EP3593897A1 - Chambre de liquéfaction dans un dispositif d'incorporation d'améliorants d'indice de viscosité dans des huiles de base ainsi que dispositif et procédé d'incorporation d'améliorants d'indice de viscosité dans des huiles de base - Google Patents

Chambre de liquéfaction dans un dispositif d'incorporation d'améliorants d'indice de viscosité dans des huiles de base ainsi que dispositif et procédé d'incorporation d'améliorants d'indice de viscosité dans des huiles de base Download PDF

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Publication number
EP3593897A1
EP3593897A1 EP18182364.2A EP18182364A EP3593897A1 EP 3593897 A1 EP3593897 A1 EP 3593897A1 EP 18182364 A EP18182364 A EP 18182364A EP 3593897 A1 EP3593897 A1 EP 3593897A1
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EP
European Patent Office
Prior art keywords
liquefaction chamber
viscosity index
base oil
index improvers
protective gas
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP18182364.2A
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German (de)
English (en)
Inventor
Gerhard Seewald
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Intervalve Research And Development GmbH
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Intervalve Research And Development GmbH
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Filing date
Publication date
Application filed by Intervalve Research And Development GmbH filed Critical Intervalve Research And Development GmbH
Priority to EP18182364.2A priority Critical patent/EP3593897A1/fr
Publication of EP3593897A1 publication Critical patent/EP3593897A1/fr
Withdrawn legal-status Critical Current

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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
    • C10M177/00—Special methods of preparation of lubricating compositions; Chemical modification by after-treatment of components or of the whole of a lubricating composition, not covered by other classes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/40—Mixing liquids with liquids; Emulsifying
    • B01F23/45—Mixing liquids with liquids; Emulsifying using flow mixing
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/40—Mixing liquids with liquids; Emulsifying
    • B01F23/47—Mixing liquids with liquids; Emulsifying involving high-viscosity liquids, e.g. asphalt
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/40—Mixing liquids with liquids; Emulsifying
    • B01F23/48—Mixing liquids with liquids; Emulsifying characterised by the nature of the liquids
    • B01F23/482—Mixing liquids with liquids; Emulsifying characterised by the nature of the liquids using molten solids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/40—Mixing liquids with liquids; Emulsifying
    • B01F23/49—Mixing systems, i.e. flow charts or diagrams
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/10—Mixing by creating a vortex flow, e.g. by tangential introduction of flow components
    • B01F25/103—Mixing by creating a vortex flow, e.g. by tangential introduction of flow components with additional mixing means other than vortex mixers, e.g. the vortex chamber being positioned in another mixing chamber
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/20—Jet mixers, i.e. mixers using high-speed fluid streams
    • B01F25/21—Jet mixers, i.e. mixers using high-speed fluid streams with submerged injectors, e.g. nozzles, for injecting high-pressure jets into a large volume or into mixing chambers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/50—Circulation mixers, e.g. wherein at least part of the mixture is discharged from and reintroduced into a receptacle
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/50—Mixing receptacles
    • B01F35/53—Mixing receptacles characterised by the configuration of the interior, e.g. baffles for facilitating the mixing of components
    • B01F35/532—Mixing receptacles characterised by the configuration of the interior, e.g. baffles for facilitating the mixing of components with guide tubes on the wall or the bottom
    • 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
    • C10M2205/00—Organic macromolecular hydrocarbon compounds or fractions, whether or not modified by oxidation as ingredients in lubricant compositions
    • C10M2205/02—Organic macromolecular hydrocarbon compounds or fractions, whether or not modified by oxidation as ingredients in lubricant compositions containing acyclic monomers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10N—INDEXING SCHEME ASSOCIATED WITH SUBCLASS C10M RELATING TO LUBRICATING COMPOSITIONS
    • C10N2030/00—Specified physical or chemical properties which is improved by the additive characterising the lubricating composition, e.g. multifunctional additives
    • C10N2030/02—Pour-point; Viscosity index
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10N—INDEXING SCHEME ASSOCIATED WITH SUBCLASS C10M RELATING TO LUBRICATING COMPOSITIONS
    • C10N2070/00—Specific manufacturing methods for lubricant compositions
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10N—INDEXING SCHEME ASSOCIATED WITH SUBCLASS C10M RELATING TO LUBRICATING COMPOSITIONS
    • C10N2070/00—Specific manufacturing methods for lubricant compositions
    • C10N2070/02—Concentrating of additives

Definitions

  • the invention relates to a method and an arrangement for mixing viscosity index improvers in base oils.
  • the invention also relates, and in particular, to a liquefaction chamber in an arrangement for mixing viscosity index improvers in base oils.
  • Viscosity index improvers made of high molecular weight polymers are usually in the form of granules, highly pasty polymer bales (mixed with a few percent by mass of a base oil) or as a highly viscous but flowable fluid (mixed with a higher percent by weight of a base oil).
  • Typical VI improvers include, for example, polyisobutylenes, polymethacrylates (PMA) and olefin copolymers (OCP), in particular olefinic ethylene-propylene copolymers.
  • the aim of mixing VIV in base oils is to reduce the drop in viscosity in mixtures when the temperature rises. This is achieved by the macromolecules being present as coils at low temperatures, which unfold more and more at higher temperatures. Intermolecular interactions in the vicinity of the elongated macromolecules maintain the viscous properties there.
  • the resulting lubricant mixtures can thus be used over wide temperature ranges (multi-grade oils) and ensure the necessary lubricating film thickness even at higher temperatures.
  • VIV and base oil eg 10 wt% VIV and 90 wt% base oil, with the VIV possibly being comminuted
  • VIV and base oil eg 10 wt% VIV and 90 wt% base oil, with the VIV possibly being comminuted
  • temperatures above 130 ° C may be required.
  • process temperature there is little scope for the value of the process temperature, since a completely homogeneous mixture is not formed at too low temperatures, or the base oil content is damaged if the temperatures are too high.
  • Mechanical mixing by means of agitators improves in accordance with the reduced viscosity.
  • the temperatures during the mixing process should be chosen so that substantial thermal decomposition or undesired chemical reactions are avoided.
  • DE 2932459 C2 presents a method and a device for mixing VIV as granules or as a powder in base oil.
  • the VIV granulate or VIV powder is weighed into a metering funnel designed as an input lock, the wall of which is constantly flushed with base oil, and the VIV-base oil mixture that forms is recurrently fed to a colloid mill in one cycle . Due to the cyclic grinding process, the VIV content in the base oil is better pre-dissolved and the time for the mixing process, which follows in another agitator tank, is significantly reduced.
  • this method is unsuitable for highly pasty bale-form viscosity index improvers.
  • CN 205127860 U discloses a processing process of base oils with a VIV that has already been liquefied, in advance through a base oil mixing.
  • a partial flow of the base oil and the liquefied and therefore also pumpable VIV are introduced separately into a first boiler and mixed with an agitator.
  • the premix enriched in this way with VIV is then fed into a mixer section second boiler combined with another partial flow of base oil, mixed with another stirrer and thus diluted to the final mixture.
  • an inert gas is used at excess pressure.
  • the individual components, the pre-mix and the final mix have a sufficiently low viscosity so that the mixing process takes place at moderate temperatures.
  • the speeds of the agitator motors are sufficiently low that no aging processes with regard to temperature or shear occur.
  • this process fails in the case of non-liquefied, highly pasty VIV in bale form.
  • additives such as corrosion inhibitors, friction reducers, antioxidants, etc.
  • additives such as corrosion inhibitors, friction reducers, antioxidants, etc.
  • the oil additives are placed in a suitable container using a dry inert atmosphere, with stirring and at slightly elevated temperatures (at about 40 ° C - 60 ° C and preferably not higher than about 40 ° C) Base oil introduced. In this way, the oil additives dissolve more easily in the oil and the lubricant becomes more homogeneous.
  • VIV viscosity index improvers
  • the process enables a batch of at least 70 wt% viscosity index improver and at most 30 wt% base oil to be mixed in a liquefaction chamber by introducing heat under protective gas at excess pressure and by fluidic circulation of the liquid components in a secondary circuit.
  • the resulting dissolved concentrate is then mixed into a main stream of base oil of suitable mass in accordance with a target mixture.
  • Liquefaction of highly paste-like viscosity index improvers normally causes much greater difficulties, since the viscosity of highly paste-like VIV is several orders of magnitude higher than that of VIV that has already been liquefied with base oil.
  • the use of protective gases also in the conditioning of the base oil, prevents aging processes such as oxidation and hydrolysis at the mixing partners.
  • a disadvantage of the described method is the still very long melting times of the VIV used and the associated increased energy density.
  • the liquefaction chamber is to be improved by shortening the melting times and the associated reduced energy density.
  • the liquefaction chamber is preferably arranged in an arrangement for carrying out the method for mixing viscosity index improvers into base oils.
  • the object of the invention is therefore also to improve an arrangement and a method for melting viscosity index improvers in base oils, the viscosity index improvers being in particular in the form of highly pasty polymer bales. This makes it possible to carry out the mixing operations in such a way that further processing of the mixtures can follow immediately
  • the object is achieved by means of a liquefaction chamber, which is preferably arranged in an arrangement for mixing viscosity index improvers into base oils.
  • the liquefaction chamber according to the invention has the following features:
  • Connections for introducing base oil and / or for introducing a concentrate of base oil and viscosity index improvers and connections for dispensing a concentrate of base oil and viscosity index improvers and / or a target mixture, at least one liquid mixing nozzle and a guide basket, the at least one liquid mixing nozzle being designed for this are to generate a coaxial flow in the liquefaction chamber and the guide basket is designed for this by means of at least one element for flow conduction, which is arranged on the guide basket, to convert the coaxial flow into a turbulent flow directed inwards to the liquefaction chamber.
  • the liquefaction chamber has further connections for use in an arrangement for mixing viscosity index improvers in base oils. These connections are preferably a connection to a first suction device and / or a connection to a first protective gas supply.
  • the liquefaction chamber also has heating elements for heating the viscosity index improvers.
  • the at least one element for flow conduction which is arranged on the guide cage, is particularly preferred, a flow guide plate and / or at least one opening in the guide cage.
  • the use of several elements for flow conduction is conceivable.
  • a uniform distribution of the elements for flow conduction on the guide cage is preferably conceivable.
  • the flow line elements divert the viscous liquids, preferably to the center of the liquefaction chamber.
  • the guide basket preferably has a combination of flow guide plates and openings in the guide basket, so that the viscous liquids pass through the guide basket into the interior of the liquefaction chamber.
  • the liquid mixing nozzles are also preferably designed to inject viscous liquids, such as the base oil or base oil with already liquefied VIV, into the liquefaction chamber.
  • the arrangement according to the invention for mixing viscosity index improvers in base oils has a main circuit with a boiler for holding a base oil, the main circuit being designed to condition the base oil by introducing heat under protective gas at excess pressure. Furthermore, the arrangement has a secondary circuit with the liquefaction chamber according to the invention, the secondary circuit being designed to liquefy viscosity index improvers and a concentrate of viscosity index improvers and base oil by introducing heat under protective gas at excess pressure and by means of a fluidic circulation of the base oil in the secondary circuit to condition. According to various embodiments, the main circuit and secondary circuit are connected to one another in such a way that the conditioned concentrate is returned to the main circuit.
  • the liquefaction chamber has liquid mixing nozzles and a guide basket.
  • the liquid mixing nozzles are designed to generate a coaxial flow in the liquefaction chamber.
  • the liquid mixing nozzles are preferably also designed to inject viscous liquids, such as the base oil, into the liquefaction chamber.
  • the guide cage is designed for this purpose by means of flow guide plates which are arranged on the guide cage to convert the coaxial flow into a turbulent flow directed inward to the liquefaction chamber.
  • the process according to the invention enables a batch of at least 70 wt% viscosity index improver and at most 30 wt% base oil to be mixed in a liquefaction chamber by introducing heat under protective gas at excess pressure and by a fluidic circulation of the liquid constituents in a secondary circuit.
  • the resulting dissolved concentrate is then mixed into a main stream of base oil of suitable mass in accordance with a target mixture.
  • Liquefaction of highly paste-like viscosity index improvers normally causes much greater difficulties, since the viscosity of highly paste-like VIV is several orders of magnitude higher than that of VIV that has already been liquefied with base oil.
  • the invention is concerned with a gentle solution mechanism, in which only the absolutely necessary heat is introduced into VIV and base oil, and in which the protective gas with overpressure prevents outgassing of important components, such as ethylene and propylene, from the olefinic copolymers.
  • important components such as ethylene and propylene
  • just bound ethylene and propylene ensure increased miscibility with base oils.
  • the dissolved concentrate consists of at least 70 wt% viscosity index improver and at most 30 wt% base oil.
  • What is essential is a combination of low-shear liquefaction by means of controlled, controllable heating of the materials and one suitable protective gas, such as nitrogen or butane or carbon dioxide.
  • the temperature is selected between 90 ° C and 100 ° C and the defined overpressure in the liquefaction chamber is selected between 100 mbar and 50 bar to prevent outgassing during the mixing of viscosity index improvers into the base oil.
  • the overpressure is preferably chosen to be less than 24 bar, and the overpressure is even more preferably less than 10 bar.
  • the defined overpressure prevents outgassing when the viscosity index improver is mixed into the base oil and the solubility time is minimized.
  • the pressure in the boiler is less than half the pressure in the liquefaction chamber in this embodiment.
  • the arrangement according to the invention for carrying out the method for mixing viscosity index improvers into base oils for producing a target mixture consists of a boiler for a base oil and a liquefaction chamber for a viscosity index improver.
  • a main circuit and a secondary circuit are arranged for separate conditioning of mixing partners of the target mixture.
  • the main circuit is arranged for filling and conditioning the base oil and the secondary circuit for liquefying and conditioning a concentrate of viscosity index improver and base oil.
  • the main circuit connects the boiler, at least one pump, at least one heater and several static mixers in series with one another via a main line.
  • the liquefaction chamber is connected to the main circuit via a branch line and to the secondary circuit via a secondary line, which leads back into the liquefaction chamber via a pump.
  • a first suction device is connected to the liquefaction chamber and a second suction device is connected to the boiler, the suction devices being operated via a common vacuum pump.
  • a first protective gas supply is with the liquefaction chamber and a second protective gas supply is connected to the boiler, the protective gas supplies being connected to a common protective gas pressure vessel.
  • the first suction device of the liquefaction chamber is defined by the vacuum pump, a suction line, a three-way valve and a connection to the liquefaction chamber
  • the second suction device of the boiler is defined by the vacuum pump, another suction line, a three-way valve and a connection to the boiler.
  • the first protective gas supply to the liquefaction chamber takes place via the protective gas pressure container, several line sections of a protective gas line, a metering valve, a three-way valve and a connection to the liquefaction chamber and the second protective gas supply of the boiler takes place via the protective gas pressure container, several line sections of a protective gas line, a metering valve, a three-way valve and a connection to Boiler.
  • the pumps of the arrangement are low-shear rotary pumps in this embodiment; however other possible pumps are not excluded.
  • the heater is a screw-in heater, although other heaters are also conceivable.
  • the main line in the boiler ends in an immersion nozzle with a freely rotatable end piece.
  • the main line ends in the boiler in a mixing nozzle.
  • the branch line below the liquefaction chamber opens into the main line and into a Venturi nozzle which is arranged in the branch line near the connection point to the main line.
  • a melting grate is arranged in the liquefaction chamber, the secondary line opening into the liquefaction chamber above it.
  • the main line, the secondary line, the branch line and the boiler are thermally insulated.
  • the use of protective gases also in the conditioning of the base oil, prevents aging processes such as oxidation and hydrolysis at the mixing partners.
  • liquid mixing nozzles and the guide basket with elements for flow conduction in addition to the introduction of heat under protective gas at excess pressure and a fluidic circulation of the liquid components in a secondary circuit, improve the permanent rinsing of the VIV and thus lead to a shortening of the melting times of the VIV.
  • the energy density introduced thus further decreases depending on the coaxial turbulent flow within the liquefaction chamber.
  • Figure 1 shows a diagram in which the dependency of the solubility temperature ⁇ L of a mixture of x wt% of a viscosity index improver based on olefin copolymers (OCP) and 100 wt% - x wt% of a base oil with a varying VIV content under atmospheric conditions in Warming cabinet (course with circles and dashed lines) and under N2 atmosphere and at overpressure (at approx. 5 bar with a star, at approx. 9 bar marked with diamond). If the solubility temperature ⁇ L is exceeded under the pressure and protective gas conditions described, the mixture is homogeneous.
  • OCP olefin copolymers
  • VIV viscosity index improvers
  • the solubility temperature ⁇ L was 145 ° C, for mixtures with a VIV content above 20 wt%, the solubility temperature ⁇ L was 185 ° C ( Figure 1 , Course with circles and semicolon).
  • the low-shear mixing system which works without the participation of oxygen and moisture, consists of a main circuit I and a secondary circuit II for separate conditioning of the mixing partners.
  • the arrangement consists of a boiler 7, which can be opened under atmospheric conditions and is initially filled with the base oil.
  • a pump 10 for example a low-shear rotary lobe pump, and a heater 9, for example a screw-in heating element, are arranged in the main line 14 for the circulation of the base oil.
  • Static mixers 11, which support the mixing process, are located at regular intervals in the main line 14.
  • the main circuit I is fed from the boiler 7 via the pump 10 back to the boiler 7 via the main line 14.
  • the main line 14 ends in the boiler 7 in an immersion connector 12 with a freely rotatable end piece to support the distribution of the inflowing fluid into the boiler 7.
  • the rotatably mounted end piece of the immersion connector 12 is set into rotation via the inflow into the boiler 7 and realizes a spiral mixing of the mixture flowing in from the main line with the liquid in the boiler 7.
  • a dissolved line m 1 at least 70 wt., is mixed in via a branch line 16 % Viscosity index improver and at most 30 wt% base oil, from the secondary circuit II into the base oil which flows through the main line 14 of the main circuit I.
  • a liquefaction chamber 1, which serves to liquefy VIV bales, is connected at its lower end via the branch line 16, in which a Venturi nozzle 6 is arranged, and via a shut-off and metering valve 5 to the main line 14.
  • a secondary line 15 branches below the liquefaction chamber 1 from the branch line 16 and leads via a further pump 4, which in this exemplary embodiment is also a rotary lobe pump, back into the liquefaction chamber 1 above a melting grate 3, which is arranged in the liquefaction chamber 1 is.
  • the secondary line 15 together with the branch line 16 forms the secondary circuit II (surrounded by a dashed line).
  • the liquefaction of VIV bales in the liquefaction chamber 1 takes place by heating on a melting grate 3.
  • the melting grate 3 has a grate support with a triangular cross section and is used to generate an inhomogeneous temperature field, as a result of which the concentrate m 1 is heated to an average temperature T m1 during the conditioning phase.
  • the melting grate 3, with the VIV bales placed on it is constantly flushed with the base oil introduced.
  • the pump 4 ensures that the liquid components circulate when the concentrate m 1 is liquefied in the secondary circuit II.
  • a vacuum pump 21 forms, together with a suction line 22, a three-way valve 23 and a connection to the liquefaction chamber 1, a first suction device 2a of the liquefaction chamber 1.
  • the second suction device 2b of the boiler 7 is operated by the vacuum pump 21, a suction line 24, a three-way valve 25 and by one Connection to boiler 7 defined.
  • the first protective gas supply 8a of the liquefaction chamber 1 takes place via a protective gas pressure container 81, a protective gas line 821 and a protective gas line 823, a metering valve 822, the three-way valve 23 and the connection to the liquefaction chamber 1.
  • the second protective gas supply 8b of the boiler 7 takes place via the protective gas pressure container 81, a protective gas line 831 and a protective gas line 833, a metering valve 832, the three-way valve 25 and the connection to the boiler 7.
  • the arrows, horizontal or vertical, indicate the direction of flow of the protective gas in the suction and filling mode.
  • the liquefaction chamber 1 is thus connected to the protective gas pressure container 81 via the suction device 2a and the protective gas supply 8a and the boiler 7 via the suction device 2b and protective gas supply 8b.
  • the suction devices 2a, 2b and the protective gas feeds 8a, 8b serve, in addition to the protective gas purging and the protective gas filling of the gas space of the liquefaction chamber 1 or the boiler 7, also to set a suitable, defined excess pressure, the excess pressure in the liquefaction chamber 1 being designated p m1 and the overpressure in the boiler 7 with p 2 .
  • the shut-off and metering valve 5 of the secondary circuit II remains closed during filling and during the conditioning phase and is only opened during the mixing process between the concentrate m 1 and the base oil in such a way that the partial flow of the concentrate m 1 from the secondary circuit II to the main stream of the base oil from the main circuit I is adjusted at most stoichiometrically, in accordance with the target mixture m 2 .
  • a veto nozzle 6 is arranged in the branch line 16 near the connection point to the main line 14. With the Veturi nozzle 6 for mixing the concentrate m 1 from the secondary circuit II into the base oil, which flows through the main circuit I, at the point where the branch line 16 meets the main line 14, the partial flow of the secondary circuit II into the partial flow of Main circuit I sucked in.
  • a screw-in heating element 9 for heating the base oil to an average temperature T 2 of 60 ° C. to 90 ° C. during the conditioning phase is arranged in the main line 14 between the pump 10 and the connection point to the branch line 16.
  • a sight glass is located in the branch line 16, between the liquefaction chamber 1 and the branch to the secondary line 15, and a sight glass is also arranged in the liquefaction chamber 1 itself. Both sight glasses are used to check that the concentrate m 1 is free of streaks and to control the mass transport from the liquefaction chamber 1.
  • FIG 3 shows the device according to the invention for mixing viscosity index improvers in suitable base oils in a further embodiment.
  • the immersion nozzle 12 is replaced by a mixing nozzle 13.
  • the liquid flowing into the boiler 7 from the main line 14 via the mixing nozzle 13 simultaneously sucks through lateral openings of the mixing nozzle 13, according to the ejector principle, Liquid from the boiler 7 into the mixing nozzle 13 and mixes both liquid flows in the mixing nozzle 13 to form a liquid-free jet which emerges from the mixing nozzle 13 below the liquid level in the boiler 7.
  • the liquefaction chamber 1, which is shut off from the main circuit I, is made up of at least 70 wt% viscosity index improver and at most 30 wt% base oil with a suitable mass of base oil and a suitable number of 25 kg bales of the viscosity index improver (macromolecular Copolymers) and sealed under atmospheric conditions and laboratory temperature.
  • a rough vacuum is generated in the gas space of the liquefaction chamber 1 via the suction device 2a.
  • the gas space of the liquefaction chamber 1 is filled with protective gas via the protective gas supply 8a. This process of inert gas flushing is repeated several times.
  • the gas space of the liquefaction chamber 1 is then filled with protective gas up to a defined excess pressure p m1 .
  • the overpressure p m1 in the liquefaction chamber 1 can be between 100 mbar and 50 bar.
  • the excess pressure p m1 is preferably less than 24 bar, and in the specific case it is less than 10 bar.
  • the VIV bales deposited over the heated melting grate 3 are washed over by the constant circulation of the introduced base oil via the pump 4 in the secondary circuit II. During the conditioning phase, more and more liquefied constituents dissolve from the VIV bales until the batch is present as a concentrate m 1 at a temperature T m1 above the solubility temperature (for example approx. 100 ° C. or 337 K at 9 bar overpressure).
  • T m1 above the solubility temperature
  • a mass of base oil suitable for the target mixture m 2 at room temperature is filled into the boiler 7.
  • a coarse vacuum is alternately generated above the gas space above in the boiler 7 by means of the suction device 2b and then filled with protective gas via the protective gas supply 8b.
  • the gas space of the boiler 7 is filled with protective gas up to an overpressure p 2 of p 2 ⁇ p m 1 .
  • the base oil is conveyed by the pump 10 via the main circuit I and heated to the temperature T 2 (of approximately 90 ° C. or 363 K) by means of a heater 9 in a temperature-controlled manner.
  • the base oil from the boiler 7 passes through the static mixers 11, which are introduced at regular intervals into the main line 14 of the main circuit I, and finally reaches the boiler 7 via the immersion connector 12.
  • the protective gas with an excess pressure p m1 is used in the liquefaction chamber 1 of the secondary circuit II, the protective gas is applied in the boiler 7 of the main circuit II with a lower excess pressure p 2 .
  • the static pressure difference p m1 - p 2 is essentially distributed as fluid mechanical energy loss over the static mixers 11 installed in the main circuit I at regular intervals.
  • the static mixers 11 installed in the main line 14 ensure a low-shear mixing of the fluid flow by generating swirl and cross components in the velocity field. Shear-induced aging processes are avoided.
  • the pressure p m1 in the liquefaction chamber 1, the pressure p 2 ( p m1 > p 2 ) in the boiler 7 and the delivery pressure p P of the pump 10 in the main circuit I, before the partial flows flow together, are selected such that on the one hand the Outflow of the concentrate m 1 from the liquefaction chamber 1 is guaranteed, and on the other hand the pressure difference p m1 - p 2 is realized via the pressure drop of the total flow at a mixing temperature T m via the static mixer 11.
  • the Venturi nozzle 6 coming from the secondary circuit II and protruding into the main circuit I has a slanted nozzle end in the main flow direction.
  • the volume flows V ⁇ 2 , V ⁇ m must be measured before and after the confluence.
  • the system is carefully returned to normal pressure, but without the addition of oxygen. Due to the significantly lower viscosity of the target mixture m 2 at the mixture temperature T m compared to the concentrate, the additional dissolved protective gas can be degassed within a very short time.
  • a rough vacuum can optionally be applied (for example p 2 ⁇ - 0.5 bar).
  • the suction device 2b can be used for this.
  • the mixing operations take place at a temperature (approx. 100 ° C.) at which further processing of the Mixtures can connect immediately without having to dissipate excess thermal energy.
  • FIG 4 a vertical sectional view of the liquefaction chamber 1 according to the invention is shown.
  • the section is located on section line B (shown in Figure 5 ).
  • the liquefaction chamber 1 is preferably in an arrangement for mixing viscosity index improvers into base oils, as is shown in FIGS Figures 2 and 3 is explained by way of example.
  • the liquefaction chamber 1 has at least one liquid mixing nozzle 1-1 and a guide basket 1-2.
  • the at least one liquid mixing nozzle 1-1 is designed to generate a coaxial flow in the liquefaction chamber 1.
  • the at least one liquid mixing nozzle 1 - 1 is preferably also designed to inject viscous liquids, such as base oil, into the liquefaction chamber 1.
  • the liquefaction chamber 1 has four liquid mixing nozzles 1-1.
  • the guide basket 1-2 is designed to convert the coaxial flow into a turbulent flow directed inward to the liquefaction chamber 1 by means of elements for the flow line 1-3, which are arranged on the guide basket 1-2.
  • the elements for flow conduction are preferred 1-3 flow baffles, as in Figure 4 displayed.
  • the liquefaction chamber 1 has heating elements 3, with which the contents of the liquefaction chamber 1, in particular the base oil and the viscosity index improvers, are heated.
  • outlets and inlets are preferably arranged on the liquefaction chamber 1.
  • An outlet can be shown, for example, as an access to the suction line in order, as already described above, to generate a rough vacuum in the gas space of the liquefaction chamber 1 via the suction device 2a.
  • An inlet can, for example, provide access to the first protective gas supply 8a.
  • the gas space of the liquefaction chamber 1 becomes coarse after the generation of the rough vacuum via the protective gas supply 8a Shielding gas filled up.
  • the gas space of the liquefaction chamber 1 is preferably filled with protective gas up to a defined excess pressure p m1 .
  • the overpressure p m1 in the liquefaction chamber 1 can be between 100 mbar and 50 bar. Further pressure ranges are conceivable.
  • Another inlet or outlet can be an inlet of a secondary circuit II or an outlet to the secondary circuit II.
  • the VIV bales deposited over a heating element 3 are washed over by the constant circulation of the introduced base oil via the pump 4 in the secondary circuit II.
  • a heating element can be a heated melting grid 3, for example.
  • T m1 above the solubility temperature (for example approx. 100 ° C or 337 K at 9 bar overpressure).
  • Built-in sight glasses made of borosilicate glass are provided for visually checking the transport of a streak-free concentrate m1 from the liquefaction chamber 1.
  • liquid mixing nozzles 1-1 and the guide basket 1-2 with elements for the flow line 1-3 causes, in addition to the introduction of heat under protective gas at excess pressure and a fluidic circulation of the liquid components in a secondary circuit II, an improved permanent rinsing of the VIV and thus leads to a reduction in the melting times of the VIV.
  • Figure 5 is a horizontal sectional view of an embodiment of the liquefaction chamber 1 according to the invention, wherein a view of the liquefaction chamber 1 is shown from above.
  • heating elements 3 which are as in Figure 5 shown can be designed in the form of heatable tubes. These can be part of a melting grate 3. Other Embodiments of heating elements 3 are conceivable.
  • the heating elements 3 With the heating elements 3, the VIV are liquefied by heat, while the VIV is washed around with the base oil.
  • the base oil is preferably introduced by means of the liquid mixing nozzles 1-1.
  • the liquid mixing nozzles 1-1 are mounted in such a way that they cause a coaxial movement of the base oil and / or the already liquefied VIV.
  • In the embodiment of the Figure 5 are four liquid mixing nozzles 1-1 evenly arranged over the circumference of the liquefaction chamber 1 at the same height at an angle of 90 °. Another arrangement of the liquid mixing nozzles 1-1 is conceivable.
  • the coaxial flow which is achieved according to various exemplary embodiments by means of the liquid mixing nozzles 1-1, is converted into a coaxial turbulent flow by means of a guide basket 1-2, which has elements for the flow line 1-3.
  • the coaxial turbulent flow is also directed inwards, into the middle of the liquefaction chamber 1.
  • this is done by a clever arrangement of the elements for flow line 1-3. These are arranged on the guide cage 1-2 in such a way that the liquid bounces against the elements for the flow line 1-3 and is deflected such that the liquid is directed inwards.
  • the guide basket has 1-2 openings, so that the liquid, in particular the base oil and / or already liquefied VIV, is passed through the guide basket 1-2 into the interior of the liquefaction chamber.
EP18182364.2A 2018-07-09 2018-07-09 Chambre de liquéfaction dans un dispositif d'incorporation d'améliorants d'indice de viscosité dans des huiles de base ainsi que dispositif et procédé d'incorporation d'améliorants d'indice de viscosité dans des huiles de base Withdrawn EP3593897A1 (fr)

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EP18182364.2A EP3593897A1 (fr) 2018-07-09 2018-07-09 Chambre de liquéfaction dans un dispositif d'incorporation d'améliorants d'indice de viscosité dans des huiles de base ainsi que dispositif et procédé d'incorporation d'améliorants d'indice de viscosité dans des huiles de base

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EP18182364.2A EP3593897A1 (fr) 2018-07-09 2018-07-09 Chambre de liquéfaction dans un dispositif d'incorporation d'améliorants d'indice de viscosité dans des huiles de base ainsi que dispositif et procédé d'incorporation d'améliorants d'indice de viscosité dans des huiles de base

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EP3593897A1 true EP3593897A1 (fr) 2020-01-15

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Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2932459C2 (de) 1979-08-10 1985-10-31 Mobil Oil Ag In Deutschland, 2000 Hamburg Vorrichtung zum Lösen eines granulatförmigen Feststoffes in einer Flüssigkeit
GB2217619A (en) * 1988-04-18 1989-11-01 Cambridge Isolation Tech Mixers
EP0519760B1 (fr) 1991-06-21 1999-02-03 Ethyl Petroleum Additives, Inc. Concentrés d'additifs pour l'huile et lubrifiants à capacité améliorée
US20080085847A1 (en) 2006-10-10 2008-04-10 Kwok-Leung Tse Lubricating oil compositions
EP2656907A1 (fr) * 2010-12-22 2013-10-30 Institute of National Colleges of Technology, Japan Mélangeur de fluide et procédé de mélange de fluide
WO2015146713A1 (fr) * 2014-03-26 2015-10-01 ヤンマー株式会社 Système de moteur à émulsion et dispositif d'alimentation de combustible à émulsion
CN205127860U (zh) 2015-11-24 2016-04-06 山东万祥润滑科技有限公司 一种润滑油调和设备

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2932459C2 (de) 1979-08-10 1985-10-31 Mobil Oil Ag In Deutschland, 2000 Hamburg Vorrichtung zum Lösen eines granulatförmigen Feststoffes in einer Flüssigkeit
GB2217619A (en) * 1988-04-18 1989-11-01 Cambridge Isolation Tech Mixers
EP0519760B1 (fr) 1991-06-21 1999-02-03 Ethyl Petroleum Additives, Inc. Concentrés d'additifs pour l'huile et lubrifiants à capacité améliorée
US20080085847A1 (en) 2006-10-10 2008-04-10 Kwok-Leung Tse Lubricating oil compositions
EP2656907A1 (fr) * 2010-12-22 2013-10-30 Institute of National Colleges of Technology, Japan Mélangeur de fluide et procédé de mélange de fluide
WO2015146713A1 (fr) * 2014-03-26 2015-10-01 ヤンマー株式会社 Système de moteur à émulsion et dispositif d'alimentation de combustible à émulsion
CN205127860U (zh) 2015-11-24 2016-04-06 山东万祥润滑科技有限公司 一种润滑油调和设备

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