143 results about "Isobutane" patented technology

The utility model relates to an energy-saving production device for preparing methyl tert-butyl ether by an isobutane dehydrogenation method. A raw material gasifier is arranged between the catalytic distillation tower feeding and discharging heat exchanger and the catalytic distillation tower, a temperature sensor is arranged on a feeding pipeline from the raw material gasifier to the catalytic distillation tower, a gas phase at the top of the catalytic distillation tower is divided into two pipelines, a compressor is additionally arranged on one pipeline, and an automatic flow regulating valve is additionally arranged on the other pipeline; a cold-side material outlet of the distillation tower feeding and discharging heat exchanger is connected with a cold-side material inlet of the raw material gasifier, a cold-side material outlet of the raw material gasifier is connected with a feeding hole in the middle lower part of the catalytic distillation tower, and a tower top discharging pipeline of the catalytic distillation tower is respectively connected with an inlet of the compressor and a hot-side material inlet of the condenser; an outlet pipeline of the compressor is connected with a hot measuring material inlet of the raw material gasifier, and a hot measuring material outlet of the raw material gasifier is connected with a liquid inlet of the return tank. According to the utility model, a heat pump technology is adopted, so that the heating power of the tower kettle reboiler is reduced, and the steam consumption is reduced; and the method is more economical.

A method for forming an extruded polystyrene foam comprises: (a) providing a thermoplastic melt and a blowing agent in the melt, the blowing agent comprising: (1) from about 10% to about 50% by weight of HCFO-1233zd (E); (2) from about 35% by weight to about 75% by weight of HFC-134a; (3) from about 10% to about 30% by weight of isobutane; and (4) optionally up to about 15% by weight of dimethyl ether; and (b) foaming the thermoplastic material.

The utility model provides a system for separating n-butane and iso-butane through differential pressure thermal coupling rectification, which comprises an iso-butane separation tower A, an iso-butane separation tower B, a tower A reflux tank, a tower B reflux tank, a tower A condenser, a cooler or heater, a tower A reboiler, a tower B reboiler, a tower A reflux pump and a tower B reflux pump, the tower A condenser, the tower A reflux tank and the tower A reflux pump are sequentially arranged on a tower top material pipeline of the isobutane separation tower A, the tower A reboiler is arranged at the tower bottom of the isobutane separation tower A, and the tower B reboiler is arranged at the tower bottom of the isobutane separation tower B. According to the system, an isobutane separation tower A serves as a low-temperature low-pressure tower, an isobutane separation tower B serves as a high-temperature high-pressure tower, condensation heat at the tower top of the isobutane separation tower B serves as a heat source of a reboiler at the tower bottom of the isobutane separation tower A, and the isobutane separation tower A and the isobutane separation tower B are thermally coupled; the steam consumption of the isobutane separation tower A is reduced, the refrigerant consumption at the tower top of the isobutane separation tower B is reduced, and the energy consumption is reduced.

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 present invention provides a blowing agent for producing extruded polystyrene foam having low lambda over time and low foam density. [Solution] The foaming agent comprises (a) a first co-foaming agent consisting of (a) about 50% to about 70% by weight of HFO and / or HFCO having three or four carbon atoms, (b) about 2% to about 15% by weight of methyl formate, (c) a second co-foaming agent consisting of about 20% to about 30% by weight of dimethyl ether, isobutane and combinations thereof, and (d) a third co-foaming agent consisting of about 2% to about 25% by weight of carbon dioxide, acetone and combinations thereof.

Systems and methods for processing a C3 and C4 hydrocarbon mixture have been disclosed. The C3 and C4 hydrocarbon mixture is first processed in an isomerization unit to isomerize n-butane to form isobutane. The resulting effluent stream from the isomerization unit comprising primarily isobutane and C3 hydrocarbons, collectively, is flowed into a separation unit configured to separate the effluent stream to form a C3 stream comprising C1 to C3 hydrocarbons and a C4 stream comprising primarily isobutane. The isobutane in the C4 stream is further dehydrogenated to form isobutene, which is further flowed into an MTBE synthesis unit as a feedstock for producing MTBE.

This invention discloses a method for the efficient conversion of isoparaffins, comprising the following steps: contacting a raw material containing isoparaffins and hydrogen with a catalyst in a reactor, reacting to obtain a product containing small molecule alkanes; wherein the isoparaffins are selected from at least one of isobutane, isopentane, neopentane, isohexane, and 3-methylpentane; wherein the small molecule alkanes are selected from at least one of ethane, propane, and n-butane; the catalyst is obtained by the following steps: mixing a metal acidic functional component, a metal basic functional component, a matrix precursor, a phosphorus auxiliary component precursor, a molding aid, and water, kneading, molding, and vacuum drying to obtain the catalyst.

The application discloses a method for producing ethylene raw material. The method comprises the following steps: mixing hydrocracking light naphtha and hydrogen into a first hydroconversion reaction zone to react, and then the reaction effluent enters a separation system to obtain hydrogen-rich gas and a first hydroconversion product; the first hydroconversion product is separated to obtain ethane, propane, isobutane, isopentane and n-pentane; the isobutane is mixed with hydrogen into a second hydroconversion reaction zone, and the reaction effluent is separated to obtain n-butane; the second hydroconversion reaction zone is filled with a hydroconversion catalyst containing ZSM-35 molecular sieve; and the isopentane is recycled to the inlet of the first hydroconversion reaction zone. The first hydroconversion reaction zone is filled with a hydroconversion catalyst containing mordenite, and at least two catalyst beds are filled; and the active metal content of the hydroconversion catalyst decreases in turn along the flow direction. The method can effectively improve the proportion of normal alkanes in the product and improve the quality of the ethylene raw material.

Ethylene, alpha olefins, and other olefinically unsaturated monomers may be polymerized under fluidized bed polymerization reaction conditions in the presence of a Ziegler-Natta catalyst. A recycle stream featuring an induced condensing agent (ICA) comprising isobutane may increase catalyst productivity while maintaining quality of the polymer product, particularly when the recycle stream is delivered to a reactor containing the fluidized bed under conditions suitable to form a condensed or super-condensed mode in the recycle stream. The recycle stream may comprise unreacted olefinic monomers, and isobutane or a mixture of isobutane and isopentane.

This invention relates to the field of chemical equipment technology, and more particularly to a propane-isobutane mixed dehydrogenation device and its usage method. The propane-isobutane mixed dehydrogenation device includes a tank body, within which are coaxial inner and outer ring plates that allow the passage of reactant gases; a disc that seals the top openings of the inner and outer ring plates; an annular lifting disc that slides against the inner and outer ring plates; and a drive mechanism for raising and lowering the lifting disc. The inner and outer ring plates, the disc, and the lifting disc together form a catalyst chamber. A catalyst inlet is located on the disc. An electric valve and a sealed discharge pipe penetrating the bottom of the tank are located at the bottom of the lifting disc. An inlet pipe, sealed and connected to the inner ring plate, is located at the bottom of the tank. An outlet pipe is located above the side wall of the tank. The propane-isobutane mixed dehydrogenation device provided by this invention has low production and manufacturing costs, is less prone to catalyst particle damage during catalyst bed filling, and exhibits high catalyst bed filling uniformity.

The invention provides a Co-based molecular sieve isobutane dehydrogenation catalyst and a preparation method and application thereof. The preparation method comprises the following steps: mixing a cobalt source, a silicon source, a template agent and an alkali source, and carrying out ball milling treatment to obtain a solid mixture; and crystallizing and roasting the solid mixture to obtain the Co-based molecular sieve isobutane dehydrogenation catalyst. The ball milling treatment is that the ball milling is paused for 10-30 minutes every 20-40 minutes, and the time of the whole ball milling treatment process is 0.5-5 hours; the rotating speed of the ball milling treatment is 500-1000 r / min; the molar ratio of cobalt in the cobalt source to silicon in the silicon source to the template agent to the alkali source is (0.0001-0.002): 1: (0.1-1): (0.01-0.1). The Co-based molecular sieve isobutane dehydrogenation catalyst has high activity in an isobutane dehydrogenation reaction, still has high stability after the reaction for a period of time, is uniform in Co component dispersion, and has a good industrial application prospect.

A process for the purification of isobutene from a C4 stream with at least 1-butene, 2-butene, isobutane and isobutene includes isomerizing 1-butene from a stream of material which is concentrated in isobutane and isobutene obtained from the C4 stream into 2-butene, using a catalyst in an isomerization reactor; supplying a product stream from the isomerization reactor to a rectification column; and providing a stream of material which is concentrated in isobutene. A processing facility is utilized for the purification of isobutene from the C4 stream.

The utility model relates to the technical field of petrochemical engineering, and discloses a pressure relief pipeline device for reducing the operating pressure of a deisobutanizer, which comprises a deisobutanizer return tank and a compressor liquid separation tank, and further comprises a tank body internally provided with a mounting area; the bearing frame is arranged on the inner side of the tank body and located in the mounting area of the tank body; the spiral cooling component is arranged on the bearing frame and located in the mounting area of the tank body, a feeding pipe is further arranged on the spiral cooling component, the other end of the feeding pipe is communicated with the deisobutanizer return tank, and an isobutane gas-liquid mixture output by the deisobutanizer return tank can enter the spiral cooling component through the feeding pipe and is cooled through the spiral cooling component. And gaseous isobutane is converted into liquid isobutane under the cooling action of the spiral cooling component. The pressure relief pipeline device for reducing the operating pressure of the deisobutanizer aims at solving the problems that a deisobutanizer in an existing alkylation device is too high in operating pressure, large in energy consumption and limited in flexibility.

The invention relates to the technical field of gas turbine waste heat utilization, and discloses a waste heat utilization power generation device and method applied to a pure condensing peak shaving gas turbine. The device comprises a closed loop taking isobutane as a cycle working medium, a waste heat-organic working medium heat exchanger, an isobutane turbine generator set, a condensation backflow part and a control system. After the gas turbine is shut down, heat storage steam or hot water is led out from the waste heat boiler steam-water system, heat energy is transmitted to isobutane through the heat exchanger, the isobutane is evaporated into superheated steam and drives the turbine generator set to generate electricity, and working media after acting are pumped into the heat exchanger again through the condensation backflow part to complete circulation. Isobutane is adopted as a working medium, the system adapts to medium and low temperature and transient heat source characteristics, stable grid connection is achieved through the clutch transmission mechanism, the control system dynamically adjusts operation parameters, the problem that heat stored in the waste heat boiler cannot be recycled after the pure condensing peak shaving gas turbine stops is effectively solved, and the energy utilization efficiency and the power plant economy are remarkably improved.

The invention provides a method and a system for producing aromatic hydrocarbon and olefin from diesel oil and application of the method and the system. According to the technical scheme, the method comprises the following steps: carrying out hydrocracking reaction on diesel oil to obtain a high-boiling-range light aromatic hydrocarbon material flow and a low-boiling-range light alkane material flow, wherein the n-butane content in the low-boiling-range light alkane is greater than the isobutane content; the high-boiling-range light aromatic hydrocarbon material flow is fed into an aromatic hydrocarbon combination device, after separation, benzene and toluene-containing fractions enter an extraction unit, C8 aromatic hydrocarbon is extracted as a product, toluene, C9 aromatic hydrocarbon and fractions obtained through separation enter a toluene disproportionation and transalkylation unit, and benzene and C8 aromatic hydrocarbon are produced to the maximum extent; the light alkane material flow is fed into an olefin device, so that olefin such as ethylene and propylene can be produced to the maximum extent. According to the technical scheme, the purpose of efficiently producing aromatic hydrocarbon and olefin from diesel oil is achieved, the diesel oil conversion efficiency is high, the aromatic hydrocarbon conversion selectivity is high, and the olefin yield is high.

The utility model discloses a pressure detection device for an isobutane / n-butane raw material storage tank. The pressure detection device comprises a pressure detection unit, a signal processing module, a central control module, a display module, an alarm module and a protection module. The pressure detection unit adopts a main / standby piezoresistive pressure sensor and is installed at the top of the storage tank through a sealing joint, and an independent shielding signal line is sleeved with a metal corrugated pipe to prevent electromagnetic interference and mechanical damage. The signal processing module integrates signal amplification, filtering and analog-to-digital conversion functions and transmits processed data to the central control module. A microcontroller is arranged in the central control module, a pressure threshold value is preset, the main sensor and the standby sensor can be automatically switched, and encrypted data can be stored. The display module displays a pressure value and a curve in real time, and the alarm module realizes multi-level early warning through sound-light alarm and short message notification. Through double-sensor redundancy design, signal anti-interference processing, intelligent fault switching and multiple alarm mechanisms, the precision, stability and safety of pressure detection are remarkably improved.

A working medium for a heat cycle includes trifluoroethylene, a low boiling point compound having a lower boiling point than the boiling point of the trifluoroethylene, and high boiling point compounds having higher boiling points than the boiling point of the trifluoroethylene. In the working medium, the low boiling point compound is at least one selected from the group consisting of carbon dioxide, R116, and R41, and the high boiling point compounds are at least two selected from the group consisting of HFC-32, HFO-1234yf, HFO-1234ze (E), HFO-1243zf, PFC-14, HFC-134, HFC-143a, HFC-227ea, cyclopropane, isobutene, isobutane, dimethyl ether, and ammonia. An application of the working medium is provided.

The invention discloses a drying control method of a clothes dryer and the clothes dryer, and belongs to the technical field of clothes dryers. The drying control method of the clothes dryer comprises the steps that the temperature of air in a clothes drying cylinder of the clothes dryer is monitored, and the humidity of air obtained after condensation and dehumidification in the internal circulation process is monitored; when the air temperature is smaller than T1 and the air humidity is larger than R1, the working medium proportion of a compressor in the clothes dryer is set as follows: propylene: isobutane = (55-60): (40-45); when the air temperature is T2-T3 and the air humidity is R2-R3, the working medium proportion of a compressor in the clothes dryer is set as that propylene: isobutane = (40-45): (55-60); and when the air temperature is T4-T5 and the air humidity is R4-R5, the humidity decreasing rate, the temperature increasing rate and the drying time for the air humidity to reach R6 are calculated, the clothes type is recognized, the working medium proportion of a compressor in the clothes dryer is adjusted according to the clothes type, and the clothes drying effect and efficiency can be improved.

This application discloses a method for the conversion of C4-C6 alkanes. In a reactor, a raw material containing hydrogen and C4-C6 alkanes is contacted with a catalyst and reacted to obtain a product containing small molecule hydrocarbons; the C4-C6 alkanes are selected from at least one of n-butane, isobutane, n-pentane, isopentane, and 2,3-dimethylbutane; the small molecule hydrocarbons are selected from at least one of ethane, propane, n-butane, and n-pentane; the catalyst is prepared by the following steps: (1) mixing clay and sol, spray drying to obtain microspheres with a diameter of 1-50 μm; (2) immersing the microspheres in an aqueous solution containing a noble metal precursor, drying I, calcining I, and treating with a hydrogen atmosphere to obtain a catalyst precursor; (3) mixing the catalyst precursor, molecular sieve, and additives, rolling to form spheres, drying II, calcining II, and reducing to obtain the catalyst.

The utility model relates to the technical field of petroleum chemical industry discloses a double loop pipe polyethylene device, including reactor, the top transverse fixedly connected with support of reactor, the top fixedly connected with mixing mechanism of support. In the utility model, through the setting of driving motor, rotating lever and stirring rod, isopropanol can be injected into the inside of reactor and isobutane is mutually soluble, driving motor works when starting at this moment, driving motor work drives rotating lever to rotate clockwise, rotating lever rotation drives stirring rod to rotate, and stirring rod rotation pushes material flow, diffusion to the kinetic energy of isopropanol fluid in the inside of reactor, and the shear force produced by stirring can break the concentration gradient and phase interface in the inside of material, promotes the diffusion mixing of molecular level to accelerate the uniform mixing of both, makes fresh isobutane more efficiently dilutes isopropanol, shortens the time of replacement to qualified concentration, reduces the time -consuming of circulating replacement in traditional craft.

The present invention relates to antiperspirant and deodorant compositions for correction of body odour, and more particularly relates to antiperspirant and deodorant compositions for human hygiene. The disclosed anti-perspirant and deodorant composition comprises isobutane, propane, butane, cyclopentasiloxane, caprylic / capric triglyceride, stearalkonium hectorite, propylene carbonate, c12-15 alkyl benzoate, parfum, silver lactate, lactic acid, aqua, zea mays starch, menthyl ethylamido oxalate, argania spinosa kernel oil. Furthermore, the active antimicrobial silver ingredient is dermatologically tested and is capable of diminishing odor-causing bacteria in addition to prevention of irritation and itching.

The application discloses a method for normalizing isomeric alkanes, which comprises the following steps: contacting isomeric alkanes and hydrogen with a catalyst in a reactor to obtain normal alkanes; the isomeric alkanes are selected from at least one of isobutane and isopentane; the catalyst is composed of an acidic carrier, a noble metal active component supported on the surface of the acidic carrier and an auxiliary element; the noble metal active component is selected from at least one of Pt and Pd; the auxiliary element is selected from at least one of Ce, Sn, La, Fe, Co, Ni and Cu; and the carrier is selected from at least one of molecular sieve, Al2O3 modified SO4 2‑ -WO3-ZrO2; the mass ratio of the noble metal active component to the acidic carrier in the catalyst is 0.0001-0.01:1; and the mass ratio of the auxiliary element to the acidic carrier is 0.0001-0.008:1.

The invention relates to the technical field of chemical energy conservation, in particular to an alkylate rectification system and method.The system comprises a deisobutanizer and an n-butanizer, a tower top outlet of the deisobutanizer is connected with an isobutane extraction pipeline, a tower bottom outlet of the deisobutanizer is connected with the upper middle section of the n-butanizer, and a tower bottom outlet of the n-butanizer is connected with the lower middle section of the n-butanizer. A tower bottom outlet of the n-butane removal tower is connected with an alkylate oil extraction pipeline; a tower top outlet of the n-butane removal tower is connected with an inlet of the compressor, a heat source inlet of the first multi-stage heat supplier at the middle and lower sections of the isobutane removal tower is connected with an outlet of the compressor, a heat source outlet of the first multi-stage heat supplier is connected with an inlet of the pressure release valve, and an outlet of the pressure release valve is respectively connected with a tower top inlet of the n-butane removal tower and an n-butane extraction pipeline. The steam at the top of the n-butane removal tower is recompressed to be used for heat supply of the isobutane removal tower, low-grade energy can be converted into high-grade energy, heat distribution in the isobutane removal tower is optimized, consumption of the high-grade energy is reduced, and energy saving is achieved.

The systems and processes described can be used to produce a high-purity isobutane stream and a high-purity 1-butene stream from mixed C4 streams having disparate starting compositions.

The invention relates to the technical field of isobutene production, in particular to a reactor system and a process method for preparing isobutene from 2-chloroisobutane. The surface modification treatment of the reactor comprises the following steps: S1, surface pretreatment; s2, carrying out surface oxidation treatment to generate an active oxide layer: calcining the reactor at 500-700 DEG C to generate an oxide layer on the surface of the reactor; s3, active component loading: dipping a reactor in Al2O3 sol, then calcining at 400-600 DEG C to form a porous Al2O3 layer, dipping the reactor in a nickel nitrate solution, freeze-drying, and then reducing in H2 or Ar atmosphere at 400-600 DEG C to form Ni nanoparticles; and the reactor is made of hastelloy. The reactor is subjected to surface modification, so that high 2-chloroisobutane conversion rate and isobutene selectivity are ensured, the equipment maintenance cost is reduced, and the problem of coking of the reactor is avoided.

The application belongs to the technical field of high-temperature wind tunnel combustion heater, and discloses an ignition starting device and method of high-total-temperature air liquid oxygen isobutane combustion heater. The ignition starting device comprises an isobutane supply system, an air supply system, a liquid oxygen supply system, an air-oxygen mixer, a combustion heater and key measurement points. The ignition starting method comprises a preparation stage, a combustion heater precooling stage and a combustion heater working stage. The ignition starting device and method of high-total-temperature air liquid oxygen isobutane combustion heater realize stable ignition starting and reliable thermal protection of the high-total-temperature working combustion heater by monitoring key point information in real time and designing valve opening sequence according to physical operation logic, and have engineering practical value.

This invention relates to the field of desulfurization and refining technology for light alkanes, and discloses a method for liquid-phase desulfurization of isobutane. This invention employs a transition metal-modified molecular sieve and a specialized liquid-phase desulfurization adsorbent that encapsulates hydrogen / hydrogen protons. Under liquid-phase conditions of 1.6-1.8 MPa and 30-40℃, various sulfides in isobutane are removed. The method operates through a dual-bed series switching mode, switching the bed sequence and replacing / regenerating the adsorbent when the total sulfur at the bed outlet is ≥0.3 ppm. For higher desulfurization precision requirements, it is preferable to switch the bed sequence earlier when the total sulfur at the bed outlet is ≥0.2 ppm, and more preferably ≥0.1 ppm. This invention can stably reduce the total sulfur in isobutane to below 0.3 ppm, preferably controlled to ≤0.2 ppm, and more preferably controlled to ≤0.1 ppm. It exhibits high adsorbent utilization and is suitable for continuous industrial production.

The invention relates to SBA-15 and SBA-16 controllable acidity molecular sieves and a preparation method thereof, a catalyst and an isobutane normalizing method, and belongs to the technical field of catalyst preparation. The preparation method of the molecular sieve comprises the following steps: mixing a silicon source, water, an organic template agent, salt of metal M and an acid solution, carrying out hydrothermal crystallization, carrying out solid-liquid separation on a crystallized product, and roasting a solid phase to obtain the molecular sieve. A surface active agent (an organic template agent) is adsorbed on the surface of layered silicate by utilizing a layered structure of the layered silicate, and after an outer layer is occupied by the surface active agent, metal and silicate of the inner layer act and are grafted to the inner layer of the layered silicate, so that loss of the metal of the outer layer is avoided; the acidity of the catalyst can be adjusted by adjusting the content of the metal. In the reaction process, an alkaline solution can be added on line, the outer layer material is dissolved, the second layer of layered material is exposed, and the reaction is circulated until the catalyst is completely inactivated, so that the service life of the catalyst is greatly prolonged.

The invention relates to the technical field of chemical rectification control, and discloses a multi-parameter cooperative control method and system of an isobutane rectification system. The method comprises the following steps: acquiring real-time operation data of a rectification system, wherein the real-time operation data comprises tower kettle temperature, reflux ratio, feeding amount and pressure; constructing a parameter relation model, and describing a mutual influence relation among the plurality of parameters based on historical data; selecting a corresponding cooperative control strategy according to preset control requirements including a product purity target and an energy consumption constraint; a to-be-adjusted parameter set is marked in the cooperative control strategy, and a parameter combination needing to be modified is determined; and finally, constructing a verification model, obtaining an optimized cooperative control strategy after the adjustment of the to-be-adjusted parameter set is completed, verifying each control node in the optimized cooperative control strategy based on the verification model, defining the control node which does not pass the verification as an abnormal node, and generating a risk prompt pointing to the abnormal node. The method assists an isobutane rectification system to better meet production requirements.

The invention discloses a method for synthesizing a hierarchical pore MFI molecular sieve membrane based on a sacrificial crystal seed layer, and belongs to the field of zeolite molecular sieve membrane synthesis. The hierarchical pore MFI molecular sieve membrane with a compact selective top layer and a macroporous transition layer with high porosity is successfully constructed on a porous carrier through a surface wet gel secondary growth technology of a sacrificial crystal seed layer. The film layer structure and the gas separation performance are optimized by regulating and controlling the composition, the aging time and the crystallization time of the synthetic gel. The prepared hierarchical pore MFI molecular sieve membrane shows high permeability and excellent selectivity in n-butane / iso-butane separation, and the preparation process is good in repeatability, high in stability and suitable for industrial gas separation application.