632results about How to "Low reaction pressure" patented technology

The present invention discloses a catalytic reaction method. Said method can make the catalytic reaction be implemented in the supergravitational field. Said method utilizes the rotary bed supergravitational field equipment as reactor, on the rotor of said rotary bed supergravitational field equipment a porous catalyst layer and/or a porous filler layer are fixed, and the described catalytic reaction is homogeneous reaction or heterogeneous reaction. Said invention cal reduce catalyst consumption, raise utilization rate of catalyst, raise stability of catalyst and can reduce denergy consumption, etc.

The invention provides a catalyst for converting diisononyl phthalate, diisooctyl phthalate, dibutyl phthalate and other long-chain esters into corresponding 1, 2-cyclohexane dicarboxylic acid binary ester through hydrogenation. The catalyst for converting the diisononyl phthalate, the diisooctyl phthalate, the dibutyl phthalate and other long-chain esters into corresponding the 1,2-cyclohexane dicarboxylic acid binary ester through the hydrogenation consists of main active ingredients, additives and carriers, wherein the main active ingredients are noble metal Ru and Pd; the additives are Fe, Co, Ni, Cu and other metals or oxides; and macroporous Al2O3, ZrO2, TiO2 and the like are selected as the carriers. Under certain temperature, certain hydrogen pressure and the action of the catalyst, the diisononyl phthalate, the diisooctyl phthalate, the dibutyl phthalate and other long-chain esters in a trickle bed reactor can be converted into the corresponding the 1, 2-cyclohexane dicarboxylic acid binary ester with high activity and high selectivity.

The invention relates to a laterite-nickel ore combination leaching process, which comprises that: limonite type laterite-nickel ore is subjected to crushing grading, and then is added with concentrated sulfuric acid to carry out primary stage normal pressure stirring self-heating leaching, serpentine type laterite-nickel ore is subjected to crushing grinding, the obtained serpentine type laterite-nickel ore and the primary stage leached ore magma are concurrently conveyed to a pressure kettle, and serpentine is leached by using the primary stage normal pressure leaching residual acid and the acid produced through iron precipitation in the pressure kettle, or mixing type laterite-nickel ore is subjected to grading, the obtained fine particle-grade ore is added with concentrated sulfuric acid to carry out primary stage normal pressure stirring leaching, ore on the sieve is subjected to crushing grinding, the grinded ore and the primary stage leached ore magma are concurrently conveyed to a pressure kettle, and coarse particle-grade ore leaching is performed by using the primary stage normal pressure leaching residual acid and the acid produced through iron precipitation in the pressure kettle. According to the invention, the process has characteristics of no special requirements on ore types and grades, wide raw material adaptability, investment reduction, energy consumption reduction, production cost reduction, and simple process, wherein the Ni recovery rate and the Co recovery rate of the whole process of the present invention are respectively more than 90% and 88%, and are higher than the Ni recovery rate and the Co recovery rate of the treatment method in the existing non-high-pressure acid leaching technology.

The invention relates to a selective hydrodesulfurization catalyst contains cobalt and molybdenum as active components. The selective hydrodesulfurization catalyst is characterized in that silicon oxide and aluminum oxide are used as carriers of the catalyst; based on the total weight of 100%, the catalyst comprises 2-6wt% of cobalt oxide, 9-15 wt% of molybdenum oxide, 2-8wt% of alkaline earth metal oxide, 2-6wt% of phosphorus oxide, 3-5wt% of alkali metal oxide, 2-6wt% of silicon oxide and 54-80 wt% of aluminum oxide; and the catalyst has the specific surface area of 200-300m<2>/g and the pore volume of 0.5-0.7mL/g. The catalyst has high hydrogenation activity and selectivity, good stability, low research octane number loss and high liquid yield. The catalyst is suitable for selective hydrodesulfrization of low-quality gasoline and is particularly suitable for selective hydrodesulfrization of low-quality FCC (Family Car China) gasoline.

The invention concerns the reaction of benzene catalyst adding hydrogen, specific speaking, it's a kind of catalyst to produce 4-ammonia base-3-F benzene fen and its application. The catalyst is made of carrier, active parts and helping dose. The main active parts are: dear metal Pt, Pd or Rh, whose weight is of catalyst 0.1%--20%. Help doses are IA, ó�A, ó¾B, ó° or Sparse soil chemical element. The catalyst has the feature of high active in reactivation, good choosing ability and many reuses. The catalyst can also be used in other replacing nitric unit benzene adding hydrogen and catalyst process.

The invention belongs to the technical field of catalysis, and particularly discloses a monolithic catalyst for catalyzing combustion of volatile organic compounds and a preparation method of the catalyst. According to the catalyst, cordierite honeycomb ceramic serves as a carrier, and the carrier is coated with a coating containing a metal active component and an auxiliary, wherein the catalyst active component is selected from any one or a combination of noble metals of Pt and Pd, and the catalyst auxiliary is selected from one or a combination of metal oxides such as aluminum oxide, titanium oxide, chromic oxide, cobaltous oxide and manganese oxide. The preparation method of the catalyst is simple, and the catalyst has the advantages that the coating is not prone to disengagement, the initiation temperature is low, the activity is good, the high-temperature-resistant property is good, and the noble metal content is low; the catalyst can be widely used for purification treatment of organic waste gas.

Disclosed is a process for the preparation of primary, secondary and tertiary amines via a catalytic hydrogenation of unsubstituted, N-substituted, and N,N-disubstituted amides. The amide is led, together with an auxiliary amine, in vaporised form in a hydrogen containing gas flow over the catalyst. The process can be carried out at relatively low pressures, between 2 and 50 bars, using typical hydrogenation catalysts like CuCr-type catalysts. The amine is obtained with high yield and high selectivity. The process can be carried out in a continuous fixed bed reactor.

A catalyst for preparing dichlorophenylamine by hydrogenating dichloronitrobenzene is composed of the activated carbon as carrier and the Pd as active component (0.2-2.0 Wt%) carried by said activated carbon. Its preparing process includes such steps as cyclically immersing activated carbon in diluted nitric acid, water washing until it becomes neutral, immersing in the aqueous solution of PdCl2, filtering, and baking the filtered cake. It has high catalytic performance and long cyclic service life.

A process for the high temperature carburization of steel comprising heating said steel in a vacuum furnace in the presence of a hydrocarbon carburizing gas in combination with hydrogen wherein said carburizing gas/hydrogen combination is administered to the vacuum furnace by cyclically reducing the pressure in the furnace followed by the pulsed addition of the hydrocarbon carburizing gas with hydrogen at partial pressure followed by a second diffusion cycle wherein the steel is further annealed for a time sufficient to allow for the additional deposition of from about 0.8% to about 3.0% m/o of said carbon onto the surface of said steel to permit the further migration of the carbon from the steel surface to the interior thereof.

The invention refers to the synthesizing method of 5-ethylene-2-norborene. The mol ratio of the butadiene and cyclopentadiene is 1-2:1. The invention chooses toluene or normal hexane as the solvent and the weight ratio of the reactants added to the solvent is between 20% and 30%. It chooses alpha-naphthol as the inhibitor and its dosage is between 50ppm and 3000ppm of the reactants. We put the material into the reaction kettle, increase the temperature when or after whisking and make them reacting for between 0.25 hour and 4 hours at the temperature of between 130deg.C and 160deg.C and at the pressure of between 1MPa and 8MPa. Or after being mixed we put the material into the reaction kettle or the tubular reactor and stay for between 0.25 hour and 1.0 hour at the temperature of between 130deg.C and 160deg.C and at the pressure of 1.8MPa. The weight ration of the dicyclopentadiene in the material of cyclopentadiene is less than between 5% and 8%. The invention obviously increases the yield of the turnoff by over 5mol%.

The invention discloses a catalyst for preparing cyclohexanediamine by phenylenediamine hydrogenation under ammonia reaction conditions. The catalyst realizes the transformation of phenylenediamine and hydrogen into cyclohexanediamine under ammonia reaction conditions and comprises a main active component, one or more auxiliary agents and a carrier. The main active component is a precious metal Ru or Pd. The one or more auxiliary agents are selected from Re, Co, Ni, Fe and their oxides. The carrier is active carbon, Al2O3 or SiO2. In a slurry-bed reactor, at a certain temperature, under the action of ammonia and catalyst, the high activity and high selectivity transformation of phenylenediamine and hydrogen into a plurality of amine products comprising cyclohexanediamine as a main product is realized.

The invention relates to a method for producing clean diesel oil and light aromatic hydrocarbons from inferior diesel oil. The method includes the following steps: (1) carrying out low-medium pressure hydrogenation on the inferior diesel oil to remove sulfur and nitrogen compounds, olefins and colloids, to obtain hydrofined diesel oil; (2) adsorbing and separating the refined diesel oil through a simulated moving bed to remove aromatic hydrocarbons and sulfides, to obtain the clean diesel oil and heavy aromatic hydrocarbons; and (3) allowing the heavy aromatic hydrocarbons to enter a lightening reactor, carrying out a hydrogenation reaction under low and medium pressure to produce BTX light aromatic hydrocarbons, a gasoline component and a small amount of light hydrocarbons. The process for producing the clean diesel oil and the light aromatic hydrocarbons from the inferior diesel oil can treat catalytic cracked diesel oil and coked diesel oil, produces the clean diesel oil and the gasoline components which can meet the country V standard, and simultaneously by-produces the BTX light aromatic hydrocarbons.

The diesel oil fraction upgrading and pour point reducing process has the mixture of diesel oil material and hydrogen passing through the hydroupgrading reaction region to result in diesel oil with low solidification point through reaction under certain condition. The catalyst in the hydroupgrading reaction region includes at least one kind of bulk phase catalyst comprising complex oxide NixWyOz and oxide MoO3 in the weight ratio 0.1-10 and accounting for 40-100 wt% of total catalyst, and at least one kind of upgrading catalyst containing beta-zeolite. The present invention can lower the solidification point, 95 vol% point temperature and sulfur content of diesel oil, and raise cetane number and oxidation stability under mild condition.

This invention relates to a method for preparing epoxide from olefin or cycloolefin by biomimetic catalytic oxygen oxidation. The method uses mononuclear metalloporphyrin or mu-O-binuclear metalloporphyrin as the catalyst, which has similar structure to bioenzyme. The concentration of the catalyst is 0.1-100 ppm. Besides, methane dichloride, benzene, toluene, methanol or ethyl acetate is used as the solvent. And isobutylaldehyde or n-butyraldehyde is also added at a mol ratio of 1 : (0.1-2) to the reactant. The reaction is performed at 40-160 deg.C in 0.1-2.0 MPa oxygen atmosphere for 5-12 h. The method has such advantages as low catalyst amount, low reaction temperature and pressure and easy operation. The catalyst has good catalytic performance on olefin or cycloolefin oxidation to obtain epoxide.

The invention discloses a method for putting the oxydone compounds into the biomimetic catalysis to prepare the lactone. With the ketone compounds as the raw materials, the invention selects the mononuclear metalloporphyrins with structure in the general formulas (I) and (II) or Mu-oxygen-binuclear metalloporphyrins with structure in the general formula (III) as the catalysts; the concentration of the catalysts ranges from 2 multiplied by 10<-5>mol/L to 2 multiplied by 10<-2>mol/L and the concentration of the ketone compounds ranges from 0.02mol/L to 0.8mol/L; with the benzene, the toluene, the xylene, the benzotrifluoride or the cyclohexane as the solvents, the benzaldehyde, isobutyraldehyde or butyraldehyde with a molar ratio to the ketone compounds ranging from 0.5 to 1 to 20 to 1 is added in the mixtures; the oxygen with a pressure ranging from 0.1MPa to 1.6MPa is pumped in the mixtures; the reaction temperature is controlled to a range from 40 DEG C to 150 DEG C and the reaction time is controlled to a range from 1 to 10 hours. The invention has the advantages of gentile reaction conditions, a small dosage of catalysts, good catalytic effects, and high product selectivity, etc.

The present invention relates to catalytical hydrogenation process to produce H acid, and solves the technological problem of providing one new type of catalyst to lower the reaction pressure, reaction temperature and production cost effectively. The process includes the following steps: 1. regulating the nitroso value of nitro T acid and its solution as material to 15-45 g/L and the pH value to 7-10; 2. catalytical hydrogenation through adding the regulated solution and Ni-Co catalyst with Co content of 0.5-25 wt% and in the amount of 0.1-5 wt% of nitro T acid into high pressure reactor, introducing H2 of 1.0-4.5 Mpa pressure at 90-220 deg.c, and hydrogenating catalytically for 2-5 hr to obtain amino T acid and its solution; 3. alkali fusing; and 4. acid out to obtain the product.