777results about "Chemical modification purification/separation" patented technology

The reduction in the sulfur-containing content of diesel fuel is achieved by oxidation in the presence of a catalyst followed by a liquid-liquid countercurrent extraction.

A process for the removal of hydrocarbon contaminants, such as dienes and olefins, from an aromatics reformate by contacting an aromatics reformate stream with a hydrotreating catalyst and / or a molecular sieve. The hydrotreating catalyst substantially converts all dienes to oligomers and partially converts olefins to alkylaromatics. The molecular sieve converts the olefins to alkylaromatics. The process provides an olefin depleted product which can be passed through a clay treater to substantially convert the remaining olefins to alkylaromatics. The hydrotreating catalyst has a metal component of nickel, cobalt, chromium, vanadium, molybdenum, tungsten, nickel-molybdenum, cobalt-nickel-molybdenum, nickel-tungsten, cobalt-molybdenum or nickel-tungsten-titanium, with a nickel molybdenum / alumina catalyst being preferred. The molecular sieve is an intermediate pore size zeolite, preferably MCM-22. The clay treatment can be carried out with any clay suitable for treating hydrocarbons.

A method for desulfurizing a hydrocarbon stream (10) containing heterocyclic sulfur compounds, which process comprises contacting the heterocyclic sulfur compounds in the gas phase (60) in the presence of oxygen (70) with a supported metal oxide catalyst, or with a bulk metal oxide catalyst (600) to convert at least a portion of the heterocyclic sulfur compounds to oxygenated products as well as sulfur-deficient hydrocarbons and separately recovering the oxygenated products separately from a hydrocarbon stream with substantially reduced sulfur.

A process for preparing a cobalt-based Fischer-Tropsch synthesis catalyst includes introducing a soluble modifying component precursor of the formula Mc(OR)x, where Mc is a modifying component selected from the group comprising Si, Ti, Cu, Zn, Zr, Mn, Ba, Ni, Na, K, Ca, Sn, Cr, Fe, Li, Tl, Sr, Ga, Sb, V, Hf, Th, Ce, Ge, U, Nb, Ta, W or La, R is an alkyl or acyl group, and x is an integer having a value of from 1 to 5, onto and / or into a cobalt-based Fischer-Tropsch synthesis catalyst precursor, which comprises a porous pre-shaped catalyst support supporting cobalt in an oxidized form. The resultant modified cobalt-based Fischer-Tropsch synthesis catalyst precursor is reduced to obtain a cobalt-based Fischer-Tropsch synthesis catalyst.

The present invention discloses a sulfur wearable and catalyzing and oxidizing method for gas abundant of firedamp; the raw material gas abundant of firedamp such as coal bed gas firstly passes through a preheater for preheating, and then enters a oxidizing reaction device; under the condition of 0-0.5MPa of pressure, 500-750 DEG C of reaction temperature, 1000-3000h-1of reaction air speed, the firedamp in the air is reacted with oxygen to produce carbon dioxide and water in manganese base sulfur wearable and catalyzing and oxidizing bed; at the same time, a small quantity of firedamp is decomposed to produce carbon and hydrogen gas; the carbon and the hydrogen after being decomposed are also reacted with oxygen so as to reach the purpose of getting rid of oxygen in the airs abundant of firedamp effectively. The present invention adopts much newer and more economical new catalyzer, which does not need to desulfurize firstly for the air; the air can directly enter the oxidization reaction device for oxidization. So the present invention can decrease the cost and simplify the technics process.

The invention discloses a catalyst removing trace olefin in aromatic hydrocarbon. The catalyst comprises the following compositions by weight percentage: 30 to 70 percent of Al2O3, 30 to 70 percent of molecular sieve, and 0 to 40 percent of one or a compound of La-based rare earth, P, W, Nb and Mo. The catalyst is an alkylate catalyst, and can maintain high catalytic activity for a long time.

Chitosan membranes chelated with silver or cuprous material may be used to separate olefins from a mixture of olefins and paraffins. The feed stream is humidified, demisted, treated to remove sulfur compounds and passed to a cell having a chitosan membrane containing chelated silver or cuprous compounds. The process has a reasonable flux rate and is operable at reasonable temperatures and pressures. The process could be used in an olefin separation train.

This invention discloses a deoxidizer of manganese system and its preparation and application. The deoxidizer of this invention is using MnO / Mn3O4 as active constituent. Add alkali metal oxide and aluminium oxide that are active accelerators. This invention provides two preparations, which adopt precurosor compound of Mn3O4 or active Mn3O4 that is produced by calcining precurosor compound of Mn3O4 to mix with alkali metal oxide or hydroxide oxide and aluminium, kneading, forming, open-air drying, at last drying or then producing deoxidizer of this invention by calcining after drying. The deoxidizer of this invention can eliminate 1- 2000ppm oxygen which is in the aethylenum or propylene, at the same time it possesses fairly high mechanical strength.

The invention relates to a method for separating oxygenated chemicals and 1-hexene from a Fischer-Tropsch synthesis oil product.The method comprises the steps that C6 fraction material flow is obtained through distillation in a predistillation tower by taking the Fischer-Tropsch synthesis oil product as a raw material, and two streams of extraction agents are fed to remove oxygenated chemicals in an extraction tower to obtain material flow rich in the oxygenated chemicals and crude C6 hydrocarbon material flow; the oxygenated chemicals contained in the crude C6 hydrocarbon material flow are further removed through a third extraction agent, tertiary olefins are converted into corresponding ethers through methyl alcohol under the action of an etherification catalyst to be removed, further purification is performed through rectification, and then C6 isoparaffin components and cycloolefin components are removed sequentially through a fourth extraction agent and a fifth extraction agent respectively to obtain 1-hexene product material flow.Compared with the prior art, the method has the advantages of being simple in technological process, low in cost and the like, and not only is 1-hexene separated and purified from the Fischer-Tropsch synthesis oil, but also the oxygenated chemicals can be separated.

The invention relates to a method for extracting high-purity squalene by taking olive oil as a raw material. A technological route formed by adopting a secondary molecular distillation and silica gel column chromatography is as follows: an olive oil unsaponifiable substance is taken, squalene is separated and purified by using two stages of molecular distillation, primary molecular distillation is carried out under the conditions of the evaporation surface temperature of 100 to 200 DEG C, the systemic pressure of 0.001 to 0.01mbar and the scraping film rotor speed of 150 to 300rpm, and secondary molecular distillation is carried out to the obtained distillate; the secondary molecular distillation is carried out under the conditions of the evaporation surface temperature of 150 to 300 DEG C, the systemic pressure of 0.001 to 0.01mbar and the scraping film rotor speed of 200 to 350rpm, and the obtained distillate is a squalene crude product; ethyl acetate-normal hexane with different concentrations is used as a mobile phase to carry out gradient elution, the obtained eluent is collected according to time and a solvent is evaporated, the same fractions are merged through chromatographic detection, and the high-purity squalene can be obtained, wherein the content of the raw material olive oil of the squalene is enhanced from 3.6% to about 98%; and especially, by considering the requirement of industrialized production to select an extraction condition especially, the large-scale production of the squalene taking the olive oil as the raw material can be realized.

The present invention provides processes for removing CO2 from an effluent stream derived from an oxygenate to olefins reaction system. In one embodiment, the invention comprises contacting the effluent stream with a first CO2 removal medium in a first CO2 removal zone under conditions effective to remove a first portion of the CO2 from the effluent stream and form a first CO2 depleted stream. The first CO2 depleted stream is contacted with a second CO2 removal medium in a second CO2 removal zone under conditions effective to remove a second portion of the CO2 from the first CO2 depleted stream and form a second CO2 depleted stream comprising less than about 0.5 vppm CO2.

A process and system for separating and upgrading bio-oil into renewable fuels is provided. The process comprises separating bio-oil into a light fraction and heavy fraction based on their boiling points. The heavy fraction is then subjected to hydrotreatment, while the light fraction is not subjected to hydrotreatment. At least a portion of the un-hydrotreated light fraction and at least a portion of the hydrotreated heavy fraction are blended with petroleum-derived gasoline to thereby provide a renewable gasoline, and at least a portion of the hydrotreated heavy fraction is blended with petroleum-derived diesel to thereby provide a renewable diesel.

Methods for separating di-olefins from mono-olefins, and olefins from non-olefins such as paraffins, oxygenates and aromatics; are provided. The methods use metal salts which complex both mono-olefins and di-olefins, but which selectively complex di-olefins in the presence of mono-olefins. The metal salts are dissolved or suspended in ionic liquids, which tend to have virtually no vapor pressure. Preferred salts are Group IB salts, more preferably silver and copper salts. A preferred silver salt is silver tetrafluoroborate. A preferred copper salt is silver CuOTf. Preferred ionic liquids are those which form stable solutions, suspensions or dispersions of the metal salts, which do not dissolve unwanted non-olefins, and which do not isomerize the mono- or di-olefins. The equivalents of the metal salt can be adjusted so that di-olefins are selectively adsorbed from mixtures of mono- and di-olefins. Alternatively, both mono- and di-olefins can be adsorbed, and the mono-olefins selectively desorbed. The latter approach can be preferred when non-olefins are also to be separated. The mono- and di-olefin-containing mixture can be in the gas phase or in the liquid phase. The flow of mono- and di-olefin-containing mixture over / through the ionic liquid can be, for example, co-current, counter-current, or staged in stirred tanks, with countercurrent being preferred.

This application relates to a composite solvent for separating aromatics by extractive distillation, comprising a main solvent, a solutizer and a modifier. Said solutizer is selected from any one or mixtures of any two of C8–C11 aromatics having different number of carbon atoms, the content of which is 3–39 wt %, and the number of carbon atoms of the lowest aromatic in the solutizer should be greater than that of the highest aromatic in the aromatics to be separated. When the solutizer is selected from any one of C8–C11 aromatics, the composite solvent contains 0.01–10.0 wt % of the modifier; when the solutizer is selected from mixtures of any two of C8–C11 aromatics having different number of carbon atoms, the composite solvent contains 0–10.0 wt % of the modifier. Said main solvent and modifier are independently selected from sulfolane derivatives, N-formyl morpholine, and N-methyl pyrrolidone, provided that the acidity and basicity of the modifier are opposite to those of the main solvent. When the composite solvent is used to recover aromatics by extractive distillation, it is possible to moderate the operation conditions of solvent recovery, increase the yield of aromatics, and make the separated aromatics to be neutral.

The invention discloses a bi-component copper-zirconium catalyst for deeply removing CO, belongs to the technical field of impurity removal, and provides the bi-component copper-zirconium catalyst inorder to solve the problems of insufficient depth for removing the CO, high CO removing temperature, short service life and the like in the prior art. The bi-component copper-zirconium catalyst comprises 0.1 to 99.9 weight percent of main component CuO and 0.1 to 99.9 weight percent of second component ZrO2; the ZrO2 exists in a morphous form; and the XRD analysis shows that the grain diameter ofthe catalyst CuO is between 1 and 30nm and the specific surface is between 1 and 300m<2> / g. The catalyst can deeply remove the micro CO in various materials to below 30ppb at a reaction temperature ofbetween 0 and 150DEG C.

A process for removing mercury of the present invention is characterized in that an ionic mercury-containing liquid hydrocarbon placed in a container equipped with a circulating means is effectively contacted with a sulfur compound represented by the general formula (I): M1-S-M2 (I) wherein M1 and M2 may be the same or different and are each independently a hydrogen atom, an alkali metal or an ammonium group, by introducing the sulfur compound into a suction side and / or a discharge side of the circulating means while circulating the ionic mercury-containing liquid hydrocarbon into the container through the circulating means. By the process for removing mercury of the present invention, the ionic mercury is effectively removed from the liquid hydrocarbon in simple manner.

A hydrocarbon gas such as methane and LPG is desulfurized in the presence of oxygen and an oxidation catalyst to convert sulfur compounds in the gas to sulfur oxides. The sulfur oxides are then trapped downstream of the oxidation by an adsorbent. The amount of oxygen added to the hydrocarbon gas to promote oxidation is such that the sulfur compounds are selectively oxidized and the oxidation of the hydrocarbon gas is minimized to reduce hydrogen formation.

A process for the catalytic alkylation of an aromatic substrate with an alkylating agent is disclosed that comprises contacting the aromatic substrate and the alkylating agent in sequential alkylation zones to obtain an alkylaromatic. The first catalyst comprises UZM-8 zeolite and the second catalyst comprises beta zeolite. The process is particularly well suited for the alkylation of benzene with propylene to produce cumene.

A process for separating para-xylene from a plurality of xylene isomers, wherein the process introduces at a first feed point a first mixed xylene stream comprising a plurality of xylene isomers into a first adsorptive separation unit to produce a first para-xylene enriched stream and a first raffinate stream, and introduces a second mixed xylene stream comprising a plurality of xylene isomers into a second adsorptive separation unit to produce a second raffinate stream. The process feeds both the first raffinate stream and the second raffinate stream into a raffinate column. The process further introduces an extract stream from the second adsorptive separation unit into a first input of a split extract column comprising an internal partition defining a first distillation zone and a second distillation zone.

Methods and apparatus relate to removal of mercury from crude oil. Such removal relies on transferring mercury from a liquid hydrocarbon stream to a natural gas stream upon contacting the liquid hydrocarbon stream with the natural gas stream. Processing of the natural gas stream after used to strip the mercury from the liquid hydrocarbon stream removes the mercury from the natural gas stream.

An energy efficient, high throughput process for aromatics recovery can be readily implemented by revamping existing sulfolane solvent extraction facilities, or constructing new ones, so as to incorporate unique process operations involving liquid-liquid extraction and extractive distillation. Current industrial sulfolane solvent based liquid-liquid extraction processes employ a liquid-liquid extraction column, an extractive stripping column, a solvent recovery column, a raffinate wash column, and a solvent regenerator. The improved process for aromatic hydrocarbon recovery from a mixture of aromatic and non-aromatic hydrocarbons requires transformation of the extractive stripping column into a modified extractive distillation column. The revamping incorporates the unique advantages of liquid-liquid extraction and extractive distillation into one process to significantly reduce energy consumption and increase process throughput. The revamp entails essentially only piping changes and minor equipment adjustments of the original liquid-liquid extraction facility, and is therefore, reversible.

The invention provides a method for extracting squalene in vegetable oil deodorizer distillate through two-stage column chromatography, which comprises the following processing steps: performing saponifying pretreatment to separate unsaponifiable matters, performing first-stage column chromatography to separate tocopherol and sterol, and performing second-stage column chromatography to purify squalene. Through the whole process, the squalene having a content of about 50% can be obtained, and meanwhile, the tocopherol having a content of 70% or above and the sterol having a content of 98% or above can be also obtained. Thus, the method provided by the invention overcomes the problem of low pertinence in the traditional squalene extraction process, achieves favorable selectivity of column chromatography and greatly increases the extraction efficiency. The process has the advantages of simple operation procedure, high separation efficiency, high squalene recovery rate, low investment and the like.

The present invention relates to a thermally integrated multi-zone process for conversion of alkanes to their corresponding alkenes, involving endothermically converting an alkane to its corresponding alkene by soft oxidant conversion in an endothermic reaction zone, in the presence of a weak oxidant, a suitable catalyst, and heat, to produce an intermediate product gas comprising the corresponding alkene and hydrogen. The weak oxidant may be, for example, carbon dioxide. The hydrogen is then removed from the intermediate product gas by contacting the intermediate product gas, in an exothermic reaction zone, with different second catalyst, and oxygen, to combust the hydrogen and produce a heated product stream comprising the corresponding alkene, water and heat. Heat is recovered from theheated product stream and recycled back to the endothermic reaction zone, while the resulting cooled product stream comprising the corresponding alkene may be subjected to further reaction and / or processing.

The invention discloses a process for refining C-4 hydrocarbon fluid. Preparation equipment includes a methanol removing tower, a first hydrogenation reactor, a second hydrogenation reactor, a depropanizing column, a dethanizing column and an adsorption tower, wherein the top of the methanol removing tower is connected with the bottom of the first hydrogenation reactor through a high-efficiency coalescer; the top of the first hydrogenation reactor is connected with the bottom of the second hydrogenation reactor through a pipeline; the top of the second hydrogenation reactor is connected with the depropanizing column through another pipeline; the top of the depropanizing column is connected with the dethanizing column through another pipeline; and the bottom of the dethanizing column is connected with the adsorption tower through another pipeline. The process mainly aims to a purification process of an alkylation raw material, and comprises the following steps: by taking mixed C-4 hydrocarbon as a raw material, extracting with water to remove methanol so as to reduce the content of methanol in C-4 hydrocarbon to be lower than 50ppm, selectively adding hydrogen and isomerizing so as to reduce the content of butadiene in C-4 hydrocarbon to be lower than 50ppm, converting more than 70% of 1-butene into 2-butene, and finally rectifying to remove dimethyl ether and C-3, thereby obtaining refined C-4 as the alkylation raw material, and a byproduct refined C-3 as a propane dehydrogenation propylene raw material.