155 results about "Reactive separation" patented technology

A reactive-separation process converts glycerin into lower alcohols, having boiling points less than 200° C., at high yields. Conversion of natural glycerin to propylene glycol through an acetol intermediate is achieved at temperatures from 150° to 250° C. at a pressure ranging from 1 and 25 bar. The preferred applications of the propylene glycol are as an antifreeze, deicing compound, or anti-icing compound. The preferred catalyst for this process in a copper-chromium powder.

A reaction-based process has been developed for the selective removal of carbon dioxide (CO₂) from a multicomponent gas mixture to provide a gaseous stream depleted in CO₂ compared to the inlet CO₂ concentration in the stream. The proposed process effects the separation of CO₂ from a mixture of gases (such as flue gas/fuel gas) by its reaction with metal oxides (such as calcium oxide). The Calcium based Reaction Separation for CO₂ (CaRS—CO₂) process consists of contacting a CO₂ laden gas with calcium oxide (CaO) in a reactor such that CaO captures the CO₂ by the formation of calcium carbonate (CaCO₃). Once “spent”, CaCO₃ is regenerated by its calcination leading to the formation of fresh CaO sorbent and the evolution of a concentrated stream of CO₂. The “regenerated” CaO is then recycled for the further capture of more CO₂. This carbonation-calcination cycle forms the basis of the CaRS—CO₂ process. This process also identifies the application of a mesoporous CaCO₃ structure, developed by a process detailed elsewhere, that attains >90% conversion over multiple carbonation and calcination cycles. Lastly, thermal regeneration (calcination) under vacuum provided a better sorbent structure that maintained reproducible reactivity levels over multiple cycles.

The invention provides a method for catalytic conversion production of propylene and light aromatics, which is characterized in that a hydrocarbon raw material and a catalytic cracking catalyst are contacted in a composite reactor for reacting under the catalytic cracking condition, the reaction products and the to-be-regenerated catalyst are separated, the separated to-be-regenerated catalyst is circularly used through stripping and performing coke burn-off regeneration, the separated reaction products is fractionated to obtain low carbon olefin, gasoline containing light aromatics and the like, and separated to obtain the light aromatics further; the composite reactor comprises a riser reactor and a fluidized bed reactor, an outlet of the riser reactor is communicated with a lower part of the fluidized bed reactor, a stripper is positioned at the lower part of the fluidized bed reactor, an upper part of the stripper is communicated with the bottom of the fluidized bed reactor, and the outlet of the fluidized bed reactor is communicated with the inlet of a gas solid separation device in a settler though a conveying pathway, a catalyst outlet of the settler is communicated with the lower part of the fluidized bed reactor. According to the invention, propylene and light aromatics enable high yield by using the method.

The invention discloses a power quality comprehensive compensation system of an electric railway and a control method thereof. The system comprises a railway static power controller RPC and two sets of thyristor switched capacitors TSC. The thyristor switched capacitors bear a large proportion of reactive power compensation, RPC performs active power compensation, harmonic suppression and a remained small proportion of reactive power compensation for two power supply arms, therefore, the capacity of RPC is effectively reduced, and negative sequence, harmonic and reactive comprehensive compensation are realized. The control method comprises a cooperative control policy of RPC and TSC, reference current detection based on reactive separation, a reactive power distribution method and an RPC control method. The power quality comprehensive compensation system of the electric railway greatly improves the power quality of the electric railway with low cost, and the corresponding control method effectively coordinates the operation of RPC and TSC and ensures that the system has good compensation performance and favorable application prospect.

The invention relates to a method for preparing propylene through a catalytic conversion of an olefin raw material. The method comprises the steps of: introducing a raw material rich in C4<=> - C8<=> olefins into a fluidized bed reactor of a catalytic conversion device so as to contact and react with a catalytic cracking catalyst, separating a reaction product and a spent catalyst, subjecting the separated spent catalyst to steam stripping and coke burning regeneration for recycling use, and fractionating the separated product so as to obtain light olefins, gasoline, diesel oil, heavy oil and other low molecular saturated hydrocarbons. The catalytic conversion device consists of a riser reactor, a fluidized bed reactor, a settler, a stripper and a regenerator, wherein, the stripper is located under the fluidized bed reactor and is communicated with the bottom of the fluidized bed reactor, the outlet of the riser reactor is communicated with the bottom of the fluidized bed reactor, the outlet of which is communicated with the inlet of gas-solid separation equipment within the settler, and the catalyst outlet of the settler is communicated with the bottom of the fluidized bed reactor. The light olefins obtained by the method of the invention have high selectivity.

This is the craft method of preparing biological diesel oil by using the coupling technology in reaction separating course. It relates to the new craft of preparing biology diesel oil (fatty diethylene glycol dinitrate) through the ester exchange reaction of vegetable oil and higher alcohols, and belongs to chemical industry craft technology field. It includes: the ester exchange reaction of vegetable oil and higher alcohols; the separation of product fatty diethylene glycol dinitrate, glycerol and reaction mixed liquid; the separation of product fatty diethylene glycol dinitrate, glycerol and higher alcohols; the separation of fat diethylene glycol dinitrate and glycerol; the condensation backflow of fatty alcohol; and the separation of glycerol. It makes the circumvolving higher alcohols carry out the product fatty diethylene glycol dinitrate and glycerol through higher reaction temperature, and realizes the separation of outcome and reactant; the non-homogeneous phase catalyst stays in the actor, and don't need to have following process to the catalyst. The invention realizes the coupling of reaction and separation courses, speeds up the speed of non-homogeneous phase reaction, and avoids the problem of the following process to catalyst in the homogeneous phase process. Besides it can save production cost, and improves the producing performance of biology diesel oil.

The invention relates to a multifunctional catalyst having a nano/micro-scale reaction and separation coupling function. The multifunctional catalyst comprises a core carrier containing a catalytic hydrogenation active component, wherein a molecular sieve shell layer having shape selection or isomerization capability is formed on the core carrier; the molecular sieve shell layer is one or two of ZSM-5, Silicalite-1 or a mordenite type molecular sieve; the molecular sieve shell layer is of a cylindrical staggered intergrowth structure; and the staggered intergrowth structure grows vertically to the outer surface of the core carrier. Through adoption of the catalyst disclosed by the invention, nano/micro-scale reaction and separation coupling can be realized; the process flow of a current hydroisomerization reaction is improved; the operation cost is reduced; the production efficiency is increased, and efficient coupling of reaction and separation processes is realized. The catalyst can be applied to various hydrogenation and isomerization processes.

The invention relates to a gas-solid phase reaction separation system and a separation method thereof. The separation method comprises the following steps that: high-temperature flue gas (a) enters an inorganic membrane cross flow filter (II), airflow makes the circular rotation movement from the upper part to the lower part along a rotation channel (5) in a filter (II), partial particles in the airflow are thrown to the filter wall by inertial centrifugal force and collected in a dust collecting chamber (7) at the bottom of the filter, and the gas enters a membrane component (3) from the bottom to the upper part along a central exhaust passage (6) and is subjected to gas-solid separation through the sieving action of an inorganic membrane; the purified clean gas (b) enters an after-treatment (A) section; concentrated dust gas (d) intercepted by the inorganic membrane filter enters a bag-type filter (III) for collecting solid dust; the gas permeating the cloth bag filter enters the after-treatment (A) section; and the dust (e) intercepted by the inorganic membrane filter (II) and the bag-type filter (III) returns to a reactor (I) to take part in reaction.

The invention discloses a thermochemical sulfur-iodine circulating hydrogen production whole-process method and device. According to the invention, a Bunsen reaction section is coupled with an HIx and H2SO4 two-phase separation section, and an HIx purification section is coupled with a concentration section. High-temperature mixed gas of the H2SO4 decomposition tower is directly introduced into the H2SO4 concentration tower, and a large amount of water in the H2SO4 solution is quickly vaporized under the condition of no external heat source, so that the purpose of concentrating the H2SO4 solution is achieved; the high-temperature mixed gas continues to enter a downstream HIx purification and concentration tower, a large amount of water in an HIx system is vaporized and taken away, and the purpose of concentrating the HI solution is achieved. H2SO4 mingled in an HIx system is converted into SO2 in an oxygen-enriched environment and is taken away, so that the purpose of purifying the HI solution is achieved. After hydrogen in the condensing tower is separated, the residual iodine-containing liquid is recycled and returns to the Bunsen reaction separation tower, and the investment and the energy consumption can be reduced by more than 40% compared with the traditional sulfur-iodine hydrogen preparation method.

The invention discloses an improved hydrotreatment and catalytic cracking combination method for hydrocarbon oil, which comprises the following steps that: under reaction conditions of the presence of hydrogen and the hydrotreatment, the contact reaction of residual oil, catalytic cracking cycle oil, optional distillate oil and a hydrotreating catalyst is performed, and gas, hydrogenerated naphtha, hydrogenerated diesel oil and hydrogenerated tail oil are obtained after a reaction product is separated; under catalytic cracking reaction conditions, the contact reaction of the optional conventional catalytic cracking raw oil, the hydrogenerated tail oil and a catalytic cracking catalyst is performed, and dry gas, liquefied gas, catalytic cracking gasoline, catalytic cracking diesel oil and catalytic cracking cycle oil are obtained after a reaction product is separated; and the conventional catalytic cracking raw oil is light or heavy distillate oil, and the contact reaction with the catalytic cracking catalyst is that the heavy raw oil and light raw oil are optionally and orderly performed along with the hydrogenerated tail oil in a reactor comprising at least two reaction regions (I and II) along the flowing direction of reaction materials respectively. The method is suitable for hydrocarbon oil conversion to produce more gasoline and diesel oil.

The present invention relates to an atmospheric pressure, reactive separation column packed with a solid acid zeolite catalyst for producing cumene from the reaction of benzene with propylene. Use of this un-pressurized column, where simultaneous reaction and partial separation occur during cumene production, allow separation of un-reacted, excess benzene from other products as they form. This high-yielding, energy-efficient system allows for one-step processing of cumene, with reduced need for product purification. Reacting propylene and benzene in the presence of beta zeolite catalysts generated a selectivity greater than 85% for catalytic separation reactions at a reaction temperature of 115 C and at ambient pressure. Simultaneously, up to 76% of un-reacted benzene was separated from the product; which could be recycled back to the reactor for re-use.

The process and system of the embodiments utilize a reactive separation unit to upgrade a bioprocess intermediate stream to higher value liquid fuels or chemicals. The reactive separation unit simultaneously enables molecular weight and density increases, oxygen content reduction, efficient process energy integration, optional water separation for potential reuse, and incorporation of additional hydrocarbons or oxygenated hydrocarbons as co-feed(s). The use and selection of particular co-feed(s) for this purpose enables tailoring of the intended product composition. The process and system yields a product of higher alcohols, liquid hydrocarbons, or a combination of these. These can be split into two (or more) boiling point fractions by the same reactive separations unit operation resulting in product(s) that can be used as chemicals, chemical intermediates, or alternative (non-fossil-based) liquid transportation fuels.

An integrated spiral-flow reaction and separation system and process for sulfur containing gas desulfuration and belongs to the field of a gas desulfuration purifcation process. The system comprises a spiral-flow reactor (4) which is characterized in that the lower part of the spiral-flow reactor (4) is connected with one side of an amine liquid storage tank (7) through a liquid-enriching and liquid-draining pipeline (6) while the other side of the liquid storage tank (7) is connected with the liquid inlet end in the upper part of the spiral-flow reactor (4) through an absorption liquid circulating pipeline (14); the upper part of the spiral-flow reactor (4) is connected with a gas-liquid spiral-flow separator (15) through an exhaust device. The system provided by the invention integrates gas-liquid mixing, reaction and separation and solves the problem that a conventional desulfurizing absorption tower is large in occupied space and great in overall pressure drop. The overall height of the spiral-flow reactor does not exceed 8m. Compared to the height which is tens of meters of a platy tower and a filler tower, the space occupied by the device and the initial investment of the device are extremely saved. The spiral-flow reactor is strong in internal adaptability, agile to operate and free of moving parts. The system is hard to malfunction, relatively small in relative volume and convenient to overhaul.

An exemplary method for substantially non-chemically-reactive separation of nanomorphic carbon species (150) comprises inter alia the steps of dissolving a crude nanomorphic carbon sample (100) in an organic solvent (110), centrifugation of the solvated sample (120) and decantation of the resulting supernatant (130). Disclosed features and specifications may be variously controlled, adapted or otherwise optionally modified to improve carbon nanospecies purification. An exemplary embodiment of the present invention representatively provides for non-oxidative cleaning of carbon nanotubes.

A catalytic conversion method for production of propylene, a petroleum hydrocarbon raw material and methanol are respectively contacted with a catalytic cracking catalyst in a petroleum hydrocarbon catalytic cracking reaction zone and a micropore modified catalytic cracking catalyst in a methanol catalytic conversion reaction zone to react, and separation is then carried out to obtain a propylene-rich product. a coked catalyst undergoes steam stripping and regeneration and then is divided into two parts: one part is directly sent into the catalytic cracking reaction zone to be recycled; and the other part is firstly sent into a catalyst micropore modification zone to be contacted with and react with a modifier, and then the other part is sent into the methanol catalytic conversion reaction zone to be recycled. By micropore modification of a catalyst, the catalytic cracking catalyst containing double active components macroporous zeolite and mesoporous zeolite has high heavy oil conversion ability and high propylene selectivity for catalytic cracking of a petroleum hydrocarbon raw material and also has high propylene selectivity for methanol catalytic conversion.

The invention relates to a solid acid catalyst for preparing bio-based para-xylene (PX) as well as preparation and application thereof. A novel solid catalyst with a mesoporous structure is prepared by carrying out acid modification on the surface of a silicon dioxide material. The catalyst has proper acidity and is used for the reaction for catalyzing addition of 2,5-dimethyl furan and ethylene and dehydrating to prepare the PX; the coupling of reaction-separation in a PX preparation process is realized and a novel method for highly selectively preparing the bio-based PX is provided; and in a reaction process, excellent catalytic activity, selectivity and stability are represented and a firm foundation is laid for industrial production of the bio-based PX.

An exemplary method for substantially non-chemically-reactive separation of nanomorphic carbon species (140) comprises inter alia the steps of suspending a nanomorphic carbon sample (100) in an aqueous surfactant suspension (110), adding nanoparticles to the sample suspension (115), sonicating the sample (120), centrifugating the sample suspension (125) and decanting off the resulting supernatant (130). Disclosed features and specifications may be variously controlled, adapted or otherwise optionally modified to improve carbon nanospecies purification. An exemplary embodiment of the present invention representatively provides for non-oxidative cleaning of carbon nanotubes via at least partial removal of amorphous carbon contaminants.

The invention provides a reaction, separation, washing, evaporation and drying integrated device and method and belongs to the field of hydrometallurgy and the chemical industry. The device is mainly composed of unit partition chambers and accessory equipment. The partition chambers are connected through partition plates with holes, and according to different process combinations of the leaching reaction process, the separation and washing process, the crystallization and drying process and the like and different treatment objects, specific filtering films are selected and used for the partition plates with the holes, and upper sealing rings and lower sealing rings are arranged to seal the partition chambers. According to the different treatment objects, certain process procedures of the leaching reaction process, the separation and washing process and the crystallization and drying process are finished continuously in the partition chambers. By the adoption of the high-diameter high-ratio independent partition chamber space, control over the pressure, the temperature, the stirring speed and other reaction conditions is facilitated; and by the adoption of stirring scrapper devices with holes, the high-solid-liquid-ratio solid-liquid phase reaction and the high-concentration liquid phase reaction are easy to accelerate, and the mass transfer rate is increased. By the adoption of the method, adaptability to the procedures and treatment capacity is high, energy, water and chemicals can be used in a cyclic manner, cleanness and environment friendliness are achieved, and operation is convenient.

The invention discloses a novel integrated solid acid catalyst with a carbon-based structure. The novel integrated solid acid catalyst is a sulfonating carbon nano tube (CNT-SO3H@) stainless steel material and is prepared by using the stainless steel material as a support material, growing a carbon nano tube on the surface of the support material, vulcanizing through polysulfide and oxidizing. The invention simultaneously discloses a preparation method of the novel catalyst and an application in preparation of biodiesel by means of catalytic distillation. The loss of an acid position of the solid acid catalyst with the carbon-based structure is reduced; because of high heat stability and structure stability, the catalyst is easily made into various shapes and is filled into a catalytic distillation tower to be used. An original element having functions of catalyzing and separating is used for coupling a reaction process with a separation process, and because of the process, the complicated processes of pre-esterification, purification and subsequent separation are avoided; meanwhile, a glycerinum product which is used for catalyzing waste oil and methyl alcohol ester to perform exchange reaction is converted into products of glyceraldehydes, glyceric acid, hexanal dimethyl acetal, acraldehyde dimethyl acetal and the like, so that the reaction is greatly intensified; finally, a biodiesel product with high purity can be directly obtained on the top of the tower and at the bottom of the tower.

The invention discloses a high-purity disilane continuous production system and a preparation process, and belongs to the technical field of chemical reaction separation. A feeding pipeline is connected with one end of a preheater; the other end of the preheater is connected with the feeding end of a reactor through a pipeline; the discharging end of the reactor is connected with one end of a filter through a pipeline; the other end of the filter is connected with a rectifying tower I through a pipeline;the top of the rectifying tower I is connected with the feeding end of the reactor through a pipeline; the bottom of the rectifying tower I is connected with a rectifying tower II through a pipeline; the top of the rectifying tower II is connected with a reaction tank through a pipeline; and the bottom of the rectifying tower II is connected with a collector. According to the system, continuous production of high-purity disilane products can be achieved, and the purity of disilane produced by the system reaches 99.999% or above.