150results about How to "Avoid flying temperature" patented technology

The invention belongs to the technical field of chemical material preparing methods, and particularly relates to a method for preparing ethylene through liquid-phase selective hydrogenation of acetylene in a slurry reactor. A liquid-phase solvent with high selective solubility for acetylene and low selective solubility for ethylene is introduced into a gas-solid catalytic system, and the relative solubility coefficient of the solvent is larger than 8; a catalyst is dispersed evenly in the liquid-phase solvent, and process coupling is achieved through the high selective solubility of the liquid-phase solvent for acetylene, so that the selectivity of ethylene is improved; and ethylene is prepared and separated through an hydrogenation reaction of acetylene. According to the method, the concentration of ethylene on the surface of the catalyst is reduced through the process coupling, therefore a path of ethane generation through deep hydrogenation is blocked to a certain extent, and the selectivity of ethylene can be improved remarkably. Simultaneously, the liquid-phase dilution thermal effect can accelerate heat transfer in the slurry reactor, and temperature runaway is avoided. The method is not only used for preparing ethylene from acetylene obtained from natural gas pyrolysis, but also is an efficient method in a process for removing acetylene in ethylene.

The invention relates to the technical field of the design of chemical reactors and discloses a novel high-throughput micro-channel reactor provided with multiple layers of spirally winding tubes. The reactor mainly comprises reactant inlet and outlet sections, inlet and outlet glands, flanges, inlet and outlet tube plates, stainless steel capillary tubes, a fixed pad strip, a drum, a winding drum, constant-temperature medium inlet and outlet sections, baffles, left and right supports, a central support tube and a support piece, wherein two ends of the central support tube are connected with the inlet and outlet tube plates, and the winding drum and the central support tube are located on a same axis and welded and connected through the support piece; the stainless steel capillary tubes spirally wind around the winding drum in a multi-layer manner, spiral directions of adjacent winding layers are opposite, multiple reaction tube bundles which take the winding drum as the circle center and have different circle diameters are formed, and two ends of each stainless steel capillary tube are connected onto the inlet and outlet tube plates respectively; the inlet and outlet glands are connected with the inlet and outlet tube plates respectively through the flanges. The reactor has the advantages of high throughput, high heat transfer capacity, high synthetic rate, safety, high efficiency, low machining cost, capability of realizing continuous production, easiness in parallel enlargement and the like.

The invention provides macro-porous aluminum oxide. The average diameter of holes is the diameter of a most probable hole; the size of the holes is 1.1-3.5 ml/g; and the specific surface area is 150-450 m<2>/g. The aluminum oxide is prepared by a two-section ageing method; the first section of ageing comprises the following steps of: adding an alkaline compound or an acidic compound into an aluminum hydroxide suspension solution to adjust the pH (Potential of Hydrogen) value of the suspension solution and then ageing; and the second section of ageing comprises the following steps of: adding fatty alcohol; after ageing, separating out the fatty alcohol; and drying and roasting slurry without the fatty alcohol to obtain the aluminum oxide with a large hole diameter, a large specific surface area and a large hole volume. The aluminum oxide is suitable for a carrier of a hydrocarbons conversion catalyst.

The invention discloses a full liquid phase hydrogenation method of coal tar, which is characterized by comprising the following steps that coal tar raw materials respectively perform full liquid phase pre-hydrogenation reaction and full liquid phase main hydrogenation reaction, and main hydrogenation generated oil respectively generates naphtha products, diesel products and tail oil products through oil gas-liquid separation and distillation. The full liquid phase hydrogenation method enables the coal tar to perform the pre-hydrogenation reaction and the main hydrogenation reaction under the full liquid phase. The method can be suitable for hydrogenation modification of full fraction coal tar of any one or more of high-temperature coal tar, middle-temperature coal tar and low-temperature coal tar. During hydrogenation, coking can be effectively inhibited, reaction heat is controlled, energy loss is reduced, long-period running of a coal tar hydrogenation device is achieved, hydrogen consumption of the whole hydrogenation device can be reduced, investment of a compressor is reduced, and clean naphtha, diesel and tail oil products with sulfur nitrogen contents smaller than 400 parts per million (ppm) can be obtained.

The invention provides a deactivated catalyst regeneration method, which comprises: (1) making a to-be-regenerated hydrogenation catalyst contact an oxygen-containing gas, and carrying out charcoal burning treatment to obtain a catalyst A; (2) making the catalyst A contact an organic compound solution, and carrying out heat treatment to obtain a catalyst B; and (3) introducing an organic sulfide and hydrazine hydrate into the catalyst B, and carrying out heat treatment to obtain a regenerated catalyst. The regeneration method of the present invention can increase the activity of the regenerated catalyst.

The invention discloses a preparation method of a prevulcanization type catalyst. The method consists of: taking an oxidation state catalyst, adding an organic solvent and elemental sulfur, conducting heat treatment, then using an appropriate organic assistant to perform aftertreatment on the catalyst, thus obtaining the final prevulcanization type catalyst. The method enables the organic assistant and sulfur to form an organic compound, which does not decompose at low temperature, thus avoiding untimely contact of hydrogen and sulfur during startup activation, release of a hydrogen sulfide gas and the consequent influence on equipment air tightness. After high pressure air sealing, the compound of sulfur and the organic assistant decomposes. Hydrogen and sulfur react, the formed hydrogen sulfide and an active metal undergo catalyst activation in the pores of the catalyst, thus raising the initial temperature of vulcanization. After high pressure air sealing, activation oil is introduced to take away the heat generated by activation timely, thus avoiding temperature runaway of the catalyst bed and ensuring a smooth startup process. The catalyst prepared by the method involved in the invention is applicable to preparation of a petroleum fraction hydrogenation catalyst.

The invention relates to a technology method for preparing 2,6-ditertbutyl-4 methylphenol by using a micro-reaction rectifying plate. The method comprises the following steps of preheating p-cresol to 70 to 90 DEG C by a first preheater, and sending into the micro-reaction rectifying plate via an upper center passage; meanwhile, preheating isobutene to 70 to 90 DEG C by a second preheater, and sending into the micro-reaction rectifying plate via a lower center passage; enabling the p-cresol and the isobutene to react in the micro-reaction rectifying plate, so as to generate a liquid-phase product; discharging via a lower side passage of the micro-reaction rectifying plate, and rectifying and separating the liquid-phase reaction product, so as to obtain the 2,6-ditertbutyl-4 methylphenol; crystallizing again, and drying, so as to obtain a finished product; discharging the excessive isobutene and a low-boiling point product from an upper side passage of the micro-reaction rectifying plate. The technology method has the advantages that the conversion rate of the p-cresol is high, the yield rate of the 2,6-ditertbutyl-4 methylphenol is high, the reaction temperature is low, and the temperature runaway is avoided.

The invention relates to a preparing method of large-pore diameter aluminium oxide. The method includes: dissolving boehmite, pseudo boehmite or a mixture of boehmite and pseudo boehmite by any ratio into deionized water to form an aluminium hydroxide suspension liquid; performing stage heating treatment, with an initial temperature being 30-120 DEG C, a temperature gradient being 30-50 DEG C, and the treating time in each temperature state being 2-6 h; subjecting the treated aluminium hydroxide suspension liquid to hydrothermal ageing; and drying and calcinating after ageing is finished to finally obtain a large-pore diameter aluminium oxide product. The average pore size of the product is 90-300 angstroms, the most probable pore diameter is 90-280 angstroms, pore volume is 0.3-1.0 mL/g, and the specific surface area is 100-300 m<2>/g. The product has advantages of a large pore diameter, large pore volume, large specific surface area, easy adjustable product properties, and the like, and can be further processed into a catalyst carrier or an adsorbent having excellent performance.

The invention relates to an eggshell type composite metal oxide catalyst applied to gas phase oxidation of isobutylene/tert-butanol for synthesis of methylacrolein. A spherical carrier and a binder are added during the preparation of the catalyst, so a metal salt undergoes a reaction on the surface of the spherical carrier and adheres onto the surface of the spherical carrier; and a part of the binder is removed by roasting so as to obtain the eggshell type composite metal oxide catalyst. The catalyst provided by the invention is simple in preparation process and low in cost, and has excellentcatalytic performance in the gas phase oxidation of isobutylene/tert-butanol for synthesis of methylacrolein; and the catalyst has long catalytic life and is suitable for industrialization.

The invention discloses a preparation method of a vulcanization type catalyst. The method comprises: adopting a dipping solution containing a sulfide precursor of active metal Mo or W and an inorganic salt of Ni or Co to dip a needed catalyst carrier, and then conducting after-treatment under certain vacuum degree and temperature, thus obtaining the vulcanization type catalyst. The method can control vulcanization of the catalyst under an appropriate temperature in a startup activation process, thus avoiding untimely vulcanization of the active metal, release of a hydrogen sulfide gas and the consequent influence on equipment air tightness. Meanwhile, in the after-treatment process, redundant water in catalyst pores are removed to prevent excess water in recycle hydrogen from influencing the catalyst activity during activation and corroding equipment. The catalyst prepared by the method provided in the invention is applicable to preparation of a petroleum fraction hydrogenation catalyst.

The invention discloses a process for preparing absorbent resin comprising, charging water, sodium hydroxide, acrylic acid, N, N'-methylene di-propenamide and potassium peroxodisulfate into stirring still, homogenizing, going through preheating section, reaction section, heat preservation section in sequence, carrying out heat exchange and polymerization reaction.

The invention relates to a Fischer-Tropsch synthesis fluidized bed reactor, wherein the fluidized bed reactor comprises a reactor cylinder and an internal component arranged in the reactor cylinder, and the internal component comprises a gas distribution mechanism, a heat exchange mechanism, a solid catalyst separation and circulation mechanism and a catalyst online feeding and discharging mechanism; the gas distribution mechanism comprises a first-stage gas distributor, a second-stage gas distributor and a third-stage gas distributor which is arranged in a main reaction dense-phase region ofthe fluidized bed reactor; the first-stage gas distributor and the second-stage gas distributor are arranged at the bottom of the reactor cylinder; a gas nozzle of the third-stage gas distributor transversely sprays gas to transversely cut longitudinally rising gas flow. Compared with the prior art, the reactor is reasonable in design structure and layout; the fluidized bed reactor is good in gas-solid contact in the reactor, uniform in fluid distribution, high in system heat transfer efficiency, uniform in temperature distribution, good in gas-solid separation effect, high in system operationflexibility and particularly suitable for design and operation of the large-scale Fischer-Tropsch synthesis fluidized bed reactor, and cavities in the fluidized bed reactor are avoided.

The invention relates to an in-device regeneration method for ethanol dehydration ZSM-5 zeolite catalyst, which mainly solves the problem of poor regeneration effect of the regeneration method in the prior art, thus affecting the life of the catalyst, reaction conversion rate and yield, and device shutdown caused by catalyst replacement It takes a long time to affect the output of the device. The present invention adopts the method for regeneration by burning carbon with oxygen-containing nitrogen in the device, including purging the whole system with nitrogen to remove the reaction mixture, stepwise combustion regeneration with oxygen-containing nitrogen, cooling the system and replacing the oxygen-containing gas with nitrogen. The problem is solved, and the method can be used in the industrial production of ethylene prepared by catalyzing ethanol dehydration with ZSM-5 zeolite catalyst.

The invention relates to a method for producing glyoxylate. The method comprises the step of enabling oxygen-containing gas to pass through a reactor with a catalyst under the condition of oxidative dehydrogenation. The reactor comprises n sections of catalyst bed layers; the contents of catalyst active components in the n catalyst bed layers from an inlet to an outlet of the reactor are graduallyincreased; and n is an integer between 2 and 10. The method can be used for industrial production of the glyoxylate.

The invention discloses a method for preparing ethylene cracking feed by hydrogenation of liquefied gas. Liquefied gas and hydrogen pass through a hydrogenation reactor in a parallel flow manner and is in contact with hydrogenation catalysts for reaction; two or more hydrogenation catalyst bed layers are arranged in the hydrogenation reactor; the hydrogen enters the two or more hydrogenation catalyst bed layers from different feeding openings respectively; the amounts of the hydrogen entering all the hydrogenation catalyst bed layers are 5 to 95 volume percent of chemical hydrogen consumption required by reaction separately; except the last hydrogenation catalyst bed layer, the sum of total amounts of the hydrogen entering other hydrogenation catalyst bed layers is smaller than the required chemical hydrogen consumption. According to the method disclosed by the invention, by controlling partial pressures of the hydrogen entering different catalyst bed layers, the reaction speed is effectively controlled, and accurate control over the conversion rate is realized, so that reaction temperature rise of all sections of catalyst bed layers in the reactor is reduced, further the carbon deposit speed of the catalyst is retarded, and the single-pass service life of the catalyst is prolonged.

The invention provides a combined type fixed bed reactor. The combined type fixed bed reactor comprises a shell, an isothermal reaction bed layer, a heat insulation reaction bed layer, a gas distributor and a gas guiding structure, wherein the gas distributor, the isothermal reaction bed layer and the heat insulation reaction bed layer are sequentially arranged in a sleeving way, and gaps are formed between every two of the gas distributor, the isothermal reaction bed layer and the heat insulation reaction bed layer; a heat exchange structure is arranged in the isothermal reaction bed layer and comprises a plurality of heat exchange pieces which penetrate through the isothermal reaction bed layer along the axial direction. According to the combined type fixed bed reactor provided by the invention, and a process gas flows along the radial direction after entering a catalyst bed layer; for a reaction of which the gas flow is increased, the gas flow speed is prevented from being increased through an external expansion type flowing way, the retention time of the process gas in the catalyst bed layer is prolonged, the reaction can be promoted to proceed completely, and the utilization rate of a catalyst is increased; meanwhile, since the heat insulation reaction bed layer is arranged at the outer part of the isothermal reaction bed layer, heat of the isothermal reaction bed layer is facilitated to be absorbed, on one hand, the heat exchange amount is reduced, and on the other hand, a heat insulation reaction is promoted to proceed.

The invention discloses a device and a process for decarburization of gas containing high-concentration CO2 and regeneration of amine liquid. The device comprises an absorption tower, an amine liquidprimary flash tower, an amine liquid secondary flash tower, a purified gas cooler, a lean/rich amine liquid heat exchanger, a lean amine liquid cooler, an amine liquid filter, an absorption tower cleaning pump, a charging pump, an amine liquid circulating pump, a purified gas-liquid separator, a charging tank, a solution buffer tank, a liquid seal tank and a regulating valve. The device is suitable for the process for regenerating the amine liquid after decarburization of high-acid natural gas or synthetic gas with the acid gas content of 35% (mol%), and the carbon content of the purified gasis controlled to be not higher than 2.5% (mol%). According to the device, the amine liquid primary flash tower and the amine liquid secondary flash tower are used for replacing a regeneration tower, only part of heat is provided for the lower portion of the primary flash tower, the heat taking amount is greatly reduced, and energy consumption of the device is reduced; a traditional amine-rich liquid flash tank is replaced by the primary flash tower, and a carbon dioxide gas-liquid separator and a regeneration tower reflux pump do not need to be arranged in the process due to the secondary flash tower, so that the quantity of equipment is greatly reduced, and the process is greatly simplified.

The invention discloses a method for preparing succinate. The method comprises the following steps of: mixing hydrogen and maleic acid ester, and performing hydrogenation with a fixed bed reactor filled with a hydrogenation catalyst to obtain the succinate; and partially circulating the generated succinate, mixing with the maleic acid ester to obtain raw materials, and feeding a product subjectedto hydrogenation into a gas-liquid separator to obtain succinate with content of over 99.6 percent, wherein the separated hydrogen can be recycled. The method has the advantages that: raw materials are diluted in a reaction product circulation mode, so that temperature runaway caused by hydrogenation heat release can be effectively avoided, by-products of the reaction is very few, and the servicelife of the catalyst is prolonged and the stability of the catalyst is improved.