85 results about "Non catalytic" patented technology

The invention belongs to the technical field of metallurgy, and relates to a carbon reduction method for a direct reduction device, which comprises the following steps: step 1, feeding a carbon-containing raw material and an oxidant into a conversion unit for oxidation reaction to obtain crude synthesis gas; 2, feeding the crude synthesis gas into a direct reduction unit for ironmaking, and respectively feeding furnace top gas discharged by the direct reduction unit into a conversion unit and a tail gas discharge unit after dust removal by a dust removal unit; 3, a part of the furnace top gas and a carbon-containing raw material are subjected to a reforming reaction in a conversion unit to obtain synthesis gas, and the synthesis gas is fed into a direct reduction unit for ironmaking; and the other part of furnace top gas is discharged after being treated by the tail gas discharge unit. According to the method, a carbon dioxide closed-loop conversion system is constructed, efficient carbon reduction is achieved through a coupling mechanism of non-catalytic partial oxidation and autothermal reforming, and compared with a traditional hydrogen-based shaft furnace ironmaking method, the carbon reduction method has the advantage that the carbon dioxide emission is reduced by at least 25%.

The invention discloses a process for preparing synthesis gas by non-catalytic and catalytic coupling of hydrocarbon-containing raw material gas. The process comprises the following steps: (S1) dividing preheated raw material gas into first raw material gas and second raw material gas; (S2) introducing the first raw material gas, water vapor and preheated oxygen into a non-catalytic reactor, and carrying out a non-catalytic conversion reaction to generate first synthesis gas; (S3) introducing the second raw material gas and supplemented water vapor into a pre-catalytic reactor, and carrying out pre-catalytic conversion reaction to generate second synthesis gas; (S4) introducing the first synthesis gas and the second synthesis gas into a catalytic reactor, and carrying out catalytic conversion reaction to prepare third synthesis gas; and (S5) carrying out heat recovery on the prepared third synthesis gas to obtain the synthesis gas. According to the invention, the non-catalytic conversion reaction and the catalytic conversion reaction are coupled, so that the material consumption is greatly reduced, and meanwhile, heat is provided for the catalytic conversion reaction through the non-catalytic conversion reaction, so that the heat is recovered to a great extent.

The invention discloses a non-catalytic and catalytic coupling synthesis gas preparation device and application thereof to synthesis gas preparation, the device comprises a non-catalytic reactor, a catalytic reactor, a pre-catalytic reactor, a waste heat boiler, a plurality of heat exchangers, a connecting pipeline and the like, and the pre-catalytic reactor is also provided with a heat exchanger structure; a pre-catalytic reaction cavity is arranged between a cold end inlet and a hot end outlet of the pre-catalytic reactor; the heat exchanger is used for preheating oxygen and part of raw materials and feeding into the non-catalytic reactor; the rest of the raw materials are preheated again and then fed into the pre-catalytic reactor and the non-catalytic reactor, reactants of the pre-catalytic reactor are fed into the catalytic reactor for continuous reaction, reactants of the catalytic reactor are used for supplying heat to the pre-catalytic reactor, the heat exchanger and the waste heat boiler, and the waste heat boiler can be used for preparing raw material steam; and heat balance adjustment of the whole device can also be participated. The device is high in heat utilization rate and conversion rate, can adjust the hydrogen-carbon ratio of the synthesis gas, and is particularly suitable for preparing methanol synthesis gas from natural gas and the like.

The invention provides a method and system for preparing synthesis gas through dry reforming parallel non-catalytic partial oxidation, and the method comprises the following steps: carrying out pretreatment operation on raw material gas to obtain pretreated raw material gas, dividing the pretreated raw material gas into two branches, introducing the first branch into a dry reforming self-heating furnace, and introducing the second branch into a dry reforming self-heating furnace; the second branch is mixed with steam and then is introduced into a non-catalytic partial oxidation converter; introducing oxygen and carbon dioxide into a dry reforming reactor, and carrying out a methane dry reforming reaction with the pretreated raw material gas in the presence of a catalyst to obtain first crude synthesis gas; introducing oxygen into the non-catalytic partial oxidation converter, and carrying out methane non-catalytic partial oxidation reaction on the oxygen and the raw material gas to obtain second crude synthesis gas; the first crude synthesis gas and the second crude synthesis gas respectively enter a first waste heat boiler and a second waste heat boiler for heat exchange operation, and after heat recovery, the first crude synthesis gas and the second crude synthesis gas are mixed to obtain mixed crude synthesis gas; and after the mixed crude synthesis gas is subjected to heat exchange operation and refining operation in sequence, the downstream required synthesis gas is finally obtained. The hydrogen-carbon ratio of the synthesis gas can be adjusted in a wide range, the utilization rate of the feed gas is high, and carbon dioxide and heat energy can be fully absorbed.

The present application belongs to the field of denitration agent preparation, and provides a selective non-catalytic reduction denitration agent and a preparation method thereof. First, urea is heat treated to change hydrogen bond strength and intermolecular force in the crystal, and increase thermal motion of urea molecules, so as to cause loose arrangement between molecules, increase exposure of reaction sites, and increase contact area of molecules, thereby increasing reaction rate. A phosphoric acid group is introduced into the urea after heat treatment, and phosphonated urea is formed through chemical reaction, so as to improve adsorption and reaction activity of the urea. This process helps to enhance the combination ability of urea and NOx, thereby improving the denitration efficiency. Appropriate amounts of sodium carbonate, sodium chloride and hydroxyl iron oxide are added to the reaction system, which helps to promote the activity improvement of the denitration agent, and can effectively deal with nitrogen oxide pollution in industrial waste gas.

The invention belongs to the technical field of hydrogenation modification of low-rank coal, and particularly relates to a method for coal blending coking through non-catalytic hydrogenation modification tackifying of low-rank coal. In order to solve the problems that the low-rank coal mixing hydrogenation process is complex, a catalyst is difficult to recycle and the like, the method comprises the following steps: weighing low-rank coal and a hydrogen-donor solvent according to different mass proportions, carrying out hydrogenation reaction according to different reaction temperatures, reaction pressures and reaction time of an autoclave, firstly, fully stirring and uniformly mixing the materials in the autoclave, and then carrying out heating reaction; and after the autoclave is cooled, directly carrying out suction filtration separation on the reaction mixture to obtain a solid product which is the modified coal with a certain caking index.

The invention relates to the technical field of flue gas treatment, in particular to a method for treating flue gas of a waste incineration plant. The problem of low flue gas treatment efficiency in the prior art is solved. The method comprises the following steps: firstly, simultaneously spraying a nitrogen oxide reducing agent and a micronized calcium-based deacidification agent into a high-temperature section of flue gas, and carrying out non-catalytic denitration and pre-deacidification treatment; then, the flue gas enters a medium-temperature composite catalytic reactor, and efficient denitration, elemental mercury oxidation and catalytic decomposition of dioxin are achieved through cooperation of a composite catalyst; then, the flue gas enters a graded circulating fluidized bed system, acid gas is efficiently removed through a first-stage circulating fluidized bed, then the flue gas enters a second-stage circulating fluidized bed after being cooled, and mercury and heavy metal are efficiently adsorbed through modified active coke; finally, the flue gas passes through a composite filter bag, and residual CO and VOCs are catalytically degraded while dust is removed. According to the invention, deep purification of various pollutants in the flue gas is realized through quality-divided cooperation and temperature-divided and zoned treatment, the treatment efficiency is high, and the operation is stable.

The invention discloses a reformer for non-catalytic hydrogen production, which belongs to the technical field of hydrogen production equipment and comprises a bottom plate, a furnace body and a heat exchange tank, and the furnace body and the heat exchange tank are arranged on the bottom plate. A spiral reaction pipe is arranged in the furnace body, the top end and the bottom end of the spiral reaction pipe are communicated with a mixed gas pipe and a converted gas outlet pipe respectively, a combustor is arranged at the bottom of the inner side of the furnace body, and the combustor is connected with a gas inlet sleeve; the heat exchange tank is filled with a heat exchange medium and is provided with a gas supply assembly and a spiral flue; the gas supply assembly communicates with the mixed gas pipe, the top end of the spiral flue communicates with the top end of the heat exchange tank, and the bottom end of the spiral flue is connected with a suction assembly. Preheating recycling can be carried out, heat in high-temperature flue gas is used for preheating feed gas, heat source waste is avoided, the energy utilization rate is increased, and the energy consumption cost is reduced.

The invention discloses a metal-doped VOOH nano-enzyme material with a hollow spherical shell structure as well as a preparation method and application of the metal-doped VOOH nano-enzyme material, and belongs to the technical field of nano-materials and biological catalysis. The invention aims to solve the problems that the peroxidase-like activity of the existing pure-phase VOOH nano material is relatively limited, the electronic structure of the pure-phase VOOH nano material is not in the optimal state of catalyzing H2O2 decomposition, and the adsorption / desorption energy barrier of a reaction intermediate is relatively high. The chemical general formula of the metal-doped VOOH nano-enzyme material with the hollow spherical shell structure is M-VOOH, and M is a doped metal element. The preparation method comprises the following steps: 1, dissolving a precursor; 2, acidity adjustment; 3, doping metal; and 4, reduction and crystallization. According to the application, the catalyst serves as a peroxidase-like catalyst to catalyze decomposition of hydrogen peroxide.

The invention discloses a kind of aromatic hydrocarbon saturation hydrogenation anti-sulfur catalyst and its preparation method and application, belong to oil catalytic hydrogenation field.The present invention utilizes the topological transformation property of hydrotalcite to introduce metal Mo, obtains the precursor of active component uniform dispersion, utilizes NaBH4 low temperature reduction this precursor, directly obtains highly dispersed NiMo / Al-LDH catalyst.The catalyst shows excellent catalytic performance and anti-sulfur performance in vacuum residue and naphthalene catalytic hydrogenation reaction, naphthalene can be completely converted under mild conditions, and the selectivity of decahydronaphthalene reaches 100%, in addition, cycloalkane content can reach 16.9% in the n-hexane solubles obtained from catalytic hydrogenation residue, is significantly higher than non-catalytic.The present invention does not need to use hydrogen, is safe and environmentally friendly, and simultaneously catalyst preparation method is simple, active, stable and has anti-sulfur performance, therefore has good application prospect in the catalytic hydrogenation of vacuum residue, various heavy oils and coal.

The utility model discloses electrolytic aluminum carbon anode roasting flue gas ultra-low emission purification equipment, relates to the field of general physical or chemical methods or devices, and aims to purify various pollutants contained in roasting flue gas and realize ultra-low emission of the roasting flue gas. According to the technical scheme, the electrolytic aluminum carbon anode roasting flue gas ultra-low emission purification equipment comprises a non-catalytic reduction denitration device, a desulfurizing tower, a dust remover, a heat storage type catalytic combustion device and a calcining device, and the non-catalytic reduction denitration device comprises a roasting furnace and an ejector for spraying a denitration agent into the roasting furnace. A flue gas outlet of the roasting furnace is connected with a flue gas inlet of the desulfurizing tower, a flue gas outlet of the desulfurizing tower is connected with the dust remover, a flue gas outlet of the dust remover is connected into the heat accumulating type catalytic combustion device, a flue gas outlet of the heat accumulating type catalytic combustion device is connected into the chimney, and a dust outlet of the dust remover is respectively connected with the desulfurizing tower and the calcining device. The carbon anode roasting flue gas purification device is used for purifying carbon anode roasting flue gas.

The utility model relates to the technical field of boiler flue gas treatment, in particular to dry SNCR (selective non-catalytic reduction) denitration equipment, which comprises a storage bin and a denitration furnace, the storage bin is connected with the denitration furnace through a pipeline conveying system, and a discharge plate is arranged between the inner walls of the storage bin. The discharging plate is slidably connected into a sliding groove correspondingly formed in the inner wall of the storage bin in an embedded mode through a T-shaped sliding block arranged on the inner wall of the discharging plate. According to the improved dry-method SNCR denitration equipment, the spray guns are annularly distributed in the denitration furnace in an equiangular mode, the number of the spray guns in the middle is larger than that of the spray guns in the upper area and the lower area, and spray gun pipe openings in different areas are obliquely distributed at different angles, so that a reducing agent can be sprayed into the furnace from different angles and uniformly cover the whole hearth space, the comprehensiveness and the uniformity of denitration reaction are improved, and meanwhile, the reduction effect is good. And the flow guide plate can change the flowing paths of the flue gas and the reducing agent, so that the retention time of the flue gas and the reducing agent in the furnace is prolonged, the reducing agent and nitric oxide can be more sufficiently subjected to selective non-catalytic reduction reaction, and the conversion rate of the nitric oxide is increased.

This invention discloses a method for preparing a bimetallic composite catalytic material and its application. The invention first obtains a bimetallic composite catalytic material by combining two transition metal elements, and then uses it to catalyze the oxidation of sulfite, achieving an oxidation rate of over 90%. Compared with non-catalytic oxidation, the oxidation efficiency of sulfite using the bimetallic composite catalytic material in this invention is increased by 20-35 times.

Processes for producing at least one of 2-chloro-3,3,3-trifluoropropene (HCFO-1233xf) or 2,3-dichloro-3,3-difluoropropene (HCFO-1232xf) from 1,1,2,3-tetrachloro-1-propene (HCO-1230xa), in the absence of a catalyst, are provided.

The invention relates to a multi-section reactor, and discloses a conversion reactor for preparing synthesis gas through non-catalytic and catalytic coupling of hydrocarbon-containing gas and application of the conversion reactor, an oxidation section is arranged at one end in a shell of the reactor, the oxidation section comprises a burner and a first raw material gas inlet connected to the burner, and the reactor further comprises a pre-catalytic section and a catalytic section; wherein the catalysis section is located in the shell, reaction gas heat of the oxidation section is used for supplying heat to the catalysis section, the pre-catalysis section is located in the shell or outside the shell, the pre-catalysis section comprises a pre-catalysis cavity filled with a catalyst, the pre-catalysis cavity is provided with a second raw material gas inlet and a pre-catalysis reaction gas outlet, and the second raw material gas inlet is communicated with the pre-catalysis reaction gas outlet. The catalytic section comprises a catalytic reaction chamber filled with a catalyst, all pre-catalytic reaction gas is introduced into the catalytic reaction chamber, the catalytic reaction chamber is provided with a synthesis gas outlet, and the synthesis gas heat of the catalytic section is used for supplying heat to the pre-catalytic section. The equipment occupied area and carbon emission can be reduced, the overall heat efficiency is high, and hydrogen and carbon components of product gas can be flexibly adjusted.

Combustion method for a glass furnace with a non-catalytic conversion furnace, wherein the system required for combustion comprises a glass furnace, a non-catalytic conversion furnace A, a non-catalytic conversion furnace B, a flue gas recovery device, a chimney, a high-temperature flue gas fan, a natural gas supply device and an oxygen supply device; wherein the non-catalytic conversion furnace A and the non-catalytic conversion furnace B are arranged on two sides of the glass furnace and connected to the glass furnace; wherein the non-catalytic conversion furnace A and the non-catalytic conversion furnace B are switchably connected to an inlet of the flue gas recovery device and an outlet of the flue gas recovery device is each connected to the chimney and the high-temperature flue gas fan, the high-temperature flue gas fan being connected to the bottom of the non-catalytic conversion furnace A and the bottom of the non-catalytic conversion furnace B; wherein the natural gas supply device is switchably connected to the bottom of the non-catalytic conversion furnace A, the upper part of the non-catalytic conversion furnace A, the bottom of the non-catalytic conversion furnace B, the upper part of the non-catalytic conversion furnace B and the glass furnace, the oxygen supply device is connected to the glass furnace; wherein an oxygen content analyzer, a flow meter, a temperature sensor and a pressure sensor are provided on a pipe through which the high-temperature flue gas fan is connected to the bottom of the non-catalytic conversion furnace A and the bottom of the non-catalytic conversion furnace B, wherein a flow control valve and a pressure sensor are provided on a pipe through which the natural gas supply device is connected to the bottom of the non-catalytic conversion furnace A, the upper part of the non-catalytic conversion furnace A, the bottom of the non-catalytic conversion furnace B, the upper part of the non-catalytic conversion furnace B and the glass furnace, and wherein a flow control valve and the pressure sensor are provided on a pipe through which the oxygen supply device is connected to the glass furnace; the combustion process includes the following steps: 1) In the initial phase, combustion is promoted by means of air, and after the generation of the flue gas, the circulating flue gas is mixed with oxygen and used as a combustion improver to gradually replace the promotion of combustion with air, whereby after a certain time of the cycle the circulating flue gas contains high levels of water vapor and carbon dioxide, and the circulating flue gas and the oxygen completely replace the promotion of combustion with air, at which point the system enters its normal operating state; 2) Conversion and Reforming Phase: When the oxygen content in the circulating flue gas is less than or equal to a set limit, the circulating flue gas enters the furnace from the bottom of the non-catalytic conversion furnace A, and natural gas also enters the furnace from the bottom of the non-catalytic conversion furnace A, whereby the natural gas undergoes a conversion and reforming reaction with water vapor and carbon dioxide in the circulating flue gas, producing hydrogen and carbon monoxide, namely high-calorific-value water gas, which are fed into the glass furnace, whereby oxygen is fed into the glass furnace and undergoes a combustion reaction with carbon monoxide and hydrogen produced by non-catalytic conversion and a small amount of natural gas that does not undergo a conversion and reforming reaction;wherein the circulating flue gas, when the oxygen content in the circulating flue gas is greater than the set limit, enters the furnace from the bottom of the non-catalytic conversion furnace A, and natural gas enters the furnace from the upper part of the non-catalytic conversion furnace A, wherein natural gas undergoes a conversion and a reforming reaction with water vapor and carbon dioxide in the circulating flue gas, thereby producing hydrogen and carbon monoxide, namely high-calorific-value water gas, which are fed into the glass furnace, wherein oxygen is fed into the glass furnace and undergoes a combustion reaction in the glass furnace with carbon monoxide and hydrogen produced by non-catalytic conversion and a small amount of natural gas that does not undergo a conversion and reforming reaction; ; 3) Flue gas purging phase: After completion of the conversion and reforming phase, the natural gas is fed directly into the glass furnace and the circulating flue gas enters the furnace from the bottom of the non-catalytic conversion furnace A to purge, replace and convert the remaining combustible gas, and enters the glass furnace, with oxygen being fed into the glass furnace to undergo a combustion reaction; 4) Heating phase of the conversion furnace: In the conversion and reforming phase and the flue gas purging phase, high-temperature flue gas from the outlet of the glass furnace enters the non-catalytic conversion furnace B to heat the furnace and store heat, and then enters the flue gas recovery device to recover heat and be dedusted and desulfurized, after which part is pressurized by the high-temperature flue gas fan and then introduced into the circulation of the non-catalytic conversion furnace A, while the remainder is discharged through the chimney or undergoes a CCUS process; 5) After a certain time, the non-catalytic conversion furnace A / B is switched over, that is, a conversion and a reforming reaction take place in the non-catalytic conversion furnace B, and the non-catalytic conversion furnace A heats up and heat is stored there; such a switching is repeated cyclically.

The utility model relates to the technical field of treatment systems for the content of CO and H2 in coal gasification gas, in particular to a post-treatment system for improving the content of CO and H2 in coal gasification gas. According to the technical scheme, the post-treatment system for increasing the content of CO and H2 in the coal gasification gas comprises a high-temperature pure oxygen non-catalytic partial oxidation reaction module, according to the utility model, the non-catalytic partial oxidation reaction equipment and the heat recovery equipment are arranged, so that the process flow of purifying the underground coal gasification product gas is greatly simplified, and the product gas can be subjected to primary purification and heat recovery; the technical process of the product gas purification treatment device matched with the underground coal gasification device is more economical and reasonable, the advantages of reliability and low cost of the underground coal gasification technology are fully played, the problems existing in the existing underground coal gasification technology are solved, CH4 in coal gas is cracked, CO and H2 are generated, and the product gas purification treatment device is more environmentally friendly. And the content of effective components in the coal gas is increased.

The utility model belongs to the technical field of non-catalytic converter burners, and relates to a stepped double-water-cooling non-catalytic converter burner which comprises a long cylindrical burner body, the head of the burner body is in a stepped shaft shape with a thin front end and a thick rear end, and a cylindrical inner cooling water pipe and a cylindrical outer cooling water pipe are arranged at the head of the burner body. The inner cooling water pipe is annularly sleeved with the outer cooling water pipe, and the inner cooling water pipe forwards extends out of the front end face of the outer cooling water pipe in the axial direction; the axial length of the outer-layer water cooling structure is smaller than that of the inner-layer water cooling structure, so that when the burner is used, the outer-layer water cooling structure is positioned outside a hearth of the non-catalytic converter, and the external cylindrical fluid channel is positioned in the burner mounting chamber; the phenomenon that the cooling water structure on the outer layer of the burner is cracked and damaged due to backflow of high-temperature hot air in the furnace is effectively prevented, so that the service life of the burner of the non-catalytic converter is prolonged, and the use cost of the burner is reduced.

The invention relates to the technical field of coke gasification processes, and discloses a method for constructing a coke non-catalytic and catalytic gasification reaction mechanism model, which comprises the following steps: collecting coke non-catalytic and catalytic gasification experimental data of different coal types under various gasification conditions; the gasification conditions comprise temperature, pressure, gasification agent type and flow, and catalyst type and dosage; the method comprises the following steps: collecting experimental data, preprocessing the collected experimental data, including data cleaning, normalization and feature extraction, screening out effective feature parameters related to the gasification reaction, and describing the non-catalytic gasification reaction process of the coke by adopting a multi-element heterogeneous reaction mechanism model. Through a multi-step and multi-path multi-element heterogeneous reaction mechanism model, the complex reaction in the coke gasification process is accurately described, key characteristic parameters are mined in combination with deep learning, model input is optimized, the model precision is improved, a high-precision basis is provided for simulation of the coke gasification process, and optimization and efficient operation of the gasification process are assisted.

Provided are a sensor element and a gas sensor in which the use amount of a noble metal catalyst supported on a porous carrier is reduced and a decrease in gas responsiveness caused by an excess catalyst is suppressed. A sensor element (100) is provided with: a plate-shaped element main body (300) that includes a detection unit (130); and two or more porous protective layers (20) that surround at least the periphery of the tip section of the element main body where the detection unit is located. At least one layer (21) of the porous protective layer is a mixed layer in which a catalyst-bearing region (60) on which a catalyst substance comprising at least one noble metal selected from the group consisting of Pt, Pd, Rh and Au is supported and a non-catalyst region that does not contain the catalyst substance are mixed. The sensor element has a gas introduction hole (113a) for introducing a gas to be measured into the detection unit, and a catalyst-bearing region in which a mixed layer is present within a virtual region (R) extending from the outline of the gas introduction hole to the outer surface of the porous protective layer in the thickness direction of the porous protective layer.

The present application provides a kind of coal-based mesophase pitch and its preparation method, belong to pitch preparation technical field.The preparation method includes the following steps: coal-based raw pitch is pretreated, and refined coal pitch is obtained;Distillation is carried out on refined coal pitch, and distillation coal pitch is obtained;Heat polycondensation reaction is carried out on distillation coal pitch, and coal-based mesophase pitch is obtained.The present application uses single coal-based raw pitch as raw material, with the help of the combination of pure physical purification of refining-distillation, cooperatively removes impurities and controls material composition, reduces the quinoline insoluble content of coal pitch to below 0.1wt%.On this basis, through non-catalytic heat polycondensation reaction, the mesophase conversion rate is significantly improved, and the performance consistency of the obtained product as carbon material precursor is improved.The process is simple, controllable, energy-saving and cost-effective, which provides a reliable technical path for the high-value utilization of coal tar pitch and the large-scale stable production of high-end carbon materials.

The invention relates to a process for decomposing nitrogen oxides in exhaust gases. In a non-catalytic reaction phase, reducing agent, e.g. NH3 or urea, is injected into the exhaust gas in a controlled manner at comparatively high temperatures, specifically directly in the combustion chamber in which the exhaust gas is produced or in a collecting device for collecting and transferring the exhaust gas. The decomposition of the nitrogen oxides takes place in said non-catalytic reaction phase by means of a non-catalytic chemical reduction, i.e. in the absence of separate catalysts, preferably as so-called SNCR (selective non-catalytic reduction). In a downstream catalytic reaction phase, the nitrogen oxides are then further decomposed in the presence of a heterogeneous catalyst, specifically by catalytic chemical reduction with reducing agent, preferably as so-called SCR (selective catalytic reduction), and / or by catalytic decomposition.

The invention provides a method for preparing an adhesive by aminating polyvinyl chloride under a non-catalytic photo-thermal action, which is characterized by comprising the following steps of: putting a polyvinyl chloride polymer or a consumed polyvinyl chloride plastic waste material into a photo-thermal reaction system, and reacting under the condition of no additional catalyst; and reacting with an amination reagent (such as butylamine, aniline, imidazole and other organic amines) at a low temperature (lower than 80 DEG C) in a green solvent under the auxiliary action of illumination for 4-18 hours to directly generate the amination modified PVC-based adhesive. The adhesive prepared by the method can be used for bonding wood building materials, glass, resin and metal plates, and has good bonding strength, water resistance, weather resistance and flame retardance. Through the non-catalytic photo-thermal synergistic effect, the direct conversion from the polyvinyl chloride waste to the high-added-value adhesive is realized in one step, the process conditions are mild, the operation is simple and convenient, a new path is provided for green recovery and value-added utilization of polyvinyl chloride, and the method has good industrial application potential.

A process for the high-pressure non-catalytic synthesis of melamine from urea wherein various heat inputs of the process are provided electrically, the process comprises reacting urea to form melamine in a synthesis reactor provided with electrical heating elements, the process further comprises heating the melamine melt electrically during transport and / or using electrically produced heat to remove water from melamine crystals.

An atmosphere total tritium sampler relates to the technical field of tritium sampling equipment and comprises a sampling head assembly, a catalysis assembly, a tritium condensation assembly, a collection assembly and a refrigerant assembly, the sampling head assembly comprises an atmosphere inlet and an atmosphere outlet, the atmosphere outlet is communicated with a catalysis pipeline and a tritium condensation pipeline which are connected in parallel, and the catalysis pipeline and the tritium condensation pipeline are respectively provided with an air inlet electromagnetic valve I and an air inlet electromagnetic valve II; a gas inlet of the catalysis assembly is communicated with the catalysis pipeline, and a gas outlet of the catalysis assembly is communicated with a gas inlet of the tritium condensation assembly; an air inlet of the tritium condensation assembly is communicated with the tritium condensation pipeline, and an air outlet of the tritium condensation assembly is communicated with the fan; the collecting assembly comprises a catalytic collecting pipeline and a non-catalytic collecting pipeline, the catalytic collecting pipeline is communicated with the reagent bottle I, and the non-catalytic collecting pipeline is communicated with the reagent bottle II; and the refrigerant assembly is communicated with the tritium condensation assembly. The tritium sampling device can perform various sampling on tritium in the atmosphere, is easy to maintain and low in cost, and can perform continuous sampling.

The invention relates to a method for preparing hydrocarbon-rich bio-oil through biomass non-catalytic hydrothermal liquefaction. The method comprises the following steps: sequentially carrying out hydrothermal liquefaction treatment and solid-liquid separation treatment on biomass to obtain the hydrocarbon-rich bio-oil, the hydrothermal liquefaction treatment comprises heat treatment, pulse pressure treatment, pressure reduction treatment and cooling treatment which are carried out in sequence; the pulse pressure treatment comprises first pulse pressure treatment, second pulse pressure treatment and third pulse pressure treatment in sequence; the target pressure of the first pulse pressure treatment is greater than the target pressure of the second pulse pressure treatment; the target pressure of the third pulse pressure treatment is greater than the target pressure of the first pulse pressure treatment. According to the method, the hydrothermal liquefaction treatment process is regulated and controlled, the content of hydrocarbon compounds in the hydrocarbon-rich bio-oil is increased, and meanwhile, the method is simple and easy to amplify and does not need to use a catalyst.

The invention is directed to a method and electrolytic cell for electrolysis of an alkaline aqueous solution. The method comprises the steps of: - providing an electrolyte (1) chamber comprising an alkaline aqueous solution; - providing a first electrode stack and a second electrode stack, both of which are in fluid contact with the alkaline aqueous solution in the electrolyte chamber and comprise a permeable electrode layer comprising catalytically active electrode material (6, 7), and a permeable non-catalytic layer (8) placed on a first face of the electrode layer facing the electrolyte chamber; - applying a potential difference between the electrode layer of the first electrode stack and the electrode layer of the second electrode stack; - flowing the alkaline aqueous solution from the electrolyte chamber through the first and second electrode stack, thereby causing an oxidation reaction at the electrode layer of one of the electrode stacks and causing a reduction reaction at the electrode layer of the other electrode stack; wherein each non-catalytic layer has a permeability of 1.0 × 10-7 m2 or lower, and / or wherein the flow velocity through the first and second electrode stack is 1.0 × 10-4 m / s or lower.

The present invention relates to a coking process capable of producing rich hydrogen and suitable for low-carbon metallurgy, which process comprises: 1) by means of coal blending and coking processes, obtaining high-temperature raw gas while producing coke by using a coke oven; 2) after cooling the coke by means of dry quenching, recovering heat to produce high-temperature superheated steam; 3) directly subjecting the high-temperature raw gas, without being cooled, to non-catalytic oxidative reforming under the action of oxygen, so as to obtain a high-temperature hydrogen-rich reducing gas; 4) cooling the high-temperature hydrogen-rich reducing gas by means of a waste heat boiler to obtain high-temperature superheated steam, and purifying the hydrogen-rich reducing gas, so as to obtain chemical byproducts; and 5) after the high-temperature superheated steam in steps (2) and (4) is combined with the grid, performing power generation using waste heat, so as to obtain electric energy. A coke product produced in the present invention meets requirements of a hydrogen-rich blast furnace; moreover, the byproduct, i.e., the high-temperature raw gas, is used for preparing the low-carbon low-cost hydrogen-rich reducing gas, thereby optimizing the whole process flow of coking; and therefore low-carbon hydrogen is obtained while coke is produced in an energy-saving and consumption-reducing manner, and carbon emissions in the whole coking production process are reduced.

The application provides a method for preparing synthesis gas by non-catalytic partial oxidation of a COREX smelting gasifier, and relates to the technical field of synthesis gas preparation. The method is to take the dome region of the COREX smelting gasifier as a reaction zone, take oxygen and natural gas as raw material gas, spray the raw material gas into the dome region by a burner on the dome of the COREX smelting gasifier, and perform non-catalytic partial oxidation reaction of methane to prepare synthesis gas mainly composed of hydrogen and carbon monoxide. The application adopts a technical scheme of non-catalytic partial oxidation of natural gas accompanied by reforming reaction of natural gas, water vapor and carbon dioxide, which does not exist in the prior art. By controlling the structure of the oxygen / natural gas burner and the circulating dust injection burner and the composition of the raw material gas, in combination with the high-temperature and high-pressure environment and high-speed airflow of the dome region, good kinetic conditions are provided for the non-catalytic partial oxidation reaction of natural gas, and the method is simple to operate, low in cost, high in efficiency, beneficial to industrial large-scale production and popularization and use.

The application discloses a methane carbon dioxide reforming system and method, which comprises a shell, an internal cavity for raw material gas to enter and to bear gas pressure, a reaction tube in the internal cavity of the shell, for the raw material gas to enter and to be discharged to the outside of the shell after sequentially passing through a non-catalytic reforming section in the internal cavity of the reaction tube for absorbing microwave heat, a transition section for gas temperature reduction and a catalytic reforming section for a reforming reaction, a heating element in the internal cavity of the shell, for providing heat to the catalytic reforming section, and a microwave generator in the internal cavity of the shell, for providing microwave heat. The application can convert methane and carbon dioxide into synthesis gas with a hydrogen-carbon ratio of less than 1, all the heat in the reaction is provided from the outside, and the problem of carbon deposition can be avoided.