Abstract: A lifting control apparatus may include: a base for holding a basket containing silicon wafers; brackets provided on an outside of both ends of the base; and a driver for driving the brackets to move up and down. The driver is provided with a lead screw. The lead screw is connected with the bracket on a same side. The lead screw on one side is driven to rotate the lead screw on another side synchronously, and the lead screws on both sides are driven to move the brackets on both sides and the base between the brackets up and down together. Or the lead screws on both sides are driven to rotate synchronously, so that the lead screws on both sides drive the base between the brackets through the correspondingly brackets to move up and down together.

Abstract: A process of methane catalytic conversion produces olefins, aromatics, and hydrogen under oxygen-free, continuous flowing conditions. Such a process has little coke deposition and realizes atom-economic conversion. Under the conditions encountered in a fixed bed reactor (i.e. reaction temperature: 750-1200° C.; reaction pressure: atmospheric pressure; the weight hourly space velocity of feed gas: 1000-30000 ml/g/h; and fixed bed), conversion of methane is 8-50%. The selectivity of olefins is 30-90%. And selectivity of aromatics is 10-70%. The catalyst for this methane conversion has a SiO2-based matrix having active species that are formed by confining dopant metal atoms in the lattice of the matrix.

Abstract: A reactor configuration comprises an inlet section I, a preheating section II, a transition section III, a reaction section IV and an outlet section V; except for the preheating section II and the reaction section IV, the existence of the inlet section I, the transition section III and the outlet section V depends on reaction conditions; and the process realizes no coke deposition synthesis of methane and high selectivity synthesis of ethylene. The methane conversion rate is 20-90%; ethylene selectivity is 65-95%; propylene and butylene selectivity is 5-25%; aromatic hydrocarbon selectivity is 0-30%; and coke deposition is zero.

Abstract: A reactor configuration comprises an inlet section I, a preheating section II, a transition section III, a reaction section IV and an outlet section V; except for the preheating section II and the reaction section IV, the existence of the inlet section I, the transition section III and the outlet section V depends on reaction conditions; and the process realizes no coke deposition synthesis of methane and high selectivity synthesis of ethylene. The methane conversion rate is 20-90%; ethylene selectivity is 65-95%; propylene and butylene selectivity is 5-25%; aromatic hydrocarbon selectivity is 0-30%; and coke deposition is zero.

Abstract: A process of methane catalytic conversion produces olefins, aromatics, and hydrogen under oxygen-free, continuous flowing conditions. Such a process has little coke deposition and realizes atom-economic conversion. Under the conditions encountered in a fixed bed reactor (i.e. reaction temperature: 750-1200° C.; reaction pressure: atmospheric pressure; the weight hourly space velocity of feed gas: 1000-30000 ml/g/h; and fixed bed), conversion of methane is 8-50%. The selectivity of olefins is 30-90%. And selectivity of aromatics is 10-70%. The catalyst for this methane conversion has a SiO2-based matrix having active species that are formed by confining dopant metal atoms in the lattice of the matrix.

Abstract: Provided is a method for the preparation of a metal lattice-doping catalyst in an amorphous molten state, and the process of catalyzing methane to make olefins, aromatics, and hydrogen using the catalyst under oxygen-free, continuous flowing conditions. Such a process has little coke deposition and realizes atom-economic conversion. Under the conditions encountered in a fixed bed reactor (i.e. reaction temperature: 750˜1200° C.; reaction pressure: atmospheric pressure; the weight hourly space velocity of feed gas: 1000˜30000 ml/g/h; and fixed bed), conversion of methane is 8-50%. The selectivity of olefins is 30˜90%. And selectivity of aromatics is 10˜70%. There is no coking. The reaction process has many advantages, including a long catalyst life (>100 hrs), high stability of redox and hydrothermal properties under high temperature, high selectivity towards target products, zero coke deposition, easy separation of products, good reproducibility, safe and reliable operation, etc.

Abstract: The present invention is related to the preparation of a metal lattice-doping catalyst in an amorphous molten state, and the process of catalyzing methane to make olefins, aromatics, and hydrogen using the catalyst under oxygen-free, continuous flowing conditions. Such a process has little coke deposition and realizes atom-economic conversion. Under the conditions encountered in a fixed bed reactor (i.e. reaction temperature: 750˜1200° C.; reaction pressure: atmospheric pressure; the weight hourly space velocity of feed gas: 1000˜30000 ml/g/h; and fixed bed), conversion of methane is 8-50%. The selectivity of olefins is 30˜90%. And selectivity of aromatics is 10˜70%. There is no coking. The reaction process has many advantages, including a long catalyst life (>100 hrs), high stability of redox and hydrothermal properties under high temperature, high selectivity towards target products, zero coke deposition, easy separation of products, good reproducibility, safe and reliable operation, etc.

Abstract: The present invention discloses a method for preparing isocyanates by liquid-phase catalytic thermal cracking. In this method, in a reaction-rectification thermal cracking reactor, using a catalyst composition comprising a superfine powder metal oxide catalyst and an ionic liquid, an alkyl or aryl dialkylurethane, or multialkylurethane being a reactant is liquid-phase thermal cracked for a reaction time of 0.5-3 h under a reaction temperature of 160-220° C. and an absolute pressure of 1000-8000 Pa so as to prepare the corresponding isocyanate. The invention has the characteristics of low thermal cracking temperature, high yield of target products, relatively simple reaction apparatus and good universality for substrates (the yields of HDI, MDI, TDI, HMDI, NDI and IPDI or the like are all>85%) and the like.

Abstract: The present invention pertains to a novel method for preparing a carbamate, in which the method comprises reacting an aliphatic substituted urea and/or its derivatives, with a hydroxyl group containing compound to obtain a carbamate. In addition, the present invention provides a novel catalyst which is suitable for catalyzing the reaction to form a carbamate, and a method for preparing the novel catalyst. The method of the present invention for preparing a carbamate does not involve the application of carbon monoxide which is toxic, and the reaction conditions are relatively mild with high catalytic activity, high reaction selectivity of the catalyst, and a relatively short reaction time. Furthermore, the catalyst is separated from the reaction system and reused easily, which will facilitates scale up and industrial application.

Abstract: The present invention pertains to a catalyst for the synthesis of organic alkyl carbamates, the method for preparing the same and the use thereof. The catalyst comprises a catalytically active component and a catalyst support, and the catalytically active component being carried by the catalyst support, wherein the catalytically active component comprises a transition metal oxide, and the general formula of the transition metal oxide is EOx, wherein E is selected from transition metal element and x is in the range of 0.5-4.

Abstract: The present invention pertains to a catalyst for the synthesis of organic alkyl carbamates, the method for preparing the same and the use thereof. The catalyst comprises a catalytically active component and a catalyst support, and the catalytically active component being carried by the catalyst support, wherein the catalytically active component comprises a transition metal oxide, and the general formula of the transition metal oxide is EOx, wherein E is selected from transition metal element and x is in the range of 0.5-4.

Abstract: The present invention discloses a method for preparing isocyanates by liquid-phase catalytic thermal cracking. In this method, in a reaction-rectification thermal cracking reactor, using a catalyst composition comprising a superfine powder metal oxide catalyst and an ionic liquid, an alkyl or aryl dialkylurethane, or multialkylurethane being a reactant is liquid-phase thermal cracked for a reaction time of 0.5-3 h under a reaction temperature of 160-220° C. and an absolute pressure of 1000-8000 Pa so as to prepare the corresponding isocyanate. The invention has the characteristics of low thermal cracking temperature, high yield of target products, relatively simple reaction apparatus and good universality for substrates (the yields of HDI, MDI, TDI, HMDI, NDI and IPDI or the like are all >85%) and the like.

Abstract: The present invention pertains to a novel method for preparing a carbamate, in which the method comprises reacting an aliphatic substituted urea and/or its derivatives, with a hydroxyl group containing compound to obtain a carbamate. In addition, the present invention provides a novel catalyst which is suitable for catalyzing the reaction to form a carbamate, and a method for preparing the novel catalyst. The method of the present invention for preparing a carbamate does not involve the application of carbon monoxide which is toxic, and the reaction conditions are relatively mild with high catalytic activity, high reaction selectivity of the catalyst, and a relatively short reaction time. Furthermore, the catalyst is separated from the reaction system and reused easily, which will facilitates scale up and industrial application.