초록 ▼

A process for producing olefins and diolefins. A flow of gas is compressed with a prime mover in a near adiabatic path. Resistance to the flow within the adiabatic path causes a temperature rise with respect to its pressure, where it enters a near adiabatic tunnel. At least one other gas is provided

A process for producing olefins and diolefins. A flow of gas is compressed with a prime mover in a near adiabatic path. Resistance to the flow within the adiabatic path causes a temperature rise with respect to its pressure, where it enters a near adiabatic tunnel. At least one other gas is provided into the tunnel at a prescribed, independently controlled temperature and pressure. The compressed flow is comingled and mixed with at least one other gas. Hydrogen and oxygen are fed into the tunnel to produce steam. Steam is applied to at least one hydrocarbon for pyrolysis or thermal cracking to yield at least one of olefins and diolefins.

대표청구항 ▼

A process for producing olefins and diolefins. A flow of gas is compressed with a prime mover in a near adiabatic path. Resistance to the flow within the adiabatic path causes a temperature rise with respect to its pressure, where it enters a near adiabatic tunnel. At least one other gas is provided

A process for producing olefins and diolefins. A flow of gas is compressed with a prime mover in a near adiabatic path. Resistance to the flow within the adiabatic path causes a temperature rise with respect to its pressure, where it enters a near adiabatic tunnel. At least one other gas is provided into the tunnel at a prescribed, independently controlled temperature and pressure. The compressed flow is comingled and mixed with at least one other gas. Hydrogen and oxygen are fed into the tunnel to produce steam. Steam is applied to at least one hydrocarbon for pyrolysis or thermal cracking to yield at least one of olefins and diolefins. to the formula R—(OH)p, where R denotes an aromatic radical and p is an integer from 1 to 4, and wherethe solvent has a boiling point of 30 to 200° C.2. A process for the separation of reaction by-products, D which are generated upon carbonylations and oxidative couplings of hydroxyaromatic compounds or phenol and quaternary salts A, and reaction product C, wherein D is at least one member selected from the group consisting of 2-phenoxyphenol, 4-phenoxyphenol, salicylic acid phenyl ester, 2-bromophenol, 4-bromophenol, 2-cumyl phenol, 4-cumyl phenol, 2,2′-dihydroxybiphenyl, 2,4′-dihydroxybiphenyl, 4,4′-dihydroxybiphenyl, as well as di- or oligo(aryl carbonates), di- and oligo(phenoxy phenols), oligo(phenoxy phenol carbonates), biphenol monocarbonates and biphenyl dicarbonates, where the total weight of D is less than the weight of a main reaction product C, comprising working up at least once the material system that contains the solution from the process of claim 1 which comprises DA, B and C, to obtain in step a) an aqueous phase containing salt A, and an organic phase which contains C and then separating C from the organic phase by crystallisation or distillation to obtain C and, D, and working up the aqueous phase obtained following step a) according to step b), and returning the organic phase which contains at least some D into the reaction.3. The process according to claim 1 in which at least one of steps a) to e) is carried out at temperatures of 28 to 98° C.4. The process according to claim 1 in which the reaction products C includes at least one reaction product of B.5. The process according to claim 1 in which B includes phenol and C includes diphenyl carbonate.6. The process according to claim 1 in which cBis greater in step b1) than in step a2).7. The process according to claim 1 in which the solvent is at least one member selected from the group consisting of hydrocarbons, halogenated hydrocarbons, aromatic solvents, ethers, chlorobenzene, dichlorobenzenes, fluorobenzene, benzene, toluene, anisole, methylene chloride, 1,2-dichloroethane, esters, ethers such as dioxane, tetrahydrofuran, tert.-butylmethyl ether and etherified glycols.8. The process according to claim 1 wherein the mass fraction CBof the organic phase used in step b1) is 3 wt. %