohol, linear pentenes, and isopentenes to an etherification reactor. The alcohol and isopentenes may be reacted in the etherification reactor to convert isopentenes to tertiary amyl alkyl ether, which may be separated from the linear pentenes, recovered as a linear pentene fraction. The tertiary amyl alkyl ether may be fed to a decomposition reactor to convert at least a portion of the tertiary amyl alkyl ether to alcohol and isopentenes. The alcohol and isopentenes may then be separated to recover an isopentene fraction and an alcohol fraction. The isopentene fraction is then fed to a skeletal isomerization reactor to convert at least a portion of the isopentenes to linear pentenes, the effluent from which may be recycled to the etherification reactor. Ethylene and the linear pentene fraction may then be fed to a metathesis reactor to produce propylene.

Mixed pentenes may be converted to propylene by feeding an alcohol, linear pentenes, and isopentenes to an etherification reactor. The alcohol and isopentenes may be reacted in the etherification reactor to convert isopentenes to tertiary amyl alkyl ether, which may be separated from the linear pentenes, recovered as a linear pentene fraction. The tertiary amyl alkyl ether may be fed to a decomposition reactor to convert at least a portion of the tertiary amyl alkyl ether to alcohol and isopentenes. The alcohol and isopentenes may then be separated to recover an isopentene fraction and an alcohol fraction. The isopentene fraction is then fed to a skeletal isomerization reactor to convert at least a portion of the isopentenes to linear pentenes, the effluent from which may be recycled to the etherification reactor. Ethylene and the linear pentene fraction may then be fed to a metathesis reactor to produce propylene.