3422 results about "Cracking reaction" patented technology

The invention disclosed a catalyst to lower the freezing point of the diesel oil. The catalyst includes carrier that contains reshaped molecular sieve and hydrogenated metal. The molecular sieve is reshaped by VIB group metal, the content of which in the molecular sieve is 1wt%-40wt% (by oxidation state). The content of the molecular sieve and the metal are 10wt%-90wt% (by oxidation state) and 0.1wt%-40wt% (by oxidation state) respectively. The reshaping agent can modify the acid substance and the bore size on the surface of the molecular sieve so as to match the catalyst's isomerizing function and structure-selective splitting function well; it can make the splitting reaction proceeds according to the lock-and-key mechnanism and ensure the reaction proceeds properly without over splitting; it can improve the quality of the diesel oil and increase its yield. The invention can be used in the deparaffinage of the material that contains wax, especially in the process to lower the freezing point of the diesel oil distillate. It can not only lower the freezing point, but also increase the diesel oil yield substantially.

The invention discloses a diesel oil hydrogenation pour point depressing method. A series flow of hydrofining and hydrogenation pour point depressing is adopted in the method, wherein a hydrogenation pour point depressing catalyst is modified by metal auxiliary agent and silicon, effectively regulates the acidity and orifice shape of the inner surface and the outer surface of a shape-selective cracking molecular sieve, is favorable for dispersing wax molecules in a diesel oil raw material into pore canals of the molecular sieve to perform shape-selective cracking reaction, and has high catalytic activity and selectivity of a target product; and because the acidity of the outer surface of the molecular sieve is weak, side reactions such as secondary cracking and the like are reduced, the pour point depressing effect of the diesel oil is good, and the fraction yield of the diesel oil is high.

The invention discloses a catalytic conversion method for preparing ethylene, propylene and aromatic hydrocarbon. Hydrocarbon raw material with different cracking performances is contacted with a catalytic cracking catalyst, and cracking reaction is carried out in a fluidized bed reactor under the conditions that the temperature is 550 DEG C to 800 DEG C, the weight hourly space velocity is 0.1-800h<-1>, the reaction pressure is 0.10MPa to 1.0MPa, the weight ratio of the catalytic cracking catalyst and the raw material is 10-150, and the weight ratio of steam and the raw material is 0.15-1.0.Then a spent catalyst and reaction oil gas are separated, the spent catalyst returns to the reactor after regeneration, and the target products comprising low carbon olefin and the aromatic hydrocarbon are obtained by separating the reaction oil gas, wherein, fraction with the temperature to be 160 DEG C to 260 DEG C returns for catalytic cracking as circulating material, and the ethylene and the propylene are further obtained by cracking of ethane, propane, butane, and the steam entered. Low carbon olefin such as ethylene, propylene, and the like, is produced from heavy feedstock to the utmost extent in the method, and the yield of the ethylene and the propylene is over 20% by weight, in addition, the aromatic hydrocarbon such as toluene, xylene, and the like, are produced in an integrated way.

The present invention relates to a process and system for gasifying biomass or other carbonaceous feedstocks in an indirectly heated gasifier and provides a method for the elimination of condensable organic materials (tars) from the resulting product gas with an integrated tar removal step. More specifically, this tar removal step utilizes the circulating heat carrier to crack the organics and produce additional product gas. As a benefit of the above process, and because the heat carrier circulates through alternating steam and oxidizing zones in the process, deactivation of the cracking reactions is eliminated.

The method according to the invention allows the formation of oil and the retention phenomenon in the mother rock to be modelled. Organic matter characterization experiments are used to establish the molecular model (MM) of the initial sample (E). The thermal cracking reaction of this molecular model is reproduced by dynamic molecular simulation computations with a reactive force field (RMD) and validated by comparison with experimental data. The reaction mechanism obtained (SR) allows to carry out a kinetic study (C) by variation of the temperature parameter. The phase equilibria (PES) of the reaction medium are determined at any time from dynamic simulation. The successive phase equilibrium assessments at various progress stages of the cracking reaction allow following the physicochemical evolution (PC) of the thermal maturation of the organic sample studied. The free hydrocarbons (liquid and gaseous) that are not retained in the solid residue can be quantified throughout numerical modelling of the sample maturation; representing, in the sedimentary basins, the hydrocarbons that are not retained in the organic matrix of the mother rock (Q). This quantity can be used as an indicator or an input value for the retention threshold in basin models.

The invention discloses a preparation method of a skeleton silicon-rich Y-shaped molecular sieve, comprising the following steps of: firstly, carrying out desiliconizing pretreatment on a NaY molecular sieve with alkali lye and secondly carrying out ammonium exchange and dealumination and silicon reinsertion on the molecular sieve treated with alkali. The alkali treatment condition is to pulp and evenly mix the NaY molecular sieve and an alkali liquor in the mass ratio of NaY (dry basis): alkali: H2O being (0.1-2): (0.05-2): (4-15) and carry out alkali treatment at 0-120 DEG C for 0.1-24h. Compared with a product obtained by carrying out ammonium exchange and silicon-rich treatment on the NaY molecular sieve, the skeleton silicon-rich Y-shaped molecular sieve subject to the desiliconizing pretreatment has higher infrared acid quantity, B acid quantity and secondary pore content. A catalyst prepared from an active component which is the skeleton silicon-rich Y-shaped molecular sieve prepared by the method has stronger heavy oil transformation capability and higher light oil recovery rate when being used for a heavy oil cracking reaction.

A catalytic conversion method for preparing propylene and high-octane gasoline comprises the following steps: raw materials which are difficult to be cracked are firstly contacted with a thermal regeneration catalytic cracking catalyst to carry out cracking reaction under the conditions that the reaction temperature is 600-750 DEG C and the weight hourly space velocity is 100-800h<-1>, the reactant flow is mixed with raw oil which is easy to be cracked to carry out the cracking reaction under the conditions that the reaction temperature is 450-620 DEG C and the weight hourly space velocity is 0.1-100h<-1>; the spent catalyst and reaction oil and gas are separated, the spent catalyst returns to a reactor after regeneration, the reaction oil and gas are separated to obtain propylene and gasoline, and hydrogenated heavy oil obtained by hydrotreating fractions above 260 DEG C is taken as raw oil of the catalytic cracking device or a conventional catalytic cracking device. The method improves the yield and the selectivity of the propylene, increases the yield of the high-octane gasoline, reduces the yield of dry gas, greatly increases the yield of liquid and realizes the high-efficient utilization of petroleum resources.

The present invention comprises a thermocatalytic cracking process for the production of diesel oil from a charge of vegetable origin made from seeds of oleaginous plants in refineries possessing at least two FCC reactors. At least -one of such reactors processes heavy gas oil or residue under conventional conditions whilst at least one of such reactors processes the charge of vegetable origin made from seeds of oleaginous plants under conditions suitable, for production of diesel oil. Said process employs the same catalyst utilised in the fluid catalytic cracking process which, simultaneously, processes a conventional charge.

The diesel, or biodiesel, oil produced by means of said process is of superior quality having a cetane number exceeding 40 given that the cracking reactions occur at low temperatures and the products obtained are less oxidised and consequently purer than products obtained by means of existing technology.

The invention provides a catalytic conversion method for producing gasoline containing rich aromatic hydrocarbon. The catalytic conversion method comprises the following steps: cutting catalytic cracking light cycle oil to obtain a light fraction and a heavy fraction, performing hydrogenation treatment on the heavy fraction to obtain a hydrogenated heavy fraction, singly and respectively conveying the light fraction and the heavy fraction into different riser reactors of catalytic cracking devices, performing a cracking reaction in the presence of a catalytic cracking catalyst, and separating reaction products to obtain a product containing the gasoline which contains rich aromatic hydrocarbon and the light cycle oil. According to the method, single catalytic cracking devices are used for processing the light fraction and the hydrogenated heavy fraction of the light cycle oil to satisfy harsh conditions necessary for the catalytic cracking reaction of different fractions of the light cycle oil to the maximum, so as to produce catalytic gasoline containing rich benzene, toluene and xylene to the maximum.

The invention relates to a catalytic conversion method for preparing lower olefins and aromatics. Raw oil with different cracking performances enters different reaction zones of a first riser reactor to contact with a catalytic cracking catalyst for cracking reaction to separate a spent catalyst from reaction oil gas, wherein the reaction oil gas is separated to obtain a product containing lower olefins, gasoline, distillates with distillation range of 180-250 DEG C and catalytic wax oil, wherein the gasoline is extracted by light aromatics to obtain light aromatics and gasoline raffinate; the raw materials are cracked to be sent into a second riser reactor to contract with a hot regenerated catalyst for catalytic conversion; and the spent catalysts of the two riser reactors are burned and regenerated in the same one regenerator and then returns to the two riser reactors. The method uses heavy raw materials to furthest produce the lower olefins, such as propylene, ethylene, and the like, particularly the propylene, the production rate can exceed 40 wt%, and at the same time the method can coproduce the aromatics, such as toluene, xylene, and the like.

The invention relates to a catalysis conversion method for producing aromatic compounds. According to the method, poor quality heavy cycle oil and residual oil are subjected to a hydrotreating reaction in the presence of hydrogen gas and a hydrogenation catalyst, and the reaction products are separated to obtain gas, naphtha, hydrogenated diesel oil and hydrogenated residue oil, wherein the hydrogenated diesel oil enters a catalysis cracking device and is subjected to a cracking reaction in the presence of a catalysis cracking catalyst, the reaction products are separated to obtain dry gas, liquefied gas, catalytic gasoline containing rich benzene, toluene and xylene, catalytic light diesel oil, distillates with a distillation range of 250-450 DEG C, and an oil slurry, and the distillates with the distillation range of 250-450 DEG C are conveyed to a residue oil hydrotreating device so as to be recycled. According to the present invention, the residue oil hydrogenation condition is completely utilized to achieve saturation of the aromatic ring in the poor quality heavy cycle oil to the maximal degree, such that the hydrogenated diesel oil maximally produce benzene, toluene and xylene during catalysis cracking.

The invention relates to a heavy oil lightening method and technique. The method comprises steps as follows: raw oil is introduced into a thermal cracking reactor through a feed system, and mixed with a high-temperature solid heat carrier from a combustion (gasifying) reactor, so that the raw oil is subjected to fluidizing heat exchange with the solid heat carrier and carries out thermal cracking reaction on the surface of the solid heat carrier; the cracking gas generated by the thermal cracking reaction and a light component product are subjected to steam stripping by fluidizing medium gas and enter a subsequent absorption and stabilization system and a purification and separation system, heavy coke (petroleum coke) is attached to the surface of the solid heat carrier and enters the combustion (gasifying) reactor via a material returning valve, and an oxidizing (gasifying) and fluidizing gas is introduced to realize combustion (gasifying) reaction in the fluidization elevation process of the petroleum coke; and after the reaction product (fume or gasified gas) and the solid heat carrier are separated by a gas-solid separator, the fume (gasified gas) is led into a waste heat recovery system and a gas purification system, the high-temperature solid heat carrier is distributed by a distribution valve and respectively enters the thermal cracking reactor and the combustion (gasifying) reactor for cyclic use, and the collected fly ash can be used after further processing, thereby complete high-value conversion and use of the heavy oil.

The invention provides a catalytic conversion method for producing gasoline containing rich aromatic compounds. The catalytic conversion method comprises the following steps: cutting catalytic cracking light cycle oil to obtain a light fraction and a heavy fraction, performing hydrogenation treatment on the heavy fraction to obtain a hydrogenated heavy fraction, singly conveying the light fraction and the hydrogenated heavy fraction into catalytic cracking devices from different nozzles in a layering manner, performing a cracking reaction in the presence of a catalytic cracking catalyst, and separating reaction products to obtain a product containing the gasoline which contains rich aromatic compounds and the light cycle oil. According to the method, single catalytic cracking devices are used for processing the light fraction and the hydrogenated heavy fraction of the light cycle oil, and the light fraction and the heavy fraction enter the catalytic cracking devices in the layering manner, so that the harsh conditions necessary for the catalytic cracking reaction of different fractions of the light cycle oil can be optimized and satisfied to the maximum, so as to produce catalytic gasoline containing rich benzene, toluene and xylene to the maximum.

The present invention relates to a technological process for producing low-sulfur low-olefin clean gasoline by using catalytic cracked gasoline and catalyst used by said process. Said invention adopts hydrofinishing and aromatization combined process, in which the aromatization adopts small-grain hydrogen type molecular sieve catalyst including IA group metal, transition metal and lanthanide series rare-earth metal oxide, and the crystal grain size of the molecular sieve is in the range of 20nm-800 nm. Said invented catalyst can reduce cracking reaction and can raise the yield of the gasoline.

The invention discloses a method for resource recovery and classification utilization of urban domestic wastes, which at least comprises the following steps of: a magnetic separation step, a waste cutting step, a elutriation flotation step, a waste extrusion dehydration step, an anaerobic treatment step and a sludge deposition concentration step; scrap iron is separated by the magnetic separationstep for the recovery and utilization of the scrap iron; anaerobic organic matter is crushed by the waste cutting step; pasty organic matter and block non-anaerobic wastes are thoroughly separated bythe elutriation flotation step so as to allow the pasty anaerobic organic matter to enter a biogas generation pool or tank for an anaerobic reaction and to allow the clean non-anaerobic wastes to be extruded, dehydrated and dried for individual treatment, and the waste decrement is above 90%; after elutriation, the left 10% non-anaerobic wastes are prepared into fuel oil by a cracking reaction; or are recycled through screening with no screening difficulty being caused by dust and organic matter containing in the wastes; or are delivered into a gasifier for fuel gas production, which preventsthe energy consumption of water-containing organic matter during waste incineration treatment, and greatly increases the thermal efficiency of waste treatment.

The invention discloses a method for enhancing the gas-liquid mass transfer of an ebullated bed hydrogenation reactor, which comprises the following processes of: introducing fresh raw oil, circulating oil and hydrogen into a microbubble generator arranged in front of the reactor, fully mixing to make the hydrogen dispersed in a liquid-phase material in the form of microbubbles, and performing hydrogenation and cracking reaction in the ebullated bed reactor. The method can improve the utilization rate of the hydrogen, reduce the volume ratio of the hydrogen to the oil, save operating cost andpromote the depth of the hydrogenation and cracking reaction.

The invention relates to a preparation method for a nano-Y-shaped molecular sieve/amorphous silicon-aluminum composite material. According to the method, a guiding agent is synthesized, and a surfactant is added during the guiding agent synthesizing process; a surfactant is added during a preparation and synthesis process of gel of the Y-shaped molecular sieve, and a hydrothermal crystallization method is adopted to synthesize the nano-Y-shaped molecular sieve; an aqueous solution of a mixture is added to the slurry containing the nano-Y-shaped molecular sieve, wherein the mixture comprises water glass and an aluminum source; an acid is added to adjust the pH value to 7-9.5 to form the gel; the gel is washed, dried and baked to obtain the composite material. According to the present invention, the grain of the Y-shaped molecular sieve in the composite material prepared by the method of the present invention is maintained to less than 100 nm, and the composite material of the present invention is suitable for catalytic cracking reactions and hydrocracking reactions of heavy oil macromolecules.

The low carbon olefin and arene producing process includes the following steps: hydroprocessing material oil to obtain hydrogenated tail oil; catalytically cracking and separating catalytically cracked oil and gas to obtain C2=-C3=, C2o-C3o, C4-C5, naphtha, LCO, etc.; returning C4-C5 to catalytical cracking, returning LCO to hydroprocessing, selectively hydrogenating and solvent extracting naphtha to obtain raffinate oil and arene as one target product; steam cracking raffinate oil, hydrogenated C2o-C4o, hydrogenated naphtha and cracked C2o-C3o and separating reacted oil and gas to obtain C2=-C3=, C2o-C3o, C4-C5, naphtha, etc.; returning C2o-C3o to steam cracking, and returning C4-C5 to catalytical cracking. The producing apparatus includes hydroprocessing unit, atalytically cracking unit, steam cracking unit, selectively hydrogenating unit and solvent extracting unit. The present invention produces low carbon olefin with heavy material and has propylene yield over 30 wt% and co-produced toluene, etc.

The invention provides a catalysis conversion method used for preparing arene and low carbon olefin; the raw material with the distilling range of 160-260 DEG C contacts a catalytic cracking catalyst, so as to carry out the cracking reaction inside a fluidized bed reactor under the conditions of 450-750 DEG C of temperature, 0.1-800h<-1> of weight hourly space velocity, 0.10-1.0MPa of pressure, 1-150 of weight ratio of catalyst to raw material and 0.05-1.0 of weight ratio of water vapour to raw material; a spent catalyst and reaction oil gas are separated, and the spent catalyst is returned to the reactor after regeneration; the reaction oil gas is separated so as to gain the object outcome: low carbon olefin and arene. The method greatly increases the yield and selectivity of the ethane and propylene, the yield of the gasoline and the yield of the arene in the gasoline are extremely high, only little heavy oil is generated; furthermore, the yield of coke is low.