1891 results about "Catalyst regeneration" patented technology

Disclosed is a process for making middle distillate and lower olefins. The process includes catalytically cracking a gas oil feedstock within a riser reactor zone by contacting under suitable catalytic cracking conditions within the riser reactor zone the gas oil feedstock with a middle distillate selective cracking catalyst that comprises amorphous silica alumina and a zeolite to yield a cracked gas oil product and a spent cracking catalyst. The spent cracking catalyst is regenerated to yield a regenerated cracking catalyst. Within an intermediate cracking reactor such as a dense bed reactor zone and under suitable high severity cracking conditions a gasoline feedstock is contacted with the regenerated cracking catalyst to yield a cracked gasoline product and a used regenerated cracking catalyst. The used regenerated cracking catalyst is utilized as the middle distillate selective catalyst.

The invention discloses a regeneration fluid for an SCR denitration catalyst, which comprises the following components: 0.001 to 1 weight percent of penetration enhancer JFC, 0.001 to 1 weight percent of surfactant OP-10, 0 to 1 weight percent of peregal, 0.6 to 4 weight percent of ammonium metavanadate, 5.5 to 12.5 weight percent of ammonium paratungstate, 0 to 6.5 weight percent of ammonium paramolybdate, and the balance of deionized water and acid. The regeneration fluid has the advantages that the regeneration fluid can also supplement active ingredients during the washing, and the activity recovery of the catalyst after the regeneration is up to between 90 and 105 percent; a nonionic surfactant is added into the regeneration fluid, so that the regeneration fluid improves the cleaning capability on the catalyst and cannot cause the damage to a catalyst carrier and other effective ingredients; and the regenerated catalyst fully can continue to be normally used, and the service life can reach more than 95 percent of that of a new catalyst.

The invention relates to a catalyst used for catalyzing and dehydrogenation of low-carbon alkane and the method of producing propylene by alkane catalyzing and dehydrogenation with the catalyst. The former catalyst used for catalyzing and dehydrogenation of low-carbon alkane, each molecule of the hydrocarbon has about 2 to 8 carbon atom, which is characterized in that: the catalyst makes a molecular sieve the carrier, the Pt family metal is loaded on the carrier as the active component, makes the IVA family metal element and alkalinity metal element as additional agent and high temperature standing inorganic oxide as connection agent; when the catalyst is used in producing propylene by alkane catalyzing and dehydrogenation, the reaction temperature is 500 to 700 DEG C., the pressure is 0 to 0.2Mpa, the quality air speed is 2 to 5h to 1, the regenerating temperature of the catalyst is 500 to 700 DEG C., the air speed is 100 to 1000h to 1, the pressure is 0 to 1.0MPa. With adopting the invention, the reaction of producing propylene by alkane catalyzing and dehydrogenation is good, the average transforming rate is 30 per cent, the selectivity above 95 per cent can keep for 50 days.

The invention relates to a catalyst for preparing olefin by dehydrogenating low-carbon alkane, and a preparation method and an application thereof, which belong to the technical field of the preparation of basic organic chemical raw materials. The catalyst is prepared by a dipping method of using an aluminium silicophosphate molecular sieve as a carrier, VIII group or VIB group elements as active constituents and IVA group elements as an auxiliary agent. In the process for preparing olefin by dehydrogenating low-carbon alkane, the catalyst is firstly reduced by hydrogen gas, then participates in a reaction, and is finally regenerated. Compared with the existing catalyst for preparing olefin by dehydrogenating low-carbon alkane, the catalyst has a pore shape selecting function and moderate acidity, thereby the selectivity of the low-carbon alkane can reach more than 90 percent in the process for preparing olefin by dehydrogenating low-carbon alkane. The preparation method of the catalyst is simple; the regeneration process flow of the reaction has a large choice, a fixed bed, a fluidized bed or a moving bed can be used as a reactor, and the catalyst can be regenerated in the reactor or outside the reactor.

The invention discloses a method for desorbing oxysulphide and/or oxynitride in the regenerated fume of a catalytic cracking catalyst, and the method comprises that the fume is kept in contact with a sorbent, wherein, the sorbent is a catalytic cracking catalyst. The method for desorbing oxysulphide and/or oxynitride in the regenerated fume of the catalytic cracking catalyst which is provided by the invention adopts the catalytic cracking catalyst to replace existing specialized sorbents, thus fully achieving effects of desorbing oxysulphide and oxynitride at the same time, and as the catalytic cracking catalyst is not easy to reach saturation, the catalytic cracking catalyst can be regenerated for a plurality of times when taken as the sorbent; furthermore, after being taken as the sorbent, the catalyst can still be used in a catalytic cracking process, and the activity and reactivity of the catalyst which is taken as the catalytic cracking catalyst are not affected.

The invention discloses a method for removing hydrogen sulfide in a gas phase through oxidization under a high gravity field, which comprises the steps of: enabling a desulfurizing agent to be in a countercurrent or cross current contact with a hydrogen sulfide containing gas in a desulfurizing high gravity machine; and then adding the desulfurizing agent rich in sulphur in a sulphur sedimentation agent and then enabling the desulfurizing agent added with the sulphur sedimentation agent to be in a countercurrent or cross current contact with air in a regeneration high gravity machine, whereinthe desulfurizing agent is a mixed solution consisting of complex iron, aqueous alkali, a sulphur modifying agent and a defoaming agent, and in the mixed solution, the concentration of iron ions is 0.1-10g/L, pH is 8.0-9.2, the concentration of the sulphur modifying agent is 10-200ppm, and the concentration of the defoaming agent is 5-50ppm. The high gravity machine is used for replacing the traditional low-transfer-efficiency reactor, and a high gravity rotary packed bed reactor is adopted during hydrogen sulfide oxidization and catalyst regeneration, thus process transfer efficiency is greatly strengthened, and time of oxidization desulfurization and regeneration of a desulfurizing agent is shortened; in addition, the sedimentation agent is adopted in a sulphur sedimentation stage and acts together with the sulphr modifying agent, thus the sulphur sedimentation time is also greatly shortened.

The invention relates to an ammonia desulfurization and denitrification dedusting method and device utilizing catalytic cracking regeneration flue gas, comprising the following steps: enabling high-temperature catalyst regeneration flue gas coming from a catalytic cracking unit and containing catalyst dust to firstly enter a waste heat boiler I, reducing the temperature of the flue gas to 280-430 DEG C, wherein the heat of the flue gas is externally supplied by steam produced by the waste heat boiler I; enabling flue gas at temperature of 280-430 DEG C to enter a denitrification device for denitrification and enter a waste heat boiler II through an outlet flue after sufficiently reacting on the surface of a denitrification catalyst in a denitrification reactor; removing sulfur dioxide, nitric oxide and byproduct ammonium sulfate by taking ammonia as a reactant, and removing catalyst dust in the regeneration flue gas to achieve clean gas up-to-standard release; the three waste free release purifying method can be applied to catalytic cracking catalyst regeneration flue gas treatment in oil refining.

The invention discloses a low temperature Claus sulfur recovery process. The process mainly comprises a thermal reaction section, a catalytic reaction section and a tail gas incineration section, wherein in a combustion furnace of the thermal reaction section, partial hydrogen sulfide reacts with oxygen to be converted into sulfur dioxide, the hydrogen sulfide and the sulfur dioxide undergo a Claus reaction to generate sulfur, and process gas after sulfur separation enters the catalytic reaction section; in the reactor of each stage of the catalytic reaction section, the hydrogen sulfide and the sulfur dioxide under conventional Claus reaction, catalyst reactivation, sub-dewpoint and sub-solid point low temperature Claus reaction in sequence; after the catalyst reaction section, the tail gas which is subjected to sulfur separation enters the tail gas incineration section, and the tail gas is incinerated and exhausted in the tail gas incineration furnace. The process adopts a lower reaction temperature, contributes to performance of chemical equilibrium towards the direction of sulfur generation, so that conversion rate and recovery rate of sulfur are improved. Moreover, the process has the advantages of simple process flow, relative small equipment and investment, low operation cost and more contribution to environmental protection. The invention also discloses a device for the low temperature Claus sulfur recovery process.

The invention provides a catalyst for alkane dehydrogenation as well as a continuous reaction regeneration device and method using the catalyst for catalytic dehydrogenation. The catalyst comprises four ingredients, the ingredient A is oxides of one kind of element or several kinds of elements from Ti, Nb, Ta, Mo, W, Re, In or Ga, the ingredient B is one kind or several kinds of materials in MgO, P2O5, ZrO2, Al2O3 or SiO2, the ingredient C is oxides of one kind of material or several kinds of materials from Zn, Cd and Sn, and the ingredient D is one kind of material or a mixture of several kinds of materials from alkali oxides or alkaline earth metal oxides. The catalyst does not contain noble metal such as Pt and the like, does not contain toxic ingredients such as Cr and the like and cannot pollute the environment. The activity of the catalyst is high, the selectivity of olefin generated by alkane dehydrogenation is high, the stability of the catalyst is good, the mechanical intensity is high, the continuous reaction regeneration device is used for alkane dehydrogenation, the reaction and the catalyst regeneration are continuously carried out, the efficiency is high, and the safety is high.

A MFI-molecular sieve catalyst for preparing caprolactam from cyclohexanone oxime by gas-phase Beckmann rearrangement is prepared through proportionally mixing MFI-molecular sieve with alkaline silica gel, shaping, drying and calcining. It has high conversion rate and selectivity.

A catalyst regenerator for regenerating spent light FCC catalyst and heating the catalyst to supply heat to an FCC reactor. The regenerator has discharge outlets for catalyst and off gas and a valve for introducing spent catalyst through a central stand pipe portion. The regenerator houses a dense phase catalyst bed. A centerwell receives a lower end of the standpipe portion and defines an annulus therebetween. The spent catalyst is introduced through the standpipe portion into the annulus. A fuel distributor introduces fuel into the centerwell for mixing with the catalyst in the annulus. A fluidization distributor introduces fluidization gas into the centerwell for fluidizing the catalyst in the annulus. A radial slot in the centerwell introduces the catalyst and fuel mixture from the annulus below the upper surface of the dense phase bed. An air distributor located below the radial slot introduces combustion air into the dense phase bed.

A process and apparatus for the dehydrogenation of paraffins is presented. The process utilizes a reactor that includes a slower flow of catalyst through the reactor, with a counter current flow of gas through the catalyst bed. The catalyst is regenerated and distributed over the top of the catalyst bed, and travels through the bed with the aid of reactor internals to limit backmixing of the catalyst.

The performance of an endothermic catalytic dehydrogenation process is increased without requiring additional catalyst regeneration and reheat air flow and compression by partially prereacting the preheated hydrocarbon feed and then reheating the partially dehydrogenated effluent from the prereactor to the same hydrocarbon preheat temperature prior to the main catalytic reactor. The preferable source of the heat for reheating is the effluent air from the reheat and regeneration of the catalyst in the main reactor. This same effluent air is used to regenerate the catalyst in the prereactor as needed.

A method is disclosed for regenerating regenerating a used catalyst mixture comprising (i) an isomerization catalyst comprising magnesium oxide and (ii) a metathesis catalyst comprising an inorganic carrier and at least one of molybdenum oxide and tungsten oxide. The method comprises (a) decoking the used catalyst mixture in the presence of an oxygen-containing gas to produce a decoked catalyst mixture; and (b) contacting the decoked catalyst mixture with steam at a temperature in the range of 100 to 300° C. to produce a regenerated catalyst mixture.

A fixed-bed catalytic reformer unit is converted to moving bed reactor/cyclic regenerator operation by re-using the fixed bed reactors of the original unit as regenerator vessels operated in cyclic regeneration mode in a new catalyst regeneration section. A flow connection, suitably a liftpipe, is provided to convey spent catalyst from the spent catalyst outlet of a new moving bed reactor section to the converted regenerator section, together with a flow connection for regenerated catalyst from the regenerator section to the regenerated catalyst inlet of the new moving bed reactor section. A flow control distributor directs spent catalyst sequentially to each of the regenerator vessels to carry out the regeneration with regeneration gas. Each regenerator vessel is cycled through a fill, regeneration, discharge sequence to maintain a continuous flow of catalyst to and from the reactor section.

A process and apparatus for the dehydrogenation of paraffins is presented. The process utilizes a reactor that includes a slower flow of catalyst through the reactor, with a counter current flow of gas through the catalyst bed. The catalyst is regenerated and distributed over the top of the catalyst bed, and travels through the bed with the aid of reactor internals to limit backmixing of the catalyst.