WO1997030956A1 - Procede pour modifier la composition qualitative et quantitative d'un melange d'hydrocarbures liquides - Google Patents

Procede pour modifier la composition qualitative et quantitative d'un melange d'hydrocarbures liquides Download PDF

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Publication number
WO1997030956A1
WO1997030956A1 PCT/US1996/002612 US9602612W WO9730956A1 WO 1997030956 A1 WO1997030956 A1 WO 1997030956A1 US 9602612 W US9602612 W US 9602612W WO 9730956 A1 WO9730956 A1 WO 9730956A1
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WIPO (PCT)
Prior art keywords
flow
liquid hydrocarbons
mixture
passage
cavitation
Prior art date
Application number
PCT/US1996/002612
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English (en)
Inventor
Oleg Vyacheslavovich Kozyuk
Alexander Anatolievich Litvinenko
Boris Kirillovich Kravets
Original Assignee
Oleg Vyacheslavovich Kozyuk
Litvinenko Alexander Anatoliev
Boris Kirillovich Kravets
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Publication date
Application filed by Oleg Vyacheslavovich Kozyuk, Litvinenko Alexander Anatoliev, Boris Kirillovich Kravets filed Critical Oleg Vyacheslavovich Kozyuk
Priority to AU49968/96A priority Critical patent/AU4996896A/en
Priority to PCT/US1996/002612 priority patent/WO1997030956A1/fr
Publication of WO1997030956A1 publication Critical patent/WO1997030956A1/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/008—Processes for carrying out reactions under cavitation conditions
    • 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
    • B01F23/41—Emulsifying
    • B01F23/4105—Methods of emulsifying
    • 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
    • B01F25/40—Static mixers
    • B01F25/42—Static mixers in which the mixing is affected by moving the components jointly in changing directions, e.g. in tubes provided with baffles or obstructions
    • 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
    • B01F25/40—Static mixers
    • B01F25/42—Static mixers in which the mixing is affected by moving the components jointly in changing directions, e.g. in tubes provided with baffles or obstructions
    • B01F25/43—Mixing tubes, e.g. wherein the material is moved in a radial or partly reversed direction
    • B01F25/433—Mixing tubes wherein the shape of the tube influences the mixing, e.g. mixing tubes with varying cross-section or provided with inwardly extending profiles
    • 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
    • B01F25/40—Static mixers
    • B01F25/42—Static mixers in which the mixing is affected by moving the components jointly in changing directions, e.g. in tubes provided with baffles or obstructions
    • B01F25/43—Mixing tubes, e.g. wherein the material is moved in a radial or partly reversed direction
    • B01F25/433—Mixing tubes wherein the shape of the tube influences the mixing, e.g. mixing tubes with varying cross-section or provided with inwardly extending profiles
    • B01F25/4335—Mixers with a converging-diverging cross-section
    • 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
    • B01F25/40—Static mixers
    • B01F25/42—Static mixers in which the mixing is affected by moving the components jointly in changing directions, e.g. in tubes provided with baffles or obstructions
    • B01F25/43—Mixing tubes, e.g. wherein the material is moved in a radial or partly reversed direction
    • B01F25/434—Mixing tubes comprising cylindrical or conical inserts provided with grooves or protrusions
    • 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
    • B01F25/40—Static mixers
    • B01F25/44—Mixers in which the components are pressed through slits
    • B01F25/441—Mixers in which the components are pressed through slits characterised by the configuration of the surfaces forming the slits
    • B01F25/4413—Mixers in which the components are pressed through slits characterised by the configuration of the surfaces forming the slits the slits being formed between opposed conical or cylindrical surfaces
    • 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
    • B01F25/40—Static mixers
    • B01F25/44—Mixers in which the components are pressed through slits
    • B01F25/442—Mixers in which the components are pressed through slits characterised by the relative position of the surfaces during operation
    • B01F25/4421—Mixers in which the components are pressed through slits characterised by the relative position of the surfaces during operation the surfaces being maintained in a fixed position, spaced from each other, therefore maintaining the slit always open
    • 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
    • B01F25/40—Static mixers
    • B01F25/45—Mixers in which the materials to be mixed are pressed together through orifices or interstitial spaces, e.g. between beads
    • 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
    • B01F25/40—Static mixers
    • B01F25/45—Mixers in which the materials to be mixed are pressed together through orifices or interstitial spaces, e.g. between beads
    • B01F25/452—Mixers in which the materials to be mixed are pressed together through orifices or interstitial spaces, e.g. between beads characterised by elements provided with orifices or interstitial spaces
    • B01F25/4521—Mixers in which the materials to be mixed are pressed together through orifices or interstitial spaces, e.g. between beads characterised by elements provided with orifices or interstitial spaces the components being pressed through orifices in elements, e.g. flat plates or cylinders, which obstruct the whole diameter of the tube
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2415—Tubular reactors
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/22—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
    • C07C5/373—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen with simultaneous isomerisation
    • C07C5/393—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen with simultaneous isomerisation with cyclisation to an aromatic six-membered ring, e.g. dehydrogenation of n-hexane to benzene
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00162—Controlling or regulating processes controlling the pressure
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00186—Controlling or regulating processes controlling the composition of the reactive mixture

Definitions

  • the present invention relates to a method that makes use of the effects of cavitation for changing the qualitative and quantitative composition of a mixture of liquid hydrocarbons.
  • the method can find application in oil processing, petroleum chemistry, and organic synthesis chemistry for producing a variety of fuels, man-made fibers, synthetic alcohols, detergents, rubber-like materials, and plastics.
  • Oil is essentially a complex composition of closely boiling hydrocarbons and high- molecular hydrocarbon compounds. Oil is the main source for producing all kinds of liquid fuels, such as, gasoline, kerosene, diesel and boiler fuel oil, as well as liquified gases and raw stock for chemical production processes.
  • liquid fuels such as, gasoline, kerosene, diesel and boiler fuel oil, as well as liquified gases and raw stock for chemical production processes.
  • Oil processing is carried out with the use of diverse production techniques initiating the chemical transformation of hydrocarbons, which results in changing the qualitative and quantitative composition of a mixture of liquid hydrocarbons.
  • the catalytic cracking process makes use of alumosilicate catalysts based on zeolites and occurs at a temperature range of 450-550°C and at a pressure range of 0.1-0.3 MPa.
  • the catalytic cracking process is used for producing motor fuels and raw stock for petrochemistry.
  • Catalytic reforming is used extensively for increasing the anti-knock properties of gasoline and producing aromatic hydrocarbons (benzene, toluene, xylene).
  • the process is carried out at a temperature range of 480-520°C and at a pressure range of 1.2-4.0 MPa in the presence of hydrogen and a catalyst.
  • hydrocracking aimed at producing light oils (gasoline, kerosene, diesel fuel). Hydrocracking is conducted at a temperature range of 370-450°C and at a pressure range of 15-20 MPa in the presence of bifunctional catalysts.
  • the foregoing objective is accomplished due to a method for changing the qualitative and quantitative composition of a mixture of liquid hydrocarbons, according to the invention, which comprises: feeding a hydrodynamic flow of liquid hydrocarbons through a flow-through duct or passage or channel provided with a baffle body placed therein, which establishes a local constriction of the hydrodynamic flow of liquid hydrocarbons; establishing the local constriction of the hydrodynamic flow in at least one portion of the flow-through passage having a cross-sectional profile design which is so selected in order to maintain a prescribed velocity of the hydrodynamic flow on the portion of the flow-through passage that provides for the initiation of a cavitation field featuring the degree of cavitation of not less than one and located past the baffle body; treating the hydrodynamic flow of a mixture of liquid hydrocarbons in the hydrodynamic cavitation field that initiates chemical transformations of liquid hydrocarbons resulting in a qualitative and quantitative change in the composition of the mixture of liquid hydrocarbons.
  • a method, according to the invention exploits the use of the effects of hydrodynamic cavitation. It has been found that, when a mixture of liquid hydrocarbons is exposed to a cavitation field, the cavitation field initiates chemical transformations of the hydrocarbons, that is, chemical reactions such as decomposition, isomerization, cyclization, and synthesis which provide for a change in the qualitative and quantitative composition of a mixture of liquid hydrocarbons without the use of catalysts.
  • the present invention provides a method for changing the qualitative and quantitative composition of a mixture of liquid hydrocarbons, which allows chemical reactions such as decomposition, isomerization, cyclization, and synthesis of hydrocarbons to be performed without the use of catalysts and hydrogen, under normal conditions, that is, at room temperature and atmospheric pressure, and, at elevated temperature and pressure levels.
  • This enables to considerably simplify the implementation of these technological processes, wherein the method is realized, and, to then reduce their energy consumption rate and specific amount of metal used, thereby rendering these processes to be conducted at lower costs.
  • the foregoing objective is possible due to a method for changing the qualitative and quantitative composition of a mixture of liquid hydrocarbons, comprising the initiation of chemical reactions such as decomposition, isomerization, cyclization, and synthesis, according to the invention, and, the initiation of chemical reactions is carried out by feeding the hydrodynamic flow of a mixture of liquid hydrocarbons through a flow-through passage having a portion that ensures the local constriction of the hydrodynamic flow, and by establishing a hydrodynamic cavitation field of collapsing air bubbles in the hydrodynamic flow that acts on the mixture of hydrocarbons.
  • Such a method enables to carry out a mixture of liquid hydrocarbons, thereby changing their qualitative and quantitative composition without the use of catalysts.
  • the occurrence of hydrodynamic cavitation consists of the formation of filled vapor to gas zones in the fluid flow or the boundary of the baffle body as a result of a localized decrease in pressure.
  • the process is carried out in the following manner:
  • the flow of processable hydrocarbons, at a velocity of 1-3 m sec. is fed into the continuous flow channel.
  • the velocity accelerates to 10-50 m/sec.
  • the static pressure in the flow decreases to 1-20 kPa.
  • the pressure of the vapor-hydrocarbons inside the cavitation bubbles is 1-20 kPa.
  • the pressure in the flow increases.
  • the increase in the static pressure drives the instantaneous adiabatic collapsing of the cavitation bubbles.
  • the bubble collapse time duration is 10 "6 - 10 "8 sec. This is dependent on the size of the bubbles and the static pressure of the flow.
  • the velocities reached during the collapse of "vacuum” cavitation bubbles are in the range of magnitude of 300-1000 m/sec.
  • elevated temperatures in the bubbles are realized with a velocity of 10 '10 - 10 "12 K/sec. Under this vaporous-gaseous mixture of hydrocarbons found inside the bubbles, the hydrocarbons mixture reaches a temperature range of 3000-15,000° K and is present under a pressure range of 100-1500 MPa.
  • each collapsing cavitation bubble presents itself as a super-position of two processes of "micro-cracking" ⁇ a gaseous phase inside the bubble and a liquous phase in the surrounding liquid bubble.
  • Each cavitation bubble serves as an "autonomous" system, where chemical action transformations of hydrocarbons are realized.
  • the concentration of cavitation bubbles in the flow formulates a magnitude in the order of l 8 - 1TM l/m J , that allows to process up to 10% of the hydrocarbons frorr, the general flow, which pass through the cavitation field.
  • the collapsing of the cavitation bubbles is accompanied by some electrical effects, luminescence, and generation of broad-spectrum shock waves and acoustic vibrations.
  • the collapsing bubbles act as a kind of catalyst that initiates the progress of chemical reactions.
  • the most important parameters determining the intensity of the energy effect of the hydrodynamic cavitation field are the degree of cavitation and the processing ratio.
  • the degree of cavitation is determined by the ratio between the characteristic lengthwise dimension of the cavitation field and the cross-sectional dimensions of the baffle body on the portion of a local flow constriction; and, the processing ratio is determined by the number of the cavitation effects zone on the flow of the components under processing.
  • the hydrodynamic flow velocity on the locally constricted portion of the flow-through passage to a great extent influences the lengthwise dimension of the cavitation field and its intensity, and is so selected that the degree of cavitation should be equal to at least one. With the degree of cavitation having such a value, energy conditions arise for an efficient action on a mixture of liquid hydrocarbons at lower temperatures, which in turn may render the process much less expensive and much less complicated.
  • the method enables to control the cavitation field intensity due to the appropriately arranged portions of the local flow constriction which depend on the shape of the baffle body.
  • the hydrodynamic flow velocity on the local flow constriction portions is influenced by the flow restriction coefficient which is the ratio between the maximum cross-sectional area of the baffle body and the area of the flow-through passage at the place of the baffle body location.
  • the hydrodynamic flow of a mixture of liquid hydrocarbons be fed through the flow-through passage with the coefficient of restriction of the hydrodynamic flow to be not less than 0.1.
  • This parameter also allows for adjusting the intensity of the cavitation field so established, that is, the degree of changing the qualitative and quantitative composition of the mixture of liquid hydrocarbons under processing.
  • a change in the qualitative composition of a mixture of liquid hydrocarbons is also influenced by the temperature of the mixture under processing effective on the portions of the local flow constriction. It is necessary to maintain the flow temperature within a range of 10 and 500°C. It is within this temperature range that the viscosity of hydrocarbons required for the hydrodynamic flow is maintained and any possibility for the formation of a gaseous phase in the mixture of liquid hydrocarbons is prevented.
  • Figure 1 is a schematic of a longitudinal-section view of a device for carrying out the herein - proposed method into effect, featuring a cone-shaped baffle body;
  • Figure 2 is a longitudinal-section view of another embodiment of a device for carrying out the herein - proposed method into effect, featuring a flow-throttling baffle body shaped as the Venturi tube;
  • Figure 3 A - 3D is a fragmentary longitudinal-section view of a flow-through passage of the device of Figure 1, featuring the diversely shaped baffle body;
  • Figure 4A - 4D is a fragmentary longitudinal-section view of a flow-through passage of the device of Figure 2, featuring a flow-throttling diversely shaped baffle body.
  • the method consists of feeding a hydrodynamic flow of a mixture of liquid hydrocarbons via a flow-through passage, wherein a baffle body is placed, with the baffle body having such a shape and being so arranged that the flow of liquid hydrocarbons is constricted on at least one portion thereof.
  • the cross-sectional profile design of the flow constriction area is selected so as to maintain such a flow velocity in a local constriction is increased while the pressure is decreased with the result that the cavitation cavities or voids are formed in the flow past the baffle body, which on having been disintegrated, form cavitation bubbles which determine the structure of the cavitation field.
  • the cavitation bubbles enter the increased pressure zone resulting from a reduced flow velocity, and collapse.
  • the resulting cavitation effects exert a physio-chemical effect on the mixture of liquid hydrocarbons, thus initiating chemical reactions such as decomposition, isomerization, cyclization, and synthesis.
  • the degree of cavitation of the cavitation field must not be below one unit. It is in only such a case that the occurring cavitation effects will provide for a change in the qualitative and quantitative composition of a mixture of liquid hydrocarbons.
  • a device schematically presented in Figures 1 and 2 is used for carrying into effect the method, according to the invention.
  • Figure 1 presents the device, comprising a housing 1 having an inlet opening 2 and an outlet opening 3, and arranged one after another and connecting to one another a convergent nozzle 4, a flow-through passage 5, and a divergent nozzle 6.
  • the flow-through passage 5 accommodates a frustum-conical baffle body 7 which establishes a local flow constriction 8 having an annular cross-sectional profile design.
  • the baffle body 7 is held to a rod 9 coaxially with the flow-through passage 5.
  • the hydrodynamic flow of a mixture of liquid hydrocarbons moves along the arrow A through the inlet opening 2 and the convergent nozzle 4 to enter into the flow-through passage 5 and moves against the baffle body 7. Further along, the flow passes through the annular local constriction 8.
  • a cavity is formed past the baffle body which, after having been separated, the cavity is disintegrated in the flow into a mass of cavitation bubbles having different characteristic dimensions.
  • the resulting cavitation field having a vortex structure, makes it possible for processing liquid hydrocarbons throughout the volume of the flow-through passage 5.
  • the hydrodynamic flow moves the bubbles to the increased pressure zone, where their coordinated collapsing occurs, accompanied by high local pressure (up to 1500 MPa) and temperature (up to 15,000°K), as well as by other physio-chemical effects which initiate the progress of chemical reactions in the mixture of liquid hydrocarbons that change the composition of the mixture.
  • the qualitatively and quantitatively changed mixture of hydrocarbons flow is then discharged form the device through the divergent nozzle 6 and the outlet opening 3.
  • the qualitative and quantitative composition of hydrocarbons was then evaluated by the gas chromatography technique with the aid of a Hewlett-Packard Model A - 5890 gas chromatograph equipment.
  • FIG. 2 presents an alternative embodiment of the device for carrying into effect the herein - proposed method, according to the invention, characterized in that the baffle body 7 is shaped as the Venturi tube and fitted on the wall of the flow-through passage 5. The local flow constriction 8 is established at the center of the flow-through passage 5.
  • the hydrodynamic flow of liquid hydrocarbons flowing along the direction of the arrow A arrives at the flow-through passage 5 and is throttled while passing through the annular local constriction 8.
  • the resultant hydrodynamic field is featured by its high intensity which is accounted for by the high flow velocity and pressure gradient.
  • the stationary-type cavitation voids are relatively oblong-shaped, and, upon their distegration, form rather large-sized cavitation bubbles which, when collapsing, possess high energy potential. This cavitation field provides for a considerable change in the qualitative and quantitative composition of a mixture of liquid hydrocarbons.
  • the baffle body 7 placed in the flow-through passage 5 is shaped as a sphere, ellipsoid, disk, impeller as shown in Figures 3A-3D, respectively.
  • the flow is throttled at the local flow constriction locations 8, which results in a local flow zone featuring high transverse velocity gradients.
  • the baffle bodies 7 ( Figures 4A, B, D) establish the constriction locations 8 at the center of the flow-through passage 5, while the disk-shaped baffle body 7 ( Figure 4B) establishes the constrictions arranged parallel to one another in the same cross-section of the passage 5.
  • the flow of a mixture of liquid hydrocarbons gets separated, which promotes the development of a cavitation field having high energy potential due to the formation of the lower pressure zone within the local areas of high transverse velocity gradients around the sink flow streams.
  • the degree of chemical transformations of hydrocarbons is very high.
  • the hydrodynamic flow of a mixture of hydrocarbons is fed to the device by a pump.
  • the flow may be fed through the device either once or repeatedly according to recycle pattern.
  • the hydrodynamic flow of a mixture of liquid hydrocarbons having a temperature of 12 °C is fed at a rate of 6.90 m/sec. through the inlet opening 2 to the device as shown in Figure 1.
  • a static pressure at the inlet of the flow-through passage 5 is 0.226 MPa, and, at the outlet, 0.058 MPa.
  • the flow restriction coefficient is 0.4.
  • the flow of hydrocarbons while passing along the flow-through passage 5 and flowing about the cone-shaped baffle body 7, is subjected to the cavitation effect which initiates the progress of chemical reactions of decomposition, isomerization, cyclization, and, synthesis, resulting in a change in the qualitative and quantitative composition of the mixture of liquid hydrocarbons.
  • the degree of cavitation is maintained at 2.3.
  • the hydrodynamic flow of a mixture of liquid hydrocarbons having a temperature of 21 °C is fed at a rate of 7.10 m/sec. through the inlet opening 2 to the devices as shown in Figure 1 having the baffle body 7 as shown in Figure 3C.
  • the static pressure at the inlet of the flow- through passage 5 is 0.265 MPa, and, at the outlet of the passage 5, 0.105 MPa, the flow restriction coefficient being 0.45.
  • the flow of hydrocarbons while passing along the flow-through passage 5 and flowing about the disk-shaped baffle body 7, is subjected to the cavitation effect which initiates the progress of chemical reactions of decomposition, isomerization, cyclization, and, synthesis, resulting in a change in the qualitative and quantitative composition of the mixture of liquid hydrocarbons.
  • the degree of cavitation is maintained at 2.50.
  • the hydrodynamic flow of a mixture of liquid hydrocarbons having a temperature of 25.4°C is fed at a rate of 7.35 m/sec. through the inlet opening 2 to the device as shown in Figure 2.
  • the static pressure at the inlet of the flow-through passage 5 is 0.258 MPa, and, at the outlet of the passage 5, 0.118 MPa, the flow restriction coefficient being 0.50.
  • the flow of hydrocarbons, while passing along the flow-through passage 5 and through the annular flow construction 8 established by the baffle body 7 shaped as the Venturi tube, is subjected to the cavitation effect which initiates the progress of chemical reactions of decomposition, isomerization, cyclization, and, synthesis, resulting in a change in the qualitative and quantitative composition of a mixture of liquid hydrocarbons.
  • the degree of cavitation is maintained at 2.55.
  • the hydrodynamic flow of a mixture of liquid hydrocarbons having a temperature of 48.6°C is fed at a rate of 7.66 m/sec. through the inlet opening 2 to the device as shown in Figure 1 provided with the baffle body as shown in Figure 3D.
  • the static pressure at the inlet of the flow-through passage 5 is 0.321 MPa, and, at the outlet of the passage 5, 0.135 MPa, the flow restriction coefficient being 0.52, and the degree of cavitation being maintained at 3.1.
  • the flow of hydrocarbons while passing along the flow-through passage 5 and flowing about the impeller-shaped baffle body 7, is subjected to the cavitation effect which initiates the progress of chemical reactions of decomposition, isomerization, cyclization, and, synthesis, resulting in a change in the qualitative and quantitative composition of the mixture of liquid hydrocarbons.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Dispersion Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

Selon le procédé proposé, on fait passer un flux hydrodynamique d'hydrocarbures liquides par un conduit de circulation directe comportant un corps de déflecteur qui assure la constriction locale du flux; on établit la constriction locale du flux sur au moins une partie du conduit dont la section transversale est sélectionnée de façon à maintenir une certaine vitesse du flux sur la partie du conduit qui favorise au-delà du corps du déflecteur le développement d'un champ de cavitation hydrodynamique ayant un degré de cavitation d'au moins un; on traite le flux d'un mélange d'hydrocarbures liquides dans le champ de cavitation hydrodynamique de façon à amorcer des transformations chimiques des hydrocarbures liquides aboutissant à une modification de la composition qualitative et quantitative du mélange desdits hydrocarbures.
PCT/US1996/002612 1996-02-20 1996-02-20 Procede pour modifier la composition qualitative et quantitative d'un melange d'hydrocarbures liquides WO1997030956A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
AU49968/96A AU4996896A (en) 1996-02-20 1996-02-20 Method for changing the qualitative and quantitative composition of a mixture of liquid hydrocarbons
PCT/US1996/002612 WO1997030956A1 (fr) 1996-02-20 1996-02-20 Procede pour modifier la composition qualitative et quantitative d'un melange d'hydrocarbures liquides

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/US1996/002612 WO1997030956A1 (fr) 1996-02-20 1996-02-20 Procede pour modifier la composition qualitative et quantitative d'un melange d'hydrocarbures liquides

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WO1997030956A1 true WO1997030956A1 (fr) 1997-08-28

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WO (1) WO1997030956A1 (fr)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1998050146A1 (fr) * 1997-05-06 1998-11-12 Oleg Vyacheslavovich Kozyuk Procede et appareil permettant d'effectuer des reactions et processus sonochimiques utilisant la cavitation hydrodynamique
WO1999039813A1 (fr) * 1998-02-06 1999-08-12 Oleg Vyacheslavovich Kozyuk Procede et appareil pour l'obtention de systemes de dispersion liquide
WO2011012186A3 (fr) * 2009-07-28 2011-04-28 Technische Universität München Réacteur de cavitation
EP1294474B2 (fr) † 2000-05-14 2013-01-23 Jörg Lehmann Procede et dispositif de traitement physicochimique de milieux fluides
US9126176B2 (en) 2012-05-11 2015-09-08 Caisson Technology Group LLC Bubble implosion reactor cavitation device, subassembly, and methods for utilizing the same
WO2016145507A1 (fr) * 2015-03-13 2016-09-22 MechCracker Corporation Raffinage d'hydrocarbures par cavitation

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US3988329A (en) * 1973-12-21 1976-10-26 Hans Heinrich Auer Process for continuous catalytic hydrogenation
US5030789A (en) * 1988-06-28 1991-07-09 Institut Francais Du Petrole Catalytic method for the dimerization, codimerization or oligomerization of olefins with the use of an autogenous thermoregulation fluid
US5264645A (en) * 1991-03-07 1993-11-23 Institut Francais Du Petrole Process and apparatus for the catalytic conversion of a charge containing an oxygen compound comprising the quenching and simultaneous separation of the products formed and the catalyst

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3988329A (en) * 1973-12-21 1976-10-26 Hans Heinrich Auer Process for continuous catalytic hydrogenation
US5030789A (en) * 1988-06-28 1991-07-09 Institut Francais Du Petrole Catalytic method for the dimerization, codimerization or oligomerization of olefins with the use of an autogenous thermoregulation fluid
US5264645A (en) * 1991-03-07 1993-11-23 Institut Francais Du Petrole Process and apparatus for the catalytic conversion of a charge containing an oxygen compound comprising the quenching and simultaneous separation of the products formed and the catalyst

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1998050146A1 (fr) * 1997-05-06 1998-11-12 Oleg Vyacheslavovich Kozyuk Procede et appareil permettant d'effectuer des reactions et processus sonochimiques utilisant la cavitation hydrodynamique
US5937906A (en) * 1997-05-06 1999-08-17 Kozyuk; Oleg V. Method and apparatus for conducting sonochemical reactions and processes using hydrodynamic cavitation
US6035897A (en) * 1997-05-06 2000-03-14 Kozyuk; Oleg Vyacheslavovich Method and apparatus for conducting sonochemical reactions and processes using hydrodynamic cavitation
WO1999039813A1 (fr) * 1998-02-06 1999-08-12 Oleg Vyacheslavovich Kozyuk Procede et appareil pour l'obtention de systemes de dispersion liquide
EP1294474B2 (fr) † 2000-05-14 2013-01-23 Jörg Lehmann Procede et dispositif de traitement physicochimique de milieux fluides
WO2011012186A3 (fr) * 2009-07-28 2011-04-28 Technische Universität München Réacteur de cavitation
US9126176B2 (en) 2012-05-11 2015-09-08 Caisson Technology Group LLC Bubble implosion reactor cavitation device, subassembly, and methods for utilizing the same
US9682356B2 (en) 2012-05-11 2017-06-20 Kcs678 Llc Bubble implosion reactor cavitation device, subassembly, and methods for utilizing the same
WO2016145507A1 (fr) * 2015-03-13 2016-09-22 MechCracker Corporation Raffinage d'hydrocarbures par cavitation

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