58results about How to "Conducive to long cycle operation" patented technology

The invention provides a hydroconversion method of deep cut anthracene oil. The method comprises the following steps of: fractionating deep cut anthracene oil into a light fraction and a heavy fraction, then separating the light fraction after hydrofining, refining the liquid phase which is obtained during the separating process to generate an oil, infusing the oil and the heavy fraction into the hydroconversion region and then separating the heavy fraction from the oil which is generated during the hydroconversion process, wherein the first fraction which is light is entered into the hydrocracking region, and the cracked product which is obtained during the hydrocracking process is infused into the fractionation system to obtain gasoline and diesel fractions. The hydroconversion method of deep cut anthracene oil provided by the invention has the advantages that the deep cut anthracene oil is inversed into light fuel oil by means of hydroconversion, an application way with high additional value is provided to coal tar, the operation of the device is stable by optimizing the process, and the running period of the device is long.

The invention discloses a method for producing light fuel oil from ethylene tar. The method is as below: fractionating ethylene tar into a light fraction and a heavy fraction; mixing the heavy fraction with a conventional coking raw material, and subjecting the mixture to delayed coking to obtain coker gasoline, coker diesel and coker gas oil; mixing the coker gasoline and the coker diesel with the light fraction of the ethylene tar, and subjecting the mixture to a hydrofining reaction; distilling the product to obtain a gasoline fraction I and a fraction heavier than the gasoline; subjecting the fraction heavier than the gasoline to a hydrogenation treatment to obtain light fuel oil, and distilling to obtain a gasoline fraction II and a diesel product; and mixing the gasoline fraction I and the gasoline fraction II to obtain a final gasoline product. The method provided by the invention utilizes the characteristics of high contents of ethylene tar aromatic hydrocarbons, colloid, carbon residue and glial and asphaltene of ethylene tar to fractionate the ethylene tar into the light fraction and the heavy fraction; different processing methods are employed to improve the added value of ethylene tar, increase yield of gasoline and diesel, improve product quality of light fuel oil and realize long-period stable operation of devices.

The invention discloses a preparation method of transformer oil base oil, and the method comprises the following steps of: sequentially carrying out hydrodewaxing reaction and hydrofinishing reaction on raw oil to obtain the transformer oil base oil. According to the method, a hydrodewaxing catalyst with a specific structure is adopted in the hydrodewaxing reaction process, and the hydrofinishing process is combined, so that the prepared transformer oil base oil is low in pour point and aromatic hydrocarbon content.

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 FCC gasoline upgrading method. FCC gasoline is subjected to a mercaptan etherification and double-bond isomerism reaction under the action of a prehydrogenation catalyst bya prehydrogenation reactor, a prehydrogenation reaction effluent is cut into light and heavy gasoline fractions, the light gasoline fraction is subjected to isomerization reaction under the action ofan isomerization catalyst, the heavy gasoline fraction is subjected to selective hydrodesulfurization under the action of a hydrodesulfurization-isomerization catalyst, and simultaneously, linear olefin is isomerized into single branched olefin or single branched paraffin; then, the heavy gasoline fraction after the reaction enters an octane number recovery unit and is in contact with an octane number recovery catalyst to be subjected to a double branched isomerization reaction; finally, the light and heavy gasoline fractions are blended to obtain a clean gasoline product with low olefin content, ultra low sulfur content and a high octane number.

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 discloses a deep desulphurization combination method of diesel oil, comprising the following steps of: allowing fresh diesel oil feedstock to enter a hydrogen mixing pot for hydrogen mixing, allowing diesel oil dissolved in hydrogen to enter a liquid phase hydrogenation reactor for refining reaction; allowing the obtained refined effluent to enter a high-temperature low-pressure flash tank for flash evaporation so as to obtain a liquid phase heavy fraction; allowing part of the heavy fraction to recycle and return to the hydrogen mixing pot and part of the heavy fraction to undergo oxidative desulfurization, mixing the heavy fraction which has undergone oxidative desulfurization and the light fraction obtained by flash evaporation, and separating to obtain the diesel oil product. According to the method, liquid phase hydrogenation is performed under mild conditions to remove simple sulfide in the diesel oil feedstock; after flash evaporation, the recycled heavy fraction continues to undergo hydrodesulfurization, and residual heavy fraction is selectively subjected to oxidative desulfurization so as to realize deep desulphurization of diesel oil. According to the method, by full utilization of advantages of hydrodesulfurization and oxidative desulfurization, equipment investment and operation cost are reduced, and energy consumption is minimized. Therefore, the method can satisfy the demand of producing clean diesel oil by deep desulphurization of diesel oil.

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 discloses a method for producing clean fuel oil from ethylene tar. The method is as follows: fractionating the ethylene tar into a light fraction, a middle fraction and a heavy fraction, mixing the heavy fraction with a conventional coking raw material, conducting delayed coking to obtain coker gasoline, coker diesel oil and coker wax oil, mixing the obtained coker gasoline with the ethylene tar light fraction, leaving the mixed material to undergo hydrofining, performing rectification/ crystallization purification on the middle fraction to obtain naphthaline, mixing naphthaline removal oil after naphthaline extraction and naphthaline post-fraction oil with the coker diesel oil and the coker wax oil for hydrotreating, and separating an obtained product and the hydrofining product of the coker gasoline and the ethylene tar light fraction to obtain gasoline diesel oil products. Directed at the characteristics of high content of aromatic hydrocarbons, colloid, carbon residue and asphaltene in the ethylene tar, the method provided in the invention fractionates the ethylene tar into the light fraction, the middle fraction and the heavy fraction, and adopts different processing processes, thus not only enhancing the additional value of the ethylene tar, improving the product quality of light fuel oil in the same time of obtaining of the chemical raw material naphthaline, but also enabling the equipment to run smoothly for a long period.