39results about How to "Improve anti-glue ability" patented technology

The invention relates to an unsaturated C5 fraction and hydrogenation method. According to the method, by the aid of a fixed bed reactor, a used catalyst is a nickel hydrogenation catalyst, and the catalyst is reduced by the aid of hydrogen or hydrogen-containing gas at the temperature of 350-500 DEG C. The catalyst comprises main active components and a silicon oxide-aluminum oxide composition, and the main active components include molybdenum, nickel, cobalt and potassium. Hydrogenation process conditions include that a reactor inlet temperature is 30-660 DEG C, reaction pressure is 1.5-6.0MPa, liquid volume per hour is 1.0-6.0h<-1>, and the volume ratio of hydrogen to oil is 100:400. According to the unsaturated C5 fraction and hydrogenation method, the used nickel-based saturated hydrogenation catalyst has high hydrogenation activity and the advantages that the catalyst is resistant to sulfur, water and colloid, and hydrogenation reaction can be performed at low temperature.

The invention relates to a hydrogenation method of C4 unsaturated hydrocarbon. According to the method, by the aid of a fixed bed reactor, a nickel saturated hydrogenation catalyst is reduced outsidea hydrogenation reactor at the temperature of 350-500 DEG C, air is led in to passivate the catalyst, the passivated catalyst is reduced in the reactor by hydrogen at the temperature of 120-200 DEG C,the C4 unsaturated hydrocarbon is added, alkyne and diolefin in the C4 unsaturated hydrocarbon are hydrogenated into corresponding alkane, the nickel saturated hydrogenation catalyst comprises activecomponents and silicon oxide-aluminum oxide composition, and the active components include molybdenum, nickel , cobalt and magnesium. Reaction process conditions include that inlet temperature of thereactor is 30-55 DEG C, reaction pressure is 1.0-4.5MPa, liquid volume per hour is 1.5-4.5h<-1>, and the volume ratio of hydrogen to oil is (120-450):1. According to the hydrogenation method of theC4 unsaturated hydrocarbon, the catalyst is good in hydrogenation activity, good in gelatine and water resistance and high in sulfur resistance.

The invention relates to a total fraction cracking gasoline selective hydrogenation method. A fixed bed reactor is used; a catalyst is reduced in hydrogen gas atmosphere; after the reduction process is completed, the process condition is regulated to the reaction process conditions; gasoline raw material total fraction cracking is performed; selective hydrogenation reaction is performed; the catalyst is prepared from silicon oxide-aluminum oxide carriers and metal active ingredients of palladium loaded on the carriers; the content of the palladium is based on 0.15 to 0.45 weight percent of thetotal weight of the catalysts. The hydrogenation process conditions are shown as follows: the reaction inlet temperature is higher than or equal to 50 DEG C; the reaction temperature is 2.0 to 4.5MPa; the hydrogen oil volume ratio is (60 to 400):1; the liquid volume air speed is 2.5 to 5.0 h<-1>. The catalyst gum resistant capability is high; the arsenic resistant, sulfur resistant and water-resistant capability is high; the stability is high.

The invention relates to a method of removing mercaptan of catalytically cracked gasoline. According to the method, a fixed bed reactor is adopted; a catalyst comprises a silicon oxide-aluminum oxidecarrier, metal active components (nickel, molybdenum, and iron) loaded on the carrier, and an auxiliary agent (phosphorus); nickel oxide accounts for 2 to 15 wt% of the catalyst, molybdenum oxide accounts for 2 to 18 wt% of the catalyst, iron oxide accounts for 0.1 to 5.5 wt% of the catalyst, the auxiliary agent (phosphorus oxide) accounts for 0.01 to 2.2 wt% of the catalyst, the silicon oxide-aluminum oxide carrier accounts for 65 to 85 wt% of the catalyst, the micro pores, mesopores, macro pores are unevenly distributed in the carrier; the reaction temperature is 110 to 220 DEG C, the reaction pressure is 1.1 to 4.5 MPa, the volume air speed is 1.2 to 5.0 h<-1>, and the volume ratio of hydrogen to oil is 7-25:1. The catalyst has the characteristics of high mercaptan removing activity, high selectivity of diolefin hydrogenation, few side reactions, and low octane value loss.

The invention relates to a selective hydrogenation method for full-range pyrolysis gasoline, which adopts a reactor of an adiabat bed reactor. The catalyst comprises silica-alumina carrier and metal active component palladium loaded on the carrier, wherein the palladium is 0.15-0.45 percent of total weight of the catalyst; and the silica-alumina carrier is prepared from the following components inpercentage by weight: 0.1-12 percent of silica, 0.1-10 percent of nickel-doped lanthanum ferrite and 0.05-7.8 percent of magnesium. According to the hydrogenation process conditions, the reaction inlet temperature is more than or equal to 50 DEG C, the reaction pressure is 2.0-4.5MPa, the hydrogen-oil volume ratio is 60-450, and the liquid hourly space velocity is 3.0-5.0h<-1>. The catalyst has good gum resistance and strong performance of arsenic resistance, sulfur resistance and water resistance.

The invention relates to a selective hydrogenation method for pyrolysis gasoline. A catalyst comprises a silicon oxide-aluminum oxide carrier and a metal active component palladium loaded to the carrier. Palladium accounts for 0.15-0.45wt% of the total weight of the catalyst. The silicon oxide-aluminum oxide carrier comprises 0.1-12wt% of silicon oxide, 0.1-10wt% of nickel doped lanthanum ferriteand 0.05-7.8wt% of magnesium. The hydrogenation process conditions are as follows: the reaction inlet temperature is lower than or equal to 45 DEG C, the reaction pressure is 2.5-4.5 MPa, the hydrogenoil volume ratio is 60-450, and the liquid volume airspeed is 3.0-5.5h<-1>. The catalyst is good in colloid resistance and high in arsenic, sulfur and water resistance.

The invention relates to a nickel selective hydrogenation catalyst. The catalyst is prepared from a silica-alumina carrier and metal active ingredients, including nickel, molybdenum and potassium, loaded on the carrier, and comprises the following components based on total weight of the catalyst: 9-25 weight percent of nickel oxide, 2.5-8 weight percent of molybdenum oxide, 0.02-2.5 weight percentof potassium oxide and 75-91 weight percent of silica-alumina carrier. The catalyst has strong colloid resistance, arsenic resistance, sulfur resistance and water resistance.

The invention relates to a first-stage selective hydrogenation method for pyrolysis gasoline. The first-stage selective hydrogenation method is implemented by the aid of heat-insulation bed reactors.The first-stage selective hydrogenation method includes carrying out reduction on nickel catalysts in the presence of hydrogen under the condition of the temperature of 400-480 DEG C; carrying out cooling and passivation and then carrying out adjustment until reaction technological conditions are met. The reaction technological conditions include the reaction inlet temperatures of 45-120 DEG C, the reaction pressures of 2.5-5.5 MPa and the hydrogen-oil volume ratios of 60-220:1. The liquid volume space velocities are 2.0-6.5 h<-1>; the catalysts comprise silicon oxide-aluminum oxide carriers and metal active components including nickel, molybdenum and potassium, and the metal active components are loaded on the carriers. The first-stage selective hydrogenation method has the advantage thatthe catalysts are applicable to first-stage selective hydrogenation for the pyrolysis gasoline.

The invention relates to a unsaturated hydrocarbon selective hydrogenation catalyst, which comprises a silicon-alumina carrier and metal active components such as nickel, molybdenum and magnesium loaded on the carrier. The catalyst comprises the following components based on the total weight of the catalyst: 7-18wt% of nickel oxide, 3.5-12wt% of molybdenum oxide, 0.05-2.0% of magnesium oxide, 75-91wt% of the silica-alumina carrier, 3-70% of mesopores of the carrier accounting for the total pores, and 1.5-55% of the macropores accounting for the total pores. The catalyst is prepared by an impregnation method. The catalyst has good colloid resistance, strong arsenic resistance, sulfur resistance and water resistance.

The invention relates to an all-fraction selective hydrogenation method for pyrolysis gasoline. The all-fraction selective hydrogenation method includes procedures of carrying out reduction on nickelcatalysts in the presence of hydrogen under the condition of the temperature of 400-500 DEG C; carrying out cooling and passivation and then carrying out adjustment until reaction technological conditions are met. The reaction technological conditions include the reaction inlet temperatures of 45-110 DEG C, the reaction pressures of 2.0-4.5 MPa and the hydrogen-oil volume ratios of 60-200:1. The liquid volume space velocities are 2.0-5.5 h<-1>; the catalysts comprise silicon oxide-aluminum oxide carriers and metal active components including nickel, molybdenum and magnesium, and the metal active components are loaded on the carriers. The all-fraction selective hydrogenation method has the advantage that the catalysts are good in colloid resistance, high in arsenic resistance, sulfur resistance and water resistance and applicable to long-period stable operation of devices.

The invention relates to a selective-hydrogenation catalyst for cracking gasoline and a preparation method. The selective-hydrogenation catalyst comprises a silicon oxide-aluminium oxide carrier and metal active-component palladium loaded on the carrier, wherein the content of the palladium is 0.15-0.45wt% of the total weight of the catalyst; the silicon oxide-aluminium oxide carrier contains silicon oxide, nickel-doped lanthanum ferrite and magnesium oxide; mesopores of the carrier account for 3-75% of total pores, and macropores account for 1.5-60% of the total pores. The selective-hydrogenation catalyst is prepared by adopting an impregnation method and is good in colloid resistance, arsenic resistance, sulfur resistance and water resistance.

The invention relates to a pyrolysis gasoline C6-C8 fraction hydrofinishing catalyst. The catalyst takes molybdenum, cobalt, nickel and potassium as active components, and silicon oxide-aluminum oxideas a carrier. Measured by the total weight of the catalyst, the catalyst comprises 6-22% of molybdenum oxide, 0.1-2.2% of cobalt oxide, 4.0-7.2% of nickel oxide, 0.1-3.0% of potassium oxide, and 75-88w% of the silicon oxide-aluminum oxide carrier. In the carrier, mesopores account for 3-70% of total pores, and macropores account for 1.5-55% of the total pores. The catalyst has good colloid resistance and high arsenic resistant, sulphur resistant and water resistant abilities.

The present invention relates to the field of cyclopentane preparation, and discloses a non-noble metal Ni-based catalyst, a preparation method thereof, and a method for preparing cyclopentane through cyclopentadiene hydrogenation, the non-noble metal Ni-based catalyst contains a carrier, and a Ni active metal component and a metal auxiliary agent component loaded on the carrier, at least part of the nickel element exists in the form of nickel elementary substance and/or nickel carbide. The catalyst can reduce the self-coalescence coking phenomenon of cyclopentadiene in preparation of cyclopentane through hydrogenation of cyclopentadiene, so that the colloid resistance of the catalyst is improved, and the catalyst has the advantages of high activity, good selectivity, high reuse rate, difficulty in inactivation and the like, and further has the advantages of simple preparation process, low cost and the like. In the process of preparing cyclopentane through cyclopentadiene hydrogenation, no extra solvent or diluent needs to be added, and inactivation is not prone to occurring. In addition, according to the method for preparing cyclopentane through cyclopentadiene hydrogenation, due to the fact that the catalyst is used and matched with a two-stage hydrogenation process, high selectivity and yield are achieved.

The invention relates to an ethylene cracking C6-C8 distillate oil hydrorefining method, which is characterized in that a heat insulation bed reactor is used; a nickel and molybdenum series catalyst is vulcanized by vulcanizing oil and then put into raw material oil; the catalyst uses molybdenum, cobalt, nickel and potassium as active ingredients; silicon oxide-aluminum oxide is used as a carrier;through being metered by the total weight of the catalyst, the catalyst contains 6 to 22 percent of molybdenum oxide, 0.1 to 2.2 percent of cobalt oxide, 4.0 to 8.2 percent of nickel oxide, and 0.1 to 3.0 percent of potassium oxide, and 75 to 88 percent by weight of the silicon oxide-aluminum oxide carrier. The reaction process conditions are as follows: the reaction pressure is 2.8MPa or higher;the inlet temperature is 220 to 380 DEG C; the volume space velocity of fresh raw material oil is 1.5 to 3.5h<-1>; through being metered by the fresh oil, the volume ratio of hydrogen to oil is from(180:1) to (350:1). The catalyst is good in anti-colloid capability; the arsenic resistance, sulfur resistance and water resistance capabilities are strong; the stability is good.

The invention relates to a FCC gasoline mercaptan etherification method. A fixed bed reactor is adopted, gasoline is introduced into the reactor, under the action of a catalyst, mercaptan in the gasoline and dialkene carry out etherification reactions, and the catalyst comprises a composite carrier and metal active components: nickel, molybdenum and magnesium. The reaction conditions are: reactionpressure 0.1-5 MPa, volume ratio of hydrogen to oil 2:1-30:1, reaction temperature 60-200 DEG C, and air speed 0.5-8 h<-1>. The catalyst has the characteristics that the mercaptan etherification activity is high and the loss of octane value is low and can adapt to various raw materials.

The invention relates to a pyrolysis gasoline one-section selective hydrogenation method. A catalyst is prepared from a silicon oxide-aluminum oxide carrier and a metal active ingredient palladium loaded on the carrier; the palladium content is 0.15 to 0.45 weight percent of the total weight of the catalyst; the pectin resistant capability of the catalyst is good; the anti-arsenic, anti-sulfur andwater-resistant capability is high. Under the hydrogenation process condition, the reaction inlet temperature is smaller than or equal to 45 DEG C; the reaction pressure is 2.5 to 4.5MPa; the hydrogen oil volume ratio is 60 to 450; the liquid volume space velocity is 3.0 to 5.5h<-1>. The catalyst has high adaptability on pyrolysis gasoline raw materials with different arsenic content, different sulphur content, water content and pectin content; the low-temperature activity of the catalyst is high.

The invention relates to a selective hydrogenation method of middle distillate unsaturated hydrocarbon of pyrolysis gasoline. The selective hydrogenation method comprises the following process: in thepresence of hydrogen and under the condition of 400 to 500 DEG C, reducing a nickel catalyst; adjusting to reaction process conditions after cooling passivation: the temperature of a reaction inlet is 45 to 110 DEG C, the reaction pressure is 2.0 to 4.5 MPa, the volume ratio of hydrogen to oil is (60 to 200) to 1 and the liquid volume airspeed is 2.0 to 5.5 h<-1> ; the catalyst comprises a silicon oxide-aluminum oxide carrier and metal active components such as nickel, molybdenum and magnesium loaded on the carrier. The catalyst has good colloid resistance, as well as high arsenic resistance,sulfur resistance and water resistance, and is suitable for long-cycle stable operation of a device.