EP1021236A1 - Methode permettant d'effectuer des reactions chimiques - Google Patents

Methode permettant d'effectuer des reactions chimiques

Info

Publication number
EP1021236A1
EP1021236A1 EP98942906A EP98942906A EP1021236A1 EP 1021236 A1 EP1021236 A1 EP 1021236A1 EP 98942906 A EP98942906 A EP 98942906A EP 98942906 A EP98942906 A EP 98942906A EP 1021236 A1 EP1021236 A1 EP 1021236A1
Authority
EP
European Patent Office
Prior art keywords
fluid
liquid
fluids
tube
supplied
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Withdrawn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
EP98942906A
Other languages
German (de)
English (en)
Inventor
Bernt Helge Torkildsen
Martin Sigmundstad
Harald Linga
Finn Patrick Nilsen
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Equinor ASA
Original Assignee
Den Norske Stats Oljeselskap AS
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Priority claimed from GBGB9719668.7A external-priority patent/GB9719668D0/en
Application filed by Den Norske Stats Oljeselskap AS filed Critical Den Norske Stats Oljeselskap AS
Publication of EP1021236A1 publication Critical patent/EP1021236A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • 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
    • B01J19/26—Nozzle-type reactors, i.e. the distribution of the initial reactants within the reactor is effected by their introduction or injection through nozzles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1475—Removing carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1493—Selection of liquid materials for use as absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • 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
    • B01F25/30—Injector mixers
    • B01F25/31—Injector mixers in conduits or tubes through which the main component flows
    • B01F25/312—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof
    • B01F25/3124—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof characterised by the place of introduction of the main flow
    • B01F25/31241—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof characterised by the place of introduction of the main flow the main flow being injected in the circumferential area of the venturi, creating an aspiration in the central part of the conduit
    • 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
    • B01J10/00—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor
    • 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
    • B01J10/00—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor
    • B01J10/002—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor carried out in foam, aerosol or bubbles
    • 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
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
    • 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
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
    • B01J2219/00103—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor in a heat exchanger separate from the reactor
    • 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
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00105—Controlling the temperature by indirect heating or cooling employing heat exchange fluids part or all of the reactants being heated or cooled outside the reactor while recycling
    • B01J2219/0011—Controlling the temperature by indirect heating or cooling employing heat exchange fluids part or all of the reactants being heated or cooled outside the reactor while recycling involving reactant liquids
    • 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
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00159—Controlling the temperature controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
    • 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
    • B01J2219/00164—Controlling or regulating processes controlling the flow
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/582—Recycling of unreacted starting or intermediate materials

Definitions

  • the present invention relates to a method for effecting a chemical reaction between components in two fluids. It is particularly concerned with a method in which the two fluids are of different phases.
  • a method of for effecting a chemical reaction between at least one component in a first fluid and at least one component in a second fluid of a different phase comprising: subjecting the two fluids to turbulent mixing, and allowing the selected components to react.
  • fluids in different phases are any two fluids which are immiscible or are only partly miscible.
  • Examples of such systems include gas/liquid, oil/water, fluidised solid/gas etc.
  • the invention also extends to the apparatus for carrying out this method.
  • the turbulent mixing is very intense and results in extremely efficient contact between the two fluids.
  • the mixing regime is preferably turbulent shear layer mixing.
  • the efficient mixing means that reaction can take place very rapidly and in a relatively small reactor volume compared to that required in conventional columns. This in turn means that any liquid duty in the equipment is dramatically reduced resulting in a consequential reduction in the size of any downstream regeneration section.
  • the mixing system used is simple and inexpensive compared to prior art systems, leading to reduced costs. Finally, an efficiency of approaching 100% can be achieved for certain applications.
  • the present invention has the advantage that any adiabatic expansion of a gas passing through a contactor reduces the contact temperature between a gas and a liquid, thereby increasing the quantity of gas which can be taken up by the liquid. Additionally, in systems where the heat of condensation and heat of solution of a gas in a liquid is significant, and normally causes the liquid temperature to rise and thus the absorption capacity of the liquid to fall, the adiabatic cooling can offset this undesirable effect.
  • the present method is also suitable for chemisorption reactions.
  • the reactions are usually exothermic, and the heat of reaction causes the liquid temperature to rise. This reduces the adsorption capacity of the liquid phase.
  • the adiabatic cooling of the gas can offset the heating effect of the reaction, thereby maintaining the adsorption capacity of the liquid. Careful design of the apparatus may eliminate the need for external cooling which is required in many chemisorption processes.
  • the short contact time needed for reaction means that short contact lines can be achieved with high interphase transport fluxes. This property makes the apparatus of this invention suitable for treating heat sensitive or chemically unstable fluids or fluid mixtures.
  • the first fluid is a gas mixture and the second fluid is in the liquid phase.
  • the first fluid is a liquid mixture or a liquid solution and the second fluid in the liquid phase.
  • the first fluid is a liquid mixture or a liquid solution and the second fluid is in the gas phase.
  • the method is carried out as a continuous process with the two fluids flowing co-currently.
  • the co-current flow eliminates any problems that might be associated with foaming and flooding, since separation can easily be effected downstream of the mixer.
  • the turbulent shear layer mixing may be achieved by any convenient means.
  • the mixing is conducted in a turbulent contactor including a first fluid inlet, a second fluid inlet, an outlet leading to a venturi passage, and a tube extending from the outlet back upstream, the tube being perforated and or being spaced from the periphery of the outlet.
  • the tube is located in a vessel, the vessel including the first fluid inlet, the second fluid inlet and the outlet.
  • the first fluid is supplied to the tube, optionally directly, and the second fluid is supplied to the vessel, and so the first fluid draws the second fluid into the venturi and the two fluids are mixed.
  • the first fluid is supplied to the vessel and the second fluid is supplied to the tube, optionally directly, whereby the first fluid is drawn into the venturi by the second fluid and the two fluids are mixed.
  • one of the fluids is in the gas phase and one of the fluids is in the liquid phase, and both fluids are supplied to the vessel, the liquid being supplied to a level above the level of the outlet, whereby the gas is forced out through the outlet via the tube, thereby drawing the liquid into the venturi so that the two phases are mixed.
  • One suitable contactor is a mixer supplied by Framo Engineering A/S and is described in EP-B-379319.
  • the contactor may be an ejector, such as a jet pump.
  • the invention is broadly applicable to any chemical reactions between components in two different fluid phases and is particularly applicable to any application where the reaction kinetics are rapid.
  • the invention therefore also extends to a method for effecting a chemical reaction between two or more components in different fluid phases which comprises: forming a homogeneous mixture of the fluid phases, the homogeneous mixture being formed by subjecting the fluid phases to turbulent mixing conditions, preferably turbulent shear layer mixing conditions, separating a first fluid phase and a second fluid phase; and optionally treating the relevant phase(s) to remove the reaction product(s).
  • the fluid mixture may be a mixture of gases or may be in the liquid phase.
  • the components to be reacted may be a finely divided solid disperse phase, a dissolved solid, a liquid or a gas.
  • the invention also extends to the apparatus for carrying out this method.
  • a method for effecting a chemical reaction between two or more components in different fluid phases which comprises: supplying the fluids to a mixer or turbulent contactor; subjecting the fluids to turbulent shear layer mixing in the contactor to form a homogeneous mixture; allowing the selected components to react; optionally cooling the homogeneous mixture; separating the cooled homogeneous mixture into separate phases; treating the separated phases to remove the reaction product(s); and, if appropriate, recycling either of the fluid phases containing unreacted reactants.
  • the separation of the homogeneous mixture into separate phases may take place in any suitable separator.
  • a gas-liquid mixture may be separated in a hydrocyclone.
  • any cooling and/or heating of either the reagents or products is achieved, at least in part, by mutual heat exchange.
  • the liquid is pumped to the contactor and thereby draws the gas mixture with it through the contactor.
  • the first fluid is a gas mixture at a high pressure
  • the second fluid is a liquid
  • the gas is conveyed to the contactor at a high pressure and thereby draws the liquid with it through the contactor.
  • the invention also extends to apparatus for carrying out such a method.
  • the contactor is a turbulent contactor as described above, or alternatively an ejector or a jet pump.
  • the invention may be considered to extend to the use of a turbulent contactor to effect a chemical reaction between at least one component in a first fluid phase and at least one component in a second fluid of a different phase.
  • reaction systems described are single operations, however it will be appreciated that multi-reactions may be performed. These may be carried out simultaneously or sequentially and may also be carried out in series or in parallel.
  • the present invention is applicable in wide variety of applications.
  • it can be used in petroleum and gas production in a number of ways - sweetening, removal of C0 2 , removal of NO x gases, stabilisation of liquid feedstocks and products, waste water treatment, in deodorising, removal of acid gas, removal of NH 3 etc.
  • It can also be used in wastewater treatment, in particular denitrification of wastewater and run off water from landfills.
  • the contactor may be used on vent lines to recover reactants from vent gas or as a tail gas scrubber to recover products or remove toxic/noxious compounds.
  • the contactor may be used to selectively recover reaction products from reactor discharge gases.
  • the contactor may be used to prepare emulsions, the device affording a method of control of emulsion form by pressure control in phase continuity drop size distribution.
  • this list is not to be regarded as exhaustive, but merely illustrative of the scope of use of the method of this invention.
  • Figure 1 is a flow diagram of the process for use when the first fluid is a gas under low pressure
  • Figure 2 is a flow diagram of the process for use when the first fluid is a gas under high pressure
  • Figure 3 a is a view of a turbulent contactor suitable for use in the method of this invention.
  • Figure 3b is a view of a contactor similar to that in Figure 3a, but with the tube connected to a fluid inlet;
  • Figure 4a is a variant of the contactor shown in Figure 3 a;
  • Figure 4b is a view of a contactor similar to that in Figure 4a, but with the tube connected to a fluid inlet;
  • Figure 5 is a view of a contactor similar to that shown in figure 3 a but with the perforated tube arranged so that all the fluid which passes through the outlet does so by way of the tube;
  • Figure 6 is a variant of the contactor shown in figure 5; and Figure 7 is a view of a jet pump which can be used as an alternative to the contactor.
  • a continuous process operation for a chemical reaction between a component in a gas phase and a second component in a liquid phase is shown in figure 1.
  • a liquid stream 1 including the second selected component is conducted by a pump 2 to a contactor 3 (though this could be an ejector) capable of inducing turbulent mixing.
  • a gas stream 4, including the first selected component is drawn into the contactor 3 by the low pressure generated in the venturi by the liquid stream after it has passed through the pump (stream la).
  • This arrangement provides an automatic means of self-regulation as the gas mixture to liquid ratio can be maintained for varying flow rates.
  • the liquid and the gas stream are in the form of a homogeneous mixture (stream 5) and the chemical reaction between the selected components may occur very rapidly.
  • the mixed two phase stream 5 may then be conveyed to a cooler 6 and on into a hydrocyclone 7 or other suitable separator device.
  • a gas stream 8, which may or may not contain a reaction product, may be taken off and the liquid stream 9, which may or may not contain a reaction product, may pass on to a regeneration system.
  • the reaction product(s) will be separated from the appropriate stream(s) by any suitable means, and any unreacted reagents may be recycled for reuse.
  • the reaction product is a liquid, this may be separated from the unreacted liquid phase by means of heating (10) and then condensing of the product stream (11) in a condenser (not shown).
  • the reaction product is a solid, the product may be removed by filtration.
  • cooler 6 and the heater 10 if they are present may be combined to form a heat exchange unit.
  • FIG. 2 An alternative system for a chemical reaction between two or more components, one or more in a high-pressure gas stream, and the rest in a liquid stream, is shown in figure 2.
  • a high-pressure gas stream 20 containing a first selected component is conveyed to a contactor 21 similar to that shown in figure 3a.
  • the high pressure of the gas draws a controlled amount of the liquid stream from the recycle stream 22 and from a reservoir 23 into the contactor 21.
  • the two phases are in the form of a homogeneous mixture (stream 24) and the chemical reaction between the selected components takes place.
  • the two-phase mixture (stream 24) may pass through a cooler 25 to a hydrocyclone unit 26 or other suitable separation device.
  • the gas stream is taken off in stream 27 and the liquid stream 28 may pass to a regeneration system.
  • the reaction product(s) may be solid, liquid or gas and will be separated from the appropriate stream using any suitable apparatus.
  • either or both of the gas and liquid streams containing unreacted reagents may be recycled.
  • a liquid product may be separated from the liquid stream 28 by means of heating 29 and then condensing the product stream 30.
  • the heater 29 and the cooler 25 if present may be combined to form a heat exchange unit.
  • the contactor used in both the above embodiments may be that shown in figure 3 a.
  • the turbulent contactor 100 comprises a vessel 101 having a first fluid inlet 102, a second fluid inlet 103 and an outlet 104 leading to a venturi passage 105.
  • the tube 106 may be open ended into the vessel 101 as shown in figure 3a, or it may be connected to the fluid inlet 103, as shown in figure 3b.
  • the first fluid e.g. a gas mixture
  • the second fluid e.g. a liquid
  • the second fluid e.g. a liquid
  • the first fluid e.g. a gas mixture
  • the second fluid e.g. a liquid
  • the first fluid e.g. a gas mixture
  • FIG 4a A fourth variant is shown in figure 4a.
  • This embodiment is similar to that shown in figure 3 a, but the contactor 110 is inverted and is suitable only for use with gas-liquid reactions. It comprises a vessel 111 with a liquid inlet 1 12, a gas inlet 113 and an outlet 114 leading to a venturi passage 115. There is a tube 116 (which may or may not be perforated) extending from the outlet 114 back into the vessel 111. The tube 116 may be connected directly to the gas inlet 113.
  • the liquid is forced up the tube 116 and the gas is drawn into the venturi passage 115 by the liquid and the two phases are mixed.
  • the gas may be drawn into the tube 116 through the perforations.
  • a fifth arrangement is shown in figure 4b.
  • This embodiment is similar to that shown in figure 4a, but the first fluid inlet 113 is connected to the tube 116 and is not open ended as in figure 4a.
  • the arrangement comprises a vessel 111 with a second fluid inlet 112, an outlet 114 leading to a venturi passage 115.
  • the fluid inlets 112 and 113 may be fed by gas as well as liquid.
  • the turbulent contactor 200 comprises a vessel 201 having a first fluid inlet 202, a second fluid inlet 203 and an outlet 204 leading to a venturi passage 205.
  • the perforated tube 206 is arranged such that there is no gap at the outlet 204 of the vessel 201 for the fluids to pass through. The result of this arrangement is that all the fluid exits the vessel 201 via the perforated tube 206.
  • the first fluid e.g. a gas mixture
  • the second fluid e.g.
  • a liquid is supplied to the tube 206 whereby the first fluid is drawn into the venturi by the second fluid and the two phases are mixed.
  • the second fluid e.g. a liquid
  • the first fluid e.g. a gas mixture
  • the second fluid and the first fluid e.g.
  • a gas mixture are supplied to the vessel 201, the second fluid being supplied to a level above the level of the outlet 204, whereby the first fluid is forced out through the outlet 204 via the tube 206, thereby drawing the second fluid into the venturi so that the two phases are mixed.
  • a fourth variant is shown in figure 6.
  • This embodiment is similar to that shown in figure 5, but the contactor 210 is inverted. It comprises a vessel 211 with a liquid inlet 212, a gas inlet 213 and an outlet 214 leading to a venturi passage 215.
  • the perforated tube 216 is arranged such that there is no gap at the outlet 214 of the vessel 211 for the gas mixture to pass through. All the fluids must pass through the perforated tube 216 to the venturi passage 215.
  • the liquid is forced up the tube 216 and the gas is drawn into the venturi passage 215 by the liquid and the two phases are mixed. Since the tube 216 is perforated, the gas is drawn into the tube 216 through the perforations.
  • FIG. 7 shows a jet pump 120 comprising a first fluid inlet 121 for the high-pressure fluid and a second fluid inlet 122 for the low-pressure fluid.
  • the high-pressure fluid draws the low-pressure fluid along the length of the jet pump 120 to the outlet 123.
  • the fluids are well mixed into a homogenised mixture in the region 124 at the outlet of the high- pressure inlet 121.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Dispersion Chemistry (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

L'invention concerne une méthode permettant d'effectuer une réaction chimique entre au moins un composant dans un premier fluide d'une phase et au moins un composant dans un second fluide d'une phase différente. Cette méthode consiste à soumettre les deux fluides à un mélange en régime turbulent et à faire réagir les composants sélectionnés.
EP98942906A 1997-09-15 1998-09-14 Methode permettant d'effectuer des reactions chimiques Withdrawn EP1021236A1 (fr)

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
GB9719668 1997-09-15
GBGB9719668.7A GB9719668D0 (en) 1997-09-15 1997-09-15 Acid gas separation
GBGB9800485.6A GB9800485D0 (en) 1997-09-15 1998-01-09 Fluid mass transfer system
GB9800485 1998-01-09
PCT/GB1998/002770 WO1999013965A1 (fr) 1997-09-15 1998-09-14 Methode permettant d'effectuer des reactions chimiques

Publications (1)

Publication Number Publication Date
EP1021236A1 true EP1021236A1 (fr) 2000-07-26

Family

ID=26312262

Family Applications (1)

Application Number Title Priority Date Filing Date
EP98942906A Withdrawn EP1021236A1 (fr) 1997-09-15 1998-09-14 Methode permettant d'effectuer des reactions chimiques

Country Status (5)

Country Link
EP (1) EP1021236A1 (fr)
AU (1) AU9087198A (fr)
CA (1) CA2303376A1 (fr)
NO (1) NO20001312L (fr)
WO (1) WO1999013965A1 (fr)

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4483826A (en) * 1980-08-12 1984-11-20 Phillips Petroleum Company Combination reaction vessel and aspirator-mixer
SE454142B (sv) * 1985-04-23 1988-04-11 Flaekt Ab Kontaktreaktor
US4744956A (en) * 1986-02-12 1988-05-17 Quantum Technologies, Inc. Continuous reaction of gases with liquids
EP0380817B1 (fr) * 1989-02-03 1993-01-13 Gerardus Louis Beusen Procédé et dispositif pour traiter ou mélanger des composants dans des courants gazeux ou liquides
GB8910372D0 (en) * 1989-05-05 1989-06-21 Framo Dev Ltd Multiphase process mixing and measuring system

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO9913965A1 *

Also Published As

Publication number Publication date
NO20001312L (no) 2000-05-12
NO20001312D0 (no) 2000-03-14
CA2303376A1 (fr) 1999-03-25
WO1999013965A1 (fr) 1999-03-25
AU9087198A (en) 1999-04-05

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