67results about How to "Improve distillation yield" patented technology

For conversion of crude oil or a heavy hydrocarbon fraction having an initial boiling point of at least 300° C., conducting a catalytic hydroconversion in a three-phase reactor operating in a boiling bed with an upward flow of liquid and gas, separating resultant effluent into a light liquid fraction boiling at less than 300° C. and a heavy liquid fraction boiling above 300° C., deasphalting the heavy liquid fraction to obtain a deasphalted hydrocarbon fraction and residual asphalt, and recycling at least one portion of the deasphalted hydrocarbon fraction upstream of the hydroconversion stage.

Integrated slurry hydrocracking (SHC) and coking methods for making slurry hydrocracking (SHC) distillates are disclosed. Representative methods involve passing a slurry comprising a recycle SHC gas oil, a coker gas oil, a vacuum column resid, and a solid particulate through an SHC reaction zone in the presence of hydrogen to obtain the SHC distillate. Recovery of an SHC pitch from fractionation of the SHC reaction zone effluent provides an additional possibility for integration with the coker, and particularly via the upgrading of the SHC pitch in the coker to provide coke and lighter hydrocarbons such as SHC vacuum gas oil (VGO).

The inventive technology may involve, in particular embodiments, novel use of a non-porous, high surface energy stationary phase to adsorb, in reversible fashion, the most polar component of a resins fraction of an input hydrocarbon when a mobile phase is passed over the stationary phase. Such reversible adsorption prevents irreversibly adsorption of such components on active stationary phase(s) downflow of the non-porous, high surface energy stationary phase, thereby conserving stationary phase costs and increasing resolution of resins elutions, and accuracy of hydrocarbon component results. Aspects of the inventive technology may also involve a novel combination of a solubility based asphaltene component fractionating and analysis method and an adsorption chromatography method for separating and/or analyzing saturate, aromatics and resins components of an input hydrocarbon.

The invention provides a method for extracting cinnamomum longepaniculatum leaf essential oil. The method comprises the following steps of A, pulverizing, wherein dried cinnamomum longepaniculatum leaves are pulverized and screened to obtain cinnamomum longepaniculatum leaf powder; B, enzymolysis, wherein an appropriate amount of water and cellulase are added into the cinnamomum longepaniculatum leaf powder obtained in the step A, water bath treatment is executed after even stirring, and continuous stirring is executed in the process; C, simultaneous distillation and extraction, wherein the mixture obtained in step B is simultaneously distilled and extracted in an organic solvent; D, oil-water separation and solvent removal, wherein an organic solvent phase is obtained through separation after the treatment in the step C, and then the organic solvent is removed to obtain crude extracted essential oil; E, dehydration, wherein the crude extracted essential oil obtained in the step D is subjected to dehydration treatment to obtain the essential oil. The essential oil in the cinnamomum longepaniculatum leaves can be fully released out by pulverization and cellulase treatment; meanwhile, the essential oil which is dissolved in a water phase by a conventional steam distillation can be extracted out by adopting a distillation extraction method. Thereby, the extraction rate of the cinnamomum longepaniculatum leaf essential oil can be significantly improved, and a cinnamomum longepaniculatum leaf essential oil product with better quality can be obtained.

The invention relates to a method for removing a base catalyst from crude biodiesel. The method comprises the following step of: removing the base catalyst from the crude biodiesel by taking glycerin as an extracting agent, wherein the extraction temperature is 60-150DEG C, the operating pressure is normal pressure, and a mass ratio of the crude biodiesel to the glycerin is 10-1. Compared with the prior art, the method has the advantages that: 1, the method for removing the base catalyst from the biodiesel by taking the biodiesel byproduct glycerin as the extracting agent avoids a problem of wastewater caused by a water washing process; 2, the base catalyst dissolved in the glycerin phase is separated in a cooling crystallization mode, the glycerin and the base catalyst can be cyclically applied to a production process mechanically, and production cost is reduced; and 3, the base catalyst is effectively removed, alcoholysis in the high temperature vacuum rectification process of the biodiesel is avoided, and the biodiesel rectification yield is improved.

The invention relates to a rectification method of piperonal. The specific steps are as follows: add 500 g of crude piperonal (wherein the raw material piperonyl ring contains 10%), 200 ml of inert solvent, connect a 10 cm rectification column, a fractionation device, and a receiving bottle into a 1000 ml single-necked flask ;Turn on the vacuum, measure the vacuum degree to be 30Pa, start to heat up, carry out total reflux at the beginning, and start to accept the previous fraction after half an hour of total reflux, the acceptance temperature of the former fraction is 100-150°C, higher than 150°C, lower than 180°C is the product pepper Aldehyde, get piperonal aldehyde rectification product 445g, content is higher than 98%. The addition of an inert solvent forms a protective layer on the surface of piperonal, which isolates the oxidation and polymerization of piperonal by a small amount of oxygen, and plays a protective role. It also reduces the risk of explosion and improves the distillation yield. .

The invention discloses a biodiesel continuous ester interchange technology, which comprises the following steps: I. mixing methanol with an alkali catalyst in a mixer; II. continuously pumping the mixed solution in the step I and low-acid or esterified waste oil into a continuous ester interchange reactor through a metering pump; III. enabling materials discharged from the continuous ester interchange reactor to continuously flow into a continuous glycerine soap separator, and separating out glycerine soap and methanol-containing crude methyl ester; and IV. enabling the glycerine soap separated in the step III to enter a continuous glycerine separator, separating out glycerin and waste oil, and recycling the waste oil for production; and V. enabling the methanol-containing crude methyl ester separated from the step III to continuously enter a methanol recycler, and enabling the recycled methanol to be used for production, and crude methyl ester to enter a rectifying tower for rectifying, to obtain crude biodiesel. The ester exchange reactivity can achieve more than 95%, the continuous production can be realized,and the conversion rate of fatty acid methyl ester can be up to more than 98%.

The invention discloses a method for separating 2,3-butanediol. The method comprises the following steps: (1) carrying out pretreatment on fermentation broth, so as to obtain clear fermentation broth; (2) adding an inorganic salt and/or an organic acid salt into the clear fermentation broth, carrying out thorough mixing, then, adding a low-polarity organic substance into the clear fermentation broth, carrying out thorough mixing, and then, carrying out standing layering, so as to obtain an upper phase, i.e., a 2,3-butanediol organic solution and a lower phase, i.e., a salt solution; and (3) carrying out electrodialysis desalination treatment on the upper phase, i.e., the 2,3-butanediol organic solution, and collecting a clear solution and concentrated liquor I; and carrying out electrodialysis desalination treatment on the lower phase, i.e., the salt solution by taking the concentrated liquor I as electrodialysis concentrated liquor circulating liquid, collecting and recycling concentrated liquor II, and distilling the clear solution, thereby obtaining the 2,3-butanediol product. According to the method, biomacromolecules such as thallus dissolved protein and lipids can be effectively removed from the fermentation broth so as to form a relatively uniform and pure liquid-phase system, and the implementation of next-step refining manners such as double-aqueous-phase and rectifying is facilitated, so that the method is applicable to large-scale production application.

The invention discloses a method for preparing 1,2-propylene glycol and normal propyl alcohol by using biologic glycerol. The method comprises the following steps: with biologic glycerol of which thepurity is more than or equal to 95% and hydrogen as main raw materials, by adopting a continuous reaction mode, first vaporizing glycerol, followed by atomizing with pre-heated hydrogen, and then carrying out a catalytic hydrogenolysis reaction on a fixed bed, wherein the reaction conditions are as follows: the temperature is 150-250 DEG C, the pressure is 0.8-2.5MPa, the molar ratio of hydrogen to glycerol is (10-50):1, and mass space velocity is 0.2-1.0/h, and while the materials are vaporized, the vaporized materials are allowed to flow through a fixed reaction bed loaded with a hydrogenolysis catalyst to be subjected to a catalytic hydrogenolysis reaction; the hydrogenolysis catalyst is a copper-based catalyst, comprising the following components according to molar ratio: 10-20% of Cu,30-40% of Al, 30-40% of Si, and 1-10% of Zr and rare earth. The method for preparing 1,2-propylene glycol and normal propyl alcohol by using biologic glycerol disclosed by the invention has the advantages of few equipment investment, low production energy consumption and low product cost.

The present invention relates to a technique for preparing an anhydrosugar alcohol using hydrogenated sugar as a raw material and, more specifically, to a technique for preparing a high-purity anhydrosugar alcohol (in particular, isosorbide, isomannide, isoidide, and the like) having a purity of 98% or higher and containing less than 0.1% of sorbitol and a sorbitan isomer, which are impurities, in a high total distillation yield of 94% or higher (more preferably, 95% or higher) by adding an acid to hydrogenated sugar (for example, hexitol) to convert same to an anhydrosugar alcohol, and then distilling the converted liquid over two or more stages by sequentially using a combination of an external condenser type wiped film evaporator and an internal condenser type short path evaporator.

The invention discloses a preparation method of trichloropyridine. The method comprises the following steps: enabling a low chlorinated pyridine compound to react with chlorine in a contact manner in the existence of a catalyst, so as to obtain a contact reaction product, wherein the catalyst is one or more of ferric chloride, zinc chloride, magnesium chloride and aluminum chloride; and leading in an inactive gas to the contact reaction product to distill. By adopting the method disclosed by the invention, the distillation yield of the trichloropyridine can be up to over 90%, and the obtained product trichloropyridine does not contain a catalyst ingredient. In addition, the distilled residue can be applied to catalyzed synthesis of the trichloropyridine.

The invention discloses an improved process method for preparing 5-chloroindanone, and belongs to the technical field of organic synthesis. The method comprises the following steps: mixing chlorobenzene with anhydrous aluminum trichloride, adding 3-chloropropionyl chloride, and carrying out Friedel-Crafts acylation reaction to obtain 3,4'-dichloropropiophenone; then carrying out catalytic cyclization under the condition of anhydrous aluminum trichloride/sodium chloride or tri(pentafluorophenyl)borane; and after the reaction is finished, washing the product with water and directly rectifying the product to obtain the 5-chloroindanone. According to the process disclosed by the invention, the direct distillation is performed after water washing, so that no subsequent operation is performed, the operation steps are reduced, the production time is shortened, the production cost is saved, the extraction effect of the product is greatly improved, the yield of the product is improved by 15% or above, low-boiling-point substances and high-boiling-point substances can be effectively removed through direct distillation, and the content of the product is improved to 99.5% or above; meanwhile, cyclization is carried out under catalysis of tri(pentafluorophenyl)borane, so that the total dosage of aluminum trichloride can be reduced, the cyclization reaction temperature is reduced, the generation of tar is reduced, and the yield of the product is improved.

This invention relates to a separation method of chlor-isoamylene. First preheats the output of isoprene react with hydrogen chloride; then send the output into the first tower central of continuous distillation tower which includes two series towers for vacuum distillation; the first tower pressure is -0.070 ~ - 0.100MPa, the top temperature of 30 ~ 60 deg C, the temperature of the tower reactor is 50 ~ 70 deg C, reflux ratio is 2 ~ 5; reflux pot of first tower has a Layered device for regular separating water; outputs component of reflux pot enter isomerism reactor for isomerism reaction, after water separating return to first tower; tower reactor components enter central of second tower, pressure is - 0.08 ~ 0.10MPa, the top temperature of 30 ~ 50deg, tower reactor temperature of 60 ~ 80 deg C, reflux ratio is 1-3, store the products of consecutive distillation in the tank with cooling jacket. Compared with existing technologies, this invention has energy-saving, high purity features.