WO1998046337A1 - Procede et installation de filtration tangentielle d'un liquide visqueux - Google Patents
Procede et installation de filtration tangentielle d'un liquide visqueux Download PDFInfo
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- WO1998046337A1 WO1998046337A1 PCT/FR1998/000746 FR9800746W WO9846337A1 WO 1998046337 A1 WO1998046337 A1 WO 1998046337A1 FR 9800746 W FR9800746 W FR 9800746W WO 9846337 A1 WO9846337 A1 WO 9846337A1
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- Prior art keywords
- liquid
- pressure
- viscous liquid
- permeate
- oils
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Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
- C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
- C10M175/0058—Working-up used lubricants to recover useful products ; Cleaning by filtration and centrifugation processes; apparatus therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D37/00—Processes of filtration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/027—Nanofiltration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/04—Feed pretreatment
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
- B01D61/145—Ultrafiltration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
- B01D61/147—Microfiltration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
- B01D61/16—Feed pretreatment
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G31/00—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for
- C10G31/09—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for by filtration
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- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B7/00—Separation of mixtures of fats or fatty oils into their constituents, e.g. saturated oils from unsaturated oils
- C11B7/0008—Separation of mixtures of fats or fatty oils into their constituents, e.g. saturated oils from unsaturated oils by differences of solubilities, e.g. by extraction, by separation from a solution by means of anti-solvents
- C11B7/005—Separation of mixtures of fats or fatty oils into their constituents, e.g. saturated oils from unsaturated oils by differences of solubilities, e.g. by extraction, by separation from a solution by means of anti-solvents in solvents used at superatmospheric pressures
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/04—Specific process operations in the feed stream; Feed pretreatment
Definitions
- the invention relates to a tangential filtration process for a viscous fluid or liquid in which a third body in the supercritical state is dissolved in this viscous fluid or liquid in order to lower its viscosity.
- the invention also relates to the installation for implementing the method.
- the invention applies in particular to the filtration of heat-sensitive organic liquids and used engine oils.
- the technical field of the invention is filtration, more precisely filtration of viscous fluids or liquids, and in particular tangential filtration of these viscous fluids or liquids.
- Filtration in the classic sense of the term is frontal filtration in which a flow of liquid meets perpendicular to its path a porous obstacle which retains all the particles larger than the size of the pores.
- the particles retained the size of which is conventionally of the order of a millimeter to the micrometer, then form a cake which in turn contributes to the performance of the filtration.
- the particles retained are smaller and smaller while the flow of filtrate decreases, this is the clogging phenomenon.
- the filtration regime never reaches the quasi-stationary state.
- the performance of filtration in retention and flow can be considered constant for a sufficiently long period of time, that is to say that the regime is almost stationary.
- organic liquids With regard to organic liquids, their viscosity, when it is not a question of pure solvents, can be very high, which makes their filtration impossible. This is particularly the case for mineral oils from petroleum fractions or vegetable or animal oils.
- the first solution consists in increasing the temperature of the fluid or liquid to be filtered in order to lower the viscosity.
- document EP-A-0 041 013 describes a process known under the name REGELUB® process in which used engine oils are treated with a view to their recycling, at a temperature of 250 to 300 ° C to lower their viscosity kinematics from 150 cSt up to 1 to 2 cSt.
- Used oils decanted beforehand to remove water, and distilled to remove diesel or petrol, are thus filtered through ceramic mineral membranes made of ⁇ or alumina
- a first batch representing 10% of the initial volume where the contaminants are concentrated by a factor of 10
- a second purified batch representing 90% of the initial volume, of commercial quality, requiring only discoloration and adjustment of the concentration of additives.
- Contaminants are mainly solid particles in the form of sediments, sulfur compounds, metals from engine wear such as iron, lead from fuels, etc., as well as calcium, magnesium, phosphorus, etc. ..
- the solution consisting in heating the liquids to be filtered in order to reduce their viscosity cannot be used on heat-sensitive products which would be degraded by heating, and it is furthermore limited by the technology of "standard” range devices. ". Therefore, temperatures of 120 to 150 ° C are not exceeded, which only provides a limited decrease in viscosity.
- a second solution to allow the filtration of viscous fluids consists in adding at atmospheric pressure, a solvent or "third body” not very viscous, soluble in the product to be filtered, to lower the viscosity.
- hexane can be added to an engine oil.
- the viscosity of the used oil will be reduced by a factor of 2 to 3, allowing a real gain in tangential filtration equal to the ratio of the viscosities divided by the volumes of each of the constituents.
- the viscosity must therefore be greatly lowered by adding small quantities of third bodies. In other words, it would be beneficial to add a weakest viscous third body.
- a third solution to allow tangential filtration of viscous fluids consists in increasing the wall stress by filtration of a biphasic gas / liquid mixture.
- the working pressure is of the same order of magnitude as the conventional ultrafiltration since it reaches a maximum of 5 to 6 bars, which can be described as atmospheric filtration since the permeate is at atmospheric pressure.
- the gas is not dissolved in the liquid phase but injected cocurrently with the liquid, generally vertically. Given the difference in density between the two phases, the gas bubbles will have a rate of rise greater than the liquid flow, they will create a "plug", the steric bulk of which will destabilize by laminating the polarization layer. In absolute value, the speed gradient will locally become very large, resulting in a significant increase in the permeate flow. This process has also been described on a laboratory scale in the document by M. MERCIER, C.
- DELORME "Influence of a gas / liquid two-phase flow on the performance of tangential filtration” - Colloque united Industrie Toulouse 13.06.96 , and is only applicable when the product to be filtered is not foaming.
- a third method which consists in using a "third body" under pressure to treat hydrocarbons is described for example in document FR-A-2 598 717 in which hydrocarbon oils are asphalted by treatment with a solvent to form a light phase oily and a heavy asphalt phase. The solvent is recovered from the oily phase, subjecting it to supercritical conditions for the solvent in order to form a new light phase enriched in solvent, and a new heavy phase.
- This new light phase very low viscosity, is subjected to tangential filtration on a porous mineral membrane. This process is rather close to a liquid / liquid extraction, because the compound in the liquid or supercritical state constitutes a separate phase, the action of which is to extract the light extractable compounds and / or in parallel to cause demixing and a precipitation of heavy compounds.
- the purpose of filtration in this process is not to fractionate compounds of different sizes dispersed in a solvent, but rather to recover the pure solvent for recycling.
- the document EP-A-0356 815 relates to the treatment of polycarbonates, polyester carbonates and aromatic polyesters melted and then treated with a supercritical gas in order to lower the viscosity, which makes their purification by filtration possible. front on fine filters, for example on stainless steel filter candles.
- the viscosities of the initial molten polymers are very high, for example of the order of 900 Pa.s and are reduced to final viscosities of around 35 Pa.s by treatment with carbon dioxide at 250 bars and 257 ° C.
- the object of the present invention is to provide a method of filtering a viscous fluid or liquid which does not have the drawbacks of the prior art and which makes it possible to overcome the problems encountered in these methods.
- the object of the present invention is also to provide a method of filtering a viscous liquid which meets inter alia the needs mentioned above.
- a method of filtering a viscous fluid or liquid having an initial viscosity under ordinary conditions of 0.01 Pa.sa 1 Pa.s characterized in that under the effect of pressure, a third body in the supercritical state is dissolved in the viscous liquid having a viscosity much lower than that of said viscous liquid, whereby a liquid monophasic solution is obtained whose viscosity is reduced relative to the initial viscosity of the pure viscous liquid, said monophasic liquid solution under pressure being treated by tangential filtration, to give on the one hand a retentate comprising the third body and heavy compounds, and on the other hand a permeate comprising the third body and light compounds.
- a part of the retentate is separated (diverted), and evacuated, generally continuously, this part is called "concentrate”.
- Another part of said retentate, which retains the name of "retentate” is generally returned to the start of the process downstream of filtration.
- the process according to the invention allows, due to the lowering of the viscosity obtained by dissolving the third body in the viscous fluid, and generally without significant increase in temperature, the tangential filtration of all types of viscous fluids or liquids.
- the viscous fluids or liquids treated by the process according to the invention generally have an initial viscosity under ordinary conditions (that is to say atmospheric pressure and 25 ° C) from 10 "2 Pa.s to 1 Pa.s .
- the viscous liquid generally designates the initial liquid or "first body” containing for example the particles and / or molecules to be separated, that is to say the "second body".
- the field of application of the process according to the invention therefore lies in the range of medium to high viscosities, in contrast to the very high viscosities encountered in processes such as the process described in document EP-A-0 356 815.
- the third body can be chosen from gaseous compounds under ordinary conditions of temperature and pressure (1 bar, 25 ° C.) and which are not reactive with respect to the initial viscous liquid.
- the third body can also be chosen from compounds which are liquid under ordinary conditions of temperature and pressure, and which are not reactive with respect to the initial viscous liquid.
- the operating conditions of the process must bring it to the supercritical state, in which it is very little viscous.
- the viscosity of the third body should preferably be much lower than the viscous liquid, that is to say that it should preferably be from 10 -5 to 10 ⁇ 3 Pa.s, that is to say a - say 100 times to 100,000 times less than that of viscous liquid.
- the third body is generally a pure compound but it can also be formed from the mixture of two or more pure compounds, each having properties of third body.
- the liquid monophasic solution (also called “liquid phase") obtained, has a reduced viscosity which is generally of the order of approximately one tenth to approximately one hundredth of the initial viscosity of the viscous liquid, the viscosity of the monophasic solution will therefore be thus generally from 10 -3 Pa.s.
- This decrease in viscosity, due to the dissolution of the third body results in a very significant gain in permeability of the filtrate compared to filtration without a third body at the same temperature.
- the process according to the invention advantageously operates at moderate filtration temperatures, for example from 20 to 200 ° C, preferably from 40 to 150 ° C, more preferably from 40 to 80 ° C.
- the process temperature can be kept within limits compatible with the absence of chemical degradation. Such temperatures are significantly lower than the temperatures in the prior art methods.
- the operating conditions of the process according to the invention are thus harmless for all organic viscous liquids, even the most heat-sensitive.
- the method according to the invention allows for the first time the tangential filtration of thermosensitive liquids and fluids which until now has been impossible to filter by conventional tangential filtration, that is to say at atmospheric pressure. Likewise, limiting the temperature allows filtration of flammable liquids in better safety conditions without having to resort to complex and expensive equipment.
- the moderate temperature range advantageously used by the process does not impose heavy constraints on the material, and is compatible with installations constructed from common materials without the need for special and expensive materials.
- the method according to the invention due in particular to the low viscosity of the liquid phase obtained by dissolving the third body, the moderate temperature used, and the reduced circulation speed used, makes it possible to obtain a significant improvement. of the energy efficiency of the process compared to the processes of the prior art.
- the circulation speeds are thus in the process of the invention from 0.5 to 10 m / s, preferably from 1 to 5 m / s, more preferably from 1 to 4 m / s, these speeds are relatively reduced compared to the methods of the prior art.
- the pressures used in the process of the invention are in all cases greater than the usual pressures of tangential filtration processes such as atmospheric microfiltration or ultrafiltration processes.
- the working pressure obviously depends on the viscous fluid and the third body used, it will generally be from 30 to 500 bars, more preferably from 50 to 300 bars, better still from 100 to 150 bars. For each viscous fluid, there is an optimal pressure which makes it possible to dissolve only the quantity necessary for lowering the viscosity without, moreover, diluting the liquid phase too much.
- the temperature and pressure conditions can be chosen under criticism with respect to the third body, or preferably supercritical with respect to the third body.
- the pressurization of the process can be ensured by the pressure of the excess third body in the gaseous or supercritical state which floats above the liquid phase.
- pressurization can also be ensured by a neutral gas such as helium, or by a gas having the characteristics of a neutral gas such as nitrogen, the partial pressure of which in the liquid phase can be neglected. It is desirable to operate in this way when the difference in density between the third body and the liquid phase becomes too small, for example at 400 kg / m 3, because in this case the circulation of the liquid phase can cause a uncontrolled two-phase mixture in the separating element such as a membrane. Tangential filtration applies to the separation of all particles or molecules contained in the initial viscous liquid or fluid, whatever their size, it can therefore be icrofiltration, ultrafiltration or nanofiltration.
- the pressure used during the tangential filtration operation depends on the technology used, it will generally be from 1 to 6 bars for microfiltration or ultrafiltration and from 5 to 50 bars for nanofiltration.
- the permeate - that is to say the fraction of the liquid phase which passes through the filtration element such as a membrane, and which is formed by the monophasic mixture of the viscous liquid more than a third body in which the "heavy” compounds, molecules and / or particles retained by the membrane, are missing, and in which the "light” compounds are found - and the separate (diverted) concentrate from the retentate - the retentate being the fraction of the liquid phase which is retained by the filtration element such as a membrane, and which is formed by the monophasic mixture of the viscous liquid over the third body in which the "heavy” compounds retained by the membrane are concentrated - are advantageously treated by lowering the pressure (depressu ⁇ sation) whereby the permeate is separated into a filtrate comprising "light” compounds and the third body, and the concentrate is separated into a residue comprising "heavy” compounds and the third body.
- the depressurization of the permeate and / or of the concentrate can be carried out in several stages, for example from 2 to 4 stages, each operating at pressures for example from 500 to 300 bars, then from 150 to 50 bars , then from 50 to 1 bar (s), depending on whether one wishes to recover fractions more or less rich in lighter elements, these will indeed be found mainly in the last stages of depressurization.
- the third body resulting from the separation of the permeate and / or that of the concentrate is recycled towards the entry of the process which contributes favorably to the mass and energy balance of the process.
- the pressure at the end of depressurization must be equal to the supply pressure of the third body.
- the process prior to tangential filtration, can advantageously include an additional step of decantation / separation.
- the initial contacting of the viscous liquid and the third body can cause the demixing of heavy compounds, soluble in the pure viscous liquid but insoluble in the liquid phase. This phenomenon is known by the term "anti-solvent effect".
- the advantage of such an additional preliminary step is to anticipate the separation with respect to a single tangential filtration step and to allow a gain in permeate flow.
- the separation of heavy compounds, difficult to separate, is very easily obtained by simple addition of third bodies thanks to this advantageous step of the process according to the invention.
- the method according to the invention can be implemented continuously or even discontinuously, that is to say in batches ("batch").
- the viscous liquid and the third body must be supplied at one time before the tangential filtration stage. This is particularly interesting for products with high added value, available in small quantities and for which continuous operation is not suitable.
- gaseous compounds at ordinary temperature which may be suitable as third bodies there may be mentioned by way of example: carbon dioxide, helium, nitrogen, nitrous oxide, sulfur hexafluoride, gaseous alkanes of 1 to 5 carbon atoms: methane, ethane, propane, n-butane, isobutane, neopentane, gaseous alkenes having 2 to 4 carbon atoms: ethylene, propylene, butene ...; gaseous alkynes: acetylene, propyne and butyne-1; gaseous dienes such as propadiene; gaseous fluorinated hydrocarbons, gaseous chlorinated and / or fluorinated gaseous hydrocarbons, for example chlorofluorocarbons called "Freon®" and also called CFCs or HCFCs, etc., and mixtures thereof.
- chlorofluorocarbons called "Freon®" and also called CFCs or HCFCs,
- alkanes of 5 to 20 ° C. such as n-pentane, isopentane, hexane, heptane , octane, liquid alkenes of 5 to 20 C, liquid alkynes of 4 to 20 C, alcohols such as methanol, ethanol, ketones such as acetone, ethers, esters, hydrocarbons chlorinated and / or fluorinated liquids etc ...
- the third body is in excess relative to the liquid phase, that is to say that it is present in an amount of 1 to 10 relative to the amount of liquid phase. In this case, thermodynamic equilibrium is considered to have been reached and the viscosity is minimal.
- the viscous fluids or liquids which can be treated by the process of the invention are for example organic or aqueous fluids or liquids, in particular organic, thermosensitive or containing thermosensitive products such as vegetable oils or animal oils, body fluids , various food products, liquids from agriculture, and the aqueous phases containing proteins.
- organic, thermosensitive or containing thermosensitive products such as vegetable oils or animal oils, body fluids , various food products, liquids from agriculture, and the aqueous phases containing proteins.
- vegetable oils there may be mentioned for example olive oil, sunflower oil, oregano oil, argan oil.
- animal oils there may be mentioned for example fish oils such as capelin oil, sardine oil, cod liver oil.
- the viscous fluid or liquid can also be chosen from mineral oils, for example from petroleum cuts, silicone oils, industrial oils or fluids, motor oils, cutting fluids, rolling oils, petroleum oils such as as distillation residues of crude oil, used oils of all origins such as used engine oils, used industrial oils etc ..., liquids or process fluids manufacturers loaded with particles and / or heavy compounds, for example catalyst particles, molten polymers such as polyethylene glycols (PEG), etc.
- mineral oils for example from petroleum cuts, silicone oils, industrial oils or fluids, motor oils, cutting fluids, rolling oils, petroleum oils such as as distillation residues of crude oil, used oils of all origins such as used engine oils, used industrial oils etc ..., liquids or process fluids manufacturers loaded with particles and / or heavy compounds, for example catalyst particles, molten polymers such as polyethylene glycols (PEG), etc.
- PEG polyethylene glycols
- the waste oil treatment process known as the REGELUB® process has the major drawback, as we have seen, of an excessively high working temperature of the order of 300 ° C.
- the method according to the invention overcomes the problems associated with this method while obtaining viscosities of the same order of magnitude, namely between 1 and 3 mPa.s.
- the monophasic liquid phase obtained by solubilization of a third body such as C0 2 and composed of crude oil and gas is then treated on ceramic membranes with cut-off threshold compatible with the compounds to be retained, generally in the range of microfiltration or ultrafiltration.
- An additional advantage of the process is the demixing of the tar which is found in these oils following the combustion of the fuel during the engine operation. This demixing is obtained directly by simple addition of C0 2 , causing an anti-solvent effect.
- the pollutants generated during the operation of the engine which are in particular metals, are concentrated in a residual phase which is easy to treat and produces lower final discharges than with the sulfuric acid process.
- the filtrate obtained conventionally representing 90% or more of the initial quantity of viscous fluid, has the same characteristics as that obtained by the REGELUB® process.
- the process of the invention can also find an application in the petrochemical industry for the elimination of asphaltenes and catalyst fines contained for example in an oil fraction.
- This operation is usually carried out after dissolving the residue in a solvent of low boiling point one.
- An alkane can be used under pressure, for example, propane as in the process
- the use of the process according to the invention makes it possible to separate the asphaltenes containing the metals. This operation is done before catalysis.
- the process according to the invention makes it possible to separate the catalyst fines, this operation being carried out after the catalytic step.
- thermosensitive liquids or fluids or containing thermosensitive products in particular liquids or fluids of animal, vegetable, food products, etc.
- the temperature is kept within the limits of chemical or biological compatibility of the product.
- a particularly preferred application is the treatment, at a temperature for example of 40 ° C., of fish oils such as capelin oil of which it is desired to enrich the triglyce ⁇ dic fraction with fatty acids polymsatures C20 and C22 (eicosapentaenoic: EPA and docosahexaenoic : DHA). These fatty acids have a beneficial effect in lowering the level of VLDL ("Very Lo Density Lipoproteins”) and reduce platelet aggregation, which justifies their interest in the prevention of coronary heart disease.
- VLDL Very Lo Density Lipoproteins
- Carbon dioxide is very suitable for this application, given its safety vis-à-vis food.
- the membrane used will preferably be a nanofiltration membrane whose cut-off threshold is close to 800 g / mole.
- the method according to the invention also applies in a particularly advantageous manner to the treatment of aqueous phases containing in particular proteins such as food proteins, for which an effect qualified as an "anti-clogging" effect which can be surprisingly observed. '' explain as follows:
- the dissolution for example, of C0 2 under the effect of pressure causes the formation of carbonic acid. This results in an increase in acidity, that is to say in a decrease in pH.
- the pH is of the order of 3.5.
- the resulting acidity results in a modification of the steric conformation of proteins.
- the decrease in the pH value causes a charging effect which tends to move the proteins away from their isoelectric point (that is to say the point of zero charge reached at pH around 4 to 5 for most dietary protein).
- the change in pH also tends to remove the ceramic constituting the membrane (or any other inorganic material or organic) of its isoelectric point (reached at pH 5.5 in the case of T ⁇ 0 2 ).
- the final and unexpected result is that proteins repel each other, thus keeping their conformation in a ball, and are also repelled by the membrane.
- the retention rate is improved at the same time as clogging is reduced.
- the process according to the invention can also be applied, when nanofiltration is used, to the reduction of the polydispersity of polyethylene glycols (PEG), or of any other polydisperse polymer.
- PEG polyethylene glycols
- the invention also relates to an installation for implementing the method described above.
- This installation is characterized in that it comprises means for supplying viscous liquid and third body, means for pressurizing the viscous liquid and the third body, means for dissolving the third body in the viscous liquid, means for tangential filtration, means for transferring and circulating the monophasic liquid solution to send said solution to said tangential filtration means.
- the installation for implementing the process according to the invention advantageously further comprises means for lowering the pressure of the concentrate and the permeate, and for separating the permeate into the filtrate and into the third body and separating the concentrate into the residue and in the third body.
- the installation also includes recycling means to the entrance of the installation of the separate third body, resulting from the separation of the permeate and the concentrate.
- the installation includes regulating means for regulating the supply and withdrawal.
- This regulation is preferably controlled by the permeate flow.
- FIG. 1 shows a schematic sectional view of an example of an installation for implementing the tangential filtration process under pressure of viscous liquids with the addition of a third body according to the invention.
- FIG. 2 is a graph which represents the density of filtrate flow J in kg / h / m 2 as a function of the transmembrane pressure ⁇ P in bars for polyethylene glycol 400 at 60 ° C. on a nanofiltration membrane.
- Curves A, B, C, D, E, F correspond respectively to partial pressures of C0 2 of 0, 30, 60, 90, 120, and 150 bars.
- FIG. 3 is a graph which represents the density of filtrate flow J in kg / h / m 2 as a function of the transmembrane pressure ⁇ P in bars for polyethylene glycol 400 at 60 ° C. on a single-channel ultrafiltration membrane.
- Curves A, B, C, D, E, F correspond respectively to partial pressures of C0 2 of 0, 52, 61, 91, 121, and 151 bars.
- FIG. 4 is a graph similar to that of Figure 3 for a temperature of 40 ° C. Curves A, B, C, D, correspond respectively to partial pressures of C0 2 of 0, 101, 122, and 152 bars.
- Figure 5 is a graph similar to that of Figure 4 for a temperature of 75 ° C.
- Curves A, B, C, D, E correspond respectively to partial pressures of C0 2 of 0, 53, 103, 122, and 153 bars.
- FIG. 6 is a graph which represents the density of filtrate flow J in kg / h / m 2 as a function of the transmembrane pressure ⁇ P in bars for new and used engine oil at 75 ° C. on an ultrafiltration membrane multichannel.
- Curves A, B, C, D, E, F, G correspond respectively to partial pressures of C0 2 of 0, 51, 76, 101, 110, 120, and 151 bars and give the results obtained for new oil.
- Curve H corresponds to a partial pressure of C0 2 of 101 bars and gives the results obtained for used oil.
- FIG. 7 is a graph showing the evolution of the permeability of used oil J / ⁇ P in kg / (hm 2. bar) as a function of time in hours.
- Curves A and B correspond respectively to transmembrane pressures ⁇ P of 1.5 and 3 bars.
- FIG. 8 is a graph showing the evolution of the filtered flux density J in kg / h. m 2 as a function of time in minutes during capelin oil filtration tests on an ultrafiltration membrane at 60 ° C.
- Curves A and B correspond respectively to partial pressures of C0 of 0 bar and 85 bar.
- the installation for implementing the method according to the invention according to a continuous operating mode therefore comprises, according to FIG. 1, means for supplying fluids for the continuous and simultaneous supply of a viscous liquid of which wants to separate by tangential filtration certain molecular or particulate compounds, and a third body.
- the supply means comprise for example a tank or tank of viscous liquid 1 and a third body tank 2 for example of C0 2 , each of these tanks is connected by means of a pipe 3, respectively 4 provided with a flow meter 5, respectively 6 to a pump 7, respectively 8.
- the two pumps 7 and 8 are preferably metered pumps coupled in order to keep the proportion of the two fluids constant even if the total flow varies.
- the type of these pumps is variable, it can be for example piston pumps, diaphragm pumps or any other type of pump suitable for ensuring a precise dosage of the constituents.
- the third body feeds is in the gaseous state, it can be fed by a compressor (not shown).
- the supply means can also play the role of other means for pressurizing all the fluids, or means for pressurizing these fluids are also provided.
- Pressurization is ensured for example by the pumping systems described above or else the pressurization means comprise means for introducing a neutral gas such as helium or nitrogen.
- a neutral gas such as helium or nitrogen.
- the means for introducing a neutral gas can be a high pressure power source, consisting of high pressure commercial cylinders, or else a compressor.
- the supply means include pumps for supplying viscous liquid and third bodies which are stopped once the loading has been carried out.
- the liquid monophasic solution also called "liquid phase" formed in the solubilization means such that function 9 by dissolving the third body in the viscous liquid is then packaged in packaging means, for example it is brought to the desired temperature by passage for example in heating means such as a hot exchanger 10.
- the solubilization means may also consist of an in-line injection base or of a static mixer.
- the installation shown in FIG. 1 further comprises means for pretreatment or for implementing an additional step, consisting of a decanter pot 11 provided for the case where an "anti-solvent" effect occurs, causing the demixing of heavy compounds. These heavy compounds are then discharged via line 12.
- the installation for implementing the method according to the invention then comprises means for transferring and circulating the single-phase liquid solution. These means comprise for example a reservoir forming a liquid phase reserve 13 and a so-called recirculation pump 14 which makes it possible to send the liquid phase into the tangential filtration means 15.
- the so-called recirculation pump 14 may for example be a vane, piston, centrifugal or gear pump.
- the discharge pressure of this pump must be greater than the pressure losses of the circuit including the filtration means such as the membrane (s) 20, that is to say conventionally of the order of 1 to 10 bars depending on the residual viscosity of the liquid phase.
- the purpose of this pump is also to ensure an adequate circulation speed in the tangential filtration means.
- the circulation means preferably also include a recirculation loop 16, for example provided with a valve 17 and a flow meter 18.
- This recirculation loop makes it possible to circulate in closed circuit part of the retentate from the reserve of liquid phase to the filtration means until the desired concentration factor is obtained.
- the filtration means 15 comprise for example a membrane, or a set of membranes 20 disposed in a housing or tangential filtration enclosure.
- the number of membranes is variable and can range, for example, from 1 to 1000 or more.
- the membrane (s) used will preferably have cutoff thresholds adapted according to the species to be separated .
- the pore diameters may for example range from about one or more micrometer (s), that is to say 100 ⁇ m, to one or more nanometer (s), that is to say 100 ⁇ m, which thus covers the range of separation given by microfiltration membranes, from ultrafiltration to nanofiltration membranes.
- the membranes used will preferably be ceramic, or composed of metal oxides such as A1 2 0 3 , Zr0 2 , Ti0 2 .
- Membranes will preferably be made of alumina, but carbon-supported membranes may also be used, or even organic membranes such as “Nafion®” type polysulfones, provided of course that the polymer constituting this membrane chemically resists the third body.
- the installation described also comprises means for lowering the pressure of the concentrate and the permeate (depressurizing) and for separating the permeate into the filtrate and into the third body, and for separating the part of the retentate called "concentrate", into the residue and in the third body.
- depressurization and separation means essentially comprise separator "pots" of conventional technology 21, 22 such as those conventionally used in the processes using a supercritical fluid, they are for example separators of degasser type or else of type kinetics (cyclone separator).
- the separators are supplied with permeate and concentrate via pipes 23, 24 provided with valves 25 and 26 respectively and with flow meters, for example mass flow meters 27 and 28. Only part of the retentate flow is evacuated as a concentrate. , then separated in the concentrate separator 22, for example, if a concentration factor of 10 has been set, 10% of the retentate is evacuated to give the concentrate, the latter giving the residue and the third body while the rest of the retentate will recirculate.
- the installation finally preferably comprises means for recycling the separate third body resulting from the separation of the permeate and the concentrate, towards the entrance to the installation, that is to say say towards the tank of third bodies 2.
- These means comprise pipes 29, 30, 31.
- the temperature is preferably adjusted by means of heat exchange means such as a cold exchanger provided upstream of the reserve of third bodies, for example of liquefied gas, as well for C0 2 at 50 bars the temperature will be brought to 10 ° C thanks to the exchanger 32.
- the installation finally comprises means of regulation, in fact in a continuous process, the concentrate and the permeate are removed simultaneously such so that the input / output material balance is balanced at all times: this is the role of regulating the supply and withdrawal systems. Overall, this regulation will be subject to the permeate flow.
- the permeate flow rate depends on the operating conditions chosen but also on the behavior of the membrane. We know that this behavior varies by itself, in particular through the effect of clogging. The conduct of the installation will therefore depend on fluctuations in the permeate flow. It is therefore this flow rate which will control the entry of fluids, namely third bodies and viscous liquid, as well as the exit of the concentrate.
- the regulation directly linked to the permeate is essentially the transmembrane pressure, as in any tangential filtration process.
- the concentrate flow is detected by a mass flow meter. For a concentration factor chosen at 10, and assuming that the solubility of the third body such as C0 2 does not vary between the permeate and the concentrate 90% of the incoming material will be evacuated in the permeate and 10% in the concentrate.
- the flow meter installed on the permeate outlet then controls the opening of the concentrate valve to this ratio.
- the feed pumps 7,8 are slaved to the sum of the output flows, either directly by the flow meters 27, 28 or by a constant level in the load pot 13 (only in the where one operates by pressurizing the liquid phase with a gas), or at a constant pressure in the recirculation loop when it is completely filled with a liquid phase.
- the fluidity of the retentate can be optimized by slaving the third-body supply pump 8 to the viscosity measurement: the proportion of the third body relative to the liquid is modified until the viscosity level is reached. This possibility makes it possible to operate at optimum viscosity whatever the changes occurring over time, for example: in the concentration of the liquid phase, in the nature of the food, etc.
- the flow rate of the recirculation pump 14 can be controlled by measuring the pressure drop between the inlet and the outlet of the membrane, in order to work at constant wall stress. This driving mode has become classic in tangential atmospheric filtration.
- the boiler and piping are designed for operation at a maximum pressure of 350 bars and a temperature of 100 ° C.
- membrane support Two types were used: a single-channel cylindrical support in ⁇ alumina manufactured by the company SCT / US Filter and a multi-channel support in the shape of a clover made in a mixture of Ti0 / Zr0 2 / Al 2 0 3 and marketed by TAMI company.
- the nanofiltration tests were carried out on a membrane manufactured by the CEA from a SCT cylindrical support.
- the Ti0 2 filter layer has an average pore diameter of 3 nm.
- the liquids studied are polyethylene glycols with a molar mass 400 g / mole supplied by the company Sigma-Aldrich as well as new or used motor oils and finally fish oils.
- the pressurization is carried out with helium supplied by the company Prodair which makes it possible to ensure a variable transmembrane pressure with a partial pressure of C0 2 equal to 0.
- the pressure is given by carbon dioxide supplied by Air Gaz, powered by a motorized compressed air pump which is a Haskel DSF 52 General Pneumatic pump
- the transmembrane pressure difference is detected by a Rosemount A 1151 differential pressure sensor. This pressure is regulated by a pneumatically controlled Kammer 81037 needle valve.
- the regulation is carried out by a Eurotherm regulator
- the membrane is contained in a high pressure membrane holder located in a thermostatically controlled enclosure.
- the circulation pump is a Micropump 5000 series gear pump with modified seals.
- the flow meter is a dep ⁇ mogene system
- This example illustrates the tangential filtration of model compounds PEG 400 (polyethylene glycol) whose molar mass is 400 g.
- the permeate flow rates in PEG and in C0 2 are measured separately, according to the operating conditions which are mainly the partial pressure of C0 2 , the temperature and the transmembrane pressure.
- the retentate flow rate is maintained at a laminar speed in the membrane.
- the circulation of the retentate is regulated so that the regime is laminar in the membrane.
- the transmembrane pressure varies from 5 to 30 bar.
- Table I The results are grouped in Table I below and are represented on the graph in FIG. 2 where the flow densities are plotted as a function of the transmembrane pressure (in bars).
- Curves A, B, C, D, E, and F correspond respectively to the partial pressures of C0 2 of 0, 30, 60, 90, 120, and 150 bars.
- test conditions are the same as in paragraph A) but for transmembrane pressures compatible with ultrafilters, ie from 0.2 to 4 bars.
- the results are grouped in Table I below and are represented on the graph in FIG. 3 where the flow densities (kg / h / m 2 ) are plotted as a function of the transmembrane pressure (in bars).
- Curves A, B, C, D, E, and F correspond respectively to partial pressures of C0 2 of 0, 52, 61, 91, 121, and 151 bars.
- the gain brought about by the solubility of C0 2 reaches 1.7.
- test conditions are the same as in paragraph B above except for the temperature.
- results are collated in the following table II and are represented on the graph of FIG. 4 where the curves A, B, C, and D correspond respectively to the partial pressures of C0 2 of 0, 101, 122, and 152 bars.
- the gain brought about by the dissolved C0 2 reaches a maximum of 3.1.
- This example illustrates the tangential ultrafiltration of new or used commercial engine oils.
- the new oil is of the SAE 15W 40 type from the ESSO brand, whose kinematic viscosity is 40 cSt at 40 ° C, and the dynamic viscosity of 5.1 mPa.s at 100 ° C according to the SAEJ 300 standard (16 ).
- the viscosity obtained at other temperatures can be estimated from ASTM charts. The results obtained are collated in the following Table IV:
- the used oil corresponds to a drain oil initially originating from a 15W40 oil after 10,000 km of use on a petrol car having traveled 80,000 km, which corresponds to an average wear engine.
- Curves A, B, C, D, E, F, and G correspond to the partial pressures of C0 2 of 0, 51, 76, 101, 110, 120 and 151 bars.
- curve H describes the value of the stabilized flux density of the used oil for a pressure of C0 2 equal to 101 bars. It is the straight line with the lowest slope.
- FIG. 7 shows the evolution of the permeability of used oil over time.
- Curves A and B correspond respectively to transmembrane pressures ⁇ P of 1.5 and 3 bars.
- This example illustrates the tangential filtration of fish oil.
- the processed fish oil is capelin oil.
- Capelin is a fish from the gadidae family, close to cod.
- the crude oil from the pressing of the flesh, and obtained after decanting, is rich in polyunsaturated fatty acids in C20 and C22.
- These fatty acids in particular eicosapentaenoic acid (EPA) and docohexapentaenoic acid (DHA) are potentially useful in the prevention of cardiovascular diseases.
- EPA eicosapentaenoic acid
- DHA docohexapentaenoic acid
- the enrichment of the triglyceride fraction of the oil containing these long chain fatty acids is possible by nanofiltration.
- the lowering of the viscosity is obtained as in the previous examples by solubilization of carbon dioxide under pressure.
- Curves A and B correspond respectively to partial pressures of C0 2 of 0 bar and 85 bar.
- the gain instantly obtained is therefore between 4 and 5.
- the proportion of C0 2 is 20%.
- This example is a comparative example intended to compare the energy efficiency of engine oil filtration by the process known as REGELUB® process described above and by the process according to the invention implementing the solubilization of a third body.
- REGELUB® i.e. 13 kg. h “1 .m " 2 . bar -1 was supplied with a circular cross-section membrane for speeds of 5 a
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- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Nanotechnology (AREA)
- General Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
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- Life Sciences & Earth Sciences (AREA)
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Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB9921165A GB2337211B (en) | 1997-04-15 | 1998-04-14 | Method and installation for tangential filtration of a viscous liquid |
JP54356398A JP2001518842A (ja) | 1997-04-15 | 1998-04-14 | 粘性液体の接線方向濾過のための方法およびプラント |
US09/402,299 US6331253B1 (en) | 1997-04-15 | 1998-04-14 | Method and plant for tangential filtration of a viscous liquid |
NO995053A NO995053L (no) | 1997-04-15 | 1999-10-15 | Fremgangsmåte og anlegg for tangensiell filtrering av en viskös væske |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR97/04619 | 1997-04-15 | ||
FR9704619A FR2761899B1 (fr) | 1997-04-15 | 1997-04-15 | Procede et installation de filtration tangentielle d'un liquide visqueux |
Publications (1)
Publication Number | Publication Date |
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WO1998046337A1 true WO1998046337A1 (fr) | 1998-10-22 |
Family
ID=9505919
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/FR1998/000746 WO1998046337A1 (fr) | 1997-04-15 | 1998-04-14 | Procede et installation de filtration tangentielle d'un liquide visqueux |
Country Status (7)
Country | Link |
---|---|
US (1) | US6331253B1 (fr) |
JP (1) | JP2001518842A (fr) |
KR (1) | KR20010006270A (fr) |
FR (1) | FR2761899B1 (fr) |
GB (1) | GB2337211B (fr) |
NO (1) | NO995053L (fr) |
WO (1) | WO1998046337A1 (fr) |
Cited By (1)
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WO2000052118A1 (fr) * | 1999-03-02 | 2000-09-08 | Commissariat A L'energie Atomique | Procede de traitement d'une huile utilisant un fluide a l'etat supercritique |
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US7128092B2 (en) * | 1999-08-31 | 2006-10-31 | Dct Double-Cone Technology Ag | Separating arrangement for treatment of fluids |
US7425232B2 (en) * | 2004-04-05 | 2008-09-16 | Naturalnano Research, Inc. | Hydrogen storage apparatus comprised of halloysite |
US7400490B2 (en) * | 2005-01-25 | 2008-07-15 | Naturalnano Research, Inc. | Ultracapacitors comprised of mineral microtubules |
US20100059443A1 (en) | 2008-09-02 | 2010-03-11 | Natrix Separations Inc. | Chromatography Membranes, Devices Containing Them, and Methods of Use Thereof |
WO2010147583A1 (fr) * | 2009-06-17 | 2010-12-23 | Exxonmobil Chemical Patents Inc. | Elimination des contaminants de type asphaltènes de courants d'hydrocarbure au moyen d'adsorbants à base de carbone |
FR2957353B1 (fr) * | 2010-03-10 | 2014-09-05 | Commissariat Energie Atomique | Procede d'elimination d'un ou plusieurs composes contenus dans une charge hydrocarbonee |
EP3427815B1 (fr) | 2011-05-17 | 2023-12-06 | Merck Millipore Ltd. | Dispositif a membranes tubulaires en couches pour chromatographie |
FR3009311B1 (fr) * | 2013-08-02 | 2017-07-21 | Lorrainergies | Procede de traitement d'une huile de friture usagee. |
US9013790B1 (en) * | 2014-06-12 | 2015-04-21 | Google Inc. | High contrast rear projection screen for use with a diverging illumination source |
RU2614287C2 (ru) | 2015-09-02 | 2017-03-24 | Закрытое Акционерное Общество "Аквафор Продакшн" (Зао "Аквафор Продакшн") | Система очистки жидкости |
EP3175897B1 (fr) | 2015-12-04 | 2018-04-04 | Evonik Degussa GmbH | Procede ameliore d'extraction de matieres aromatiques a partir de phases liquides aqueuses et/ou contenant des graisses |
US10597588B2 (en) | 2016-10-27 | 2020-03-24 | Fccl Partnership | Process and system to separate diluent |
RU2686199C1 (ru) * | 2018-09-27 | 2019-04-24 | Общество С Ограниченной Ответственностью "Аквафор" (Ооо "Аквафор") | Система очистки жидкости |
US11072542B2 (en) | 2019-01-17 | 2021-07-27 | A. O. Smith Corporation | High water efficiency TDS creep solution |
TWI786468B (zh) | 2019-11-21 | 2022-12-11 | 愛爾蘭商默克密理博有限公司 | 將配體偶合至複合材料的方法 |
CN112973446A (zh) * | 2019-12-17 | 2021-06-18 | 淮北国科环保科技有限公司 | 利用提高温度和选择性过滤来增加过滤膜处理效率的方法 |
CN115838600A (zh) * | 2022-12-07 | 2023-03-24 | 陕西延长石油(集团)有限责任公司 | 超临界二氧化碳混合煤焦油预处理降粘除杂系统及方法 |
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- 1998-04-14 WO PCT/FR1998/000746 patent/WO1998046337A1/fr not_active Application Discontinuation
- 1998-04-14 JP JP54356398A patent/JP2001518842A/ja active Pending
- 1998-04-14 US US09/402,299 patent/US6331253B1/en not_active Expired - Fee Related
- 1998-04-14 KR KR1019997009354A patent/KR20010006270A/ko not_active Application Discontinuation
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FR2598717A1 (fr) * | 1986-05-14 | 1987-11-20 | Inst Francais Du Petrole | Procede de desasphaltage d'une huile d'hydrocarbure renfermant de l'asphalte |
JPS6451115A (en) * | 1987-08-21 | 1989-02-27 | Jgc Corp | Separating method for solids from high viscosity substance |
EP0356815A2 (fr) * | 1988-08-30 | 1990-03-07 | Bayer Ag | Procédé pour la réduction de la viscosité à l'état fondu des polycarbonates aromatiques, des polyesters aromatiques et/ou araliphatiques |
WO1996018445A1 (fr) * | 1994-12-12 | 1996-06-20 | Commissariat A L'energie Atomique | Procede et installation de separation de composes lourds et legers, par extraction par un fluide supercritique et nanofiltration |
WO1996036426A1 (fr) * | 1995-05-16 | 1996-11-21 | Bucher-Guyer Ag | Procede et installation de filtration a courant transversal pour separer un liquide d'une substance coulante |
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Cited By (2)
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WO2000052118A1 (fr) * | 1999-03-02 | 2000-09-08 | Commissariat A L'energie Atomique | Procede de traitement d'une huile utilisant un fluide a l'etat supercritique |
FR2790479A1 (fr) * | 1999-03-02 | 2000-09-08 | Commissariat Energie Atomique | Procede de traitement d'une huile utilisant un fluide a l'etat supercritique |
Also Published As
Publication number | Publication date |
---|---|
GB2337211B (en) | 2001-07-25 |
GB9921165D0 (en) | 1999-11-10 |
FR2761899A1 (fr) | 1998-10-16 |
NO995053D0 (no) | 1999-10-15 |
KR20010006270A (ko) | 2001-01-26 |
FR2761899B1 (fr) | 1999-05-28 |
GB2337211A (en) | 1999-11-17 |
US6331253B1 (en) | 2001-12-18 |
NO995053L (no) | 1999-11-16 |
JP2001518842A (ja) | 2001-10-16 |
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