Abstract: Methods, compositions and systems using isoprene from a bioisoprene composition derived from renewable carbon for production of a variety of hydrocarbon fuels, fuel additives, and additives for fine chemistry and other uses is described.

Abstract: The present invention relates to a zinc ferrite catalyst, a method of producing the same, and a method of preparing 1,3-butadiene using the same. Specifically, the present invention relates to a zinc ferrite catalyst which is produced in a pH-adjusted solution using a coprecipitation method, a method of producing the same, and a method of preparing 1,3-butadiene using the same, in which the 1,3-butadiene can be prepared directly using a C4 mixture including n-butene and n-butane through an oxidative dehydrogenation reaction. The present invention is advantageous in that 1,3-butadiene can be obtained at a high yield directly using a C4 fraction without performing an additional process for separating n-butene, as a reactant, from a C4 fraction containing impurities.

Abstract: Process for making a bio-diesel and a bio-naphtha and optionally bio-propane from a complex mixture of natural occurring fats & oils, wherein said complex mixture is subjected to a refining treatment for removing the major part of the non-triglyceride and non-fatty acid components, thereby obtaining refined oils; said refined oils are subjected to a fractionation step for obtaining: an unsaturated or substantially unsaturated, liquid or substantially liquid triglyceride part (phase L); and a saturated or substantially saturated, solid or substantially solid triglyceride part (phase S); and said phase L is transformed into alkyl-esters as bio-diesel by a transesterification; said phase S is transformed into linear or substantially linear paraffin's as the bio-naphtha: by an hydrodeoxygenation or from said phase S are obtained fatty acids that are transformed into linear or substantially linear paraffin's as the bio-naphtha by hydrodeoxygenation or decarboxylation of the free fatty acids or from said

Abstract: 1,3-butadiene is obtained by extractive distillation with a selective solvent from a C4 cut comprising C4 acetylenes as secondary components in a dividing wall column having a bottom evaporator, in which a dividing wall is disposed in the longitudinal direction of the column to form a first subregion, a second subregion and a lower combined column region. The column is disposed upstream of an extractive wash column. The energy input into the dividing wall column via the bottom evaporator is controlled in such a way that a bottom stream containing solvent, C4 acetylenes and 1,3-butadiene restricted such that the loss of 1,3-butadiene is economically acceptable, is drawn off and fed to an acetylenes outgasser where the C4 acetylenes are stripped out overhead and purified solvent is obtained as the bottom stream.

Abstract: A process for recovering crude 1,3-butadiene from a C4 fraction by extractive distillation using a selective solvent in a dividing wall column (TK) in which a dividing wall (T) is arranged in the longitudinal direction of the column to form a first subregion (A), a second subregion (B) and a lower common column region (C) and which is preceded by an extractive scrubbing column (K), wherein the operation of the dividing wall column (TK) is set by regulation of the energy input into the dividing wall column (TK) via a bottom vaporizer (V) and setting of the number of the theoretical plates in the lower common column region (C) so that a bottom stream (17) consisting of purified solvent is obtained from the dividing wall column (TK), is proposed.

Abstract: A process for recovering crude 1,3-butadiene from a C4 fraction by extractive distillation using a selective solvent in a dividing wall column (TK) in which a dividing wall (T) is arranged in the longitudinal direction of the column to form a first subregion (A), a second subregion (B) and a lower common column region (C) and which is preceded by an extractive scrubbing column (K) is proposed.

Abstract: A process for obtaining pure 1,3-butadiene from crude 1,3-butadiene by distillation is carried out in a dividing wall column in which a dividing wall is located in the longitudinal direction of the column to form an upper common column region, a lower common column region, a feed section and an offtake section.

Abstract: A cyclic process for the purification of a diolefin hydrocarbon stream produced in a naphtha steam cracker to produce a high quality diolefin hydrocarbon stream having extremely low levels of acetylene over an extended period because of the ability to readily cyclically regenerate catalyst contained in an off-line selective hydrogenation reaction zone. The spent or partially spent catalyst is contacted with a stream containing naphtha and hydrogen to restore at least a portion of the fresh catalyst activity by the extraction of polymer compounds therefrom.

Abstract: An alpha-tocopherol is disclosed as a polymerization inhibitor effective against vinyl monomer polymerization. Alpha-tocopherol was found to inhibit polymerization of acrylonitrile and diolefines such as isoprene and butadiene. Alpha-tocopherol was found to interact synergistically with hydroquinone in inhibiting polymerization of acrylonitrile.

Abstract: Described is a process for the production of depolymerized natural rubber, which makes it possible to obtain, at high reaction efficiency, of depolymerized natural rubber in the liquid form and having a narrow molecular weight distribution; and also a process for the production of depolymerized natural rubber which is free from odor or coloring peculiar to natural rubber and is also free from the danger of immediate allergy derived from protein.The process according to the present invention comprises adding a carbonyl compound to a natural rubber latex, and then subjecting the resulting natural rubber to air oxidation in the presence of a radical forming agent or adding a carbonyl compound to the latex of deproteinized natural rubber and then subjecting the deproteinized natural rubber to air oxidation optionally in the presence of a radical forming agent.

Abstract: Improved operation of the ACR process is achieved by regulating the reactions within a small area in the combustion feedstock mixing zone, "Scorch Zone", by the addition of steam or other fluid such as ethane at the point of feed injection.

Abstract: The present invention relates to a process for the preparation of olefins and diolefins by the cracking of hydrocarbons in the presence of steam, consisting in passing a mixture of hydrocarbons and steam flowing in a cracking tube disposed inside a radiation zone of a furnace. The process is characterized in that the mean dwell time of the mixture of flowing in the cracking tube between the inlet and the outlet of the radiation zone is from 300 to 1800 milliseconds, and the reaction volume is greater in the first half of the tube length than in the second one. The present invention relates also to a cracking furnace in which the ratio between the length and the mean diameter of the cracking tube is from 200 to 600, and the tube diameter decreases from the inlet to the outlet of the radiation zone.

Abstract: The present invention relates to a process for the preparation of olefins by the cracking of hydrocarbons consisting in passing a mixture of hydrocarbons and steam flowing in a cracking tube disposed inside a radiation zone of a furnace. The process is characterized in that an increase of the cracking temperature of the mixture between the inlet and the outlet of the radiation zone is associated to a non-homogeneous distribution of the thermal power of the furnace, greater at the beginning of the cracking tube than at the end, and to a reaction volume which is greater in the second half of the length tube than in the first one.The present invention relates also to a cracking furnace in which between the inlet and the outlet of the radiation zone the diameter of the cracking tube increases and the thermal power of the heating means decreases.

Abstract: Methane is converted to higher, more reactive, hydrocarbon products by a diffusion flame. Methane is converted to C.sub.2 + products by pyrolysis in the interior of the flame with oxidizing gas flowing outside of the flame. More reactive products are withdrawn from the center of the flame by a probe tube and cooled by the flowing oxidizing gas to stop the reaction.

Abstract: A diffusion flame reactor for cracking hydrocarbon gas has an oxygen-deficient zone in the center of the flame or in the center of an array of flames. Propane, n-octane, iso-octane and decalin are cracked to ethylene, acetylene, propylene, butenes, and butadienes which are withdrawn from the flame.

Abstract: A continuous process for the selective production of ethylene by the diacritic cracking of heavy hydrocarbon feeds such as residual oils, heavy vacuum gas oils, atmospheric gas oils, crude oils and coal-derived liquids. The diacritic cracking takes place in a non-tubular multi-zone reactor at elevated pressures (e.g. 70-1000 p.s.i.a.) A fuel is combusted with oxygen in the first section of the multi-zone reactor. The high temperature products of combustion of the first zone pass into a second section of the reactor where the feed is atomized and cracked to yield products including ethylene, acetylene and synthesis gas. The reaction products of the second zone then pass into a third section in which they are quenched. In each stage of the reactor the present process seeks to prevent the build-up of coke deposits on the walls of the reactor. In the first two stages, a film of gas such as CO.sub.2 or N.sub.2 is injected along the inner walls to prevent build-up of coke.