Classifications

• • 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
  • B01F25/313—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit
  • B01F25/3131—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit with additional mixing means other than injector mixers, e.g. screens, baffles or rotating elements
• • 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
  • B01F33/00—Other mixers; Mixing plants; Combinations of mixers
  • B01F33/80—Mixing plants; Combinations of mixers
  • B01F33/81—Combinations of similar mixers, e.g. with rotary stirring devices in two or more receptacles
• • 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
  • 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
  • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
  • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
  • B01F23/20—Mixing gases with liquids
  • B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
• • 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
• • 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

Definitions

• the present invention relates to fluid separation systems. It is particularly concerned with the selective removal of a component or components from a mixture of gases using liquid solvent, for example it is concerned with the absorption of acid gases such as C0 2 , N0 X , H 2 S, oxides of sulphur etc. from natural gas and from combustion gases .
• acid gases such as C0 2 , N0 X , H 2 S, oxides of sulphur etc.
• Conventional systems for the absorption of acid gases employ a liquid solvent; typical solvents include amines such as methyldiethanolamine (MDEA) , monoethanolamine (MEA) or diethanolamine (DEA) and mixtures of solvents. These solvents absorb C0 2 , N0 X , H 2 S and other acid gases.
• MDEA methyldiethanolamine
• MEA monoethanolamine
• DEA diethanolamine
• the solvent is contacted with the sour gas mixture (gas mixture including acid gases) in a column which may be a packed column, a plate column or a bubble-cap column, or a column with some other form of contact medium.
• a column which may be a packed column, a plate column or a bubble-cap column, or a column with some other form of contact medium.
• the gas and liquid streams flow countercurrently .
• a method of absorbing a selected gas component from a gas stream which comprises : bringing the gas stream into contact with a liquid including a solvent or a reagent for the selected gas component and subjecting the gas stream and liquid to turbulent mixing conditions in an ejector, thereby causing the gas component to be absorbed by the solvent or reagent .
• the invention also extends to the apparatus for carrying out this method.
• the turbulent mixing is very intense and results in extremely efficient gas liquid contact .
• the mixing regime is preferably turbulent shear layer mixing.
• the liquid entrained in the gas may be in the form of droplets for gas continuous fluid phase distribution.
• the efficient mixing means that absorption can take place very rapidly and in a relatively small amount of solvent compared to that required in conventional absorption columns. This in turn means that the 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.
• an efficiency of approaching 100% for the removal of acid gas can be achieved for certain applications.
• conventional absorbtion methods involve the evolution of heat which must then be removed from the system. While the method of the invention is capable of operation with a relatively low pressure drop across the mixing means, when greater pressure drop is employed, a cooling effect is achieved and this may render the need for additional cooling unnecessary.
• the absorption may be achieved by simply dissolving the gas or by way of a chemical reaction with the solvent .
• the ejector is a jet pump.
• the term "jet pump" is to be interpreted as an ejector further comprising a venturi passage.
• the method further includes the step of separating a gas phase and a liquid phase after the turbulent mixing.
• the liquid phase is subsequently treated to remove the absorbed gas component .
• the method is carried out as a continuous process with the gas mixture and solvent flowing co-currently.
• the co-current flow eliminates the problems associated with foaming, since separation can easily be effected downstream of the ejector.
• the turbulent mixing may be achieved by any convenient means, preferably an ejector, more preferably a jet pump.
• the gas stream is supplied to the nozzle in the ejector, whereby the liquid is drawn downstream by the gas stream and the two phases are mixed.
• the liquid is supplied to the nozzle in the ejector, whereby the gas is drawn downstream by the liquid and the two phases are mixed.
• the invention is applicable to any absorption application where the reaction kinetics are rapid, for example the absorption of acid gas.
• the invention is also applicable to chemical reactions with fast reaction kinetics, where good mixing of the reactants is a requirement .
• a method for removing a single selected component from a mixture of gases extends to removing a plurality of gas components from a gas stream, either using a common solvent or reagent, or by respective solvents or reagents .
• the gas stream is a single gas which is absorbed.
• the gas stream and the liquid are formed into a homogeneous mixture by the ejector, the homogeneous mixture being cooled prior to separation into a gas phase and a liquid phase.
• this phase separation occurs in a hydrocyclone.
• the solvent or reagent in the liquid phase is subjected to a regeneration treatment to remove the absorbed selected gas component.
• the regenerated solvent-containing liquid phase is recycled to the ejector.
• the regeneration is carried out by heating and/or by flashing off the absorbed gas component in a flash tank.
• the post mixing cooling and the regenerative heating are achieved, at least in part by mutual heat exchange.
• the liquid is pumped to the ejector and thereby draws the gas stream with it through the ejector.
• the gas stream is at high pressures, it is conveyed to the ejector at a high pressure and thereby draws the liquid with it through the ejector.
• the invention also extends to apparatus for carrying out such a method, comprising: an ejector; a cooler for the fluid stream from the outlet of the ejector; a hydrocyclone arranged to separate the cooled fluid stream into a gas phase and a liquid stream; a regenerator arranged to treat the separated liquid stream; and a recycle line arranged to convey the regenerated liquid stream to the ejector.
• the apparatus may include a pump arranged to supply liquid to the ejector.
• the regenerator is a heater and/or a flash tank.
• the ejector is a jet pump.
• the invention may be considered to extend to the use of an ejector for absorbing a selected gas component from a gas stream by bringing the gas stream into contact with a liquid including a solvent or a reagent for the selected gas component, thereby causing the gas component to be absorbed by the solvent or reagent .
• the ejector is a jet pump.
• separation/absorption/reaction systems described are single operations, however it will be appreciated that multi separation/absorption/reactions may be performed. These may be carried out simultaneously or sequentially and may also be carried out in series or in parallel.
• the improved efficiency possible for the removal of, for example, acid gases makes the present invention particularly valuable as awareness is increased of the potential damage to the environment that can be caused by acid gases in effluents such as combustion gas.
• the small size of the apparatus compared to conventional absorption columns render the invention especially applicable to use in marine applications, such as on board shuttle tankers.
• Figure 1 is a flow diagram of the process for use when the gas is under low pressure
• Figure 2 is a flow diagram of the process for use when the gas is under high pressure
• Figure 3 is a view of an ejector which is preferably used in this invention to generate turbulent mixing conditions
• Figure 4 is a block diagram of the apparatus as used in the batch test procedure for a mixture of N 2 and C0 2 as the test gas
• Figure 5 is a block diagram of the apparatus as used in the batch test procedure for exhaust gas as the test gas ;
• Figure 6 is a view of the contactor as used in the batch test procedure.
• the embodiments and experiments refer to a contactor, it will be appreciated that the method is applicable to ejectors, particularly jet pumps, since they generate similar homogeneous gas/liquid mixtures and turbulent mixing conditions.
• a continuous process operation for the removal of carbon dioxide (and other acid gases) from exhaust gas is shown in figure 1.
• the mixed two phase stream 5 is then conveyed to a cooler 6 and on into a hydrocyclone 7.
• the gas stream 8 is taken off and the liquid stream 9 passes on to a regeneration system. At this point in the circuit all the C0 2 is in the liquid phase (stream 9) and the gas stream 8 is free of C0 2 .
• the regeneration of the liquid solvent is achieved by boiling off the C0 2 in a heater 10.
• the C0 2 is taken off as a gas stream 11 and the liquid solvent is optionally passed through a flash tank (not shown) to remove any residual dissolved gas before being recycled into the feed stream 1.
• the liquid solvent in stream 1 is topped up from the reservoir 12 as necessary to maintain a regular flow rate around the system.
• cooler 6 and the heater 10 may be combined to form a heat exchange unit .
• FIG. 1 An alternative system for the removal of C0 2 from a high pressure gas stream is shown in figure 2.
• a high pressure gas stream 20 containing the C0 2 which is to be removed is conveyed to an ejector 21.
• the high pressure of the gas draws a controlled amount of liquid solvent, for example MEA, from the recycle stream 22 and, if necessary, from a reservoir 23 into the ejector 21.
• liquid solvent for example MEA
• the two phases are in the form of a homogeneous mixture (stream 24) and the mass transfer of the C0 2 from the gas phase to the liquid solvent takes place.
• the residence time may be as little as 0.1 seconds since, for example, the reaction kinetics for the absorption of C0 2 by MEA are very rapid, although this residence time will vary with the solvent used and the gas to be transferred from the gas to the liquid.
• the two phase mixture (stream 24) passes through a cooler 25 to a hydrocyclone unit 26.
• the gas stream free of C0 2 is taken off in stream 27 and the remaining liquid stream 28 including the C0 2 is passed to a regeneration system.
• the liquid stream 28 is fed into a heater 29 to remove the C0 2 as a gas stream 30.
• This solvent (stream 22) is then drawn into the ejector 21 by the low pressure generated in the ejector. Any shortfall in the solvent liquid is made up by addition from the reservoir 23.
• the heater 29 and the cooler 25 can be combined to form a heat exchange unit.
• FIG. 3 shows an ejector 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 ejector 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.
• the gas stream is supplied to the nozzle 121, whereby the liquid is drawn downstream by the gas stream.
• the liquid is supplied to the nozzle 121, whereby the gas is drawn downstream by the liquid.
• the gas stream was a mixture of nitrogen (N 2 ) and C0 2 and the liquid solvent was a mixture of MEA and water.
• the reservoir pipe was kept under pressure using nitrogen gas.
• the contactor used was a Framo contactor generally as described in EP 379319 and shown in figure 6.
• the contactor injection pipe was adjusted to yield gas/liquid ratios in the range of about 3 to 5, depending upon the total flow rate.
• the method employed by the contactor is equally applicable to ejectors, particularly jet pumps, since they generate similar homogeneous gas/liquid mixtures and turbulent mixing conditions.
• FIG. 4 A schematic diagram for the first series of experiments is shown in figure 4.
• the contactor 51 is charged with an amount of the liquid solvent mixture from the reservoir 54 which is controlled by a valve 55.
• a gas source 50 of the experimental N 2 /C0 2 gas mixture is conveyed to the contactor 51 via a pipe 52 controlled by a valve 53.
• a 1 metre section of pipe 56 in which the mass transfer occurs. This section provides the residence time for the contacting materials.
• a set of 2 simultaneously acting fast closing valves 57 and 58 form a 1.5 metre analysis section 59 where the gas/liquid mixture can be captured, separated and sampled.
• At the top end of the analysis section there is a sampling point where a sample of the gas can be drawn off (not shown) .
• At the lower end of the section there is a further sampling point where a sample of the liquid can be drawn off (not shown) .
• the lower section of the sampling section is provided with means for cooling the liquid sample prior to its removal (not shown for clarity) .
• a further valve 60 separates the sampling section from a reservoir pipe 61 and is used to control the flow rate through the system.
• the reservoir pipe 61 is pressurised to a predetermined pressure by an independent nitrogen gas source 62 via a pipe 63 controlled by a valve 64. This pressure will be lower than that in the contactor to provide a pressure difference which will force the fluids through the system.
• the reservoir pipe 61 is inclined with respect to the horizontal to enable the liquid collected to be drained off via a pipe 65 controlled by a valve 66 to a measurement drum 67 which is used to determine the amount of liquid passing through the system on each run.
• the drum 67 has a drainage pipe 68 controlled by a valve 69.
• the contactor 51, pipe section 56 and analysis section 59 are filled with the suitable strength solvent solution.
• the simultaneously acting valves 57 and 58 are closed and valve 60 is set to a position carefully adjusted to yield the required mass flow rate through the system for the predetermined pressure difference between the mixer and the reservoir pipe.
• the contactor 51 is pressurised with the test gas of C0 2 -rich nitrogen to a pressure of 50 barg.
• the reservoir pipe 61 is pressurised with nitrogen to a predetermined value typically between 16 and 48 barg, providing a range of flow rates through the system.
• a sample of the test gas is taken to determine the level of C0 2 in the gas.
• the experiment commences with the activation of . the simultaneously operating valves 57 and 58.
• the liquid and the gaseous solution flow co-currently through the system to the reservoir pipe 61.
• the pressure in the mixer is maintained at 50 barg during the 10 second test run by manual supply of the test gas from a cylinder fitted with an accurate manometer. This makes it possible to record the amount of spent gas for each experiment.
• a liquid sample of the amine solution in the analysis section is taken from the lower sampling point .
• the liquid in the analysis section is cooled using nitrogen gas surrounding the pipe section 59.
• the liquid sample is analyzed using a titration technique specially developed for C0 2 .
• the liquid from the reservoir pipe 61 is released into the measurement drum 67 to measure the amount of liquid expended in the course of the run. The results of the tests are shown in Table 1 below:
• the only change to the apparatus from the first set of experiments is the addition of a small hydrocyclone at the top of the gas pipe to separate the gas and liquid after reaction. This means that there are no entrained droplets in the gas sample.
• the liquid solvent mixture is a 50% solution of MEA and the gas feed composition was 9.4 mol per cent C0 2 in nitrogen.
• the test run lasted for 10 seconds and the pressure in the contactor was maintained by manual supply of the test gas . The results are shown in table 2 below.
• the contactor 51, pipe section 56 and analysis section 59 are charged with an amount of the liquid solvent mixture from the reservoir 54.
• the exhaust gas comes from a diesel engine 75 and passes through the contactor with a minimum loss of temperature.
• the contactor 51 is not pressurised.
• the gas mixture is exhaust gas from a Yannmar 4TN84E 15 KVA water cooled diesel engine 75.
• a 30% load was placed on the diesel engine to increase the exhaust gas temperature and to obtain a higher level of C0 2 in the exhaust gas.
• An orifice plate 74 is provided in pipe 71 for continuous flow measurement of the exhaust gas .
• a sample of the exhaust gas is taken at point 72 to measure the C0 2 content in the exhaust gas.
• the valve 70 is closed, allowing exhaust gas to enter the contactor 51.
• the two valves 57 and 58 are opened simultaneously.
• the liquid and the gaseous solution flow co-currently through the system for 10 seconds into the reservoir pipe 61 before the valves 57 and 58 are closed simultaneously .
• a sample of gas from the analysis section 59 is extracted from the upper sampling point immediately after the valves are closed.
• the sample is tested for content of C0 2 by gas chromatography using a Chromopack Model CP-2002.
• the expended liquid is released from the reservoir pipe 61 to the measurement drum 67 and weighed.
• the liquid solvent mixture is a 50% solution of MEA. The results for these tests are shown in Table 3 below:

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• Chemical & Material Sciences (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Engineering & Computer Science (AREA)
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• General Chemical & Material Sciences (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• Organic Chemistry (AREA)
• Dispersion Chemistry (AREA)
• Gas Separation By Absorption (AREA)
• Treating Waste Gases (AREA)

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• 1998
  • 1998-09-14 EP EP98942899A patent/EP1021234A1/en not_active Ceased
  • 1998-09-14 WO PCT/GB1998/002760 patent/WO1999013962A1/en not_active Application Discontinuation
  • 1998-09-14 AU AU90864/98A patent/AU749450B2/en not_active Withdrawn - After Issue
  • 1998-09-14 CA CA002303374A patent/CA2303374A1/en not_active Abandoned
• 2000
  • 2000-03-14 NO NO20001311A patent/NO20001311L/no unknown

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