633results 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 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.

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 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.

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.