41results about How to "Long stable operation time" patented technology

The present invention relates to a selective hydro-desulfurization catalyst of gasoline and process for using said catalyst. Said invented catayst uses alumina as carrier, uses molybdenum and cobalt as active component, at the same time contains adjuvant potassium and phosphorus, and the optimized atomic ratio of phosphorus and potassium is 1-2. Said invented catalyst has good selectivity and stability, and at the same time has proper activity, and is mainly used for selective hydro-desulfurization of catalytic cracked gasoline.

The invention discloses a method for preparing epichlorohydrin by the epoxidation of chloropropene by means of catalyzing, which is characterized in that under the conditions of temperature of 0 DEG C to 180 DEG C and pressure of 0.1 MPa to 3.0 MPa, chloropropene, oxygen, hydrogen, diluents, a solvent and a catalyst are mixed and contacted for reaction; the mole ratio of the chloropropene, the oxygen, the hydrogen, the diluents, the solvent and the catalyst is 1: (0.1 to 10): (0.1 to 10): (0 to 100); the mass ratio of the chloropropene and the catalyst is (0.1 to 50):1; the mass ratio of the solvent and the catalyst is (20 to 1000):1; the catalyst refers to a cellular titanium silicon material or a composite containing the cellular titanium silicon material; the composition of the cellular titanium silicon material expressed in the manner of oxides is xTiO2 question mark 100SiO2 question mark yEm question mark On question mark zE, wherein, the value of X is between 0.001 and 50.0; the value of (y plus z) is between 0.005 and 20.0 and y divided by z is less than 1; E represents one or more noble metals selected out of Ru, Rh, Pd, Re, Os, Ir, Pt and Au; m and n are numbers meeting the need of E at oxidation state; and the grains of the material are partially hollow or completely hollow. The method obviously promotes the transformation rate of chloropropene and has high selectivity and hydrogen effective utilization rate and long running period.

The invention discloses a method for producing ethanol by hydrogenating acetic acid. The method is as follows: at a temperature of 250-400°C, a pressure of 0.5-10.0 MPa, a mass space velocity of 0.2-8.0 hours-1, and a feed molar ratio of hydrogen to acetic acid Under the condition of 1:1~20:1, mix acetic acid and hydrogen, contact and react with the supported transition metal carbide catalyst, and hydrogenate acetic acid to produce ethanol; the process of the invention is simple, the price of the catalyst is low, and the performance of the catalyst is stable Well, the stable operation time of the device is long, which can avoid the frequent switching operation of reactor reaction and regeneration, the catalyst can be regenerated, can avoid the post-treatment of a large amount of spent catalyst, and has little impact on the environment.

The invention discloses a method for removing micro-quantity alkene in aromatic hydrocarbon. The method comprises the following steps of: contacting and reacting the aromatic hydrocarbon with a solid acid catalyst under the condition of temperature of 30-350 DEG C, pressure of 0.1-12MPa and feeding quality airspeed of 0.1-15 h<-1>, so that micro-quantity alkene in the aromatic hydrocarbon undergoes adsorbing, overlapping and alkylation reaction so as to remove the micro-quantity alkene in the aromatic hydrocarbon. The method is simple in process procedure, free of oxygen consumption and low in device investment and operation expense; and the catalyst is good in activity stability, the device is long in stable operation time, the aromatic hydrocarbon loss is small, the frequent switching operation between reactor reaction and regeneration is avoided, and the catalyst can be regenerated, so that a great deal of waste catalyst is prevented from being buried, and the environment is less polluted.

The invention discloses an aromatic hydrocarbon purifying method which comprises the step of carrying out a contact reaction on aromatic hydrocarbon and a solid acid catalyst under the conditions that the temperature is 50-400 DEG C, the pressure is 0.1-12MPa and the feeding mass space velocity is 0.1-15h<-1> to obtain purified aromatic hydrocarbon. The aromatic hydrocarbon purifying method is simple in process without consuming hydrogen, low in device investment and operation cost, good in catalyst activity stability, long in device stable operation time and less in aromatic hydrocarbon loss; and reactor reaction and regeneration frequent switching operation can be avoided, the catalyst can be regenerated, a large quantity of waste catalysts can be prevented from being stacked and embedded, and environment influence is little.

The invention relates to a solid-acid-catalyzed method for synthesizing straight-chain alkyl-benzene, comprising the steps of: with straight-chain olefin having 10 to 14 carbon atoms and benzene as raw materials, and carrying out alkylation reaction with catalysis of a solid acid catalyst to obtain the straight-chain alkyl-benzene under the reaction condition that the temperature is 10-450 DEG C, the pressure is 0.1-15MPa, the mass ratio of the benzene to olefin substance is (2-100):1 and the total mass airspeed of feedstock is 0.1-20h<-1>, wherein the solid acid catalyst is mesoporous molecular sieve catalyst of M-KIT-1 type or a composite solid acid catalyst obtained by loading a modified compound on the mesoporous molecular sieve catalyst of M-KIT-1 type. The catalyst adopted in the method disclosed by the invention is free of corrosiveness, friendly to environment and has good activity stability. Stable operation time of a device is long so that a reactor is prevented from being switched between reaction and regeneration frequently.

The invention discloses a synthesizing method of straight-line alkyl benzene, which comprises the following steps: adopting straight-line olefin with carbon atom number between 2 and 20 and benzene as raw material; inputting in the reactor; reacting benzene and olefin with molar rate at 2-100:1 at 290-450 deg. c under 5-15Mpa hypercritical condition; setting the air speed at 0. 1-20h-1; making solid acid as catalyst; adopting one of loaded modified (1) SBA-15 typed molecular sieve, (2) HY typed molecular sieve, (3) USY typed molecular sieve, (4) H beta typed molecular sieve, (5) H-Moderite typed molecular sieve, (6) HZSM-20 typed molecular sieve as composite typed solid acid catalyst. The invention improves transmitting rate of olefin with stable operation, which possesses good using prospect.

The invention discloses a catalytic hydrogenation method for reducing the linear alkylbenzene bromine index. The method is as follows: at a temperature of 60-400°C, a pressure of 0.3-10.0MPa, and a mass space velocity of 0.2-8.0 hours-1, hydrogen Under the condition of oil volume ratio of 300:1~8000:1, the hydrogenation raw material is mixed with hydrogen, and reacted with transition metal phosphide supported catalyst to saturate olefins, thereby reducing the linear alkylbenzene bromide index and improving product quality The raw material for hydrogenation is linear alkylbenzene obtained by distillation and separation of the alkylation mixture of benzene and C10-C14 linear olefins, or the alkylation mixture of benzene and C10-C14 linear olefins; the process flow of the present invention is simple, The catalyst has good activity and stability, and the stable operation time of the device is long, which can avoid the frequent switching operation of reactor reaction and regeneration, the loss of linear alkylbenzene is small, the catalyst can be regenerated, and the post-treatment of a large amount of spent catalyst can be avoided, and the impact on the environment is small.

The invention discloses a method for removing olefin in aromatic hydrocarbon by an M-SBA-15 type mesoporous molecular sieve. The method comprises the step of carrying out contact reaction of aromatic hydrocarbon with a solid acid catalyst to obtain aromatic hydrocarbon without olefin at 30-350 DEGC, at a pressure of 0.1-10MPa, and at an air speed of 0.1-15 / h for feed quality, wherein the aromatic hydrocarbon is aromatic hydrocarbon generated by reforming generated oil, reforming aromatic hydrocarbon or steam cracking. The method is simple in process flow, free of hydrogen consumption and low in device investment and operating cost. The catalyst activity is good in stability, the stable operation of the device is long and the aromatic hydrocarbon loss is small, so that the frequency switching operation between reaction and regeneration of a reactor is avoided. The catalyst is reproducible, so that a great amount of dead catalysts is not buried, therefore, the environmental influence is small.

The invention discloses a method for removing trace olefin from aromatic hydrocarbon. The method comprises the step of carrying out contact reaction on aromatic hydrocarbon and a solid acid catalyst under the conditions that the temperature is 30-400 DEG C, the pressure is 0.1-12MPa and the feeding mass space velocity is 0.1-15h<-1> to obtain aromatic hydrocarbon after the olefin is removed. The method is simple in process without consuming hydrogen, low in device investment and operation cost, good in catalyst activity stability, long in device stable operation time and less in aromatic hydrocarbon loss; and reactor reaction and regeneration frequent switching operation can be avoided and a large quantity of waste catalysts can be prevented from being stacked and embedded, and environment influence is little.

The invention discloses a process for synthesizing butanone oxime ethyl ether through continuous microtube reaction. The process adopts continuous microtube reaction technology, under the conditions of temperature 30-45℃, pressure 0.1MPa and strong base, butanone oxime and diethyl sulfate are reacted to directly synthesize butanone oxime ethyl ether; the strong base is hydrogen Sodium oxide, potassium hydroxide or alcohol amine compounds. In this process, diethyl sulfate, lye and butanone oxime are respectively fed by precision micropumps, butanone oxime is mixed with lye and diethyl sulfate in turn, and then reacted in a microtube reactor. After the heater, it is condensed and collected at low temperature, the chromatographic separator is left to stand for stratification, the water phase is extracted and separated by a micro-extraction tower, and the oil phase product containing butanone oxime ether is purified by rectification in a rectification tower to obtain the final product butanone oxime ether. The process has high selectivity of butanone oxime ethyl ether, can significantly enhance mass transfer and heat transfer, effectively avoid the hydrolysis of diethyl sulfate, has simple process, long stable operation time, low cost, is easy to scale up, and meets the requirements of industrial production.