56results about How to "Reduce coke yield" patented technology

An improved delayed coking process utilizing a coking unit and a coking unit product fractionating column which includes the steps of:

• • heating a mixture of a fresh whole crude oil feedstream and the bottoms from the coking unit product fractionator in a furnace to a coking temperature in the range of 480° C. to 530° C./896° F. to 986° F.;
  • introducing the heated mixed whole crude oil and bottoms feedstream directly into the delayed coking unit;
  • optionally passing the vaporized liquid and gaseous coking unit product stream into a flash unit;
  • recovering a light product gas stream that includes H₂S, NH₃ and C1 to C4 hydrocarbons from the flash unit;
  • transferring the bottoms from the flash unit to the coking unit product fractionating column;
  • recovering as separate side streams from the fractionating column naphtha, light gas oil and heavy gas oil;
  • recycling a portion of the heavy gas oil by introducing it into the fractionating column optionally with the bottoms from the flash unit;
  • mixing the fractionating column bottoms with the whole crude oil feedstream to form the mixed feedstream; and
  • introducing the mixed whole crude oil and fractionating column bottoms feedstream into the furnace.

The method of raising liquid yield during delayed coking is to add one kind of low-boiling point evaporant capable of shortening the setting period of distillate oil in coking tower, and reducing the possibility of secondary cracking and re-condensation of hydrocarbon to form coke. The evaporatn may be gasoline, hydrogenated coked gasoline, organic alcohol, gaseous hydrocatbon or their mixture; and may be added into the fed material before coking tower, into the distillate oil in the back of coking tower and/or into the coking tower. The present invention can raise liquid yield by 2-8% and lower coke yield by over 2%.

Integrated slurry hydrocracking (SHC) and coking methods for making slurry hydrocracking (SHC) distillates are disclosed. Representative methods involve passing a slurry comprising a recycle SHC gas oil, a coker gas oil, a vacuum column resid, and a solid particulate through an SHC reaction zone in the presence of hydrogen to obtain the SHC distillate. Recovery of an SHC pitch from fractionation of the SHC reaction zone effluent provides an additional possibility for integration with the coker, and particularly via the upgrading of the SHC pitch in the coker to provide coke and lighter hydrocarbons such as SHC vacuum gas oil (VGO).

A fluid catalytic cracking catalyst exhibiting reduced coke make comprises a zeolite cracking component in a matrix of gibbsite having a median particle size of not more than 0.4 microns and preferably not more than 0.3 microns. The zeolite cracking component will normally be a faujasite, with preference to zeolite Y in its various forms such as Y, HY, REY, REHY, USY, REUSY and secondary zeolite additives may be present, including ZSM-5.

The invention discloses a device and a method for reducing the temperature of catalytic cracking regenerated catalyst in the field of petrochemical industry catalytic cracking and aims to solve the problems that the method for reducing the temperature of catalytic cracking regenerated catalyst has a small application range in the prior art, and the like. The device comprises a regenerated catalyst cooler (4) arranged below a regenerator (1) and the bottom head of the cooler is internally provided with a cooling main air distributor (8). A sleeve (5) is arranged between the top of a taper section of the regenerated catalyst cooler and the bottom of the regenerator and provided with a regenerated catalyst conveying pipe (3) internally, and an annular space (6) is formed between the sleeve and the conveying pipe. A regenerated inclined pipe (11) is arranged between the regenerated catalyst cooler and a heavy oil riser reactor (12) of a catalytic cracking device. The invention also discloses a method for reducing the temperature of catalytic cracking regenerated catalyst by adopting the device. The device and the method can be used for setting a catalytic cracking device of a single heavy oil riser reactor and a plurality of riser reactors.

The invention relates to a revivification method for a catalytic cracking waste catalyst, which is characterized in that composite acid and ammonium salt are treated, and at least one of a supported rare earth treatment process and a phosphorus-containing acid treatment process is employed. a principle is characterized in that by improving a tunnel structure of the catalyst, composite acid is used for dredging the tunnel of the catalyst, a part of structure of molecular sieve is reconstructed through reaction and calcinations, acidity of the catalyst is adjusted by a rare earth compound-containing and/or phosphate-containing compound, so that waste catalyst performance can be recovered, the specific surface and activity of the recovered catalyst can be obviously increased, stability is obviously increased, good liquefied gas and low carbon olefin selectivity can be presented, green coke is reduced, liquid recovery is increased, gasoline RON is increased by 0.5-3 points, propylene and butylene yield can be respectively increased by more than 20-40% and 10-30%.

The present invention provides a modified Y-type molecular sieve, characterized by having a unit cell size of 2.420-2.440 nm; as percent by weight of the modified Y-type molecular sieve, a phosphorus content of 0.05-6%, a RE₂O₃ content of 0.03-10%, and an alumina content of less than 22%; and a specific hydroxyl nest concentration of less than 0.35 mmol/g and more than 0.05 mmol/g,

wherein M_{200° C.}, M_{500° C.} and M_{800° C.} respectively represent the weight loss percents of a sample measured at 200° C., 500° C. and 800° C., and C is the crystallinity of the sample. The modified Y-type molecular sieve has few defect in the crystal lattice. The application of the zeolite in the catalytic cracking catalyst as active component can maintain a long period stable activity, effectively control the coke yield and increase the heavy oil utilization. The present invention also relates to the preparing method and the use of the modified Y-type molecular sieve.

The present invention discloses a catalytic cracking catalyst and a preparation process therefor. The catalytic cracking catalyst comprises a cracking active component, 10 wt %-70 wt % of a clay on the dry basis, and 10 wt %-40 wt % of an inorganic oxide binder (as oxide), relative to the weight of the catalytic cracking catalyst, wherein said cracking active component contains, relative to the weight of the catalytic cracking catalyst, 10 wt %-50 wt % of a modified Y-type zeolite on the dry basis and 0-40 wt % of other zeolite on the dry basis, wherein said modified Y-type zeolite is characterized by having a unit cell size of 2.420-2.440 nm; as percent by weight of the modified Y-type zeolite, a phosphorus content of 0.05-6%, a RE₂O₃ content of 0.03-10%, and an alumina content of less than 22%; and a specific hydroxy nest concentration of less than 0.35 mmol/g and more than 0.05 mmol/g.

A catalytic conversion method of hydrocarbon oil comprises the following steps: leading the mixture of preheated light hydrocarbon oil and heavy hydrocarbon oil in a reactor from the bottom to contact a catalyst from a regenerator to carry out catalytic cracking reaction, the mixture and the catalyst flowing upward together, leading the reaction product and a spent catalyst with coke out of the reactor from an outlet on the upper part of the reactor, the reaction product and the spent catalyst entering into an oiling agent separation system, recycling the separated catalyst after stripping, burning and regenerating and the separated reaction oil and gas entering into a subsequent separation system to separate the product. The method provided by the invention can reduce the yield of the coke and increase the yields of the gasoline and the liquefied gas.

The invention discloses a catalytic cracking method and device employing double lift pipes in the petrochemical industry. The method comprises the following steps: carrying out heavy oil fluid catalytic cracking and light dydrocarbon catalytic reforming by adopting two lift pipes respectively, wherein the heavy oil catalytic cracking oil agent contact time is 0.2-1.5 seconds; carrying out gas-solid separation on two material flows by virtue of special cyclone separators; feeding a spent catalyst into a first turbulent bed regenerator after steam stripping, and contacting main air of the first turbulent bed regenerator in a down-flow manner, so as to burn off 40%-50% of generated coke; lifting a first section of semi-regenerated catalyst by smoke which is generated by the first turbulent bed regenerator to enter a tubular regenerator, and contacting the smoke which is generated by the first turbulent bed regenerator in a down-flow manner, so as to burn off 40%-50% of generated coke; feeding a second section of semi-regenerated catalyst into a second turbulent bed regenerator, and contacting main air of the second turbulent bed regenerator in a countercurrent manner, so as to burn off the residual generated coke; and returning the regenerated catalyst to the two lift pipes to recycle. The invention discloses a catalytic cracking device employing double lift pipes for achieving the method.

The present invention provides a delayed coking process comprising a step of subjecting a mixed feed comprises residual heavy hydrocarbon feedstock and bio oil obtained from fast pyrolysis of lignocellulosic biomass of one or more of Jatropha, Cashew nut, Karanjia and Neem to a delayed coking process and a system for the delayed coking process.

The present invention provides an ultra-stable rare earth type Y molecular sieve and the preparation method thereof, which method is carried out by subjecting a NaY molecular sieve as the raw material to a rare earth exchange and a dispersing pre-exchange, then to an ultra-stabilization calcination treatment. The molecular sieve comprises 1 to 20% by weight of rare earth oxide, not more than 1.2% by weight of sodium oxide, has a crystallinity of 51 to 69%, and a lattice parameter of 2.451 nm to 2.469 nm. In contrast to the prior art, in the molecular sieve prepared by this method, rare earth ions are located in sodalite cages, which is demonstrated by the fact that no rare earth ion is lost during the reverse exchange process. Moreover, the molecular sieve prepared by such a method has a molecular particle size D(v,0.5) of not more than 3.0 μm and a D(v,0.9) of not more than 20 μm. Cracking catalysts using the molecular sieve as an active component is characterized by a high heavy-oil-conversion capacity and a high yield of valuable target products.

The invention discloses a supported hierarchical-pore HZSM-5 catalyst. The catalyst is prepared by the following steps: depositing active metal on carbon nano particles by an atomic layer deposition method, putting the carbon nano particles into a precursor solution prepared from an aluminum source, a silicon source, an organic template agent and water, carrying out a hydrothermal reaction, and carrying out ion exchange with a NH4Cl solution, so as to obtain the supported hierarchical-pore HZSM-5 catalyst. The supported hierarchical-pore HZSM-5 is synthesized with the combination of the atomiclayer deposition technology, and the active metal is positioned in the pore canals of a molecular sieve, so that the active metal is introduced, and meanwhile mesoporous is also introduced. Differentfrom the common impregnation method, the preparation method provided by the invention reduces the metal supported on the surface of the molecular sieve, and thereby reduces the acidity influence on the surface of the molecular sieve. Meanwhile, when the catalyst provided by the invention is applied to the catalytic pyrolysis reaction of cellulose, the yield rates of aromatic hydrocarbons and olefins are greatly improved compared with the yield rates of aromatic hydrocarbons and olefins by using a conventional molecular sieve, and the coke yield rate is greatly reduced compared with the coke yield rate by using the conventional molecular sieve.

A method for improving the distribution of products in catalytic cracking process features that an enhancer is proportionally used as one of raw materials to increase the output rate of light oil andtotal rate of liquid, and decrease the output rate of coke.

The invention discloses a double-lifted pipe catalytic cracking device. The double-lifted pipe catalytic cracking device mainly comprises a heavy oil lifting pipe, a light hydrocarbon lifting pipe, a settlement device, regenerators and a catalyst cooler. The regenerators comprise a baffle plate regenerator and a turbulent bed regenerator, the baffle plate regenerator, the turbulent bed regenerator, and the catalyst cooler are coaxially arranged from top to down, the baffle plate regenerator is composed of an outer tube and an inner tube; a top of a circle bench-type cylindrical shell of the catalyst cooler is taken as a main wind outlet of the catalyst cooler for connecting with the bottom of a prevulcanization segment of the inner tube of the baffle plate regenerator; the bottom of the settlement device is communicated to a spent catalyst of the baffle plate regenerator, and the bottom of the catalyst cooler is respectively communicated to the bottom of the heavy oil lifting pipe and the light hydrocarbon lifting pipe through pipelines. By adopting the device disclosed by the invention, various heavy oil feed stocks and light hydrocarbon feed stocks are processed, a relatively short oiling agent contact time can be achieved, and the product quality is improved.

The invention relates to a large-pore-diameter high-bulk-density continuous reforming catalyst, preparation thereof and applications of the catalyst. The catalyst comprises following components by mass, based on elements, 0.01-1.0% of a VIII-group metal, 0.01-1.0% of an IVA-group metal, and 0.2-3.0% of a halogen, wherein the VIII-group metal is platinum, the IVA-group metal is germanium or tin, the bulk density of the catalyst is 0.58-0.90 g/mL, the most probable pore diameter is 8-20 nm, and the specific surface area is 170-210 m<2>/g. The catalyst is applied in a continuous reforming process, and is high in activity, high in xylene yield and low in coke yield.

The invention discloses a fluid catalytic cracking device in a petrochemical industry. The device mainly comprises a first tubular reactor with reaction section length of 5-15m, a second tubular reactor with reaction section length of 5-10m, a sedimentation device, a gas-solid separator, a regenerator composed of a baffle pipe-type separator and a turbulent bed separator, a first-grade regenerated catalyst cooler, a second-grade regenerated catalyst cooler, a low-temperature regenerated catalyst tank and pipes connected to corresponding devices. The baffle pipe-type separator mainly comprises a housing, an outer pipe and an inner pipe. The housing comprises a housing pipe, a transition section and an outlet pipe connected in series from top to bottom. Circular passages are formed between the housing pipe and the outer pipe and between the outer pipe and the inner pipe. The separator wall at the bottom of the inner pipe is provided with a regenerated catalyst inlet and an inlet of a catalyst to be regenerated. The separator wall at the bottom of the housing pipe is provided with a main air inlet pipe. The device can be used for heavy oil catalytic cracking and gasoline catalytic modification.

The present invention relates to a catalytic conversion process for improving the product distribution, characterized in that a feedstock oil of good quality is contacted with a hot regenerated catalyst having a lower activity in a reactor to carry out a cracking reaction, the reaction product is separated from the spent catalyst to be regenerated, then the reaction product is fed into a separation system, and the spent catalyst to be regenerated is stripped, regenerated and recycled in the process. The isobutene content in the liquefied petroleum gas (LPG) produced by the process is increased by a factor of more than 30%, and the olefin content in the gasoline composition may be increased to more than 30 wt. %. The product distribution is optimized, and the yields of dry gas and coke are decreased, so as to sufficiently utilize the petroleum resources.

A method for producing chemicals from crude oil by double-tube parallel multi-zone catalytic conversion is provided. The method may include the following steps: feeding the crude oil directly or separating the crude oil into light and heavy components by flash evaporation or distillation after desalination and dehydration; strengthening the contact and reaction between oil gas and catalyst by using two parallel reaction tubes with novel structure, controlling the reaction by zones, carrying out optimal combination on feeding modes according to different properties of reaction materials, controlling suitable reaction conditions for different materials, and increasing the production of light olefins and aromatics.

The invention discloses a double-riser catalytic cracking method and device in petroleum chemical industry. The catalytic cracking method is as follows: respectively performing heavy oil catalytic cracking reaction and light hydrocarbon catalytic modification reaction by use of double risers, wherein the heavy oil catalytic cracking oil agent contact time is 0.2-1.5e; respectively performing gas-solid separation on two reaction material flows by use of respective special cyclone separators; respectively entering two reaction oil and gas flows into respective special fractionating towers for fractional distillation; after steam stripping of a spent catalyst, entering the spent catalyst into a baffle tubular regenerator, after mixing with a uncooled cycle regenerated catalyst, burning off more than 90% of generated coke by main air co-current contact with the baffle tubular regenerator, entering a semi regenerated catalyst into a turbulent bed regenerator, burning off the rest generated coke by main air countercurrent contact with the turbulent bed regenerator, and returning the regenerated catalyst into the risers for recycling use. The invention discloses a double-riser catalytic cracking device for realizing the catalytic cracking method. The double-riser catalytic cracking method and device can be used for heavy oil catalytic cracking and light hydrocarbon catalytic modification.