8542 results about "Fixed bed" patented technology

A multi-stage catalytic hydrogenation and hydroconversion process for heavy hydrocarbon feed materials such as coal, heavy petroleum fractions, and plastic waste materials. In the process, the feedstock is reacted in a first-stage, back-mixed catalytic reactor with a highly dispersed iron-based catalyst having a powder, gel or liquid form. The reactor effluent is pressure-reduced, vapors and light distillate fractions are removed overhead, and the heavier liquid fraction is fed to a second stage back-mixed catalytic reactor. The first and second stage catalytic reactors are operated at 700-850.degree. F. temperature, 1000-3500 psig hydrogen partial pressure and 20-80 lb./hr per ft.sup.3 reactor space velocity. The vapor and light distillates liquid fractions removed from both the first and second stage reactor effluent streams are combined and passed to an in-line, fixed-bed catalytic hydrotreater for heteroatom removal and for producing high quality naphtha and mid-distillate or a full-range distillate product. The remaining separator bottoms liquid fractions are distilled at successive atmospheric and vacuum pressures, low and intermediate-boiling hydrocarbon liquid products are withdrawn, and heavier distillate fractions are recycled and further upgraded to provide additional low-boiling hydrocarbon liquid products. This catalytic multistage hydrogenation process provides improved flexibility for hydroprocessing the various carbonaceous feedstocks and adjusting to desired product structures and for improved economy of operations.

The invention relates to a method for the catalytic hydro-processing of a petroleum feedstock of the gas oil type and of a biological feedstock containing vegetal oils and/or animal fats, in a catalytic fixed-bed hydro-processing unit, said method being characterised in that the petroleum feedstock is introduced into the reactor upstream from the biological feedstock. The invention also relates to a catalytic hydro-processing unit for implementing said method, and to a corresponding hydro-refining unit.

The average propylene cycle yield of an oxygenate to propylene (OTP) process using a dual-function oxygenate conversion catalyst is substantially enhanced by the use of a combination of: 1) moving bed reactor technology in the catalytic OTP reaction step in lieu of the fixed bed technology of the prior art; 2) a separate heavy olefin interconversion step using moving bed technology and operating at an inlet temperature at least 15° C. higher than the maximum temperature utilized in the OTP reaction step; 3) C₂ olefin recycle to the OTP reaction step; and 4) a catalyst on-stream cycle time of 700 hours or less. These provisions hold the build-up of coke deposits on the catalyst to a level which does not substantially degrade dual-function catalyst activity, oxygenate conversion and propylene selectivity, thereby enabling maintenance of average propylene cycle yield for each cycle near or at essentially start-of-cycle levels.

This invention relates to methods for reacting a hydrocarbon, molecular oxygen, and optionally water and/or carbon dioxide, to form synthesis gas. The preferred embodiments are characterized by delivering a substochiometric amount of oxygen to each of a multitude of reaction zones, which allows for optimum design of the catalytic packed bed and the gas distribution system, and for the optimization and control of the temperature profile of the reaction zones. The multitude of reaction zones may include a series of successive fixed beds, or a continuous zone housed within an internal structure having porous, or perforated, walls, through which an oxygen-containing stream can permeate. By controlling the oxygen supply, the temperatures, conversion, and product selectivity of the reaction can be in turn controlled and optimized. Furthermore the potential risks of explosion associated with mixing hydrocarbon and molecular oxygen is minimized with increased feed carbon-to-oxygen molar ratios.

The invention relates to a selective hydrogenation method of high unsaturated hydrocarbons in C4 fractions, which is characterized in that salvage stores which are rich in acetylene hydrocarbon and prepared by extracting butadiene are used as the material, and a fixed bed reactor is adopted to obtain 1, 3-budiene by selective hydrogenation under the existence of a catalyst. The adopted process conditions are as follows: the reaction temperature is between 30 DEG C and 90 DEG C, the reaction pressure is between 1.0 MPa and 4.0 MPa and the liquid space velocity is 7 to 20h<-1>. The catalyst is preferably a palladium system catalyst with alumina as a carrier, the specific surface is 50 to 150m<2>/g and the specific pore volume is 0.25 to 1.0ml/g. The method has remarkable good effects on reducing waste of resources and improving economic benefits by effectively utilizing the salvage stores rich in acetylene hydrocarbon and prepared by extracting butadiene.

This invention relates to a novel integrated method for economically processing vacuum residue from heavy crude oils. This is accomplished by utilizing a solvent deasphalter (SDA) in the first step of the process with a C₃/C₄/C₅ solvent such that the DAO product can thereafter be processed in a classic fixed-bed hydrotreater or hydrocracker. The SDA feed also includes recycled stripper bottoms containing unconverted residue/asphaltenes from a downstream steam stripper unit. The asphaltenes from the SDA are sent to an ebullated-bed reactor for conversion of the residue and asphaltenes. Residue conversion in the range of 60-80% is achieved and asphaltene conversion is in the range of 50-70%. The overall residue conversion, with the DAO product considered non-residue, is in the range of 80 W %-90 W % and significantly higher than could be achieved without utilizing the present invention.

Particulate skeletal iron catalyst is provided which contain at least about 50 wt. % iron with the remainder being a minor portion of a suitable non-ferrous metal and having characteristics of 0.062-1.0 mm particle size, 20-100 m2/g surface area, and 10-40 nm average pore diameter. Such skeletal iron catalysts are prepared and utilized for producing synthetic hydrocarbon products from CO and H2 feeds by Fischer-Tropsch synthesis process. Iron powder is mixed with non-ferrous powder selected from aluminum, antimony, silicon, tin or zinc powder to provide 20-80 wt. % iron content and melted together to form an iron alloy, then cooled to room temperature and pulverized to provide 0.1-10 mm iron alloy catalyst precursor particles. The iron alloy pulverized particles are treated with NaOH or KOH caustic solution at 30-95° C. temperature to extract and/or leach out most of the non-ferrous metal portion, and then screened and treated by drying and reducing with hydrogen and to provide the smaller size skeletal iron catalyst material. Such skeletal iron catalyst is utilized with CO+H2 feedstream for Fischer-Tropsch reactions in either a fixed bed or slurry bed type reactor at 180-350° C. temperature, 0.5-3.0 mPa pressure and gas hourly space velocity of 0.5-3.0 L/g Fe/hr to produce desired hydrocarbon products.

Porous-material-supported polymer sorbents and process for removal of undesirable gases such as H₂S, COS, CO₂, N₂O, NO, NO₂, SO₂, SO₃, HCl, HF, HCN, NH₃, H₂O, C₂H₅OH, CH₃OH, HCHO, CHCl₃, CH₂Cl₂, CH₃Cl, CS₂, C₄H₄S, CH₃SH, and CH₃—S—CH₃ from various gas streams such as natural gas, coal/biomass gasification gas, biogas, landfill gas, coal mine gas, ammonia syngas, H₂ and oxo-syngas, Fe ore reduction gas, reformate gas, refinery process gases, indoor air, fuel cell anode fuel gas and cathode air are disclosed. The sorbents have numerous advantages such as high breakthrough capacity, high sorption/desorption rates, little or no corrosive effect and are easily regenerated. The sorbents may be prepared by loading H₂S—, COS—, CO₂—, N₂O, NO—, NO₂—, SO₂—, SO₃—, HCl—, HF—, HCN—, NH₃—, H₂O—, C₂H₅OH—, CH₃OH—, HCHO—, CHCl₃—, CH₂Cl₂—, CH₃Cl—, CS₂—, C₄H₄S—, CH₃SH—, CH₃—S—CH₃-philic polymer(s) or mixtures thereof, as well as any one or more of H₂S—, COS—, CO₂—, N₂O, NO—, NO₂—, SO₂—, SO₃—, HCl—, HF—, HCN—, NH₃—, H₂O—, C₂H₅OH—, CH₃OH—, HCHO—, CHCl₃—, CH₂Cl₂—, CH₃Cl—, CS₂—, C₄H₄S—, CH₃SH—, CH₃—S—CH₃-philic compound(s) or mixtures thereof on to porous materials such as mesoporous, microporous or macroporous materials. The sorbents may be employed in processes such as one-stage and multi-stage processes to remove and recover H₂S, COS, CO₂, N₂O, NO, NO₂, SO₂, SO₃, HCl, HF, HCN, NH₃, H₂O, C₂H₅OH, CH₃OH, HCHO, CHCl₃, CH₂Cl₂, CH₃Cl, CS₂, C₄H₄S, CH₃SH and CH₃—S—CH₃ from gas streams by use of, such as, fixed-bed sorbers, fluidized-bed sorbers, moving-bed sorbers, and rotating-bed sorbers.

A fixed bed hydroprocessing system, and also a method for upgrading a pre-existing fixed bed hydroprocessing system, involves preliminarily upgrading a heavy oil feedstock in one or more slurry phase reactors using a colloidal or molecular catalyst and then further hydroprocessing the upgraded feedstock within one or more fixed bed reactors using a porous supported catalyst. The colloidal or molecular catalyst is formed by intimately mixing a catalyst precursor composition into a heavy oil feedstock and raising the temperature of the feedstock to above the decomposition temperature of the precursor composition to form the colloidal or molecular catalyst in situ. Asphaltene or other hydrocarbon molecules otherwise too large to diffuse into the pores of the fixed bed catalyst can be upgraded by the colloidal or molecular catalyst. One or more slurry phase reactors may be built and positioned upstream from one or more fixed bed reactors of a pre-existing fixed bed system and/or converted from one or more pre-existing fixed bed reactors.

The invention discloses a hydrocracking treatment technique for coal tar total distillate, which comprises: first mixing with homogeneous catalyst, or adding impurity, gum, asphaltene and coal oil total distillate contained much oxygen element directly into suspended-bed hydrogenation device; cutting the stream with distilling plant to discharge water, distillate less than 370Deg that enters fixed bed reactor for hydrorefining reaction to cut gasolene less than 150Deg and diesel oil 150-370Deg, and tail oil less than 370Deg that recycles to said reactor and converts into light oil product. Compared with prior art, this invention is simple, but high conversion rate and stability.

A reactor system and process for hydrotreating a heavy feedstock contaminated with metals sulfur and carbon residue using an upflow fixed bed reactor with at least two catalyst layers having different hydrogenation activity.

The average propylene cycle selectivity of an oxygenate to propylene (OTP) process using a dual-function oxygenate conversion catalyst is substantially enhanced by the use of a combination of: 1) moving bed reactor technology in the hydrocarbon synthesis portion of the OTP flow scheme in lieu of the fixed bed technology of the prior art; 2) a hydrothermally stabilized and dual-functional catalyst system comprising a molecular sieve having dual-function capability dispersed in a phosphorus-modified alumina matrix containing labile phosphorus and/or aluminum anions; and 3) a catalyst on-stream cycle time of 400 hours or less. These provisions stabilize the catalyst against hydrothermal deactivation and hold the build-up of coke deposits on the catalyst to a level which does not substantially degrade dual-function catalyst activity, oxygenate conversion and propylene selectivity, thereby enabling maintenance of average propylene cycle yield near or at essentially start-of-cycle levels.

The invention discloses a hydrotreating guard catalyst for residual oil and application thereof. The catalyst has the advantages of large pore volume, large aperture, high porosity, rational pore distribution, larger external orifice, high pore canal penetrability and over 36 percent of 1,000nm pore canals, and is particularly applied to a hydrotreating method of a residual oil fixed bed to ensure that precipitated metals are uniformly deposited on the whole catalyst bed and impurities, namely vanadium and calcium, can be deposited inside the pore canals so as to improve the utilization ratio of pores and maintain long-period running.

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.

A gasifier is disclosed combining a fixed bed gasification section where coarse fuel is gasified and an entrained flow gasification section where fine fuel is gasified. The fixed bed section includes upper and lower sections. Coarse fuel is devolatilized in the upper fixed bed section and subjected to elevated temperatures sufficient to crack and destroy tars and oils in the effluent gases. The entrained flow gasification section is disposed in a lower plenum adjacent the lower fixed bed section. A plurality of injection ports are configured to introduce oxygen, steam, or air into different sections of the gasifier to control temperature and operating conditions. Activated carbon may be formed in the upper fixed bed section and in the entrained flow section. The activated carbon may be used as a sorbent to remove pollutants from the effluent gases. The gasifier may be used with various coarse and fine fuel feedstocks.

A shaped, activated, fixed-bed Raney metal catalyst prepared by a method comprising preparing a mixture of powders comprising at least one catalyst alloy of (1) at least one catalytically active Raney process metal, a leachable alloy component and optionally a promoter, (2) at least one binder containing at least one pure Raney metal and (3) a moistening agent. Shaping, calcining and activating said catalyst and doping said catalyst with rhenium.

A feedstream to a hydrocracking unit is treated to remove or reduce the content of polynuclear aromatics and nitrogen-containing compounds by contacting the feedstream with an adsorbent compound selected from attapulgus clay, alumina, silica gel and activated carbon in a fixed bed or slurry column and separating the treated feedstream that is lower in the undesired compounds from the adsorbent material. The adsorbent can be mixed with a solvent for the undesired compounds and stripped for re-use.

A desulfurizing-denitrating catalyst contains cellular activated carbon (90-99.9 wt.%) and V2O5. It is applied through putting it on supporter in fixed-bed reactor and reacting on fume at 150-250 deg.C and 500-5000/hr of space speed. Its advantage is high transform rate of 80% for SO2 and 50-100% for NO.

The invention relates to a method of preparing butadience with a butylene oxydehydrogenation device in a fixed bed, which belongs to the chemical technical field. The butylene, air and water vapor give an oxydehydrogenation reaction in an axial fixed bed reactor and generate the butadience. The axial fixed bed reactor has two segments. Process equipment consists of a first segment of axial fixed bed reactor, an inter -segment heat exchanger, a second segment of axial fixed bed reactor, a waste heat boiler and a back heat exchanger in turn. The reactor is filled with iron-based catalyst. The ingredient of the water vapor of the first segment of reactor acts with the first segment via the inter-segment heat exchanger to generate gas in addition to exchanging heat and raising temperature and then is mixed with the ingredient butylene and the air of the first segment to achieve the inlet temperature of the first segment of reactor. The ingredient of the first segment enters to the first segment of reactor to react. After heat exchange and temperature reduction through the inter-segment heat exchanger, the gas generated in the first segment is mixed with the feed butylene of the second segment and the air to achieve the inlet temperature of the second segment of reactor and reacts in the second segment of reactor. The invention has the advantages of high yield coefficient, high selectivity and steam of low unit consumption. Heat energy can be used reasonably.

A process for preparing ethylene and propylene from the hydrocarbon mixture containing C4 (or C5) olefine includes such steps as contacting the zeolite contained catalyst in fixed-bed reactor, reacting at 350-500 deg.C and 1-10 /hr of space speed under 0.6-1.0 MPa to obtain the mixture of ethylene and propylene, and cooling separating. Said catalyst contains Al2O3 or SiO2, high-Si zeolite and modifier.

The invention provides a method for continuous production of polyformaldehyde dimethyl ether. The method is characterized by comprising the following steps: a) feeding dimethoxymethane and hot-melted paraformaldehyde into a fixed bed reactor and adopting an acidic resin catalyst, so as to prepare polyformaldehyde dimethyl ether (DMM3-8), wherein the reaction temperature is 120-180 DEG C and the pressure is 0.1-10 MPa; b) cooling the reaction product, and then performing adsorptive separation through a dehydrating tower, so as to obtain polyformaldehyde dimethyl ether of which most water, cytidine glycol and hemiacetal are desorbed; c) feeding the polyformaldehyde dimethyl ether subjected to desorption into a distillation tower for separation, wherein most of a low-boiling component (dimethoxymethane (DMM)), poly-di-formaldehyde dimethyl ether (DMM2), a by-product (methanol) and triformol are extracted first, and then the materials in a tower kettle are fed into a rectifying tower in the next step, so as to extract the rest of the DMM2 and the triformol; and d) returning the low-boiling component (dimethoxymethane (DMM)), the methanol, the DMM2 and the triformol, which are evaporated out by the distillation tower and the rectifying tower in the last step, into the fixed bed reactor to continue to react to prepare polyformaldehyde dimethyl ether.

A continuous fixed-bed catalytic reactor includes an inflow path for raw material gas for a catalytic reaction and an outflow path for reformed gas, a catalytic reaction container that is connected to the inflow path and the outflow path and holds a clumpy catalyst, catalyst holders that have a ventilation property and hold the clumpy catalyst, and a driving mechanism that moves the clumpy catalyst up and down by moving the catalyst holders up and down.