882 results about "Catalytic reforming" patented technology

Described herein is a highly heat integrated steam reformer/combustor assembly that can be used in a fuel processor for hydrogen production from a fuel source. The assembly comprises a reforming section and a combustion section separated by a wall. Catalyst able to induce the reforming reactions is coated on the wall facing the reforming section. Catalyst able to induce the combustion reactions is coated on the wall facing the combustion section. A steam and fuel mixture is supplied to the reforming section where it is reformed to product hydrogen. A fuel and air mixture is supplied to the combustion section where it is combusted to supply the heat for the reformer. Catalytic combustion takes place on the combustion catalyst coated on one side of the wall while catalytic reforming takes place on the reforming catalyst coated on the other side of the wall. Heat transfer is very facile and efficient across the wall. Multiple such assemblies can be bundled to form reactors of any size.

Disclosed is a gasification technique for converting biomass, which is difficult to treat, into clean gas fuel able to be burned in a cogeneration system. The gasification technique includes first stage fluidized-bed catalytic gasification, and second stage gasification of tar and catalytic reforming to convert nitrogen in tar, and HCN in a flammable gas into NH₃, unlike conventional gasification techniques. In addition, since the temperature of a total gasification process is lower than a melting point of ash, powdery ash is generated and thus easily treated. Also, little heat is released due to the low process temperature, and therefore, a compact reactor may be designed to produce gas having a high caloric value. Further, the generated tar is recovered and reused in other processes, and the gas fuel contains a small amount of ammonia.

A method for starting a fast light-off catalytic reformer for producing hydrogen-rich reformate fuel from hydrocarbon fuel and air, the reformer having means for receiving flows of fuel and air, a reforming catalyst for reforming the fuel and air mixture, and an ignition device. A control system selects fuel and air flow rates to form a lean fuel/air mixture and operates the ignition device to ignite the lean mixture to produce hot exhaust gases that flow over and heat the reforming catalyst for a first length of time. Fuel flow is then stopped temporarily for a second length of time, and further ignition is terminated. Fuel flow is then restarted and adjusted to provide a rich fuel/air mixture which is directed to the heated catalyst for reforming into reformate fuel. Air flow may also be adjusted in setting the lean and/or rich fuel/air mixtures.

The invention discloses a medium and low temperature coal tar deep processing method. Medium and low temperature coke material is pretreated and fractionated to obtain light fraction, carbolic oil and heavy fraction, dephenolization treatment is carried out on the carbolic oil to obtain phenols product and dephenolized oil, the dephenolized oil and the above heavy fraction carry out pyrogenetic reaction jointly to obtain various carbonized products, wherein carbonized naphtha, at least one of carbonized diesel oil and carbonized wax oil is mixed with the light fraction obtained by material fractionation to carry out hydrofining and hydrocracking reaction, hydrogenated naphtha obtained by hydrocracking carries out catalytic reforming-aromatics extraction to obtain benzene, toluol, xylene, solvent oil and other products. Compared with the prior art, gasoline fraction and diesel oil fraction obtained by the inventive method are clean and stable in properties. In addition, the invention can produce a plurality of chemical products with high added value, truly realizes the effective utilization of medium and low temperature coal tar, and greatly improves the service life of devices.

The invention discloses a method by adopting biomass fast pyrolysis oil which carries out two sections of fixed bed reactors and water vapor catalytic reforming for producing hydrogen; the two sections of fixed bed reactors are connected in series, the natural dolomite which is relatively cheap and easily available is taken as catalyst in water vapor reforming reaction at the first section of fixed bed reactor, while the second fixed bed reactor adopts Ni/Mgo as catalyst to further improve the purity and yield of the target product gas. Comparatively high temperature and comparatively high S/C (more than 12) are extremely important for the effective transformation of the biomass pyrolysis oil in the first fixed bed reactor. However, for any temperature point, low mass space velocity can facilitate the increasing of the yield of any gas product and the total gas phase transformation ratio of the biomass oil is increased accordingly. The Ni/MgO catalyst is extremely effective in the purification stage, when S/CH4 is not less than 2 and the temperature is not lower than 800 DEG C, the transformation ratio of methane can reach 100 %. Low mass space velocity can facilitate effective transformation of methane; when mass space velocity is not higher than 3600h<-1>, the potential hydrogen yield can reach 81.1%.

A fast light-off catalytic reformer and method includes at least one preferably substantially cylindrical reactor tube having an inlet for receiving a flow of fuel and a flow of air, a reforming catalyst disposed within the reactor tube for converting the fuel and air to a reformate stream, and an outlet for discharging the produced reformate stream. An ignition device disposed within the reactor tube initiates an exothermic reaction between the fuel and air. Heat generated thereby provides fast light-off of the reforming catalyst. An associated control system selects fuel and air flow delivery rates and operates the ignition device to achieve fast light-off of the reforming catalyst at start-up and to maintain the catalyst at a temperature sufficient to optimize reformate yield. The rapid production of high yields of reformate is particularly suitable for use in an on-board reforming strategy for meeting SULEV emissions with spark-ignition engines, especially with larger, higher emitting vehicles.

This invention relates to a hydrocracking preparation of chemical materials production. Poor quality catalytic cracking Diesel and heavy hydrocracking material is mixed according to a proportion, and then hydrogenation and hydrocracking are conducted. The yield of heavy naphtha reaches 40wt% by controlling operating conditions, making sure the yield of tail oil 20wt%. The quality features of this poor quality catalytic cracking Diesel are high density, high content of aromatic hydrocarbon and low value of hexadecane. The density of the poor quality catalytic cracking diesel oil is above 0.95g/ml, and the aromatic hydrocarbon is over 90wt% and the value of hexadecane is under 20. Comparing with present technology, this invention combines poor quality catalytic cracking diesel and VGO organicly. High quality chemical material is effectively transformed with obtaining low BMCI value of tail oil, which is high quality material for ethylene preparation by steam cracking.

Disclosed is an apparatus and process for controlling the sulfur content of effluent from a hydrocarbon fractionation column. The effluent includes a low boiling stream, a middle boiling stream and a high boiling stream. Either of the feed or the low boiling stream may be subjected to a mercaptan removal treatment such as thioetherification or mercaptan oxidation treatment. The high boiling stream is subjected to hydrotreatment which will rid the high boiling stream of almost all organic sulfur compounds. The middle boiling stream may be subjected to a sulfur treatment complex which may comprise a sulfur removal unit and/or a catalytic reforming unit which may already be present in the refinery. Control valves govern the flow of adding the middle boiling stream to the low boiling stream and the high boiling stream in response to the sulfur concentration of the overhead stream downstream of the mercaptan removal treatment.

The present invention generally relates to a method for producing a naphtha product from a renewable feedstock. The method includes hydrotreating the renewable feedstock to produce a hydrotreating unit heavy fraction that includes n-paraffins, and hydrocracking the hydrotreating unit heavy fraction to produce a hydrocracking unit product that includes the naphtha product. The method also includes separating the naphtha fraction and optionally recycling the hydrocracking unit heavy fraction through the hydrocracking unit. The present invention also relates to a biorenewable naphtha product suitable for use as feed stock for steam crackers and catalytic reforming units, and for use as fuel, or fuel blend stock.

The invention relates to a naphtha catalytic reforming method which includes the steps as follows: the naphtha is pumped into the reactor of a catalytic reforming device; gas-liquid separation is carried out on the reformed product for separating gas components, the light component of C8<-> as well as the heavy component of C9<+>; then a light aromatics reaction is carried out on the heavy component of C9<+> under the existence of a light aromatics catalyst; the hydrogen used by the light aromatics reaction is from the circulated hydrogen generated from a reforming device; then gas-liquid separation is carried out on the product after the light aromatics reaction; the liquid returns to the liquid product distilling system of the reforming device. The method can fully utilize the heavy component of C9<+> and convert the heavy component into light aromatic hydrocarbon, improve the aromatic hydrocarbon yield or the yield of the reformed gasoline during the whole process and improve the character of the gasoline.

The invention discloses a method for preparing chloroethylene by catalytic reforming, which relates to a method for preparing the chloroethylene. The method comprises: a step of preparing a catalyst by using active carbon as a carrier, in which a barium salt is used as a catalyst, the active carbon is used as the catalyst carrier, and the barium salt is dissolved in water, absorbed by the active carbon and dried to obtain the catalyst carried by the active carbon; and a step of synthesizing the chloroethylene, in which acetylene gas and dichloroethane vapour are mixed and introduced to a reactor containing the catalyst carried by the active carbon to react, the reaction effluent is cooled to room temperature, unreacted dichloroethane is condensed to be separated out, and the remaining gas is compressed and frozen to give liquid chloroethylene. In the invention, a mercury free catalyst is adopted, the mercury pollution of the chloroethylene production industry is eliminated, and the reaction is performed spontaneously with little energy consumption.

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.

The present invention discloses a continuous catalytic reforming moving bed radial reactor. Said reactor adopts a circular container with catalytic bed as reaction equipment, the reactant inlet is positioned in the upper end of said reaction equipment, and its outlet is positioned in lower end of said reaction equipment, said catalytic bed is formed from external porous wall and internal porous wall cylinder in which the catalyst is filled. Said catalyst can be continuously flowed from top to bottom by means of gravity, at the same time the reaction material can be centrifugally flowed from centre toward exterior in the reaction equipment, and can be concurrently flowed from top to bottom in the distributary channel and collecting channel. Said invention is a Z-type centrifugal radial moving bed reactor, and its structure is simple and catalyst utilization rate is high.

A method of catalytically reforming a reactant gas mixture using a pyrochlore catalyst material comprised of one or more pyrochlores having the composition A_2-w-xA′_wA″_xB_2-y-zB′_yB″_zO_7-Δ. Distribution of catalytically active metals throughout the structure at the B site creates an active and well dispersed metal locked into place in the crystal structure. This greatly reduces the metal sintering that typically occurs on supported catalysts used in reforming reactions, and reduces deactivation by sulfur and carbon. Further, oxygen mobility may also be enhanced by elemental exchange of promoters at sites in the pyrochlore. The pyrochlore catalyst material may be utilized in catalytic reforming reactions for the conversion of hydrocarbon fuels into synthesis gas (H₂+CO) for fuel cells, among other uses.

The invention discloses a self-heating type alcohol reforming hydrogen production micro channel reactor with the micro-lug boss array structure. Three layers of platy reaction carriers are all provided with micro-lug boss array structures; an upper layer and a lower layer are single-side micro-lug boss array structures; a middle layer is a double-side micro-lug boss array structure; the micro-lug bosses are arranged in the mode of parallel array; the three layers are cascaded to form a reaction channel with an inlet of 90 degrees; both ends of the channel are respectively provided with connector lugs; the gas inlet is provided with a detachable adapter and an outlet is provided with a fixed-type adapter. An upper layer channel is a catalytic reforming hydrogen production channel, and a lower layer channel is a combustion channel. The two layers of channel structures both adopt an open structural type being beneficial for the sediment of the catalytic coating. Fuel gases such as hydrogen and the like are combusted in the combustion channel and generate lot of heat which is transferred into the catalytic reforming hydrogen production channel by the middle layer of the reactor so as to meet the requirement of the steam reforming hydrogen production reaction; the reactor can produce hydrogen in a self-heating type. The invention increases the specific volume of the reactor and increases the yield of the alcohol reforming hydrogen production.

The invention discloses a new method for preparing fuel oil by co-pyrolysis of biomass and waste plastic, belonging to the field of solid waste disposal and utilization technology and biomass energy. The method comprises the following steps: mixing evenly the biomass and the waste plastic according to a certain ratio; placing the mixture in a pyrolysis reactor; heating the mixture to the needed pyrolysis temperature for a pyrolytic reaction; introducing the gas generated from the pyrolysis into a refined reaction tower for catalytic reforming; carrying out rectification on the reformed liquid product to obtain fuel oil with different cut fractions; and returning a small quantity of the combustible gas and the residues to the pyrolysis reactor for burning and being used as supplementary heat source. In the method, the biomass and the waste plastic are comprehensively utilized in co-pyrolysis and synergetic promotion is generated by the biomass and the waste plastic, so that the oil productivity and the oil quality are improved. The novel method not only resolves the environmental problems caused by white pollution, but also relieves the energy crisis caused by petrochemical resource exhaustion, thereby having wide application prospect and being able to generate huge social and economic benefits.

The invention discloses a kind of fixed bed reactor for catalytic reforming and dehydrogenation, the reactor uses a round pressure container which has a catalytic bed. The inlet and the outlet is at one side of the container, the catalytic bed is made up of outer multi-hole wall and round inner multi-hole wall, catalyst is filled in them, there has a cover sealing structure on the catalyst, the round inner multi-hole wall can uses variable hole-rate or zone structure. The reacting gas in the device flows centrifugally, the gas in the centre inner barrel and multi-hole outer barrel flow reversely.

The present invention generally relates to a method for producing a naphtha product from a renewable feedstock. The method includes hydrotreating the renewable feedstock to produce a hydrotreating unit heavy fraction that includes n-paraffins, and hydrocracking the hydrotreating unit heavy fraction to produce a hydrocracking unit product that includes the naphtha product. The method also includes separating the naphtha fraction and optionally recycling the hydrocracking unit heavy fraction through the hydrocracking unit. The present invention also relates to a biorenewable naphtha product suitable for use as feed stock for steam crackers and catalytic reforming units, and for use as fuel, or fuel blend stock.

The invention relates to a method for producing aromatic hydrocarbon and ethylene taking naphtha as a raw material. The method comprises the following steps of: (1) contacting naphtha with a reforming catalyst in a catalytic reforming region to carry out a shallow catalytic reforming reaction in the presence of hydrogen at the pressure of 0.15-3.0 MPa, the temperature of 300-540 DEG C and the volume space velocity of 2.1-50 h<-1>, enabling the conversion rate of naphthenic hydrocarbon in the naphtha to be higher than 85wt%, and enabling the conversion rates from alkane to aromatic hydrocarbon and C4-hydrocarbon to be lower than 30wt%; (2) carrying out aromatic hydrocarbon separation on reformate produced by catalytic reforming in a first aromatic hydrocarbon separation region, so as to obtain aromatic hydrocarbon-rich cut fraction and alkane-rich cut fraction; (3) introducing the aromatic hydrocarbon-rich cut fraction and liquefied gas produced by the catalytic reforming into a steam cracking region, and carrying out a cracking reaction to produce ethylene. According to the method for producing the aromatic hydrocarbon and the ethylene taking naphtha as the raw material, the ethylene can be maximally produced when the naphtha is adequately utilized in a shallow catalytic reforming reaction manner.

This invention discloses a hydrocracking method.It includes that the heavy distillate oil and poor quality catalytic cracking diesel refining separately by hydrogenation, and the mixture enters into hydrocracking reactivator, then its cracking products is conducted gas liquid separation. Light naphtha, heavy naphtha, aviation kerosene, diesel oil and end oil will be obtained by distillating the liquid phase. The density of the poor quality catalytic cracking diesel oil is above 0.9g/ml, and the aromatic hydrocarbon is over 60wt% and the value of hexadecane is under 30. It is a adequate utilization of catalytic cracking craft to produce High aromatic hydrocarbon heavy naphtha and high quality end oil with heavy distillate oil and poor quality catalytic cracking diesel, which can be separately used as catalytic reforming material and making ethylene material by steam cracking method. High aromatic hydrocarbon heavy naphtha in this invention will produce a large amount of reforming hydrogen after catalytic reforming treatment, which can be used in the process of hydrocracking to make this preparation more ecnomical and reasonable.

A hydrogen engine system is a low-carbon engine system which takes hydrogen-enriched gas produced by using alcohol cracking as fuel. The hydrogen engine system comprises a fuel storage tank and a fuel conveying device, a fuel heating gasifying and cracking device, a hydrogen-enriched gas compressor and an exhaust discharging pipe, wherein the fuel storage tank is connected with the fuel conveying device and then connected to the fuel heating gasifying and cracking device; fuel passes through the hydrogen-enriched gas compressor and is then input into an automobile engine to do work; the fuel heating gasifying and cracking device is installed inside a high-temperature chamber formed by an exhaust discharging device. The hydrogen engine system rarely changes an original gasoline-fueled automobile, keeps a function that the original automobile uses gasoline as fuel, and has unchanged dynamic performance; when an engine is started through cold start and no alcohol is supplied or a storage battery is low in power in the running process, common gasoline can be still used for driving the automobile or heating up a cracker to reach heat and temperature which are required by catalytic reforming hydrogen production, so that the hydrogen engine system has a good development prospect.

The present invention relates to internal combustion engine afterheat utilizing technology, and is especially methanol catalytically reforming hydrogen producing apparatus utilizing afterheat of internal combustion engine and its control method. The apparatus includes mainly methanol aqua gasifying cavities in the front part, middle part and back part of the reformer casing, catalytically reacting cavity and reformed gas product cavity. In the middle part inside the reformer casing, there are porous honeycomb ceramic with inside catalytically reacting cavity; and the inner wall of the catalytically reacting cavity has set honeycomb pores with reforming catalyst coated to the inner wall. One heat exchange pipe penetrates the porous honeycomb ceramic axially. The present invention has integrated heat exchange pipe and porous honeycomb ceramic, and possesses compact structure, high heat exchange efficiency, high hydrogen rate and other advantages.

One embodiment is a catalyst for catalytic reforming of naphtha. The catalyst can have a noble metal including one or more of platinum, palladium, rhodium, ruthenium, osmium, and iridium, an alkali or alkaline-earth metal, a lanthanide-series metal, and a support. Generally, an average bulk density of the catalyst is about 0.300 to about 1.00 gram per cubic centimeter. The catalyst has a platinum content of less than about 0.375 wt %, a tin content of about 0.1 to about 2 wt %, a potassium content of about 100 to about 600 wppm, and a cerium content of about 0.1 to about 1 wt %. The lanthanide-series metal can be distributed at a concentration of the lanthanide-series metal in a 100 micron surface layer of the catalyst less than two times a concentration of the lanthanide-series metal at a central core of the catalyst.