CN102247709B - Environment-friendly type low-temperature extraction agent and preparation method thereof - Google Patents
Environment-friendly type low-temperature extraction agent and preparation method thereof Download PDFInfo
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- CN102247709B CN102247709B CN201110090298.6A CN201110090298A CN102247709B CN 102247709 B CN102247709 B CN 102247709B CN 201110090298 A CN201110090298 A CN 201110090298A CN 102247709 B CN102247709 B CN 102247709B
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Abstract
The invention relates to a preparation method of an environment-friendly type low-temperature extraction agent. In the preparation method, 6# solvent oil which is refined through hydrogenation and isomerized is taken as a raw material and 2-methylpentane, 3-methylpentane, n-hexane, and the like which have higher content are separated, so that the purity of a plant oil low-temperature extraction agent reaches 95 percent or more than 95 percent, and the requirements for production of an environment-friendly type plant oil low-temperature extraction agent solvent are met. The invention has the advantages of moderate reaction condition, convenience for quality control during production operation, good stability and reliability of product purity, high removal rate of olefin, arene and toxicants, good product quality and high safety.
Description
Technical field
The invention belongs to petrochemical industry, specifically by a kind of by the 6# solvent naphtha after hydrofinishing and isomerization, be raw material, the higher 2-methylpentane of content, 3-methylpentane, n-hexane etc. are separated, made its purity reach the preparation method that more than 95% technological innovation method is produced a kind of environment-friendly type type low-temperature extraction agent.
Background technology
Varsol industrial products particularly the application in the production process of vegetable oil industry belonged to conventional production method.Its purposes is wide, also can be applicable to the industrial circles such as aerosol, coating, rubber except vegetable oil industry.But along with the development of modern industry, modern civilization, modern society's life, the mankind are more and more higher to the attention degree of environmental protection for foodsafety, the production process of edible oils product, and the improvement of environmental pollution requires more and more stricter with control.While just hydrocarbons product being applied to vegetable oil extracting industry as solvent naphtha as states such as European Union, to the alkene in product and arene content, the impurity in solvent naphtha or the content of noxious material have very harsh and strict requirement.
But in China and even overwhelming majority of countries, the technical method adopting in production exists many problems.As, the 6# solvent naphtha using in conventional production be boiling range scope at 60～90 ℃ of oil products, the width of its boiling range has determined that this product is the mixture of multiple petroleum distillate.Currently marketed 6# solvent naphtha flow process scope is many between 58～75 ℃, and key component is wherein four kinds, accounts for more than 85% ratio.Respectively 2-methylpentane 25～30%, 3-methylpentane 25～30%, n-hexane 30% left and right, methyl cyclopentane 5～10%.Remaining component is approximately 2% C5, and approximately 5% boiling point is higher than the component of methyl cyclopentane.
Summary of the invention
Distillation is a kind of common method of each component of fractionation liquid phase homogeneous mixture, separated according to being that in mixed liquor, each component volatilization ability there are differences.
Liquid can be vaporized into steam, and this performance is referred to as the volatility of liquid.The volatilization ability of different pure component liquid has difference.Low-boiling pure component under the high or identical pressure of saturated vapor pressure at the same temperature, its volatilization ability is strong; Otherwise, a little less than.
With water, compare with ethanol, under normal pressure, the boiling point of water is 100 ℃, 78.3 ℃ of the boiling points of ethanol; In the time of 35 ℃, the saturated vapor pressure of ethanol is 100mmHg, and water saturation vapour pressure is 41.8mmHg, so ethanol is more volatile than water.
In blended liquid phase, the volatilization ability of different component there are differences equally.When vapor liquid equilibrium, can not be merely from vapour phase the size of each component vapor partial pressure weigh the volatilization ability of each component, minute concentration difference because of each component in balance liquid phase, the chance of transferring to vapour phase from liquid phase differs, different component should be connected in the dividing potential drop of vapour phase and its equilibrium concentration in liquid phase, could contrast the difference of volatility therebetween.
In admixture of gas according to Dalton's law (of partial pressures) in any container, if there is not chemical reaction between each component, each gas is all evenly distributed in whole container, and the pressure that the pressure that it produces produces while occupying whole container separately with it is identical.That is to say, the pressure of a certain amount of gas in the container of a constant volume is only relevant with temperature.For example, during zero degrees celsius, the pressure of 1mol oxygen in 22.4L volume is 101.3kPa.
If add 1mol nitrogen and keep container volume constant in container, the pressure of oxygen or 101.3kPa, but total pressure in container increases and is twice.Visible, the pressure that 1mol nitrogen produces is in this state also 101.3kPa.British scientist John dalton has summed up these experimental facts, draws following results: the dividing potential drop that a certain gas produces in admixture of gas equals the pressure producing when it occupies whole container separately; And the total pressure of admixture of gas equals wherein each partial pressure sum, Here it is law of partial pressure (law of partial pressure).
As everyone knows, all operations of carrying out component separation according to distillation principle all belong to distillation procedure.Common distillation procedure has flash distillation, simple distillation, continuous rectification, batch fractionating etc.
In various types of distillation operations, can be divided into binary distillation and multicomponent distillation according to the difference of component of mixture number again, according to the difference of operation pressure, be divided into normal pressure, pressurization or vacuum distillation.In addition, be to improve the separation degree of component, add in addition other component in distillation procedure, this distillation is special distillation, comprising sequence of constant boiling and rectification, extracting rectifying, salt adding rectifying etc.
Wherein, rectifying be in same equipment, realize material repeatedly part vaporization with partial condensation to obtain a kind of distillation procedure that improves separating effect, can obtain purer product, most widely used.
Certain binary mixture is housed in distillation still, with indirect steam heating to bubble point, solution vaporization, the steam of producing congeals into liquid collection in product storage tank through condenser, Here it is simple distillation procedure.
The relative volatility of supposing solution is greater than 1, in still-process, in the balance steam being produced by solution due to arbitrary moment, in volatile components concentration ratio solution, the concentration of volatile components is high, carrying out along with still-process, in still, in solution, volatile components content is also more and more low, and in the steam thereupon producing, the content of volatile components is also more and more low.In production, often require to obtain the product of variable concentrations, available different storage tank is collected the product of different time.
Now analyze the simple distillation process through infinitely small time interval dr, with the differential expression of process of establishing.
If certain in a flash in still liquid measure be W, strength of fluid is x, in solution, volatile components amount is Wx.Through the dr time, evaporation capacity is dw, and solution concentration is reduced to (x-dx), in solution the amount of volatile components be (w-dw) (x-dx).At dr in the time, although the vapour concentration y of balance is variable, because dr is dimensionless, according to Differential Principle, the instantaneous y value of desirable beginning as dr in the time invariable y value process, so can list following differential expression.
(x-dx), its simplified style is dw/W=dx/ (y-x) to Wx=ydw+ (W-dw).
To above formula integration, can obtain formula: y
flat=x
1+ w
2(x
1-x
2)/(w
1-w
2)
Bi-component continuous rectification, when saturated vapor contacts with the saturated liquid lower than vapor phase temperature under adiabatic condition, vapour, liquid can reach new equilibrium state.
When state point is 1 to contact with 2 vapour, liquid, through abundant mass transfer, reach the vapour, liquid phase of new equilibrium state as shown in figure 3,4 again.The effect of mass transfer is that vapour phase concentration improves, liquid concentration reduction.The vaporization of the partial condensation of vapour phase and the part of liquid phase has occurred in this process, and vapour phase partial condensation liberated heat is mainly used in liquid partly vaporize (change and compare very littlely with latent heat with the corresponding sensible heat of phase temperature change, can omit).It is the important means that realizes component fractionation that this declaratives vaporization combines with partial condensation.Distillation operation is according to this operation as separation principle.
Wish strengthens separating effect, must carry out multistage partial condensation and the process that part vaporization combines, and conventionally uses multilayer column plate to realize this operation.
Plate column has many types.For illustrating principles of rectification, only introduce the simplest a kind of tower---drench and fall sieve-plate tower.This column plate is a flat board, is drilled with many regularly arranged small sircle holes on plate, forms by " sieve plate ".During operation, liquid leaks down from sieve aperture, and gas upwards flows through sieve aperture.On sieve plate, there is certain thickness hydrops.Gas through liquid layer, is full of foam with bubbling form in liquid layer on plate.Vapour, liquid are partly vaporized to realize vapor portion condensation and liquid with form of foam two-phase contact mass transfer.
Meanwhile, in the tower of an adiabatic multilayer column plate, the n piece column plate of take is example, and through vapour, liquid contact, saturated vapor concentration is by y
n+1increase to y
n, liquid concentration is by x
n-1be down to x
n.If without azeotrope, gas by tower at the bottom of step by step tray rise, when concentration is brought up to tower top gradually, y1 can reach the degree that approaches pure volatile components; Liquid is flowed down by tower top step by step tray, and when concentration step by step tray is reduced at the bottom of tower, xm can reach the degree that approaches pure difficult volatile component.
This explanation, wish obtains the separation to component very high level by the rectifying separation of many layer column plates, must solve two problems.With concentration x
0very high liquid adds and concentration Y from tower top
m+1very low steam is introduced in tower at the bottom of tower.The method that solves these two problems in engineering is, goes out the gas of tower top after condenser total condensation is liquid, and wherein a part is as overhead product in order, and another part is reintroduced back to tower top.This part liquid that flows back to tower top is called " backflow " liquid.Equally, make that liquid is in distillation still after being heated to bubble point at the bottom of tower, at the bottom of the steam of generation is reintroduced back to tower, the still liquid of discharge is as bottom product.Steam at the bottom of introducing tower is " backflow " steam.When raw material is after suitable column plate place enters in tower, if raw material is saturated liquid, on the approaching plate of liquid concentration and material concentration, enter onboard; If raw material is saturated vapor, the approaching plate upper feeding of vapour phase concentration and material concentration onboard.
Rectifying is the process of a component separation, reduces to cause that because of charging the mixing of variable concentrations material is favourable to separation.
If inlet amount is F, input concentration is Z
f, tower top, end product are respectively D, W, and overhead product concentration is X
d, bottom product concentration is X
w, for stationary state operation, have:
F=D+W, FZ
f=DX
d+ WX
w; (material balance)
By above formula, can be solved: D/F=(Z
f-X
w)/(X
d-X
w); D/W=(Z
f-X
w)/(X
d-Z
f).This formula is the expression formula of lever principle.
Conventionally tower the section more than column plate of charging is become to rectifying section, be intended to make the concentration of ascending air progressively to improve.Comprise that the tower section below the feedboard of feedboard is called stripping section, be intended to make in dropping liq volatile components to be progressively suggested and concentration declines.Overhead reflux fluid flow is R times of overhead product flow, therefore phegma flow is RD.R is called " reflux ratio ".
First the present invention breaks through from separated theory has been realized to critical essence the most at all, and it has broken through the traditional idea thoughtcast of a certain distillation mode of application separately, and distillation fractionation principle is put in a larger system and is applied.In large system, simple distillation can comprise high-purity distillation, and high-purity distillation can comprise simple distillation, does not make separately by some way but adopts the mode combining.
The present invention take simple distillation as basis, in the process of simple distillation using rectifying as process means.This separation is had any different in continuous distillation process, also has any different in simple still-process.Technique bag of the present invention does not have the concept of head tank, if because adopt the flow process head tank of two towers configurations to that is to say products pot (or cry product purification tank more definite).From production process, see that some product raw mixture belongs to continuous rectification process; Some product belongs to the process of repeatedly simple distillation, has the advantages that interruption is produced in batches.Owing to having the basic characteristics of simple distillation, so separation process can't not be all products simultaneously, but product output successively from light to heavy goes out different products according to the production phase in the production process of same batch, switches different products pots in good time.This compares and does not need to use multitower to realize multi-component while fractionation with simple employing distillation process, only uses single tower or double tower to realize stage by stage multi-component separation.With the raw mixture of separated equal number, this manufacture method is compared with the energy consumption of classical production process substantially without increasing, but operation easier but declines to a great extent, and does not exist process control fluctuation to cause products pot contaminated so that underproof risk.When going out stage by stage every kind of product, still that method by rectifying obtains, because manufacture method of the present invention does not need a fractionation, just can not realize object product is all extracted, therefore can adopt gentle mode of operation, make thermal source, low-temperature receiver, operator's level no longer become the restraining factors of product quality, guaranteed in itself the stable and reliable of product quality.
Accompanying drawing explanation
Below in conjunction with drawings and Examples, the preparation method of a kind of environment-friendly type type low-temperature extraction agent of the present invention is further described.
Accompanying drawing 1 is the preparation method's of a kind of environment-friendly type type low-temperature extraction agent of the present invention schematic flow sheet.
The specific embodiment
With two tower flow process configurations, it is example that the 6# solvent naphtha of take is produced high purity product, and the basic craft course of the inventive method is as follows.
When two tower flow processs are configured in tower 1 and go out successively compared with light component, can gradually a small amount of restructuring be separated at tower 2.
In above four kinds of object products, there are three kinds of object product purities to require more than 95%, i.e. 2-methylpentane, 3-methylpentane, n-hexane; N-hexane purity requirement in food industry hexane is more than 60%, and wherein C5 and restructuring are divided into non-object product.According to the needs of product, need products pot >=5 of configuration, i.e. A2-methylpentane tank, A3-1 methylpentane tank, A3-2 n-hexane tank; Food industry hexane tank A4 and heavy constituent tank A5; C5 amount is few does not establish separately products pot, is called in other products or in heavy constituent.Head tank A1 is used as purification tank simultaneously.Because this technique bag does not need intermediate products tank, therefore cancel pans concept.
More detailed production process of the present invention is further described in conjunction with following embodiment:
Embodiment 1
Go C5 process.Charging from purification tank enters tower V1, and this process is controlled at 55～58 ℃ by tower V1 bottom temp, refluxes and control reflux ratio 5～8 in top, and the C5 deviating from enters corresponding storage tank as required.It is not principle containing the above component of C6 that process control be take in flow process up-sampling C5.Tower V1 bottom discharge enters tower V2.Tower V2 top does not need to maintain larger backflow, sets up in principle stable backflow, reflux ratio 2～3.Tower V2 bottom is controlled at 80 ℃ of left and right, first removes the component heavier than methyl cyclopentane, and taking less reflux ratio is not wish excessive fractionation at the bottom of tower, takes away valuable normal hexane product resource.Tower V2 top discharge is controlled load according to material balance, turns back to purification tank.When the basic product-free in tower V1 top can go out, go C5 process to finish; When tower V2 bottom can go out without heavy constituent, remove than the process of methyl cyclopentane heavy constituent and finish.
Embodiment 2
Produce 2-methylpentane process.After going C5 process to finish, enter this process.This process is controlled at 59～61 ℃ by tower V1 bottom temp.Reflux to control according to operating capacity of returns more easily and control in top.Tower top discharging, according to carrying out balance lower than 2-methylpentane total content, is guaranteed more than 10 reflux ratios.Overhead product enters 2-methylpentane tank, goes out before this certain amount of 2-methylpentane of seldom measuring C5 that contains and enters head tank or other tank, until C5 content meets the demands.It is not principle containing the above component of 2-methylpentane that process control be take in flow process up-sampling 2-methylpentane.Tower V1 bottom discharge enters tower V2.Tower V2 top does not need to maintain larger backflow, sets up in principle stable backflow, reflux ratio 2～3.Tower V2 bottom is controlled at 75 ℃, and part removes methyl cyclopentane, and taking less reflux ratio is not wish excessive fractionation at the bottom of tower, takes away valuable normal hexane product resource.Tower V2 top discharge is controlled load according to material balance, turns back to purification tank.When the basic product-free in tower V1 top can go out, produce 2-methylpentane process and finish; When tower V2 bottom can go out without heavy constituent, the process that this stage partly removes methyl cyclopentane component finishes.
Embodiment 3
Produce 3-methylpentane process.Produce after 2-methylpentane process finishes and enter this process.This process is controlled at 62～63 ℃ by tower V1 bottom temp.Reflux to control according to operating capacity of returns more easily and control in top.Tower top discharging, according to carrying out balance lower than 3-methylpentane total content, is guaranteed more than 10 reflux ratios.Overhead product enters 3-methylpentane tank, goes out before this certain amount of 3-methylpentane that contains a small amount of 2-methylpentane and enters food industry hexane tank or light isohexane tank, until 2-methylpentane content meets the demands.It is not principle containing the above component of 3-methylpentane that process control be take in flow process up-sampling 3-methylpentane.Tower V1 bottom discharge enters tower V2.Tower V2 top does not need to maintain larger backflow, sets up in principle stable backflow, reflux ratio 2～3.Tower V2 bottom is controlled at 72 ℃, substantially removes methyl cyclopentane, and taking less reflux ratio is not wish excessive fractionation at the bottom of tower, takes away valuable normal hexane product resource.Tower V2 top discharge is controlled load according to material balance, turns back to purification tank.When the basic product-free in tower V1 top can go out, produce 3-methylpentane process and finish; When tower V2 bottom can go out without heavy constituent, the process that this stage removes methyl cyclopentane component substantially finishes.
Embodiment 4
Production food industry hexane process.After production 3-methylpentane process finishes, the material in purification tank has far surpassed the requirement of narrow boiling range food industry hexane.Therefore purifying tank material now can be directly to food industry hexane tank, the requirement according to client to product content and composition, and allotment is dispatched from the factory.
Embodiment 5
Produce n-hexane process.Produce after 3-methylpentane process finishes and enter this process.This process is using tower V1 as feed preheater, and bottom temp is controlled at 64～65 ℃.Reflux and to maintain less backflow in top, the safe operation of pump of take is principle.Tower top discharging is only limited to transition stage, and this stage goes out Ta Nei and intrasystem 3-methylpentane to the greatest extent completely, to return tank analyze 3-methylpentane content qualified till.This part overhead product enters food industry hexane tank.Tower V1 bottom discharge enters tower V2.Tower V2 top need to maintain larger reflux ratio, should be not less than 5, with capacity of returns, can easily reach, and counter rolling back carried out material balance.Tower V2 bottom is controlled at 69～70 ℃, discharging feed product industrial hexane tank at the bottom of tower.By above theoretical explanation and embodiment, illustrate, a kind of environmental-friendly plant oil low temperature extractant of the present invention and preparation method have realized following object.
1, can produce in batches.If belong to discontinuity Discontinuous manufacture in single tank raw material.Head tank is as purification tank, and last a kind of high purity product is a concentrated process of purifying gradually.
2, arrive on the lenient side heavy output product successively.If in single tank raw material, the principle of the simple distillation that is based on.When going out every kind of product, do not expect that a step all put forward this component, take progressively to propose the strategy of object product.And the proposition process of object product is highly efficient distilling process.
When 3, product switches, there is changeover portion.At changeover portion, in next object product, contain an a small amount of upper object product.The tank that this part transitional discharging can enter byproduct tank or can not pollute product.
4, the control of process control column bottom temperature is particularly important.Column bottom temperature has determined the position to boiling range cutting.Therefore after having determined the cutting temperature of object product, to operate than being easier to realize temperature controlled load, guaranteed the reliability of cutting products purity.When switching product successively, adjust successively the control range of column bottom temperature.
5, the ratio of product discharge is dynamic change.Because it is concentrated gradually that this technique purification tank is heavy constituent, the process that light component reduces gradually, so the load of product is the process reducing gradually.Therefore to follow the tracks of and regulate discharging ratio to maintain the stable of return tank liquid level.If have ready conditions, use two purification tanks, the discharging ratio in purification process a period of time that can realize is stablized simultaneously.
6, because product is the process proposing gradually, therefore, in whole proposition process, should guarantee the purity that product is enough, as long as hold the not principle of superelevation of column bottom temperature, be easy to realize.
7,3 kinds of modes are taked in the control of product quality.The one, the detailed hydrocarbon analysis on goods batch, guarantees the process purity that product is enough; The 2nd, the monitoring analysis of products pot detailed hydrocarbon; The 3rd, the analysis of purification tank detailed hydrocarbon, is mainly a certain product will carry time, instructs the opportunity of switching product.
8, can guarantee loose operating environment and larger operating flexibility.Because product is the process proposing gradually, can be according to anti-decision machining loads that pushes back of many factors such as thermic load, refrigeration duty, pump loads.
9, be applicable to take the distilation process that fine chemical product is target market.Because this technique is to produce in batches, be more suitable for market capacity absolute value little, but the very high products' realization process of added value.
10, the preparation method's of a kind of environment-friendly type type low-temperature extraction agent of the present invention technique is surrounded by very strong versatility, can promote to similar process and product object field.
11, there is stronger technique extension.According to enterprise investment quantity and desirable control procedure, can be configured to general automatic control process, the analysis of this Model Products be take sampling analysis as means, and opportunity and the process of switching product artificially realize; Can also be configured to full automatic process, this pattern adopts on-line analysis, according to on-line analysis data, automatically or artificially switches product, realizes the transparent control of overall process.
Claims (1)
1. the preparation method of an environment-friendly type type low-temperature extraction agent, it is characterized in that, take by the 6# solvent naphtha after hydrofinishing and isomerization is raw material, by the higher 2-methylpentane of content, 3-methylpentane, n-hexane is separated, 2-methylpentane, 3-methylpentane, the product purity of n-hexane requires more than 95%, n-hexane purity requirement in food industry hexane is more than 60%, wherein C5 and restructuring are divided into non-object product, need products pot >=5 of configuration, the few products pot of not establishing separately of C5 amount, called in other products or in heavy constituent, head tank is used as purification tank simultaneously,
Step is as follows:
The first step: go C5 process: the charging of the tank of certainly purifying enters tower V1, tower V1 bottom temp is controlled at 55-58 ℃, reflux and control reflux ratio at 5-8 in tower V1 top, the C5 deviating from enters corresponding storage tank as required, it is not principle containing the above component of C6 that process control be take in flow process up-sampling C5, tower V1 bottom discharge enters tower V2, tower V2 top reflux ratio is controlled at 2-3, tower V2 bottom temp is controlled at 80 ℃, first remove the component heavier than methyl cyclopentane, tower V2 top discharge is controlled load according to material balance, turn back to purification tank, when tower V2 bottom can go out without heavy constituent, the process that removes the component heavier than methyl cyclopentane finishes, when the basic product-free in tower V1 top can go out, go C5 process to finish,
Second step: produce 2-methylpentane process: tower V1 bottom temp is controlled to 59-61 ℃, tower top discharging is according to carrying out balance lower than 2-methylpentane total content, guarantee more than 10 reflux ratios, overhead product enters 2-methylpentane tank, go out before this certain amount of 2-methylpentane of seldom measuring C5 that contains and enter head tank or other tank, until C5 content meets the demands, it is not principle containing the above component of 2-methylpentane that process control be take in flow process up-sampling 2-methylpentane, tower V1 bottom discharge enters tower V2, tower V2 top reflux ratio is controlled at 2-3, tower V2 bottom is controlled at 75 ℃, part removes methyl cyclopentane, tower V2 top discharge is controlled load according to material balance, turn back to purification tank, when tower V2 bottom can go out without heavy constituent, the process that this stage partly removes methyl cyclopentane component finishes, when the basic product-free in tower V1 top can go out, producing 2-methylpentane process finishes,
The 3rd step: produce 3-methylpentane process: tower V1 bottom temp is controlled to 62-63 ℃, tower top discharging is according to carrying out balance lower than 3-methylpentane total content, guarantee more than 10 reflux ratios, top of tower product introduction 3-methylpentane tank, go out before this certain amount of 3-methylpentane that contains a small amount of 2-methylpentane and enter food industry hexane tank or light isohexane tank, until 2-methylpentane content meets the demands, it is not principle containing the above component of 3-methylpentane that process control be take in flow process up-sampling 3-methylpentane, tower V1 bottom discharge enters tower V2, tower V2 top reflux ratio is controlled at 2-3, tower V2 bottom is controlled at 72 ℃, substantially remove methyl cyclopentane, tower V2 top discharge is controlled load according to material balance, turn back to purification tank, when tower V2 bottom can go out without heavy constituent, the process that this stage removes methyl cyclopentane component substantially finishes, when the basic product-free in tower V1 top can go out, producing 3-methylpentane process finishes,
The 4th step: production food industry hexane process: producing after 3-methylpentane process finishes, by the material of purification tank directly to food industry hexane tank;
The 5th step: produce n-hexane process: using tower V1 as feed preheater, bottom temp is controlled at 64-65 ℃, reflux and maintain less backflow in top, the safe operation of pump of take is principle, tower top discharging is only limited to transition stage, this stage goes out Ta Nei and intrasystem 3-methylpentane to the greatest extent completely, till qualified to return tank analysis 3-methylpentane content, this part overhead product enters food industry hexane tank, tower V1 bottom discharge enters tower V2, tower V2 top reflux ratio is not less than 5, counter rolling back carried out material balance, tower V2 bottom is controlled at 69-70 ℃, discharging feed product industrial hexane tank at the bottom of tower.
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4315802A (en) * | 1980-05-12 | 1982-02-16 | The Lummus Company | Process and apparatus for fractionating close boiling components of a multi-component system |
| CN1106710A (en) * | 1994-11-18 | 1995-08-16 | 天津大学 | Single-tower atmospheric intermittent extractive rectification method |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4315802A (en) * | 1980-05-12 | 1982-02-16 | The Lummus Company | Process and apparatus for fractionating close boiling components of a multi-component system |
| CN1106710A (en) * | 1994-11-18 | 1995-08-16 | 天津大学 | Single-tower atmospheric intermittent extractive rectification method |
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