315 results about "Continuous distillation" patented technology

Fluid sensor methods and systems adapted for monitoring and/or controlling distillation operations in fluidic systems, such as batch distillation operations or continuous distillation operations, are disclosed. Preferred embodiments are directed to process monitoring and/or process control for unit operations involving endpoint determination of a distillation, for example, as applied to a liquid-component-switching operation (e.g., a solvent switching operation), a liquid-liquid separation operation, a solute concentration operation, a dispersed-phase concentration operation, among others.

The invention describes a global method for extracting sterols, vitamin E, squalene and other vegetable hydrocarbons from deodorization distillates of vegetable oils. After esterification of the free fatty acids, followed by trans-esterification of the combined fatty acids (glycerides and sterides) with the same short alcohol, three successive distillations allow successive recovery of a first fraction of the hydrocarbons, the main fraction of alkyl esters, and then the heaviest alkyl esters with squalene. The third distillate will be used for producing squalene and a second fraction of hydrocarbons. The residue of the third distillation will be used for producing sterols and vitamin E. By using bio-ethanol, vegetable glycerol and the vegetable hydrocarbons of the method, with the method it is possible to extract each of the four unsaponifiables without any solvent of petroleum origin and claim the labels of products obtained by natural physical and chemical methods.

The invention relates to production technology for cracking butyl octanol residual liquid into C4 and C8 by means of an alkaline liquid cracking agent. The technology is characterized by comprising the following steps of: preparing the alkaline liquid cracking agent, wherein the alkaline liquid cracking agent consists of sodium hydroxide, potassium hydroxide, water, isopropanol, ethylene glycol, potassium permanganate, ethanol, barium nitrate and diboron trioxide; preheating the alkaline liquid cracking agent and the butyl octanol residual liquid through a preheater and adding into a distilling still, wherein the tower bottom temperature of the distilling still is between 200 and 280 DEG C, the tower top temperature is between 130 and 190 DEG C, and the tower top pressure is between 0.08 and 0.1Mpa below zero; and extracting the C4 and C8 generated by cracking from the tower top of the distilling still, pumping the C4 and C8 into a fractionating column at the downstream for fractionation, and extracting a small amount of uncracked heavy components from a tower bottom pump. The production technology has the advantages of high production capacity, high cracking selectivity, high content of the cracked useful components, low cost, simple process, and batch distillation or continuous distillation.

This invention is a making and refining method of cyclopentanol, which includes: 1) the materials comprises cyclopentene, phenylic acid solvent, water activator continuously pass through catalyst fixed bed to carry out hydration reaction, and the volume space velocity is 2-15hr to the power -1, the mole ratio of cyclopentene and water is 0.8-5.0, the weight ratio of phenylic acid and cycloamylene is 0.5-1.0. the intensity of activator is 0.01-0.2wt%, the reaction temperature is 130-180deg.C, the reaction pressure is 1.0-3.0MPa, the catalyst is strong acid cation exchange resin with sulfo group anchored on the surface, and the activating solvent is trialkylamine; 2)the reacted materials cool to house temperature and demix into oil phase and aqueous phase, the oil phase materials through continuous distilling separation procedure get non-reacting cycloamylene, refined cyclopentanol and phenylic acid full of solvent. The strong points of this invention are that the conversion of cyclopentene and selectivity of cyclopentanol are high, and the refining of cyclopentanol is simple and low energy consumption.

The invention relates to an improved process for alkyl phenol-formaldehyde thermoplastic tackifying resin. Liquid formaldehyde and solid formaldehyde are added, while water generated by a condensation reaction is continuously distilled out. The reaction speed of the condensation reaction of alkyl phenol and the formaldehyde is reduced due to water in the system, so the production efficiency as well as the production output is improved.

The invention relates to a process and a system for producing ethanol through solid-state continuous fermentation and distillation of sorgo straws, wherein the process comprises a raw material pulverizing and preprocessing step, a strain adding step, a solid-state fermentation step and a solid-state distillation step; the solid-state fermentation step is continuously finished in a multilayer multisection solid-state continuous fermentation device, and the solid-state distillation step is continuously finished in a multilayer differential pressure type solid-state continuous distillation device, thereby radically overcoming the abuse that the past solid-state fermentation and distillation processes can not continuously produce, realizing continuous, mass and automated production and processing, greatly improving the production efficiency of preparing the fuel ethanol from the sorgo straws, and achieving the purposes for lowering the production cost, improving the yield and improving the economic benefit; an adopted continuous production system device is particularly suitable for industrialized large-scale production, thereby promoting the generalization and the application of a biological energy source technology.

A process to re-refine used petroleum oils by extraction with aliphatic solvents, wherein after eliminating the extract solvent, the process consists of the following treatments, (a) flash, continuous vaporization, at atmospheric pressure or near atmospheric pressure, to separate the light fractions, in the presence of small amounts of a basic compound or a reducing agent or a combination of both and (b) continuous distillation, in a fractionating column, of the bottom liquid obtained in stage (a), under vacuum and moderate temperatures, in the presence of a basic compound or a reducing compound or a combination of both, with recirculation from the bottom of the column to its feed; separating, as lateral extractions, the vacuum gas-oil or spindle oil and the lubricant bases and, as bottom product, a fuel-oil or asphaltic component.

The invention discloses a production method of biological diesel oil, which takes oil feet acidified oil of vegetable oil, animal fat, drain oil and restaurant waste oil as material; and contains four steps of grease no-catalysis high-pressure hydrolysis, fatty acid gas-phase esterification, neutralization dealcoholization and washing, fatty acid methyl ester high-vacuum continuous distillation, etc. The production method of the invention has the advantages that the reaction time is short, the raw material conversion rate is high, the production cost is low, and the product quality is high; therefore the invention is applicable for industrial production.

The invention relates to a differential pressure type solid continuous distillation process, comprising the steps of: placing solid materials on a tower plate in a distillation tower, introducing vapor to the bottom of the tower plate for heating, collecting vapor by vaporizing materials from an outlet pipe at the upper part of the tower plate, and condensing the collected vapor by a condenser toobtain the product, wherein the heating process comprises a preheating loop, a distilling loop and a residual distilling loop. In the invention, the distillation process has scientific and reasonabledesign, realizes fast and efficient continuous distillation process by arranging different operation conditions in each loop, has the advantages of simple operation, large processing load, high production efficiency, high yield and the like, and can efficiently guarantee the consistency stability of the final product of distillation simultaneously.

The invention discloses a continuous distillation technology used for regeneration of spent lubrication oil. The continuous distillation technology includes a heat exchange process of the spent lubrication oil and distilled cut fraction, a visbreaking heat treatment process and a flash distillation-reduced pressure distillation process. By means of visbreaking heat treatment, clean dispersing additives in the spent lubrication oil can be broken down effectively to enable suspended impurities such as metal in the spent lubrication oil to be deposited more easily, and part of metal salt additives and corrosive organic acid can be decomposed or deteriorated. By means of flash distillation-reduced pressure distillation, light components and base oil fractions can be pulled out effectively. Additionally, an optimized heat exchange system is capable of lowering energy consumption caused by continuous distillation, the total pull-out rate of the technological spent lubrication oil is more than 85%, the continuous distillation technology is good in technological economy, low in impurity content (particularly in metal content), and distilled products can serve as quality raw materials for subsequent hydrofining directly.

The invention relates to a multilayer fluidized solid continuous distillation column which comprises a column body, a mixed steam outlet at the top of the column body, a feed inlet at a sidewall of the upper part of the column body, a superheated steam inlet at a sidewall of the lower part of the column body, and a slag outlet and a cleaning liquid outlet at the bottom of the column body. A set of gas distribution plates are staggerly installed at intervals on the internal wall of the column body between the feed inlet and the slag outlet, and included angles between the set of gas distribution plates and a horizontal plane are adjustable; each gas distribution plate is provided with steam pores; places of the column body corresponding to side edges of bottom ends of gas distribution plates are all provided with a material blanking control unit. The distillation column provided in the invention has the advantages of simple construction, convenient operation, great treatment capacity and a high degree of automation; multilayer gas distribution plates arranged in the distillation column allow a ferment material to be fluidized or periodically fluidized in the process of distillation, which enables rapid and high efficiency continuous distillation technology to be realized, and therefore, the multilayer fluidized solid continuous distillation column provided in the invention is update equipment for existing solid distillation columns.

A process for preparing pure triethanolamine (TEOA) by continuously distillatively separating an ethanolamine mixture comprising TEOA and diethanolamine (DEOA), by distilling off DEOA in a distillation column (DEOA column) and supplying the resulting bottom stream comprising TEOA to a downstream column (TEOA column) in which the pure TEOA is withdrawn as a side draw stream, wherein the residence time of the ethanolamine mixture in the bottom of the DEOA column is <20 minutes.

The invention relates to a testing device for simulating the equipment corrosion of a continuous distillation industrial device. The testing device comprises a continuous distillation system, a pressure control system and a corrosion sample system, wherein the top interface of a multi-mouth flask is connected with the bottom of a main reactor; the top interface of the main reactor is connected with the bottom of a main condenser; the top of the main condenser is connected with a non-condensable gas receiving tank, a cold trap, a gas buffering tank and an exhaust system through connecting pipes respectively, and is connected to a vacuum pump through the cold trap; and the corrosion sample system comprises a sample hanging device for placing samples into a steam phase and a liquid phase. A skillful reflow design is adopted in the invention, so that a condensed low-boiling-point liquid does not flow through the high-temperature main reactor, so that re-vaporization before reflowing to the bottom of the multi-mouth flask is avoided. Under the action of a reflow bypass, condensed low-boiling-point components and high-boiling-point components left at the bottom of the multi-mouth flask are fully mixed forcedly, and the distillation process is started once again, so that accurate simulation of continuous distillation is realized.

The invention provides a tester for simulating high-temperature corrosion in a continuous distillation apparatus, comprising a feeding module, a kettle corrosion detection module, a vacuumizing module, a control module of the vacuumizing module and a temperature and pressure control module, wherein the feeding module comprises a filter 2, an experiment oil material tank 4 and a plunger-type feeding pump 5; the kettle corrosion detection module comprises a reaction kettle 19 with condensers 14 and 15; a nitrogen inlet 8, the first condenser 14 and the second condenser 15 are arranged on a cover of the reaction kettle 19; the first condenser 14 is connected with a discharge tank 20, and the second condenser 15 is orderly connected with a vacuum cold trap 10, a vacuum buffer tank 12 and a vacuum pump 11 of the vacuumizing module. According to the invention, accurate simulation of a corrosion problem in a continuous industrial process can be realized by continuously updating experiment medium of the corrosion test part, and real simulation problems of gas-liquid phase corrosion in petroleum refining and chemical processes, such as continuous normal pressure distillation, reduced pressure distillation and the like, are solved.

The invention discloses a making method of high-purity L-lactic acid, which comprises the following steps: a) extracting; crystallizing; decoloring; proceeding ion exchange or film separation; transmitting predisposed L-lactic acid into condenser under 0.5-0.95Mpa at 50-90 deg.c to condensate; b) transmitting L-lactic acid into at least two-grade cascading short-path distill devices to distill; setting one-grade short-path under 50-500Pa at 50-130 deg.c to distill; transmitting the heavy component into two-grade short-path distill device; collecting light component to obtain high-purity L-lactic acid; distilling heavy component from two-grade short-path distill device under 10-500Pa at 100-120 deg.c to distill; collecting light component as high-purity product.

The invention discloses a process for continuously producing N-monomethylethanolamine, which comprises the following steps of: (1) pumping an ethylene oxide raw material and a monomethylamine raw material into a mixer or a two-stage mixer through a metering pump respectively, mixing the raw materials, and then reacting the mixed materials in a reactor to generate a mixture containing the N-monomethylethanolamine, wherein the mass ratio of the ethylene oxide raw material to the monomethylamine raw material is 1: 2-3; (2) delivering the mixture containing the N-monomethylethanolamine to an amine distillation tower, separating monomethylamine and an N-monomethylethanolamine coarse product by distillation, and conveying the distilled monomethylamine to a monomethylamine raw material container; and (3) conveying the N-monomethylethanolamine coarse product to a light component distillation tower and a reduced pressure rectifying tower in which efficient pore plate ripple fillers are filled and which are connected in series, separating an N-monomethylethanolamine product by continuous distillation, and continuously discharging the N-monomethylethanolamine product from the side or the topof the reduced pressure rectifying tower. The process is characterized in that the production process is continuous, the produced product has stable quality and high yield, and meanwhile, the processcan improve the yield and reduce the energy consumption and the material consumption, and is suitable for industrialized popularization and application.

The invention discloses a method for producing electronic grade hydrochloric acid, sequentially comprising the following steps of: (a) providing a 31% hydrochloric acid raw material with a national standard reagent grade; (b) carrying out microfiltration on the hydrochloric acid raw material, preheating in a preheater and putting into a reboiler; (c) heating the reboiler by utilizing saturated steam and obtaining an end product after hydrochloric acid steam generated through the heating passes through a condenser; (d) absorbing hydrochloric acid tail gas by utilizing running water; and (e) putting the end product obtained in the step (c) into an end product storage tank, carrying out ultrafiltration to remove grains and obtaining final hydrochloric acid which is applied to electronic industry. The method for producing the electronic grade hydrochloric acid, which is provided by the invention, is used for obtaining 37% electronic grade hydrochloric acid by adopting the method of carrying out direct and continuous distillation and purification on the 31% hydrochloric acid with the national standard reagent grade, has the characteristics of large ratio of yield to energy consumption,production continuity, simple process and equipment and good stability; furthermore, the concentration of the hydrochloric acid raw material has no specific requirement and the concentration of the end product can be adjusted at will.

The invention relates to a method and a device for refining crude products of m-phthaloyl chloride. The crude products are heated to evaporate light components. The light components with boiling points lower than that of m-phthaloyl chloride are separated from bulk solution through a gasification and transferred into a light components continuous distillation system from an evaporation unit to be refined to obtain a small amount of light components and m-phthaloyl chloride in the tower and the light component products at tower top, which meet the requirements of national standards. The liquid of m-phthaloyl chloride crude products without the light components is transferred into an m-phthaloyl chloride continuous distillation system from the evaporation unit to be refined to obtain m-phthaloyl chloride product with a purity of 99.96% and a yield of over 90% at tower top. With the adoption of the device, a continuous treatment process is realized and the problems of low productivities of a single set of batch or semi-batch refining device and serious environmental pollutions caused by unqualified products are solved.

The invention discloses a preparation method based on a rotary kiln-type continuous distillation pyrolysis and gasification incinerator. The rotary kiln-type continuous distillation pyrolysis and gasification incinerator comprises a feeding device, a kiln body rotary device, a distillation pyrolysis and gasification device and a waste gas purification device. The feeding device is arranged on the right end of the kiln body rotary device; the distillation pyrolysis and gasification device is arranged on the left end of the kiln body rotary device; the waste gas purification device is arranged on the left end of the distillation pyrolysis and gasification device; the kiln body rotary device comprises a rotary kiln; the distillation pyrolysis and gasification device comprises a distillation gasification chamber and a secondary combustion chamber; the waste gas purification device comprises a cyclone dust collector, a waste heat boiler, a fast cooling tower, a neutralizing tower, a bag-type dust collector, an induced draft fan and a spray scrubber; and the preparation method comprises the following steps of material primary combustion, material distillation gasification, smoke primary combustion, smoke primary dust collecting, smoke heat exchange, smoke fast cooling, smoke neutralizing, smoke secondary dust collecting, smoke disacidifying, and smoke up-to-standard releasing. By adopting the preparation method, medical wastes or industrial wastes can be subjected to drying and distillation pyrolysis by utilizing high-temperature smoke; fuel is saved; emission is environment-friendly; and the management cost of an enterprise is lowered.

The invention discloses a separation and purification method of coarse diglycolamine. The method comprises the following steps: sequentially carrying out continuous distillation on coarse diglycolamine which is prepared from diglycol in a manner of catalytic ammoniation through eight towers under the pressurized or atmospheric condition; separating out diglycolamine, morpholine and diglycol from un-reacted raw materials and impurities to obtain a diglycolamine product with the purity being over 99%; and simultaneously generating a byproduct morpholine and recovering un-reacted diglycol, wherein the eight towers are sequentially a deamination tower, an atmospheric azeotropic tower, a vacuum dehydrating tower, a vacuum morpholine recovery tower, a vacuum diglycolamine refining tower, a vacuum diglycolamine tower, a vacuum diglycol refining tower and a vacuum diglycol recovery tower. The separating and refining processes of the method are low in energy consumption, simple in flow, and easy to operate; the diglycolamine product with the purity being over 99% and the morpholine byproduct with the purity being over 99.5% are obtained; and the yield reaches 99.5%.

A process for recovering N-vinyl-2-pyrrolidone is provided which allows to recover N-vinyl-2-pyrrolidone efficiently and steadily and in high purity by continuous distillation from a mixed liquid containing N-vinyl-2-pyrrolidone, N-(2-hydroxyethyl)-2-pyrrolidone, compounds having a higher boiling point than N-vinyl-2-pyrrolidone and water. The process includes continuously distilling the mixed liquid using a distilling column, controlling the temperature of the bottom liquid of the distilling column at 180° C. or less.