134results about "Absorption purification/separation" patented technology

The invention relates to a device and a method for preparing isobutene and methanol by cracking methyl tert-butyl ether. The device comprises a methyl tert-butyl ether vaporization refining tower, a reactor, a cooling tower, an absorption tower, a methanol extraction tower, an isobutene light component removal tower and an isobutene heavy component removal tower which are sequentially connected along a material conveying direction, a top discharge hole of the cooling tower is connected with a lower gas-phase material inlet of the absorption tower; an absorbent outlet at the bottom of the absorption tower is circularly connected with a cooling absorption liquid inlet at the top of the cooling tower; the bottom extract liquor outlet of the methanol extraction tower is circularly connected with the top absorbent inlet of the absorption tower; an isobutylene discharge hole is formed in the top of the isobutylene heavy component removal tower; the device further comprises a methanol recovery tower and a methanol refining tower which are connected in sequence along the material conveying direction; a bottom cooling absorption liquid outlet of the cooling tower is connected with the methanol recovery tower; a methanol discharge hole is formed in the bottom of the methanol refining tower. The device provided by the invention not only can relax the limitation of the purity of methyl tert-butyl ether in raw materials, but also can prepare high-purity isobutene and high-purity methanol at the same time.

The utility model provides a recovery system which comprises a reactor, an absorption tower, a condenser, a first compressor, a crude product storage tank, a second compressor, a rectifying tower and a gas-liquid separation tank, the top of the reactor is communicated with a first pipeline, the bottom of the absorption tower is communicated with the bottom of the reactor through a second pipeline, and the top of the absorption tower is communicated with the first pipeline through a third pipeline; the condenser is installed on the second pipeline, the first compressor is installed on the third pipeline, the crude product storage tank is communicated with the bottom of the absorption tower through a fourth pipeline and a fifth pipeline, the second compressor is installed on the fifth pipeline, and the middle of the rectifying tower is communicated with the crude product storage tank through a sixth pipeline; the gas-liquid separation tank is communicated with the rectifying tower through at least two eighth pipelines so as to be used for separating rectified materials and realizing reflux of the rectifying tower, and the gas-liquid separation tank is communicated with the crude product storage tank through a ninth pipeline so as to be used for guiding separated gas into the crude product storage tank. The recovery system provided by the utility model is beneficial to improving the raw material utilization rate so as to reduce the production cost.

A method of absorbing a solvent from a gas stream can involve flowing a gas stream comprising air and a hydrocarbon through an absorption tower in a counter-current direction with a first lean absorbent liquid to absorb a solvent from the gas stream and produce a first conditioned gas stream and a first rich absorbent liquid. The method can subsequently involve flowing the first conditioned gas stream through the absorption tower in a co-current direction with a second lean absorbent liquid to absorb a solvent from the first conditioned gas stream and produce a second conditioned gas stream and a second rich absorbent liquid, the second conditioned gas stream having a reduced concentration of the hydrocarbon compared to the first conditioned gas stream.

The venturi-type scrubber may be used in conjunction with the removal of solids and quench gas-phase reaction products from the gas-phase reaction products. A method can include: providing a reaction product comprising a hydrocarbon gas and a solid; introducing the reaction product into a venturi type scrubber; introducing a scrubbing fluid into the venturi-type scrubber, wherein the scrubbing fluid is at a lower temperature than the reaction product; generating, by the venturi scrubber, a heterogeneous product comprising a scrubbed reaction product and a waste scrubbing fluid, the scrubbed reaction product comprising the hydrocarbon gas, and the waste scrubbing fluid comprising the scrubbing fluid and the solids; and separating the hydrocarbon gas from the multiphase fluid. A system may include a reactor; a venturi-type scrubber having a first inlet fluidly connected to the reactor and a second inlet configured to receive a scrubbing fluid; and a separation column configured to receive a multiphase stream from the venturi scrubber after solids are removed.

A process for preparing an olefin stream for oligomerization includes fractionating the olefin stream to provide a light gas stream and an olefin-rich stream. Oxygenates are absorbed from the olefin-rich stream into a water wash stream to provide an oxygenate-rich water wash stream and a washed olefin stream. The washed olefin stream can then be oligomerized.

A process for separating 1-butene from a C4 raffinate gas composition includes introducing the C4 raffinate gas composition to a reactor containing an adsorbent material and passing the C4 raffinate gas composition through the adsorbent material; adsorbing the 1-butene from the C4 raffinate gas composition onto the adsorbent material to separate the 1-butene from the C4 raffinate gas composition and form a residue gas composition; and desorbing the 1-butene by heating the adsorbent material after the adsorbing to form the 1-butene and regenerate the adsorbent material. The adsorbent material is at least one of a zeolite adsorbent and an alkali-modified zeolite adsorbent having at least 99% by weight selective towards 1-butene for adsorption in comparison to iso-butene and iso-butane.

The invention relates to the technical field of dry gas treatment, and discloses a method and a device for preparing polymer grade ethylene by recovering C2 components in dry gas and application, the method comprises the following steps: (1) compressing the raw material dry gas and carrying out gas-liquid separation to obtain a gas phase and a liquid phase; (2) contacting the gas phase with an absorbent for C2 component absorption to obtain absorption tail gas and an absorption rich solution; (3) performing methane desorption on the liquid phase to obtain desorbed gas and a rich absorbent; (4) desorbing and separating the rich absorbent to obtain a lean absorbent and concentrated gas; (5) the concentrated gas is subjected to acid gas removal, dehydration and impurity removal and then sent to a deethanizer for separation of light components and heavy components, and a gas phase at the top of the tower serves as feed to enter an ethylene rectifying tower for separation of ethylene and ethane; and (6) extracting a polymer-grade ethylene product from the side of the body of the ethylene rectifying tower. The C2 component recovered by the method has the advantages of high purity, high recovery rate, simple process, low steam consumption, no need of a deoxidation reactor and a demethanizer, and low energy consumption of the device.

The invention discloses an after-deacetylation product gas separation process for methanol-to-olefin, which belongs to the field of organic chemical industry and comprises the following steps: pre-treated and dehydrated product gas enters a C2 and C3 cutting tower, a tower top gas phase is condensed and then partially refluxed, and the rest enters the tail section of a product gas compressor; and the tower kettle material enters a depropanizing tower. And a liquid-phase material at the top of the depropanizing tower is selectively fed into the downstream demethanizing tower or deethanizing tower through a pump. The C2 and C3 cutting and fractionating system is adopted, the material flow direction is optimized, the suction load of the tail section of a product gas compressor and the propylene refrigerant consumption of a subsequent demethanizing tower are greatly reduced, and meanwhile, the material circulation amount and the washing liquid requirement in the system are reduced, so that the equipment investment and the device operation energy consumption are remarkably reduced; and the technological process is simplified.

The application discloses a process for purifying and separating n-hexane waste gas in grain oil production and belongs to the technical field of waste gas treatment of agricultural and sideline products. Mixed adsorbents are introduced into a solvent absorption tower, n-hexane waste gas is adsorbed by the solvent absorption tower to obtain mixed absorption liquid, and the mixed absorption liquid is treated by a desorption tower to realize separation of n-hexane and the mixed adsorbents. The whole process does not involve catalytic reaction, mainly relies on physical absorption and desorption process to realize separation and recovery of n-hexane, and does not need to suspend grain oil production, realizes synchronous performance of grain oil production and n-hexane tail gas separation, and can effectively improve grain oil processing efficiency.

The invention relates to the technical field of aromatic hydrocarbon separation and purification, in particular to a system and process flow for removing C8 non-aromatic hydrocarbon in xylene through membrane separation, and the system comprises a membrane separation unit, a feeding unit, a permeation side system, an interception side system, an adsorption tower feeding buffer tank outlet line and a crossover line; the membrane separation unit is provided with a membrane feeding pipeline, one end of the membrane separation unit is connected to an outlet of the membrane separation feeding buffer tank, and the other end of the membrane separation unit is connected to an inlet side pipe orifice of the separation pipeline; a membrane feeding booster pump is arranged on the membrane feeding pipeline; a spiral-wound membrane assembly is arranged in the separation pipeline; the feeding unit is provided with a xylene redistillation tower top outlet line which is connected to an inlet of the membrane separation feeding buffer tank from the xylene redistillation tower top. According to the membrane separation process adopted by the method, the non-aromatic hydrocarbon removal rate can be more than 98% under the operation conditions that the feeding pressure is 1.68 MPa, the permeation side is 20 kPa and the interception side is 1.6 MPa, and the method has definite industrial feasibility and technical advantages.

The application discloses a biomass fermentation process for preparing green methanol, which comprises the following steps: providing a biomass raw material, and fermenting to obtain biogas; obtaining rich-methane gas after crude purification of the biogas; obtaining qualified rich-methane gas after super-precision detoxification of the rich-methane gas; adding medium-pressure steam into the qualified rich-methane gas, and performing a methane steam reforming reaction to obtain a mixed gas; performing PSA treatment on the mixed gas to obtain a resolved gas and a raw material gas; and feeding the resolved gas into a normal-temperature catalytic heat exchange system, and taking the raw material gas as one of raw materials for methanol synthesis to prepare refined methanol. The application realizes full-chain coupling and efficient utilization, combines biomass fermentation, biogas purification and methane steam reforming, and adopts a CO2 circulation technology. The application realizes full-process energy integration: the waste heat in the fermentation process, the waste heat of the PSA resolved gas and the waste water of rectification are utilized to drive the methane steam reforming reaction, the system energy consumption is reduced, and the economic efficiency and sustainability of the system are further improved.

The invention belongs to the technical field of natural gas treatment, and discloses a process and a system for recovering ethane and other light hydrocarbon components from oilfield associated gas. A washing tower is arranged before dehydration, heavy hydrocarbon components in the oilfield associated gas are removed, the influence of the heavy hydrocarbon components on a molecular sieve dehydration device is reduced, the service life of a molecular sieve is prolonged, and a liquid phase separated by a low-temperature separator is cooled by a cold box to be cooled and throttled to enter the top of a demethanizing tower; and the low-temperature freezing blockage influence of the carbon dioxide component on the demethanizer can be well reduced.

A hydrocarbon isomerization system for an iC4 feed stream that provides for removal of C3s from an isomerization reactor feed stream by the addition of a depropanizer column to remove C3s from the reactor effluent stream after it has passed through a stabilizer column. This configuration prevents a buildup of C3s in the system and provides significant savings by reducing the size of the chloride treaters that are used to remove chlorides from off gas, increasing chlorides recovered to the hydrocarbon feed stream for use in combination with the isomerization catalyst. Significant utility savings are provided as well as a reduction in the amount of perchloroethane (PERC) and adsorbent that are required.

The utility model belongs to the technical field of methyl tert-butyl ether cracking, and particularly relates to a device for producing isobutene by cracking methyl tert-butyl ether. The device for producing isobutene by cracking methyl tert-butyl ether comprises an MTBE refining tower, the MTBE refining tower is connected with a cracking reactor, the bottom of the cracking reactor is sequentially connected with a condensate water cooler and a circulating water cooler, the circulating water cooler is connected with an absorption cooling tower, the absorption cooling tower is connected with a compressor inlet buffer tank, and the compressor inlet buffer tank is connected with a compressor outlet buffer tank. The compressor inlet buffer tank is connected with the gas production compressor; and the gas production compressor is connected with the isobutene water washing tower. According to the device for producing isobutene by cracking methyl tert-butyl ether, the condensate water cooler and the circulating water cooler are arranged and are matched with the light component removal tower reboiler, so that the cyclic utilization of heat is realized, and the energy consumption of the device is reduced; meanwhile, the isobutene water washing tower and the methanol water collecting tank are arranged, so that the loss of methanol is reduced, and the purity of an isobutene product is improved.

Provided is a method for upgrading a bio-based material, the method including the steps of pre-treating bio-renewable oil(s) and / or fat(s) to provide a bio-based fresh feed material, hydrotreating the bio-based fresh feed material, followed by separation, to provide a bio-propane composition.

The present invention relates to a method for dehydrating isopropanol to produce propylene, a method for producing propylene from acetone as a raw material including the process, and a related production apparatus. The dehydration method of the present invention includes a step of dehydrating a raw material containing isopropanol in the presence of a dehydration catalyst containing alumina to produce a product containing propylene, wherein the water content of the raw material is 0.1-10.0 wt% (, relative to the total mass of the raw material being 100 wt%), and the content of C3-C4 unsaturated impurities in the product is 30 ppm or less. According to the present invention, the production of undesirable by-products can be significantly suppressed while improving the conversion rate of isopropanol.

The present invention aims to provide a separation apparatus that can relatively improve the purity of ethylene and propylene while relatively reducing the amount of coolant used, as well as a method for separating ethylene and propylene. [Solution] The separation apparatus according to the present invention is a separation apparatus for separating ethylene and propylene from a gas composition containing ethylene, propylene, water and an organic compound, and has a gas-liquid contact region in which the gas composition and a water-absorbing coolant are supplied from opposite directions and brought into countercurrent contact, and has a first separation unit that separates the gas composition into a gas component (A) containing ethylene and propylene and a liquid component (B) containing water, an organic compound and a water-absorbing coolant by countercurrent contact, and has a first return path that returns at least a portion of the liquid component (B) to an intermediate flow region between the upstream end and the downstream end in the flow direction of the water-absorbing coolant in the gas-liquid contact region, and a first cooling unit is interposed in the first return path to cool the returned liquid component (B).

A system including an absorption column configured to receive an acetylene-rich gas stream flowing upwards and a cooled acetylene-lean solvent stream flowing downwards to generate an acetylene-lean gas effluent and an acetylene-rich solvent effluent, one or more heat exchangers for receiving the acetylene-rich solvent effluent, the one or more heat exchangers being configured to transfer heat to the acetylene-rich solvent effluent to generate a heated acetylene-rich solvent stream, and one or more hydrogenation reactors each having one or more catalyst beds, wherein at least a first one of the one or more hydrogenation reactors is configured to convert at least a portion of acetylene in the heated acetylene-rich solvent stream to ethylene in the presence of a first hydrogenation catalyst and hydrogen under first hydrogenation reaction conditions to generate a first hydrogenation effluent including ethylene and a first acetylene-lean solvent effluent.

The invention provides a device and a method for separating olefin and CO2 from product gas for preparing olefin from synthesis gas, the device comprises a first absorption tower, the bottom of the first absorption tower is connected with a first flash tank, and the bottom of the first flash tank is connected with a second flash tank; the upper part of the first absorption tower is connected with a second absorption tower, the bottom of the second absorption tower is connected with a third flash tank, and the bottom of the third flash tank is connected with a fourth flash tank; an absorbent in the first absorption tower comprises an amine aqueous solution; an absorbent in the second absorption tower comprises one of propyl alcohol and N-methyl-2-pyrrolidone or dimethylformamide; and high-content C2-C4 olefins are obtained from upper outlets of the first flash tank, the second flash tank, the third flash tank and the fourth flash tank. According to the method, effective separation of impurity components in the product gas for one-step preparation of olefin from the synthesis gas is realized, the recovery rate of C2-C4 olefin reaches 98.5% or above, and the loss of hydrocarbons in a traditional recovery method is effectively reduced; and automatic production is achieved, and the large-scale industrial production requirement in the chemical industry field is met.

A process, a system, and an apparatus are provided for converting a lower alkane to an alkene. Oxygen and the lower alkane are provided to an ODH reactor to convert at least a portion of the lower alkane to an alkene. An ODH stream comprising the alkene, an oxygenate, steam, and a carbon-based oxide is produced. The bulk of the oxygenate is removed from the ODH outlet stream by non-dilutive cooling, with residual oxygenate being removed using dilutive quenching with a carbonate. Subsequently, separation of the carbon-based oxide from the alkene is achieved using a caustic tower, which also produces spent caustic in the form of a carbonate, which is then used as the carbonate for dilutive quenching. Dilutive quenching using a carbonate allows conversion of the oxygenate to an acetate, which can then be used to simplify separation of the oxygenate from water.

A method for preparing a hydrocarbon stream for oligomerization is provided. The method uses a stripping column to strip dimethyl ether from an olefin stream. Lighter olefins, such as C3-olefins, are also removed. The C4+ olefins can then be sent for further processing, including selective hydrogenation followed by oligomerization.

A method of absorbing a solvent from a gas stream may involve flowing a gas stream comprising air and a hydrocarbon through an absorption column in a countercurrent direction with a first lean absorbent liquid to absorb solvent out of the gas stream and generate a first conditioned gas stream and a first rich absorbent liquid. The method can then involve flowing the first conditioned gas stream through the absorption column in a co-current direction with a second lean absorbent liquid to absorb solvent out of the first conditioned gas stream and generate a second conditioned gas stream having a reduced concentration of the hydrocarbon than the first conditioned gas stream and a second rich absorbent liquid.

The application discloses a kind of light response porous liquid adsorbents and its preparation method and application.Light response porous liquid adsorbents with the mass fraction of 0.2% to 10% of porous main body and macromolecular ionic liquid space steric solvent are prepared after dissolving.Light response metal organic cage is obtained by the coordination self-assembly of isomolar transition metal salt and mixed m-phenylenediamine derivative ligand with photoresponsive azobenzene derivative ligand and long-chain alkyl ligand under the promotion of 2,6-dimethylpyridine.Azobenzene ligand gives the light response of porous liquid, and long-chain alkyl ligand creates a suitable environment for the isomerization of azobenzene, significantly improving the light response efficiency of porous liquid.The number of external pores and the opening and closing of internal pore windows are adjusted under light conditions using light response molecules, the gas adsorption capacity is changed, and the remote control of material on gas adsorption is realized, so that it can be applied to olefin / alkane separation.

A method for dehydrating isopropanol to propylene, comprising a step of producing a propylene-containing product by dehydrating a raw material containing isopropanol in the presence of a dehydration catalyst containing aluminum oxide, wherein the raw material has a water content of 0.1 to 10.0 mass% (the total mass of the raw materials is taken as 100 mass%) and the sum of the content of C2 unsaturated impurities and the content of C3-C4 unsaturated impurities is 80 ppm or less (the total mass of the product is taken as 100 mass%).

The invention discloses an acetylene purification device and an acetylene purification method. The acetylene purification device comprises an absorption mechanism, a first desorption mechanism, a second desorption mechanism, a third desorption mechanism and an adsorption mechanism, the absorption mechanism is internally provided with an absorption cavity used for containing absorption liquid, the absorption mechanism further comprises an acetylene raw material feeding pipe and a cooler used for cooling the absorption liquid in the absorption cavity, and the gas outlet end of the acetylene raw material feeding pipe is inserted into the absorption liquid in the absorption cavity. According to the acetylene purification device disclosed by the invention, an original single desorption tower is divided into three stages of desorption mechanisms, so that not only can 4N-stage acetylene be obtained, but also impurities in the absorption liquid can be removed, the recycling times of the absorption liquid can be prolonged, and the production cost can be reduced. The purification cost is reduced and the purification efficiency is prolonged.

Processes for recovering hydrogen and hydrocarbons from a process stream are described. The processes incorporate a membrane separation unit to reject hydrogen preferentially from the net gas and recover the C3+ hydrocarbons from the hydrogen depleted retentate stream from the membrane unit using a retentate absorber. The invention eliminates the need for a large tail gas compressor package, while still achieving the target C3+ recovery of 85-90% or more with a smaller refrigeration package in the net gas section and membrane and retentate absorber equipment. It does not require any additional compressors, resulting in a significant reduction in plot space and power consumption.

The present application relates to a new method for preparing methane, a method for preparing methane from H2S and CO2 mixed gas, a metal modified molecular sieve is placed in the reaction cavity of a wire cylinder type reactor, nitrogen is introduced to remove air in the reactor, then H2S and CO2 mixed gas is introduced, a plasma power connected with a high voltage electrode and a grounding electrode is turned on, the reaction gas is purified by a low temperature methanol washing method, pure CH4 gas is obtained, and the washed H2S and CO2 gas is returned to the raw gas for reaction. The present application also relates to a wire cylinder type reactor, i.e. a reaction device, used in the method for preparing methane from H2S and CO2 mixed gas.

The present invention relates to a process for recycling a solid rubber-based material, a recycling unit for carrying out said process. The present invention further relates to a process a process for manufacturing a solid rubber-based material, preferably a tire, using a product obtainable or obtained by the aforementioned process and a recycling process for preparing a pyrolysis oil from a solid rubber-based material obtained from the aforementioned process.

The utility model discloses acetylene gas pickling equipment which comprises a bottom plate, a pickling tank arranged on one side of the top end of the bottom plate through a support, a gas inlet / outlet formed in one side of the top end of the pickling tank, a first water pump mounted at the top end of the bottom plate on one side of the pickling tank, and a filter box mounted at the top end of the bottom plate on one side of the first water pump. A second water pump is mounted at the top end of the bottom plate on one side of the filter box, a cooling box is arranged at the top end of the bottom plate on one side, far away from the filter box, of the second water pump, a snakelike cooling pipe is mounted in the cooling box, and one end of the snakelike cooling pipe extends out of the cooling box and is provided with a liquid outlet pipe fitting; the other end of the S-shaped cooling pipe extends out of the cooling box and is provided with a liquid inlet pipe fitting, and a fan is installed on the outer wall of one side of the cooling box. According to the acetylene gas pickling device, waste of acid liquor is effectively reduced, the production cost is reduced, meanwhile, environmental protection is facilitated, the acetylene gas pickling effect is guaranteed when the pickling device is used, and the convenience of the pickling device is improved when the pickling device is used.

The invention relates to a process for separating butenes from C4-hydrocarbon streams containing butanes as well as butenes by means of extractive distillation with a suitable solvent. The process according to the invention is characterized in that in the inlet region of at least one packed bed of the absorber there are packing elements of lower specific surface area than in the rest of the packed bed.