EP2627442A2

EP2627442A2 - Method and device for chemical conversion by means of an equilibrium reaction between reactants, and method for determining at least one parameter of such a chemical conversion

Info

Publication number: EP2627442A2
Application number: EP11832106.6A
Authority: EP
Inventors: Pierre Guillot; Inès VASCONCELOS
Original assignee: Rhodia Operations SAS
Current assignee: Rhodia Operations SAS
Priority date: 2010-10-15
Filing date: 2011-10-13
Publication date: 2013-08-21
Also published as: FR2966057A1; WO2012049427A3; FR2966057B1; CN103237598A; WO2012049427A2

Abstract

The invention relates to a chemical conversion method which can be used to controllably force the evolution of an equilibrium chemical reaction between reactants, particularly in a milli-fluidic system. According to the method, a single-phase liquid reaction flow stream containing the reactants is obtained and then segmented to form a two-phase gas-liquid flow stream, such as to extract a co-product of the reaction in the gas phase of the two-phase flow stream from the liquid phase from said two-phase flow stream. Subsequently, at least one fraction of the gas phase is separated from the two-phase flow stream by means of gas permeation of the co-product.

Description

CHEMICAL PROCESSING METHOD AND DEVICE

BALANCED REACTION BETWEEN REAGENTS AND METHOD OF DETERMINING AT LEAST ONE PARAMETER

SUCH A CHEMICAL TRANSFORMATION

The present invention relates to a method and a device for chemical transformation by equilibrium reaction between reagents. It also relates to a method for determining at least one parameter of a chemical reaction by equilibrium reaction between reagents.

The invention relates to the field of millifluidics, that is to say to the manipulation of fluids on a millimetric or even lower scale, which in this case is sometimes referred to as microfluidics. Millifluidics and microfluidics are now recognized as providing excellent tools for the acquisition of basic physicochemical data because they allow, among other things, improved heat transfer compared to conventional chemical tanks, low consumption of reagents , great flexibility of implementation, as well as a match between distance and residence time for a flowing system.

In this context, the invention is more specifically concerned with the observation of a chemical reaction between liquid reagents, which reaches its chemical equilibrium quite rapidly within the observed system. In this case, it is understood that the progress of the reaction can not be increased since the product (s) and coproduct (s) of the reaction are obtained in respective balanced amounts, which significantly limits the possibilities of observation, in particular for determining parameters relating to the chemical kinetics of the transformation.

The object of the present invention is to provide a method and a device which make it possible, in particular within a millifluidic flow system, to "force" in a controlled manner the progress of the observed chemical reaction.

For this purpose, the subject of the invention is a process for chemical transformation by equilibrium reaction between reagents, in which:

a liquid monophasic reaction flow containing the reagents is available,

the liquid monophasic flow is then separated to form a two-phase gas-liquid flow, so as to extract from the liquid phase of this two-phase flow a co-product of the reaction in the gaseous phase of this two-phase flow,

and then at least a fraction of its gaseous phase is separated from the two-phase flow by gas permeation of the co-product. One of the basic ideas of the invention is to provide, in a flow-through reaction system, a controlled elimination of the co-product or products of the chemical reaction. Thus, according to the invention, after having formed a liquid monophasic reaction flow, two separation operations are successively carried out: the first is a gas-liquid extraction of the coproduct thanks to a segmented gas-liquid flow, obtained from the flow monophasic liquid, while the second is a gas-liquid separation of the gas injected and produced during the extraction, thanks to a gas permeation of at least the co-product. More precisely, the first gas-liquid extraction operation is linked to the relative volatility of the co-product in the gaseous and liquid phases of the two-phase flow: the presence of the gas phase in the flow causes the partial evaporation of the co-product present. in the liquid phase, so that the chemical system is then out of chemical equilibrium and the reaction evolves in the direct direction, to compensate for the loss of the co-product, until reaching both the gas-liquid equilibrium and the equilibrium chemical. The gas phase is therefore saturated in coproduct and, to further "intensify" the chemical transformation process, the second separation operation makes it possible to separate, at least partially or completely, the two phases of the flow: to do this at least one gaseous fraction, containing the co-product, of the two-phase flow is removed from the latter by gas permeation, which further advances the chemical reaction in a controlled manner. In practice, the two aforementioned operations, gas-liquid extraction and gas-liquid separation, are advantageously repeated in a loop in order to eliminate more and more the co-product and to achieve a progress of the higher reaction and therefore masses of the reaction product or more and more important.

In practice, the process according to the invention can advantageously be carried out at relatively high operating temperatures and pressures, typically greater than 100% and 30 bars, respectively. It is thus understood that it is advantageous to apply the process according to the invention to polymerization reactions, in particular to polycondensation reactions. It is also in this context that the inventors have highlighted a number of additional advantageous features, which will be described in more detail below.

According to advantageous additional aspects of the process according to the invention, taken separately or in any technically possible combination:

after having formed the two-phase flow, the entire gaseous phase is separated off by gas permeation and then subjected to one or more additional segmentation and separation cycles; to separate from the two-phase flow at least a fraction of its gaseous phase, a gas permeation membrane having a higher co-product permeability, preferably at least twice as high, as its permeability to the other constituents of this phase is used; gaseous;

an organic permeation membrane is used, in particular based on polymeric materials;

an inorganic permeation membrane is used, in particular based on ceramic and / or zeolite;

in order to segment the liquid monophasic flow, a gas which is inert with respect to the reaction between the reactants is injected co-currently;

the injected gas flow rate is chosen between 5 and 95% of the total volumetric flow rate of the two-phase flow;

the flow rate of the monophasic flow is between 0.01 and 1000 mL / h, preferably between 1 and 50 mIJh;

the chemical transformation reaction is a polymerization reaction, in particular polycondensation.

The invention also relates to a method for determining at least one parameter of a chemical reaction by equilibrium reaction between reagents, in which:

a chemical transformation is carried out according to the process as defined above, and

measurements are made on the two-phase flow from which at least a fraction of its gaseous phase has been separated in order to deduce the said at least one parameter.

The invention further relates to a chemical transformation device by equilibrium reaction between reagents, comprising:

a gas-liquid segmentation module adapted to segment a liquid monophasic flow containing the reactants into a two-phase gas-liquid flow so as to extract from the liquid phase of the two-phase flow a co-product of the reaction in the gaseous phase of the two-phase flow, and

a gas-liquid separation module, the inlet of which is connected to the outlet of the gas-liquid segmentation module and which is adapted to separate from the two-phase flow at least a fraction of its gaseous phase, by gas permeation of the co-product .

According to a preferred embodiment, the gas-liquid separation module comprises a gas permeation membrane which is arranged, in a supported manner, between a two-phase flow circulation duct and an evacuation duct. gases that originate from the gaseous phase of the two-phase flow and have passed through the permeation membrane.

The invention will be better understood on reading the description which follows, given solely by way of example and with reference to the drawings in which:

FIG. 1 is a diagram of an installation for implementing a chemical transformation process according to the invention;

FIG. 2 is a diagrammatic section along line II-II of FIG. 1; and

- Figure 3 is a view similar to Figure 2, illustrating an alternative embodiment according to the invention.

The installation of FIG. 1 comprises, first of all, an upstream duct 10 fed by a liquid monophasic reaction mixture. The flow rate in the duct 10 is advantageously between 0.01 and 1000 mL / h, preferably between 1 and 50 mIJh. Thus, with this flow rate range, the installation of FIG. 1 can be described as a millifluidic or even microfluidic installation, and the duct 10 is typically made in the form of a capillary, for example made of stainless steel, whose diameter is of the order of a millimeter.

The liquid reaction flow produced in the conduit 10 is obtained by mixing, upstream of the conduit 10, two or more liquid reagents, and this by any suitable means which will not be described here further.

Within the flow made in the conduit 10, a balanced chemical reaction occurs between at least two reagents R1 and R2, obtaining at least one product P and a C co-product. subjected to several manipulations by the inventors, the reagents R1 and R2 are adipic acid and ethylene glycol, these components reacting in a polyesterification reaction to form as product P of ethylene polyadipate, accompanied by water C. In other words, the above example is a polycondensation reaction giving ethylene polyadipate, with formation of water, in respective predetermined proportions related to the balanced nature of the polycondensation chemical reaction taking place in upstream and in the duct 10.

In practice, the liquid monophasic reaction flow, carried out along the conduit 10, is advantageously implemented under satisfactory temperature and pressure conditions for carrying out the expected chemical reaction. To do this, the conduit 10, as well as the means for mixing the reagents R1 and R2 are designed accordingly, it being specified that the corresponding arrangements will not be described here further insofar as they are part of the instrument knowledge of the skilled person. In the context of the example of polycondensation As mentioned above, the reaction flow in line 10 is carried out at about 200 ° C. and at a pressure of 50 bar.

Due to the balanced nature of the chemical reaction occurring in line 10, the progress of this reaction is necessarily limited since, after a certain residence time in line 10, the reaction reaches its chemical equilibrium with obtaining predetermined quantities of the product P and the co-product C.

According to the invention, the downstream outlet of the duct 10 feeds a gas-liquid segmentation module 20. As shown diagrammatically in FIG. 1, this module 20 comprises a T-shaped element 21 whose main branch is connected to the duct 10, while its transverse branch is provided with a gas injection capillary 22 fed by a source 23. Thus, downstream of the transverse branch of the T-shaped element 21, the module 20 comprises a conduit 24 in which The liquid reaction mixture flowing from the conduit 10 and a gaseous stream escaping from the capillary 22, the latter and the conduit 24 extending coaxially with each other, flow co-currently. As for the conduit 10, the conduit 24 is for example made in the form of a stainless steel capillary, whose diameter is of the order of a millimeter. In the duct 24, the gas injected by the capillary 22 generates gas bubbles, separated in pairs by volumes of liquid. In other words, the module 20 is able to segment the single-phase liquid flow from the conduit 10 into a two-phase gas-liquid flow. The instrumentation arrangements of the module 20 will not be described further here since they are well known to those skilled in the art. The reader will be able to refer in particular to the previous documents "The Role of Gas Bubbles and Liquid Slug Lengths on Mass Transfer in the Taylor Flow Through Capillaries" by G. Bercic and A. Pinrat (Chem Eng Eng Sci 1997, 52, 3709). and "Bubble-Train Flow in Capillaries of Circular and Square Cross-Section" by TC Thulasidas, MA Abraham and RL Cerro (Chem Eng Sci 1995, 50, 183).

In practice, an important operating parameter for obtaining a two-phase flow in the duct 24, segmented in a very regular manner, is related to the gas flow rate injected by the capillary 22. Advantageously, the volume fraction of the gas injected, that is to say say the ratio between the gas flow rate injected on the total volume flow in the conduit 24 is chosen between 5 and 95%. If the volume fraction of gas is chosen larger, the regularity of the segmentation of the two-phase gas-liquid flow can be compromised, in the sense that the flow could be the site of "creeping" phenomena along the walls of the duct. 24, which would pose problems of control of residence times within the facility. Conversely, a relatively The volume fraction of the gas is still important, for the reasons given below.

The gas injected into the duct 24 is intended to drive the extraction, in the gaseous phase of the flow of the duct 24, of the coproduct C present in the liquid phase of this flow. The driving force of this extraction is the relative volatility of the co-product C in the aforementioned gaseous and liquid phases. In practice, it is therefore understood that the gas used is a gas which is inert with respect to the reactants R1 and R2, the product P and the co-product C. It is typically a neutral gas. In the case of the example of the polycondensation reaction mentioned above, this gas is for example argon: the presence of argon bubbles causes the partial evaporation of the water present in the liquid phase of the flow of the duct 24, as indicated by the arrows 25 in FIG. The chemical system of the liquid phase of the flow of the conduit 24 is then found out of chemical equilibrium and the reaction between the reactants R1 and R2 evolves in the forward direction, to compensate for the loss of water in the liquid phase, up to to reach both the gas-liquid equilibrium and the chemical equilibrium in the liquid phase. The gas phase is then saturated with water.

Of course, it is understood that the operating conditions of temperature and pressure, present in the duct 10, must be maintained within the segmentation module 20, in order to increase the progress of the reaction between the reagents R1 and R2, without being disturbed by the conditions of temperature and pressure.

Also according to the invention, the outlet of the duct 24 is connected to a gas-liquid separation module 30, visible in FIGS. 1 and 2. In the schematic exemplary embodiment considered in these figures, the module 30 comprises two bodies 31 and 32 which, in use, are mechanically assembled one on the other. In its face facing the body 32, the body 31 is hollowed out of a duct 33 whose upstream end is connected to the outlet of the duct 24. In its face turned towards the body 31, the body 32 is, meanwhile , hollowed out of a duct 34 disposed facing the duct 33. The ducts 33 and 34 are similar to millifluidic channels, similar to the ducts 10 and 24, and have a cross section whose maximum dimension is of the order of one millimeter . These ducts 33 and 34 are separated from each other by, at the same time, a gas permeation membrane 35 and a support 36 for this membrane. The membrane 35 and the support 36 are arranged one against the other, being interposed and mechanically retained between the bodies 31 and 32.

The membrane 35 is made of a material capable of promoting the permeation therethrough of the coproduct C, compared with the inert gas of the source 23. In practice, this is because the material constituting the membrane 35 has a permeability to the co-product C higher, preferably at least twice as high, as its gas permeability of the source 23. The support 36 is, for its part, made of a porous material, typically a porous metal, through which the gaseous constituents having permeated through the membrane 35 freely circulate, until joining the duct 34. It is thus understood that the support 36 has a main function, or even exclusive mechanical maintenance of the membrane 35, in particular for the portion of the latter arranged in between the conduits 33 and 34. In other words, in the absence of the support 36, the membrane 35 would risk irreversible damage under the effect of the pressure of the flow in the conduit 33, towards the duct 34.

Advantageously, the permeation membrane 35 is a so-called dense membrane, that is to say a membrane whose separation principle is based on a mechanism of sorption and diffusion within a selective layer of this membrane. Such a dense membrane has the advantage that it can be used at high operating pressures, typically greater than 30 bar, or even 50 bar, as is the case for the example of the polycondensation reaction mentioned above. In particular, the inventors have turned towards a dense permeation membrane 35 made of an organic material, in particular based on polymeric materials. Thus, in the context of the example of the polycondensation reaction mentioned above, the inventors have identified, as preferred material for producing the membrane 35, the material marketed under the reference TEFLON-AF-2400 by the company DUPONT (the word "TEFLON" is a registered trademark). This material has been retained because of its high permeability to low molecular weight gases, particularly water vapor.

Alternatively, the dense permeation membrane 35 may be made of an inorganic material, in particular based on ceramic, zeolite, etc.

Still in the context of the operating conditions of temperature and pressure mentioned above, it may be pointed out that, for example, the bodies 31 and 32 of the module 30 are made of stainless steel and are assembled to one another. by a plurality of screws distributed along the periphery of these bodies. The support 36 is, for its part, for example made in the form of a porous steel plate.

In service, as the two-phase flow from the duct

24 flows along the duct 33, the coproduct C contained in the gaseous phase of the flow enters the permeation membrane 35, to cross it, as well as the porous support 36, and thus join the duct 34, as indicated by the arrows 37 in FIGS. 1 and 2. It is understood that, thanks to the selectivity of the permeation membrane 35 for the co-product C, compared with the other gases present in the gaseous phase of the two-phase flow and coming from the source 23, the action of the membrane 35 makes it possible to separate from the two-phase flow at least a fraction of its gaseous phase, depleting the latter of the coproduct C present. In other words, by virtue of this selectivity of permeation with respect to the coproduct, it is avoided to supersaturate the gas phase of the two-phase flow by coproduct, which could lead to the condensation of this coproduct to the liquid phase of the flow. In the case of the example of the polycondensation reaction mentioned above, this amounts to saying that, within the separation module 30, the water of the gaseous phase of the two-phase flow permeated more rapidly than the argon, which causes a depletion of the gas bubbles in water vapor, thus causing evaporation of the water from the liquid phase of the flow, in order to restore the gas bubbles water vapor.

The permeation membrane 35 thus causes additional evaporation of the water, more generally of the coproduct C, which obviously favors the reaction in the forward direction and thus obtaining a greater advance of this reaction. Of course, the membrane 35 is chosen to let through only the gaseous phase of the two-phase flow, the entire liquid phase remaining in the conduit 33.

In practice, with a suitable dimensioning of the gas-liquid separation module 30, the entire gas phase present in the two-phase flow coming from the duct 24 is advantageously separated from this flow, which is to say that, at the outlet of the duct 33, the evacuated flow is monophasic liquid.

The gases having joined the duct 34 are evacuated via its downstream end, as indicated by the arrow 38 in FIG. Advantageously, to avoid stagnation of these gases in the duct 34, the upstream end of this duct may be fed with a slight gas overpressure, in order to induce a sweeping effect in the duct 34, towards its downstream end, as indicated by the arrow 39.

The duct 10, the gas-liquid segmentation module 20 and the gas-liquid separation module 30 thus form a millifluidic device, which may be described as a millireactor, capable of controlling the displacement of the advance of the reaction at the balance of the latter.

The outlet of the conduit 33 is, in turn, connected to a downstream conduit 40 of the installation, which, as shown in FIG. 1, passes through a measurement unit 50. This unit 50 makes it possible, thanks to ad hoc arrangements, to carry out measurements, such as viscosity or composition measurements, on the flow flowing in the duct 40. By way of example, particularly in the context of the example of the polycondensation reaction mentioned above, this unit of measure 50 is a high performance liquid chromatography unit, often referred to by the acronym HPLC. In practice, various independent or complementary measuring means can be integrated within the unit 50, in order to perform as many types of measurement as desired on the flow of the duct 40.

On the basis of the measurements carried out with the unit 50, one or more parameters of the chemical transformation related to the reaction between the reagents R1 and R2 are deduced, in particular the parameters relating to the chemical kinetics of this transformation, such as the progress of the reaction, as well as its speed and activation energy.

For the purposes of this document, the technical considerations relating to unit 50 and to the operation of the measurements carried out by this unit are not further described to the extent that they are within the abilities of those skilled in the art, while recalling that they can take very different forms, without limiting the present invention.

As an option, the installation of FIG. 1 also comprises a return line 60, represented only in dashed lines in FIG. This line 60 is designed to return all or part of the flow flowing in the downstream duct 40 into the upstream duct 10. In this way, the installation makes it possible to subject the liquid monophasic reaction mixture several successive cycles of segmentation and deformation. separation, respectively via the gas-liquid segmentation module 20 and the gas-liquid separation module 30.

Furthermore, various arrangements and variants of the installation of Figure 1 and its implementation method are conceivable.

Thus, for example, the gas-liquid separation module 30 can be made in the form of the variant 30 'shown in Figure 3: for sealing purposes, joints 30'.1 and 30'. 2 are respectively reported between a body 31 ', functionally similar to the body 31 of the module 30, and a permeation membrane 35', functionally similar to the membrane 35 of the module 30, and between a support 36 'for the membrane 35', functionally similar to the support 36 of the module 30, and a body 32 ', functionally similar to the body 32 of the module 30. By way of example, the joints 30'.1 and 30'.2 are made of epoxy. Advantageously, in this variant embodiment, the conduit 33 'for circulating the two-phase flow is delimited at least in part by the seal 30'.1. Similarly, the duct 34 'of gas evacuation having passed through the membrane 35' is partially delimited by the seal 30'.2.

Similarly, as a variant not shown for the gas-liquid separation modules 30 and 30 ', the conduit 33 or 33' for circulation of the two-phase gas-liquid flow is not limited to a single branch, but, at contrary, may consist of a plurality of tree or branched channels, which connects the upstream and downstream of the conduit 33 or 33 '. It is the same for the duct 34 or 34 'of evacuation of gases.

Claims

1. - Process for chemical transformation by equilibrium reaction between reagents, in which:

a liquid monophasic reaction flow containing reagents (R1 and R2) is available,

the liquid monophasic flow is then separated to form a two-phase gas-liquid flow, so as to extract from the liquid phase of this two-phase flow a co-product (C) of the reaction in the gaseous phase of this two-phase flow,

and then at least a fraction of its gaseous phase is separated from the two-phase flow by gas permeation of the co-product (C).

2. - A method according to claim 1, characterized in that, after forming the two-phase flow, the entire gas phase is separated by gas permeation, then it undergoes one or more additional cycles of segmentation and separation .

3. - Process according to one of claims 1 or 2, characterized in that, to separate from the two-phase flow at least a fraction of its gas phase, a gas permeation membrane (35; permeability to the co-product (C) higher, preferably at least twice as high, as its permeability to the other constituents of this gaseous phase.

4. - Process according to claim 3, characterized in that a permeation membrane (35; 35 ') organic, especially based on polymeric materials.

5. A process according to claim 3, characterized in that an inorganic permeation membrane is used, in particular based on ceramic and / or zeolite.

6. A process according to any one of the preceding claims, characterized in that, in order to segment the liquid monophasic flow, a gas which is inert to the reaction between the reagents (R1 and R2).

7. A process according to claim 6, characterized in that the injected gas flow rate is chosen between 5 and 95% of the total volume flow of the two-phase flow.

8. Process according to any one of the preceding claims, characterized in that the flow rate of the monophasic flow is between 0.01 and 1000 mJh, preferably between 1 and 50 mIJh.

9. - Process according to any one of the preceding claims, characterized in that the chemical transformation reaction is a polymerization reaction, in particular polycondensation.

10. - Method for determining at least one parameter of a chemical reaction by equilibrium reaction between reagents, in which:

a chemical transformation is carried out according to the method according to any one of the preceding claims, and

1 1 .- Chemical transformation device by balanced reaction between reagents, comprising:

a gas-liquid segmentation module (20) adapted to segment a liquid monophasic flow containing the reagents (R1 and R2) into a two-phase gas-liquid flow so as to extract a co-product from the liquid phase of the two-phase flow ( C) the reaction in the gas phase of the two-phase flow, and

a gas-liquid separation module (30; 30 ') whose input is connected to the output of the gas-liquid segmentation module (20) and which is adapted to separate from the two-phase flow at least a fraction of its gaseous phase, by gas permeation of the co-product (C).

12.- Device according to claim 1 1, characterized in that the gas-liquid separation module (30; 30 ') comprises a gas permeation membrane (35;

35 ') which is arranged, in a supported manner, between a duct (33; 33') for circulation of the two-phase flow and a duct (34; 34 ') for evacuating the gases which come from the gaseous phase of the two-phase flow and which have passed through the permeation membrane.