RU2432984C1 - Method of extracting and concentrating organic substances from aqueous media - Google Patents

Abstract

FIELD: process engineering. ^ SUBSTANCE: invention relates to chemistry, particularly, to separation of fluid mixes and may be used in various industrial branches and agriculture. This method exploits thermal gradient pervaporation separation of fluid mixes in target component-selective membrane by accumulating permeate vapors by condensation on solid surface with its temperature is lower than that of separated mix wherein membrane material represents poly(1-trimethylsilyl-1- methyl acetylene) of general formula , where n is the number of links in chain, of molecular mass MM=100800-1900000, while extraction and concentration of organic substances is performed at atmospheric pressure. ^ EFFECT: simplified and relatively cheap procedure. ^ 3 dwg, 8 tbl, 31 ex

Description

The invention relates to the field of chemistry, namely the separation of liquid mixtures, and can be used in various industries and agriculture. At the same time, the use of membrane technology allows not only solving technological problems, but also preventing environmental problems associated with environmental pollution.

One of the membrane processes of separation of liquid mixtures, still limitedly used on an industrial scale, is pervaporation. The pervaporation process allows you to effectively separate various aqueous-organic mixtures (drying of organic solvents and wastewater treatment) and mixtures of organic substances. The prospectivity of pervaporation is related both to the relevance of the tasks being solved and to the high efficiency of the pervaporation process compared to other separation processes, with the possibility of separation of azeotropic mixtures, low energy consumption, non-reactivity and compactness of equipment.

Pervaporation is the process of membrane separation of liquids, in which the separated mixture (feed stream) is brought into contact with one side of a selectively permeable non-porous membrane, and the components (permeate) penetrated through the membrane are removed as vapor from its back side.

Most often, in practice, the driving force of the process is the activity gradient, which is achieved by artificially lowering the vapor pressure of the separated liquid mixture from the back of the membrane using one of the methods:

- either by evacuation;

- either by blowing off the vapor of the penetrating mixture with an inert gas;

- either by condensation on the surface of the cooled heat exchanger.

Only the measured method has found application (for economic reasons) in large pervaporation units (at least for the processes of dehydration of organic solvents), when the permeate is continuously condensed in an evacuated cooled heat exchanger and removed from the system (VV Volkov. Separation of liquids by evaporation through polymer membranes. Izv. Akademii Nauk. Chemical series, 1994, No. 2, p.208).

However, the main disadvantage of vacuum pervaporation is the use of special equipment, devices, pumps to create a vacuum, which makes the process difficult. In addition, evacuation is an energy-intensive process. Both of these circumstances make the vacuum pervaporation process expensive and complicated in terms of hardware design.

Two other methods are more commonly used in laboratory research.

For example, there is a known method for concentrating solutions of water-soluble organic substances and a device for its implementation (US Pat. JP 2005177535 (A), IPC B01D 63/00, publ. 2005.07.07), based on the use of thermal energy using a separation membrane with a limited area . This method consists of two successive stages of vapor concentration in the vapor separation module and subsequent pervaporation separation in the pervaporation module. First, steam is separated in the steam separation module, which is obtained by distillation of the initial mixture, then the mixture enriched in the target component is enriched in the pervaporation module, obtaining as a final product a highly concentrated solution of organic matter in water.

However, the described technical solution, although it ultimately reaches a high concentration of the target component in the solution, is not optimal in solving the problem, since in the process of concentration of the substance there is a stage of distillation of the initial mixture, which is an extremely energy-intensive process and, therefore, reduces the profitability of concentration .

A known method of separating liquid mixtures, steam or vapor-gas mixtures described in patent EP 218019, B01D 61/36, 04/15/1987, by thermal vaporization using a composite membrane, in which the upper selective non-porous layer is a hydrophilic polymer (cellulose acetate, polysulfone or polyvinyl alcohol ), which in turn is deposited on a hydrophobic polymer porous substrate. The method is used to isolate and concentrate water from aqueous-organic mixtures, and it is the closest analogue.

Its main disadvantage is the fact that the condensation of permeate is carried out in the flow of coolant, a mandatory requirement for which is the absence of its flowing into the pores of a hydrophobic porous substrate. However, the partial transfer of the organic component with water leads to an increase in the affinity of the condensed permeate to the material of the porous substrate and, as a result, to leak and fill the pore space of the substrate with a mixture of coolant and permeate, which leads to a decrease in the mass transfer characteristics of the membrane and the inability to use this method for the isolation and concentration of organic substances.

There is a method for isolating a dissolved component using a vapor-permeable membrane and subsequent condensation of steam on a cooled wall, described in US patent 3563860, B01D 1/22, 1971. In this case, the membrane passes only one component of the mixture to be separated (the second is usually salts or surfactants that are not go into the gas phase). The method is implemented using an installation consisting of a chamber closed on both sides by a membrane. A hot liquid stream circulates through it, from which the desired component, for example water vapor, must be isolated. The installation also contains a chamber, closed on both sides by a waterproof heat-conducting wall. Coolant circulates through this chamber, which can be used as the fluid to be processed. Between these chambers there is a distillate collection chamber, one wall of which is a specified membrane that passes steam, and the other is a specified waterproof heat-conducting wall on which steam condenses. Hot and cold liquid flows from distribution pipelines connected respectively to a heat exchanger and a cold water pump are supplied in parallel flows to each respective chamber and circulate countercurrently in them.

The scope of the described technical solution is limited, since it is almost impossible to choose a membrane that passes only one component of the solution. This method is mainly used for desalination of water, since salts dissolved in water do not pass into steam. However, for the isolation and concentration of organic compounds from aqueous media, it is not applicable.

It is known that using an asymmetric polyvinyltrimethylsilane (PVTMS) membrane, thermo-vaporization separation of inorganic substances, including volatile acids, can be carried out if the PVTMS membrane is modified in a plasma of a low-frequency glow discharge in an atmosphere of air (A. B. Gilman, I. B. Elkina, V. .V. Ugrov, VVVolkov. Plasma-chemical modification of the polyvinyltrimethylsilane membrane for thermal vaporization. High Energy Chemistry, 1998, Volume 32, No. 4, p.305-309).

But the described method is not suitable for the isolation and concentration of organic substances from aqueous media, since the surface of a plasma-modified PVTMS membrane acquires hydrophilic properties and is applicable only for the isolation of water.

в камеру конденсации и нагревается до температуры

за счет энтальпии конденсации пермеата. Затем питающий поток нагревается до температуры

с использованием внешнего источника тепла и подается в мембранную камеру. За счет разницы давления паров с обеих сторон мембраны (со стороны исходного потока и пермеата) часть питающего потока проникает через мембрану в виде пара и конденсируется на непроницаемой пластине камеры конденсации. Этот принцип был экспериментально исследован для выделения этанола из смесей этанол-вода, и показано, что можно получить возврат тепла до 33% и реализовать потоки пермеата через мембрану до 0,5 кг/м² ч при факторе разделения этанол/вода около 3.The closest in technical essence and the achieved result is the method described in the work of ESFernandez, P.Geerdink, ELVGoether, Desalination, 2010, V.250, p.1053-1055, according to which the use of thermal transfer for the purpose of efficient heat recovery in the process of pervaporation separation is described by using the condensation heat of permeate to directly heat the flow of the mixture to be separated (feed stream). The membrane module consists of a membrane chamber with a separation membrane and a condensation chamber with an impermeable plate on which the permeate is condensed. The membrane chamber and the condensation chamber are located close to each other (distance - 2 mm) so that the membrane is opposite the impermeable plate. Between the chambers there is an air gap that allows you to remove the condensed permeate from the impermeable plate. The stream of the initial shared mixture (feed stream) is supplied at a temperature

into the condensation chamber and heats up to a temperature

due to the enthalpy of condensation of permeate. Then the feed stream is heated to a temperature

using an external heat source and is fed into the membrane chamber. Due to the difference in vapor pressure on both sides of the membrane (from the side of the feed stream and permeate), part of the feed stream penetrates through the membrane in the form of steam and condenses on the impermeable plate of the condensation chamber. This principle was experimentally studied for the separation of ethanol from ethanol-water mixtures, and it was shown that heat recovery of up to 33% can be achieved and permeate flows through the membrane can be realized up to 0.5 kg / m ² h with an ethanol / water separation factor of about 3.

From the point of view of the tasks of separation and concentration of organic substances from aqueous media, the main disadvantage of the described method is the insufficiently high values of permeate flow up to 0.5 kg / m ² h and a separation factor of about 3.

In addition, a permeate flux of 0.5 kg / m ² h was obtained at a concentration of more than 50% ethanol in an ethanol-water mixture, while pervaporation is known to be used only when a component with a low content in the separation is selectively penetrated through the membrane. mixtures (N. Winn, Chem. Eng. Prog. 2001, V.97, p. 66-72). This is due to the fact that the latent heat of evaporation must be spent on the permeate permeability through the membrane to transfer the permeate from a liquid to a vapor state. However, when the ethanol concentration in the ethanol-water mixture is reduced to 10%, as the authors of the work indicate, the permeate flow decreases to values below 0.2 kg / m ² h.

The objective of the invention is to develop a method for the isolation and concentration of liquid organic substances from aqueous media by a simple and effective method of thermal evaporation, providing the same selectivity for the separation and mass transfer of the selected target component, as in vacuum pervaporation.

The problem is solved in that a method for the separation and concentration of organic substances from aqueous media using a thermogradient pervaporation separation of liquid mixtures through a membrane selective for the target component, by collecting permeate vapor by condensation on a solid surface, the temperature of which is lower than the temperature of the separated mixture, in which the material of the membrane is poly (1-trimethylsilyl-1-propine) of the general formula

,

,

where n is the number of links in the chain, molecular weight MM = 100800-1900000, and the selection and concentration of organic substances is carried out at atmospheric pressure.

The technical result that can be obtained from the use of the proposed technical solution is to increase the flow of permeate and the separation factor during the isolation and concentration of organic compounds from aqueous media.

The thermo-vaporization unit consists of the thermo-vaporization module (1) and two circuits of different temperatures. The installation diagram is shown in figure 1. The first circuit consists of a thermostatically controlled tank with refrigerant (2), which circulates in the circuit using a pump (3). The second circuit consists of a thermostatic tank with a shared liquid (4) and a peristaltic pump (5), with which the fluid is circulated in the circuit. In the assembled state, the two parts of the cell are separated by a membrane (6) and a solid surface (7), between which an air gap of 0.5-4.0 mm (8) is maintained. During the experiment, permeate vapors evaporate from the membrane surface and condense on a solid surface. Condensate drains from a solid surface under the action of gravity and accumulates in a container for collecting permeate (the module is oriented in such a way that the membrane and the solid surface of condensation are located vertically).

The permeate mass was determined from the mass difference of the container for collecting permeate before and after the experiment. The time of the experiment is 4-6 hours.

In the case of thermal vaporization of binary aqueous-organic mixtures, the concentration of the initial mixture and permeate were determined by refractometry and gas chromatography.

The composition of multicomponent mixtures was analyzed by gas chromatography using a Crystallux 4000 M chromatograph using a flame ionization detector.

The total permeate flow is determined by the weight method according to the formula:

where m is the mass of permeate (kg), penetrated through a membrane with an area of S (m ² ) for a time t (h).

The separation factor α is determined by the formula:

where x _o and x _in are mass fractions of the organic component and water, respectively, in the mixture to be separated, and y _o and y _in are mass fractions of the organic component and water, respectively, in permeate.

The following examples illustrate the proposed technical solution, but in no way limit the scope of its application.

Examples 1-4

Thermo-evaporation is carried out and 1-butanol is concentrated from 1-butanol / water with a concentration of 1-butanol in a separable solution equal to 2.0 wt%, changing the thickness of the air gap from 1.0 to 4.0 mm.

The temperature of the divided initial mixture is maintained equal to 60 ° C, and the temperature of the condensing surface is equal to 15 ° C. The process is conducted through a PTMSP membrane (MM = 210000), the thickness of which is 19 μm.

The results of the isolation and concentration of 1-butanol are presented in table 1.

Table 1 Example No. Air gap thickness, mm Permeate flow, kg / m ² h The concentration of 1-butanol in permeate,% wt. Separation factor one 0.5 0.10 24 15,5 2 1,0 0.16 33 24.1 3 2.0 0.17 35 26,4 four 4.0 0.09 16 9.3

Examples 5-10

Thermal pervaporation is carried out and 1-butanol is concentrated from 1-butanol / water with a concentration of 1-butanol in a separable solution equal to 2.0 wt% through a PTMSP membrane (MM = 450,000), whose thickness is 19 μm.

The temperature of the shared initial mixture is changed from 41 to 74 ° C, while the temperature of the condensing surface is maintained equal to 15 ° C. The thickness of the air gap is 2 mm.

The results of the isolation and concentration of 1-butanol are presented in table 2.

table 2 Example No. The temperature of the shared solution, ° C Permeate flow, kg / m ² h The concentration of 1-butanol in permeate,% wt. Separation factor 5 41 0,050 10 5,4 6 44 0.051 fourteen 8.0 7 48 0,062 twenty 12,2 8 55 0,091 25 16.3 9 65 0.184 32 23.0 10 74 0.266 37 28.8

Examples 11-15

Thermal pervaporation is carried out and 1-butanol is concentrated from 1-butanol / water with a concentration of 1-butanol in a separable solution equal to 2.0 wt%, at a temperature of the separable initial mixture equal to 65 ° С, while the temperature of the condensing surface is kept equal 15 ° C. Isolation and concentration of 1-butanol is carried out through a PTMSP membrane (MM = 1200000), the thickness of which is changed from 4 to 60 μm. The thickness of the air gap is 2 mm.

The results of the separation, isolation and concentration of 1-butanol are presented in table 3.

Table 3 Example No. Membrane thickness, microns Permeate flow, ct / m ² h The concentration of 1-butanol in permeate,% wt. Separation factor eleven four 0.9 19 11.5 12 16 0.5 29th 20,0 13 26 0.35 40 32,7 fourteen 40 0.25 49 47.0 fifteen 60 0.17 57 64.9

Examples 16-19

Thermal pervaporation is carried out and 1-butanol is concentrated from 1-butanol / water with a concentration of 1-butanol in a separable solution equal to 2.0 wt% through a PTMSP membrane (MM = 630000), the thickness of which is 40 μm.

The temperature of the separated initial mixture is maintained equal to 40 ° C, but the temperature of the condensing surface is changed from 0.5 to 20.0 ° C. The thickness of the air gap is 2 mm.

The results of the isolation and concentration of 1-butanol are presented in table 4.

Table 4 Example No. Condensation temperature ° С Permeate flow kg / m ² h The concentration of 1-butanol in permeate,% wt. Separation factor 16 5 0.058 45 40.1 17 9 0,048 48 45,2 eighteen fifteen 0,037 38 30,0 19 twenty 0.016 5 2.6

Examples 20-24

Thermal pervaporation is carried out and 1-butanol is concentrated from 1-butanol / water, changing the concentration of 1-butanol in the solution to be separated from 2.0 to 7.0% by weight.

The temperature of the divided initial mixture is maintained equal to 65 ° C, and the temperature of the condensing surface is equal to 15 ° C. The process is conducted through a PTMSP membrane, the thickness of which is 19 μm. The thickness of the air gap is 2 mm.

The results of the isolation and concentration of 1-butanol are presented in table 5.

Table 5 Example No. The concentration of 1-butanol in a separable solution,% wt. Permeate flow kg / m ² h The concentration of permeate 1-butanol in% of the mass. Separation factor twenty 2.0 0.180 35 25.8 21 3,5 0.314 52 30.8 22 4,5 0.520 58 28.8 23 5.5 0.577 61 26.3 24 7.0 0.770 66 25.8

Examples 25-26

Thermal pervaporation is carried out and ethanol is concentrated by separation of ethanol / water mixtures with different concentrations at a temperature of the initial solution of 60 ° C, a temperature of the condensing surface of 15 ° C and a membrane thickness of 4 μm. The results of the separation and concentration of ethanol are presented in table 6.

Table 6 Example No. The concentration of ethanol in the initial mixture,% wt. Permeate flow, kg / m ² h The concentration of ethanol in permeate, wt.% Separation factor 25 5,0 0.735 fifteen 3 26 10.0 1,542 33 four

From the analysis of the data of table 6 it is seen that when carrying out the separation and concentration of ethanol by the proposed method, when the ethanol concentration in the separated mixture is 10% by mass, the permeate flow is about 1.5 kg / m ² h. And at the same initial ethanol concentration in the separated mixture during thermal re-ventilation under the conditions of the prototype, the permeate flow is slightly lower than 0.2 kg / m ² h, which is almost 7 times lower than during the pervaporation of the proposed method.

Example 27

Thermal pervaporation isolation and concentration of an aqueous solution of organic substances is carried out, simulating a multicomponent fermentation mixture of acetone-1-butanol-ethanol fermentation (ABE fermentation) at a temperature of the initial solution of 60 ° C, a temperature of the condensing surface of 15 ° C and a membrane thickness of 4 μm.

The results of the selection and concentration of the permeate components are presented in table 7.

Table 7 Enzymatic mixture Composition,% wt. Ethanol 1-butanol Acetone Shared mixture 0.15 1.00 0.45 Permeate 0.62 17.55 1,53

From the data of table 7 it can be seen that the proposed method allows to isolate and concentrate organic substances from multicomponent aqueous solutions.

Examples 28-31 (comparative).

Isolation and concentration of 1-butanol from a mixture of 1-butanol / water with a concentration of 1-butanol in a separable solution equal to 2.0 wt% was carried out through a PTMSP membrane with a thickness of 44 μm under vacuum pervaporation.

The temperature of the divided initial mixture is maintained equal to 25 ° C, but the temperature of the condensing surface is changed from 0 to -196 ° C.

The results of the isolation and concentration of 1-butanol are presented in table 8.

Table 8 Example No. Condensing surface temperature, ° С Permeate flow kg / m ² h The concentration of 1-butanol in permeate,% wt. Separation factor 28 0 0,029 fifteen 8.6 29th -19 0,046 twenty 12,2 thirty -79 0.058 35 26,4 31 -196 0,067 58 67.7

For clarity, a comparison of the flow of permeate and the separation factor for the process of separation and concentration of organic substances from aqueous media, carried out under conditions of thermal vaporization and vacuum pervaporation, are shown in figure 2. Comparison of vacuum pervaporation and thermal vaporization: permeate flow (data from tables 4 and 8) and FIG. 3. Comparison of vacuum pervaporation and thermal pervaporation: separation factor (data from tables 4 and 8, from which it can be seen that at comparable temperature differences, the greater the value of the flow passing through the membrane and the separation factor is realized under the conditions of the thermal vaporization process).

Thus, the proposed technical solution allows the process of selective pervaporation separation and concentration of organic substances from aqueous media in the absence of vacuum, mainly at atmospheric pressure, with comparable values of permeate flux and separation factor for the target organic substance, which is also simpler in the case of vacuum pervaporation and less expensive way.

In addition, the proposed method can be effectively applied for pervaporation isolation and concentration of organic substances in the processes of their production by biomass fermentation, for example, the enzymatic production of ethanol or the enzymatic production of 1-butanol, the so-called acetone-1-butanol-ethanol fermentation (ABE fermentation). When producing alcohols in this way, a large amount of non-condensing CO ₂ gas is formed, which makes the use of vacuum pervaporation for this application uneconomical. This is due to the fact that in order to remove penetrating together with organic components through the CO ₂ membrane, constant evacuation (operation of a vacuum pump) is necessary to remove CO ₂ from the vacuum part of the system.

Claims (1)

The method of separation and concentration of organic substances from aqueous media using thermogradient pervaporation separation of liquid mixtures through a membrane that is selective for the target component, by collecting permeate vapor by condensation on a solid surface, the temperature of which is lower than the temperature of the separated mixture, characterized in that poly (1-trimethylsilyl-1-propine) of the general formula

where n is the number of links in the chain, molecular weight MM = 100800-1900000, and the selection and concentration of organic substances is carried out at atmospheric pressure.

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