Abstract: A production plant and a method for production of a synthetized gasoline product from a synthetic hydrocarbon mixture produced from a mixture of reactive oxygenates, the method including a. separating the synthetic hydrocarbon mixture in at least a light hydrocarbon fraction, and a higher boiling hydrocarbon fraction, wherein the higher boiling fraction comprises at least 70% of the molecules including 10 or more carbon atoms and less than 20% of the molecules comprising exactly 9 carbon atoms, b. directing at least an amount of said higher boiling hydrocarbon fraction as a hydrocracking feedstock to contact a material catalytically active in hydrocracking under effective hydrocracking conditions providing a hydrocracked hydrocarbon stream, wherein at least an amount of said hydrocracked hydrocarbon stream is combined with at least an amount of said light hydrocarbon fraction, to provide said synthetized gasoline product having a T90 being below T90 of said synthetic hydrocarbon mixture.

Abstract: This disclosure provides processes for reforming hydrocarbons by using a series of adiabatic reactors and catalysts, in which the catalyst(s) in at least one front or upstream catalyst bed or reactor includes a higher fluoride concentration, higher chloride concentration, or both than the respective halide concentrations in the catalysts in one or more downstream catalyst beds or reactors, which has been unexpectedly discovered to extend the useful life and/or the selectivity of the catalyst system.

Abstract: A process includes a.) supplying a biomass feedstock, a fluidizing gas having hydrogen, and a catalyst recirculation stream having deoxygenating catalyst to a mixing zone of a fluidized bed reactor; b.) allowing the biomass feedstock, the fluidizing gas and the deoxygenating catalyst to move upwards through the fluidized bed reactor from the mixing zone to a bulk reactor zone; c.) allowing the biomass feedstock to contact the deoxygenating catalyst in the presence of the fluidizing gas in the bulk reactor zone of the fluidized bed reactor to produce a hydropyrolysis reactor output including at least one non-condensable gas, a partially deoxygenated hydropyrolysis product and char; and d.) withdrawing at least a portion of the deoxygenating catalyst from the bulk reactor zone to form the catalyst recirculation stream that is supplied to the mixing zone in step a).

Abstract: A fluidized bed reactor, a device, and a method for producing low-carbon olefins from oxygen-containing compound are provided. The fluidized bed reactor includes a reactor shell, a reaction zone, a coke control zone and a delivery pipe, where there are n baffles arranged in the coke control zone, and the n baffles divide the coke control zone into n sub-coke control zones which include a first sub-coke control zone, a second sub-coke control zone, and an nth sub-coke control zone; at least one catalyst circulation hole is provided on each of the n-1 baffles, so that the catalyst flows in an annular shape in the coke control zone, where n is an integer. The device and method can be adapted to a new generation of DMTO catalyst, and the unit consumption of production ranges from 2.50 to 2.58 tons of methanol/ton of low-carbon olefins.

Abstract: A selective hydrogenation catalyst that can be obtained by the process comprising at least the following steps: a) the alumina support is brought into contact with at least one organic additive; b) the alumina support is brought into contact with at least one nickel metal salt, the melting point of said metal salt of which is between 20° C. and 150° C.; c) the solid mixture obtained on conclusion of steps a) and b) is heated with stirring; d) the catalyst precursor on conclusion of step c) is dried; e) a step of heat treatment of the dried catalyst precursor obtained on conclusion of step d) is carried out.

Abstract: According to one or more embodiments of the present disclosure, a fluidization promoter useful for dehydrogenation includes from 0.1 wt. % to 10 wt. % gallium, from 5 ppm to 500 ppm platinum, less than 5 wt. % alkali metal or alkaline earth metal, and a support material. A median particle size of the fluidization promoter is from 20 ?m to 50 ?m. Catalyst systems useful for dehydrogenation and methods for producing olefins using the same are also disclosed.

Abstract: Methods and systems are provided for the conversion of waste plastics into various useful downstream recycle-content products. More particularly, the present system and method involves integrating a pyrolysis facility with a cracker facility by introducing at least a stream of r-pyrolysis gas into the cracker facility. In the cracker facility, the r-pyrolysis gas may be separated to form one or more recycle content products, and can enhance the operation of the facility.

Abstract: A fluidized catalytic conversion method for maximizing the production of propylene includes the steps of: 1) contacting a heavy feedstock oil with a catalytic conversion catalyst having a temperature of 650° C. or higher for reaction; 2) contacting a hydrocarbon oil feedstock having an olefin content of 50 wt % or more with the catalytic conversion catalyst after the reaction of step 1); 3) separating a first catalytic cracking distillate oil and a second catalytic cracking distillate oil from the resulting reaction products; 4) separating an olefin-rich stream from the first catalytic cracking distillate oil; and 5) recycling the olefin-rich stream. The method can effectively improve the yield of propylene and realize an effective utilization of petroleum resources.

Abstract: A process for producing lower olefins from oxygenates includes the steps of contacting a feedstock comprising oxygenates with molecular sieve catalyst in fluidized bed reaction zone under effective conditions, to produce product including ethylene and/or propylene; the effective conditions include that in the fluidized bed reaction zone, the weights of catalysts having various carbon deposition amounts are controlled, calculated as the weight of the molecular sieve in the catalysts, to have the following proportions based on the total weight of the catalysts in the fluidized bed reaction zone: the proportion of the weight of the catalyst having a coke deposition amount of less than 3 wt % is 1-20 wt %; the catalyst having a coke deposition amount of from 3 wt % to less than 5 wt % represents 10 to 70 wt %; and the catalyst having a coke deposition amount from 5 wt % to 10 wt % represents 10 to 88 wt %.

Abstract: A method for upgrading a naphtha feed includes passing the naphtha feed to an adsorption unit to produce at least a paraffin stream and an isoparaffin stream, wherein the isoparaffin stream comprises isoparaffins and aromatics. Passing the isoparaffin stream to an isoparaffin aromatization catalytic unit that contacts the isoparaffin stream with at least one aromatization catalyst produces aromatics from the isoparaffins thereby yielding an aromatization effluent. The at least one aromatization catalyst may comprise ZSM-5 zeolite. Benzene, toluene, and/or xylene (BTX) may be separated from the aromatization effluent by separating the aromatics effluent into a gas stream and a liquid stream in a gas/liquid separator, wherein the liquid stream contains BTX. Passing the liquid stream to a BTX-separation unit may produce a BTX stream and a recycle stream, wherein the BTX stream contains benzene, toluene, and/or xylene.

Abstract: A process and a device for continuous flow side-chain alkylation which relate to the technical field of organic synthesis. In this process and the device for continuous flow side-chain alkylation, an ibuprofen raw material is prepared with alkylbenzene as a raw material. This raw material alkylbenzene is easily available and has a low cost, and is suitable for scale-up production. Moreover, an entire preparation process adopts continuous chemical synthesis, and a reaction time of each stage can be precisely controlled, which is beneficial to control a total reaction time and reduce an amount of impurities produced. In this way, a purity and a yield of the ibuprofen raw material are improved. In summary, a continuous synthesis method for side-chain alkylation of alkylbenzene provided by the present disclosure shows a low cost and a high yield.

Abstract: A process for oligomerizing olefin streams comprising sending olefin streams comprising a C2? olefin vapor stream and a C3+ olefin liquids stream to a first stage oligomerization reactor containing a solid acid oligomerization catalyst to produce a first stage oligomerized stream; oligomerizing said first-stage oligomerization stream in a second stage oligomerization reactor containing a metal catalyst to provide a second stage oligomerized stream.

Abstract: Methylparaffins having limited methyl branching may be prepared by contacting at least one linear olefin with hydrogen in the presence of a dual-function supported catalyst comprising a solid acid component and a hydrogenation component under conditions sufficient to catalytically isomerize the at least one linear olefin into an intermediate product comprising one or more branched olefins, and hydrogenating the one or more branched olefins to form an isoparaffin product comprising one or more methylparaffins. Heat transfer fluids comprising such methylparaffins may be used in various thermal management systems, such as within various systems of electric vehicles, server farms, or other locales in need of efficient heat transfer.

Abstract: A process for producing isooctane by introducing a butane feed stream (containing n-butane, i-butane) and hydrogen into a catalytic hydrogenolysis reactor to produce a hydrogenolysis product stream; separating the hydrogenolysis product stream into a butane stream (i-butane, optionally n-butane); feeding the butane stream to a catalytic dehydrogenation reactor to produce a dehydrogenation product stream comprising saturated and unsaturated four-carbon hydrocarbons; and feeding the dehydrogenation product stream to an oligomerization unit to produce isooctene and dehydrogenating the isooctene to produce isooctane.

Abstract: The preset invention provides an energy-saving process and device for recovering C2 from refinery dry gas. The process is as follows: dry gas is cooled and then sent to a multi-stage absorption tower for treatment; the gas phase from the multi-stage absorption tower is sent to a fuel gas pipeline network or PSA unit, and the liquid phase is sent to a high-pressure flash zone for treatment; the gas phase from the high-pressure flash zone is returned to a compression section of a dry gas pretreatment system; the gas phase from the low-pressure flash zone is sent to a C2 concentrated gas compressor system; and the gas phase from the desorption tower is mixed with the gas phase obtained from the low-pressure flash zone and sent to an ethylene cracking furnace as a C2 concentrated gas product, most of the liquid phase is returned to the multi-stage absorption tower.

Abstract: A process for selectively producing oligomers may comprise bringing at least one antifouling agent into contact with a first amount of at least one aluminum alkyl compound to form at least one antifouling compound comprising the structure or its dimeric form; and feeding the at least one antifouling compound, an additional amount of the at least one aluminum alkyl compound, at least one titanate compound, and ethylene into a jet loop reactor and oligomerizing ethylene to produce one or more of 1-butene, 1-hexene, or 1-octene. One or more of the chemical groups R1, R2, and R3 may be the antifouling agent comprising the structure —O((CH2)nO)mR4. n may be an integer of from 1 to 20. m may be an integer of from 1 to 100. R4 may be a hydrocarbyl group. In embodiments, the chemical groups R1, R2, or R3 that do not comprise the antifouling agent, if any, may be hydrocarbyl groups.

Abstract: A system and a method for catalytically cracking hydrocarbons. The system includes a fluidized bed riser reactor, and a separation zone configured to separate the effluent from the riser reactor to produce a product stream and a spent catalyst. A stripping zone is fluidly coupled to the outlet of the separation zone such that the spent catalyst is stripped to remove the hydrocarbons adsorbed thereon. The stripping zone encompasses at least a portion of the riser reactor such that stripping internals in the stripping zone are used to provide reaction heat to the riser reactor.

Abstract: The invention comprises methods of catalytically pyrolyzing plastics. Since it has been discovered that plastics provide insufficient coke to provide adequate heat during catalyst regeneration, heat-forming additives can be introduced into the methods. Systems and compositions useful in the catalytic pyrolysis of plastics are also described.

Abstract: Disclosed herein are processes and systems for removing heavy C5+ hydrocarbon components from a natural gas feed gas by subjecting the natural gas feed gas stream to an adsorber. The adsorber in the processes and systems described herein operating at a pressure that may be associated with improved adsorption capacity and longer breakthrough time.

Abstract: A method of performing an oxidative coupling of methane (OCM) reaction to produce C2+ compounds using a low temperature gas mixture feed is provided. The method includes introducing a gas mixture feed containing methane, oxygen, hydrogen, and carbon monoxide at a temperature of less than or equal to 300° C. to an inlet of an OCM reactor, which contains a combustion catalyst and an OCM catalyst. At least a portion of the gas mixture feed is combusted using the combustion catalyst to generate a heated gas mixture having a temperature of at least 450° C. The heated gas mixture contacts the OCM catalyst to initiate an OCM reaction and produce an OCM effluent that includes C2+ compounds. A system for performing an OCM reaction using a low temperature feedstock gas mixture is also provided.