224results about "Absorption purification/separation" patented technology

A system for generating methane includes a scrubber, a stripper, a vacuum pump, a water separator, and a Sabatier reactor. The scrubber is configured to absorb one or more contaminants from an air stream into a liquid sorbent, in which the one or more contaminants include carbon dioxide. The stripper is configured to desorb the one or more contaminants from the liquid sorbent. The vacuum pump is configured to pressurize the desorbed contaminants to a reaction pressure of the carbon dioxide. The water separator is configured to remove water from the pressurized, desorbed contaminants. The Sabatier reactor is configured to generate the methane from the carbon dioxide of the pressurized, desorbed contaminants.

A process for operating a biorefinery plant (10) comprises at least the following processes: a biogas upgrading process (18) in which a biogas mixture (16) is split into a biomethane part (22) and a carbon dioxide part (24); a biomethane cracking process (26) in which the biomethane part (22) is split into a carbon part (34) and a hydrogen part (36); and a biomethanol synthesis process (38) in which biomethanol (40) and water (42) are produced on the basis of the hydrogen part (36) and the carbon dioxide part (24).

The invention relates to the technical field of waste gas treatment, and particularly discloses a method and system for recycling xylene in high-concentration xylene waste gas, the system comprises a precooler, an absorption system, a regeneration system and a receiving tank, the absorption system is composed of an absorption tower, a heat exchanger and a recooler, the precooler is connected with a lower inlet pipeline of the absorption tower, and the absorption tower is connected with a lower outlet pipeline of the heat exchanger; a booster fan is arranged in a pipeline connecting the precooler and the absorption tower, a bottom outlet of the absorption tower is connected with a first inlet pipeline of the heat exchanger, and a rich liquid pump is arranged on a pipeline connecting the absorption tower and the heat exchanger; the regeneration system comprises a regeneration tower, a condenser, a vacuum buffer tank, a vacuum pump tail cooler and a vacuum pump tail gas recooler. According to the invention, the high-concentration xylene waste gas can be stably and continuously treated, xylene in the xylene waste gas can be efficiently recovered, the quality of the recovered product is ensured, the absorbent can be recycled, the absorbent does not need to be replaced during treatment work, the production cost is saved, and the production efficiency is improved.

The invention discloses a butadiene washing system, and relates to the technical field of butadiene washing, the butadiene washing system comprises: a fixing frame arranged on the ground; the treatment tank is fixedly mounted on the inner wall of the fixing frame; the air inlet pipe is communicated with the treatment tank; the flow guide frame is fixedly mounted on the inner wall of the fixing frame; the L-shaped pipe is fixedly mounted on the surface of the air inlet pipe; the protective umbrella is fixedly mounted at the bottom of the L-shaped pipe; one end of the water circulation device is fixedly installed on the outer wall of the fixing frame, the other end of the water circulation device is fixedly installed at the bottom of the flow guide frame, and the water circulation device is used for purifying and recycling a solution obtained after water washing; and the connecting pipe is fixedly installed on the surface of the water circulation device, the spraying range can be widened through rotation of the rotary spraying pipe, the spraying effect is improved, and the purity and quality of butadiene are improved.

Processes and apparatuses for separating carbon monoxide from ethylene. The ethylene may be produced from biobased alcohol. The separation utilizes a fractionation column which produces a carbon monoxide depleted ethylene stream and an overhead stream comprising carbon monoxide and ethylene. The ethylene from the overhead stream may be recovered in an absorption zone with an absorbing liquid. A oxygenate fractionation zone may be utilized to remove oxygenates from the carbon monoxide depleted ethylene stream.

The invention provides a method for preparing allyl acetate and recovering propylene and propane, which comprises the following steps: introducing a gas raw material into a reactor for reaction, pumping out gas in the material from the top of a first absorption tower by using a first compressor to serve as a recycle gas flow, conveying one part of the recycle gas flow into the reactor, and conveying the other part of the recycle gas flow into a second absorption tower; and conveying a part of the exhaust gas flow to the bottom of the second absorption tower, discharging the rest of the exhaust gas flow, and sequentially discharging liquid in the material into a crude product storage tank and a rectifying tower from the bottom of the first absorption tower, and condensing a part of an extracted material flow entering the gas-liquid separation tank from the top of the rectifying tower, introducing the condensed material flow into the top of the second absorption tower as a first absorption liquid to obtain a rich solution, discharging the rich solution into a crude product storage tank, and pumping gas flashed from the crude product storage tank back to the bottom of the first absorption tower. The method provided by the invention is beneficial to reducing the production cost, improving the selectivity of the target product and reducing the carbon dioxide emission of the system.

The invention discloses a method and a system for separating low-carbon hydrocarbons. The method comprises the following steps: cooling synthesis gas, introducing the cooled synthesis gas into a low-temperature methanol tower, and carrying out low-temperature methanol washing to separate gas-phase CO and H2 and a liquid-phase low-temperature methanol base solution; the liquid-phase low-temperature methanol base solution enters an evaporation tower to be separated to obtain gas-phase low-carbon hydrocarbons, carbon dioxide and liquid-phase low-temperature methanol; gas-phase low-carbon hydrocarbons and carbon dioxide enter a carbon dioxide absorption tower, carbon dioxide is absorbed by adopting an alcohol amine solution, the gas phase is low-carbon hydrocarbons, and the liquid phase is carbon dioxide-rich absorption liquid. According to the invention, the recovery rates of CO and H2 reach 96.40% and 99.28%, which are far higher than those of the existing PSA technology. Meanwhile, the absorption efficiency of CO2 reaches 99.95%; except that the ethylene absorption efficiency is 0.7357 * 100 which is equal to 73.57%, the absorption efficiency of other low-carbon hydrocarbons (C2, C3 and C4 olefin alkanes) is greater than 99% and even reaches 100%.

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 invention provides a method for preparing allyl acetate and recovering propylene, which comprises the following steps: gas raw materials are introduced into a reactor for reaction to generate allyl acetate, and the gas raw materials comprise propylene, acetic acid, oxygen and inert gas; condensing the material discharged from the bottom of the reactor by using a condenser, so that the condensed material is discharged into the bottom in the absorption tower; pumping gas in the material back into the reactor from the top of the absorption tower by using a first compressor, and discharging liquid in the material into a crude product storage tank from the bottom of the absorption tower; pumping gas in the material back to the bottom in the absorption tower from the crude product storage tank by using a second compressor, and discharging liquid in the material from the crude product storage tank into a downstream rectifying tower for separation; gas separated by a gas-liquid separation tank communicated with the top of the rectifying tower is introduced into a crude product storage tank, and the second compressor also pumps gas recovered from the gas-liquid separation tank into the crude product storage tank. The method provided by the invention is beneficial to improving the raw material utilization rate so as to reduce the production cost.

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.

Provided are a process and a system for treating both a high-pressure (HP) and a low-pressure (LP) acid gas-containing gas streams. The system includes a HP absorber unit, a flash drum coupled downstream of the HP absorber unit, and a LP absorber unit coupled downstream of the flash drum. The process includes introducing a HP rich amine solution from a HP absorber unit into a flash drum, operating the flash drum such that a flashed sour gas and a flash drum rich amine solution are produced, and introducing the flashed sour gas and the LP acid gas-containing gas stream into a LP absorber unit.

Processes and apparatuses for separating carbon monoxide from ethylene. The ethylene may be produced from biobased alcohol. The separation utilizes a fractionation column which produces a carbon monoxide depleted ethylene steam and an overhead steam comprising carbon monoxide and ethylene. The ethylene from the overhead steam may be recovered in an absorption zone with an absorbing liquid. A oxygenate fractionation zone may be utilized to remove oxygenates from the carbon monoxide depleted ethylene stream.

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 provides a method and a device for recovering ethylene in ethylene gas containing seal oil, relating to the technical field of ethylene recovery. In the present invention, ethylene glycol diacetate is used as a solvent to absorb ethylene in the ethylene gas containing seal oil, and the obtained ethylene-rich liquid is analyzed, so as to realize the efficient separation and recovery of ethylene. The recovery rate of ethylene is high, and the recovered ethylene can be directly used in the production of vinyl acetate by the ethylene method, greatly reducing the consumption of ethylene raw materials in the process of producing vinyl acetate by the ethylene method. Moreover, ethylene glycol diacetate is produced as a by-product in the process of producing vinyl acetate by the ethylene method. In the present invention, ethylene glycol diacetate (EGDA) is used as a solvent, and no new impurities are introduced.

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).

Provided is a method for recovering a conjugated diene-based monomer including: supplying a feed stream including a conjugated diene-based monomer to a condensation part and performing condensation to obtain a stream including a condensed conjugated diene-based monomer and a stream including an uncondensed conjugated diene-based monomer; recovering a conjugated diene-based monomer from the stream including a condensed conjugated diene-based monomer, and supplying the stream including an uncondensed conjugated diene-based monomer to a first absorption tower and bringing it into contact with a sorbent to obtain an absorbed solution in which the conjugated diene-based monomer is absorbed into the sorbent; and supplying the absorbed solution to a stripping column to separate the absorbed solution into the sorbent and the conjugated diene-based monomer, circulating a lower discharge stream from the stripping column including the separated sorbent to the first absorption tower, and circulating an upper discharge stream from the stripping column including the separated conjugated diene-based monomer to the condensation part.

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.