36results about How to "High deoxygenation rate" patented technology

The invention relates to a method and system for low temperature liquid phase hydrofinishing of Fischer-Tropsch syncrude. The method comprises the following steps: (1) Fischer-Tropsch syncrude and hydrogen are uniformly mixed in a hydrogen oil mixer in order to prepare a gas-liquid two-phase mixture of hydrogen bubbles and dissolved hydrogen oil, and the gas-liquid two-phase mixture is preheated in order to obtain a preheated material; (2) under a condition of low temperature liquid phase hydrofinishing reaction, the preheated material is added from the top of a fixed bed reactor with a liquid level control valve through a catalyst bed layer which is arranged in the fixed bed reactor from top to bottom, at the same time supplemented hydrogen is added into a catalyst bed layer, and reaction products are obtained at bottom of the fixed bed reactor; (3) reaction products are added into a low pressure separator for carrying out separation, separated reaction oil part is used as cycle oil and added into the gas-liquid two-phase mixture obtained in the step (1); wherein the temperature for the low temperature liquid phase hydrofinishing reaction is 200-249 DEG C. The method can guarantee low temperature alkene reduction and deoxidation, and equipment is saved.

The invention provides a Fischer-Tropsch synthesis oil hydrofining method which comprises the following steps: S1, mixing Fischer-Tropsch synthesis oil with hydrogen, carrying out a low-temperature pre-hydrogenation reaction, and converting unsaturated olefins in the Fischer-Tropsch synthesis oil into corresponding saturated hydrocarbons to obtain a pre-hydrogenation product; S2, performing a deephydrodeoxygenation reaction on the pre-hydrogenation product to obtain a hydrofining product; and S3, circulating a part of the hydrofining product, conducting mixing with Fischer-Tropsch synthesis oil, and then carrying out a low-temperature pre-hydrogenation reaction. Through circulation of a part of the hydrofining product, reaction temperature rise can be reduced, coking carbon deposition andinactivation of a catalyst are prevented, stable operation of the reaction is easy to maintain, and a high olefin conversion rate and a high oxygen-containing compound conversion rate are maintainedfor a long time.

The invention discloses an oil product hydrodeoxygenation upgrading catalyst and a preparation method and application thereof. The oil product hydrodeoxygenation upgrading catalyst comprises a catalyst carrier, and an active component and an auxiliary agent which are loaded on the catalyst carrier, wherein the active component comprises ruthenium oxide, molybdenum oxide, nickel oxide and/or cobaltoxide; the catalyst carrier comprises gamma aluminum oxide, zeolite and activated carbon; the auxiliary agent comprises phosphorus oxide; in the active component, the molar ratio of ruthenium oxide to molybdenum oxide to nickel oxide and/or cobalt oxide is (0.2-1): (10-28): (2-10). The oil product hydrodeoxygenation upgrading catalyst has the characteristics of high activity and conversion rate of low-temperature hydrodeoxygenation, good selectivity, repeated long-term recycling, good stability, strong coking resistance, good hydrothermal stability and good acid and water resistance, and thepreparation method is simple and wide in application prospect.

The invention relates to a non-supported mesoporous hydrodeoxygenation catalyst, which comprises elemental nickel and diniobium pentaoxide, wherein a molar ratio of the elemental nickel to the diniobium pentaoxide is 7:2-18:1. The preparation method comprises the following steps: dissolving a nickel salt and citric acid in an ethanol solution, dissolving a niobium salt in water, mixing, adjusting the pH value to 1-4 by using nitric acid, placing in an oil bath at a temperature of 80-100 DEG C, heating and stirring until the mixture is viscous, ultrasonically oscillating for 15-30 minutes, drying at a temperature of 80-120 DEG C for 4-10 hours, roasting at a temperature of 400-600 DEG C for 3-6 hours, and reducing at a temperature of 300-500 DEG C for 3-5 hours in a 10vol% H2/Ar atmosphere, wherein BET determination results show that the catalyst is of a mesoporous structure; and putting the catalyst and bio-oil into a batch reactor, and carrying out hydrodeoxygenation reaction for 1-8 hours at a hydrogen pressure of 1-4 MPa and a temperature of 180-250 DEG C to obtain a bio-oil hydrodeoxygenation product. The method is simple and efficient in synthesis and mild in reaction condition.

The invention discloses a hydrodeoxygenation process for biodiesel. The hydrodeoxygenation process is characterized in that a fixed bed reactor filled with a hydrodeoxygenation catalyst is adopted, and the hydrodeoxygenation catalyst comprises a carrier and an active component; the carrier is SAPO-5 doped with a heteroatom Cu<2+> in a synthetic skeleton structure; the active component is a mixture of dimolybdenum nitride Mo2N, tungsten nitride W2N, molybdenum carbide Mo2C and tungsten carbide WC; the catalyst further contains a catalysis aid which is a mixture of TiO2, CeO2, V2O5 and NbOPO4; and the reaction conditions of the fixed bed reactor are as follows: the reaction temperature is 300-450 DEG C, the hydrogen pressure is 2.5MPa-3.5MPa, the volume ratio of hydrogen to oil is 500 to 800, and the volume space velocity is 1.0h<-1>-2.5h<-1>. According to the hydrodeoxygenation process, the hydrodeoxygenation of the biodiesel can be maintained at a relatively high deoxidizing ratio (99.8% or above), and the catalytic activity is not obviously decreased after the continuous working for 500 hours.

The invention discloses a deoxidizing alloying agent. The deoxidizing alloying agent is prepared from an aluminum electrolyte waste inner lining brick. The particle size of the aluminum electrolyte waste inner lining brick is broken to be 5 mm or less firstly, the aluminum electrolyte waste inner lining brick obtained in the step (1) is dried under the temperature below 300 DEG C till the water content of the aluminum electrolyte waste inner lining brick is smaller than 1% of the total weight of the inner lining brick, and then the deoxidizing alloying agent is obtained. According to the deoxidizing alloying agent and a preparation method thereof, the deoxidizing alloying agent is prepared from the aluminum electrolyte waste inner lining brick, the aluminum electrolyte waste inner lining brick mainly adopts a furnace slag method for deoxidizing to make quickly contact with oxygen in steel slag, thus the speed of the deoxidizing reaction is high, and the deoxidizing rate is high; and the component of the deoxidizing alloying agent is stable, meanwhile smelting energy consumption is low, and production cost is low, so that recycling for aluminum electrolyte waste silicon-carbide brick solid waste is achieved, and additional value of the solid waste is promoted.

The invention disclsoes a hydrogenation and deoxygenation process of biodiesel. The hydrogenation and deoxygenation process is characterized in that the process adopts a fixed bed reactor; the fixed bed reactor is filled with a hydrogenation and deoxygenation catalyst; the catalyst comprises a carrier and an active component; the carrier is a compound or mixture of MSU-G, SBA-15 and HMS (Hexagonal Mesoporous Silica); the active component is a mixture of dimolybdenum nitride (MO2N), tungsten nitride (W2N), molybdenum carbide (Mo2C) and tungsten carbide (WC); the catalyst further contains a catalytic auxiliary agent; the catalytic auxiliary agent is a mixture of Cr2O3, ZrO2, CeO2, V2O5 and NbOPO4; reaction conditions of the fixed bed reactor are as follows: the reaction temperature is 300 DEG C to 450 DEG C, the hydrogen pressure is 2.5MPa to 3.5MPa, the hydrogen-oil volume ratio is 500 to 800 and the volume space velocity is 1.0h<-1> to 2.5h<-1>. By adopting the process provided by the invention, the hydrogenation and deoxygenation of the biodiesel can be controlled to be a relatively high deoxygenation rate (99.8 percent or more) and the catalytic activity does not fall significantly after 500 hours of continuous operation.

The invention discloses a double-activity Ni2P/Zr-SBA-15 catalyst and a preparation method and application thereof. The active component of the catalyst is Ni2P, and a carrier is Zr-SBA-15. The double-activity Ni2P/Zr-SBA-15 catalyst has the advantages that the preparation is simple, and the price is low; the activities of hydrodeoxygenation and isomerization are high, the anti-carbon accumulationability is strong, the oxygen removal rate reaches 98% or above, and the curcas oil with low price can be converted into biofuel with high content of straight-chain paraffin, high calorific heat andhigh price; after reaction is finished, the coking rate of the catalyst is lower than 1.66%; the main components of the biofuel are petroleum diesel and aviation kerosene, the combustion property is good, the stability is high, the petroleum diesel and aviation kerosene can be replaced, and the good industrial application prospect is realized.

The invention discloses a biodiesel hydrodeoxygenation process. The biodiesel hydrodeoxygenation process is characterized in that a fixed bed reactor is adopted for the process and filled with a hydrodeoxygenation catalyst, and the catalyst comprises a carrier and an active component; the carrier is SAPO-5 with heteroatom Co2+ doped in a synthetic skeleton structure; the active component is a mixture of molybdenum nitride (MO2N), tungsten nitride (W2N), molybdenum carbide (Mo2C) and tungsten carbide (WC); the catalyst further contains a catalytic promoter, the catalytic promoter is a mixture of TiO2, CeO2, V2O5 and NbOPO4; according to the reaction conditions of the fixed bed reactor, the reaction temperature ranges from 300 DEG C to 450 DEG C, the hydrogen pressure ranges from 2.5 MPa to 3.5 MPa, the hydrogen-oil volume ratio ranges from 500 to 800, and the volume air speed ranges from 1.0 h<-1> to 2.5 h<-1>. By means of the process, hydrodeoxygenation on biodiesel can be controlled at a high deoxidation rate (99.8% or above), and catalytic activity is not obviously reduced after continuous operation is carried out for 500 hours.

The invention discloses a hydrodeoxygenation process of biodiesel. The hydrodeoxygenation process of the biodiesel is characterized in that the process adopts a fixed bed reactor, the fixed bed reactor is filled with a hydrodeoxygenation catalyst, and the catalyst comprises a carrier and an active component; the carrier is SAPO-5 which is doped with heteroatoms Co<2+> in a synthetic skeleton structure; the active component is a mixture of MO2N, W2N, Mo2C and WC; the catalyst also comprises a catalytic promoter, wherein the catalytic promoter is a mixture of Cr2O3, ZrO2, CeO2, V2O5 and NbOPO4; the reaction conditions of the fixed bed reactor are that the reaction temperature is 300 to 450 DEG C, the hydrogen pressure is 2.5-3.5 MPa, the volume ratio of hydrogen to the oil is 500 to 800, and the volume space velocity is 1.0 to 2.5 h<-1>. The process can control hydrodeoxygenation of the biodiesel in a higher deoxidation rate (99.8% or above) and the catalytic activity is not decreased obviously after 500-hour continuous operation.

The invention discloses a biodiesel hydrodeoxygenation process which is characterized by comprising a fixed bed reactor filled with hydrodeoxygenation catalysts, the catalysts include carriers, active components and catalytic auxiliaries, the carriers are KIT-1 with synthetic skeleton structures doped with heteroatoms Co2+, the active components are molybdous nitride MO2N, tungsten nitride W2N, molybdenum carbide Mo2C and tungsten carbide WC mixture, and the catalytic auxiliaries are TiO2, CeO2, V2O5 and NbOPO4 mixture. The reaction condition of the fixed bed reactor includes reaction temperature of 300-450 DEG C, hydrogen pressure of 2.5-3.5MPa, hydrogen to oil volume ratio of 500-800, and volume space velocity of 1.0-2.5h<1>. By the process, the hydrodeoxygenation rate of biodiesel can be controlled to be high (99.8% or more), and catalytic activity cannot be obviously reduced in continuous running for 500 hours.

The invention discloses a biodiesel hydrodeoxygenation process. The biodiesel hydrodeoxygenation process is characterized in that a fixed bed reactor is adopted in the process, the fixed bed reactor is filled with a hydrodeoxygenation catalyst, and the catalyst comprises a carrier and an active component; the carrier is KIT-1 formed by doping heteroatom Cu2+ in a synthetic framework structure. The active component is a mixture of molybdenum nitride (MO2N), tungsten nitride (W2N), molybdenum carbide (Mo2C) and tungsten carbide (WC). The catalyst further comprises a catalytic promoter, and the catalytic promoter is a mixture of TiO2, CeO2, V2O5 and NbOPO4. According to the reaction conditions of the fixed bed reactor, the reaction temperature ranges from 300 DEG C to 450 DEG C, the hydrogen pressure ranges from 2.5 MPa to 3.5 MPa, the hydrogen-oil volume ratio ranges from 500 to 800, and the volume air speed ranges from 1.0 h<-1> to 2.5 h<-1>. According to the process, hydrodeoxygenation of biodiesel can be controlled at a high deoxygenation rate (99.8% or above), and catalytic activity is not obviously reduced after the process continuously runs for 500 hours.

The invention discloses a biodiesel hydrodeoxygenation process. The process is characterized in that a fixed bed reactor is adopted, a hydrodeoxygenation catalyst is filled into the fixed bed reactor, the catalyst contains a carrier and an active component; the carrier is KIT-1 doped with heteroatom Cu2+ in a synthetic skeleton structure; the active component is the mixture of molybdous nitride MO2N, tungsten nitride W2N, molybdenum carbide Mo2C and tungsten carbide WC; the catalyst further contains a catalytic promoter, the catalytic promoter is the mixture of Cr2O3, ZrO2, CeO2, V2O5 and NbOPO4; the reaction conditions of the fixed bed reactor are as follows: the reaction temperature is 300-450 DEG C, the hydrogen pressure is 2.5-3.5MPa, the hydrogen oil volume ratio is 500-800, and the volume space velocity is 1.0-2.5h-1. Through the adoption of the process disclosed by the invention, the catalytic activity has no obvious decrease when the hydrodeoxygenation energy to the biodiesel is controlled at high deoxygenation rate (99.8% and more) and the hydrodeoxygenation is continuously operated for 500 hours.

The invention discloses a biodiesel hydrodeoxygenation process. The process is characterized in that a fixed bed reactor is adopted, a hydrodeoxygenation catalyst is filled into the fixed bed reactor, the catalyst contains a carrier and an active component; the carrier is MCM-41 doped with heteroatom Cu2+ in a synthetic skeleton structure; the active component is the mixture of molybdous nitride MO2N, tungsten nitride W2N, molybdenum carbide Mo2C and tungsten carbide WC; the catalyst further contains a catalytic promoter, the catalytic promoter is the mixture of Cr2O3, ZrO2, CeO2, V2O5 and NbOPO4; the reaction conditions of the fixed bed reactor are as follows: the reaction temperature is 300-450 DEG C, the hydrogen pressure is 2.5-3.5MPa, the hydrogen oil volume ratio is 500-800, and the volume space velocity is 1.0-2.5h-1. Through the adoption of the process disclosed by the invention, the catalytic activity has no obvious decrease when the hydrodeoxygenation energy to the biodiesel is controlled at high deoxygenation rate (99.8% and more) and the hydrodeoxygenation is continuously operated for 500 hours.

The invention discloses a hydrodeoxygenation technology for biodiesel. The technology is characterized in that a fixed bed reactor is adopted and filled with a hydrodeoxygenation catalyst, and the catalyst is prepared from a carrier and an active component, wherein the carrier is MCM-41prepared by doping a synthetic framework structure with heteroatom Cu<2+>, and the active component is a mixture of dimolybdenm nitride MO2N, tungsten nitride W2N, molybdenum carbide Mo2C and tungsten carbide WC; reacting of the fixed bed reactor is conducted under the conditions that the reacting temperature ranges from 300 DEG C to 450 DEG C, the hydrogen pressure ranges from 2.5 MPa to 3.5 MPa, the hydrogen-oil volume ratio is 500-800, and the liquid hourly space velocity is 1.0-2.5 h<-1>. According to the technology, hydrodeoxygenation on the biodiesel can be controlled at high deoxygenation rate (99.8% or above), the catalytic activity is not obviously reduced after operation is continuously conducted for 500 hours.

The invention discloses a biodiesel hydrodeoxygenation technology. The biodiesel hydrodeoxygenation technology is characterized in that a fixed bed reactor is adopted in the technology and filled with a hydrodeoxygenation catalyst, and the catalyst contains a carrier and active ingredients; the carrier is heteroatom Co2+ -doped MCM 41 in a synthesized skeleton structure; the active ingredient is a mixture of dimolybdenum nitride Mo2N, tungsten nitride W2N, molybdenum carbonate Mo2C and tungsten carbonate WC; the reaction conditions of the fixed bed reactor are as follows: the reaction temperature is 300-450DEG C, the hydrogen pressure is 2.5-3.5MPa, the hydrogen-oil volume ratio is 500-800, and the volume idle speed is 1.0-2.5h/l. By adopting the technology, the higher deoxygenation rate (more than 99.8%) of the biodiesel can be controlled in hydrodeoxygenation, and the catalytic activity after continuous running for 500 hours is obviously reduced.