WO2016009177A1 - Réacteur à déflecteur oscillatoire et procédé de réaction gaz/liquide - Google Patents

Réacteur à déflecteur oscillatoire et procédé de réaction gaz/liquide Download PDF

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Publication number
WO2016009177A1
WO2016009177A1 PCT/GB2015/051975 GB2015051975W WO2016009177A1 WO 2016009177 A1 WO2016009177 A1 WO 2016009177A1 GB 2015051975 W GB2015051975 W GB 2015051975W WO 2016009177 A1 WO2016009177 A1 WO 2016009177A1
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WIPO (PCT)
Prior art keywords
fluid
orifice
oscillatory
gas
baffle
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PCT/GB2015/051975
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English (en)
Inventor
Nuno REIS
Gianluca LI PUMA
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Loughborough University
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Publication of WO2016009177A1 publication Critical patent/WO2016009177A1/fr

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    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
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    • B01F23/20—Mixing gases with liquids
    • B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
    • B01F23/231—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids by bubbling
    • B01F23/23105—Arrangement or manipulation of the gas bubbling devices
    • B01F23/2312—Diffusers
    • B01F23/23126—Diffusers characterised by the shape of the diffuser element
    • B01F23/231266—Diffusers characterised by the shape of the diffuser element being in the form of rings or annular elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • B01F23/23761—Aerating, i.e. introducing oxygen containing gas in liquids
    • B01F23/237613—Ozone
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Definitions

  • the present invention relates generally to a multi-orifice oscillatory baffled reactor useful in gas-liquid reaction processes, and methods of removing contaminants from fluids using such reactors.
  • OBRs Oscillatory baffled reactors
  • OBRs have been used to provide a reactor which promotes mixing without the use of stirrers or turbulent flow within the reactor.
  • OBRs usually take the form of an elongated tube containing a number of baffles spaced along the tube.
  • the baffles are usually plates which partially obstruct the internal cross-section of the tube, and include one or more orifices for the passage of liquid. It is well known that if a liquid flowing through the tube is oscillated or pulsated, the presence of the baffles causes the formation of vortices within the liquid, thereby providing an excellent mixing mechanism without the use of stirrers.
  • the most common OBRs include single-orifice baffles equally spaced along the reactor tube.
  • Each baffle is a plate containing a single, central orifice.
  • single-orifice OBRs are scaled up, beyond a certain point the advantageous mixing effects cannot be achieved and therefore different baffle geometries which allow for the OBR effect to be scaled up have been provided, and these include multi-orifice OBRs.
  • Multi-orifice OBRs contain baffle plates each of which includes a plurality of orifices, usually of equal size and arranged in a regular pattern. The use of multi-orifice OBRs allows the mixing effects observed at laboratory scale to be scaled up to industrial scale.
  • gas-liquid reactions The efficiency of gas-liquid reactions depends in a large part on the efficiency of mass transfer of the gas to the liquid in dissolution.
  • One important gas-liquid reaction is ozonation, in which ozone reacts with and decomposes organic contaminants of concern from water in water treatment plants.
  • Pollutants of concern include pharmaceuticals and antibiotics (e.g., ibuprofen, trimethoprim); personal care products (e.g., benzophenone in sunscreens); herbicides (e.g., atrazine, isoproturon); hospital x-ray contrast media (e.g., diatrizoate, iopamidol); recalcitrant industrial (pulp and paper, textile, metal working fluids). Other strong oxidising gases such as chlorine are often also used to remove such contaminants from water supplies.
  • antibiotics e.g., ibuprofen, trimethoprim
  • personal care products e.g., benzophenone in sunscreens
  • herbicides e.g., atrazine, isoproturon
  • hospital x-ray contrast media e.g., diatrizoate, iopamidol
  • Other strong oxidising gases such as chlorine are often also used to remove such contaminants from water supplies.
  • WWTPs wastewater treatment plants
  • Ozone is very expensive and waste of ozone during ozonation processes represents the biggest cost factor in ozone treatment of contaminated water.
  • Syngas also known as producer gas or synthesis gas
  • CO2 carbon monoxide
  • H2 hydrogen
  • CO2 carbon dioxide
  • the CO and H2 present in syngas can be converted by anaerobic microorganisms into a range of useful bio-based compounds such as bioplastics, ethanol, butanol, acetic and butyric acid and methane.
  • CO and H 2 both have low solubility, and it is believed that CO fermentation is controlled by gas-liquid mass transfer rates.
  • OBRs provide a promising solution to the problems associated with existing reactors, but so far no satisfactory reactor design or reaction process has been provided which can substantially increase the efficiency of the gas-liquid reaction.
  • a first aspect of the invention is a multi-orifice oscillatory baffled reactor (OBR), comprising; a reactor tube; a baffle within the reactor tube, defining a plurality of orifices and having a free open area of up to 30%; a gas source having an outlet within the reactor tube; and oscillatory means which, during use, provide oscillatory flow of a fluid relative to the baffle.
  • OBR multi-orifice oscillatory baffled reactor
  • the free open area is a property of a single baffle.
  • the free open area of a multi-orifice baffle is a percentage value defined as (A J A) x 100, where A 0 is the total area of the orifices within the baffle and A is the total cross-sectional area of the baffle.
  • the use of a small baffle open area in a multi-orifice baffle is responsible for the generation of these microbubbles as the fluid oscillates relative to the baffle.
  • the strong radial mixing which occurs due to the fluid pulsation and/or baffle reciprocation in the reactor tube causes the microbubbles to become trapped within the tube for relatively long periods of time (e.g. for at least 1 , at least 2 or at least 3 oscillatory cycles).
  • the result is that a very large gas-liquid interfacial area is created which greatly increases the efficiency of the gas-liquid reaction.
  • the bubbles are trapped within the reactor tube for periods of time long enough to achieve reactant gas consumption close to 100%; that is, little or no reactant gas is wasted and a substantial saving on cost is achieved.
  • the microbubbles produced within the OBR by the oscillatory motion of fluid relative to the baffle are not simply delayed in their transition through the reactor tube, but are effectively trapped within it.
  • the microbubbles exhibit a downward movement (against the net flow of fluid) which effectively ensures a residence time within the reactor tube sufficient to provide a gas utilisation efficiency of up to 100%.
  • the gas utilisation efficiency achieved by the OBR may be at least 90%, for example up to 100%, 99%, 98%, 97%, 96%, 95%, 94%, 93%, 92% or 91 %.
  • the energy costs required for fluid and/or baffle pulsations are more than offset by the energy saving in preventing gas (especially oxidising gas such as ozone) wastage, making the OBR economically viable to provide a means for more efficient gas-liquid reactions, such as in the removal of contaminants from water such as wastewater.
  • the use of a multi-orifice baffle in the OBR allows the reactor to be scalable, such that it may be used in both small to medium scale applications (laboratory, households, small wastewater treatment plants and hospitals) and large scale industrial applications. Large scale application is not possible with single-orifice OBRs, as explained above.
  • the reactor tube contains a plurality of baffles, each baffle defining a respective plurality of orifices and having a free open area of up to 30%.
  • An OBR having two or more baffles provides one or more inter-baffle regions where radial mixing is strong and vortices are generated. The trapping of microbubbles generated by the oscillatory flow is therefore more effective.
  • the number of baffles within the reactor is not particularly limited and depends upon the dimensions of the reactor tube.
  • baffles Any number of baffles may be employed within the reactor provided that the appropriate amount of radial mixing is produced to allow for the formation and trapping of microbubbles. It will be clear to the skilled person that the exact number of baffles used within the reactor tube will depend on its design including, inter alia, the length and diameter of the tube being used. Thus the number of baffles within the reactor tube may be chosen accordingly.
  • the OBR may further contain one or more baffles having a free open area greater than 30%, in addition to the one or more baffles having a free open area of up to 30%.
  • the OBR may further contain one or more baffles defining a single orifice, in addition to the one or more baffles each defining a plurality of orifices.
  • all baffles within the reactor tube each define a respective plurality of orifices and have a baffle free open area of up to 30%.
  • the baffle free open area may be up to 25% e.g. up to 20%. Further reducing the free open area of each baffle within the reactor to at or below 20% produces an even greater quantity of microbubbles, the microbubbles being further reduced in size. The gas-liquid interfacial area is further increased, with a resultant increase in reaction efficiency.
  • the baffle free open area may be up to 19%, 18%, 17%, 16%, 15%, 14%, 13%, 12%, 11 % or 10%.
  • the baffle free open area may be at least 5%, for example at least 6%, 7%, 8%, 9% or 10%
  • the gas source may be an oxidising gas source, a CO2 gas source or a syngas gas source.
  • the reactor according to the present invention may therefore find application in processes such as ozonation, CO 2 sequestration or syngas bioconversion.
  • the gas source may be an oxidising gas source selected from ozone and chlorine.
  • ozonation using standard bubble columns is already employed in the treatment of water, such as wastewater, to remove organic contaminants.
  • the use of an ozone gas source in the present device can provide a highly efficient ozonation reactor to supplement or replace the existing inferior reactors in order to provide a cost efficient water treatment solution in waste water treatment plants and other similar locations.
  • a chlorine gas source could be employed in the disinfection of water supplies.
  • the device is fully compatible with existent ozonation and chlorination technologies.
  • the gas source may be an ozone gas source, the oscillatory baffled reactor being adapted for ozonation.
  • An ozonation reactor is a particularly important device in the treatment of water and wastewater, as described above.
  • the use of the ozonation reactor to decontaminate water and wastewater will make it possible to reuse water and reduce the level of discharge of recalcitrant chemicals into the environment, therefore presenting simultaneously major economic and environmental benefit for local communities and wildlife.
  • the inventors have found that the chemical reaction for degradation of contaminant with ozone is fast and occurs at the gas-liquid interface, and therefore it is important to produce very small bubbles of ozone and to achieve trapping of those bubbles in order to achieve dissolution and high mass transfer efficiency.
  • the present invention achieves this.
  • the OBR provides up to a 10-fold reduction in the amount of reactant gas required to treat a given volume of fluid, with a resultant up to 10- fold reduction in cost per cubic metre of treated fluid.
  • the gas source may be a sparged gas source.
  • the sparged gas source may comprise a sparger to deliver gas to the internal volume of the reactor tube.
  • the sparger may comprise a perforated gas delivery element such that gas may pass through the perforation into the reactor tube.
  • the perforated gas delivery element may comprise a tube made from suitable rigid material, such as plastics material, ceramic or other microporous material.
  • a sparged gas source provides a more controllable introduction of gas into the reactor so that the gas source may be easily adjusted to provide optimal conditions for microbubble production.
  • the gas source may be adapted to provide a gas aeration rate Q gas during use of between 0.01 and 0.1 vvm, i.e. between 0.1 and 1 L min- .
  • the multi-orifice oscillatory baffled reactor may have a hydraulic diameter d h between 5 mm and 50 mm, wherein dh is defined as: where d c is the internal diameter of the reactor tube and n is the number of orifices in the baffle.
  • dh do where do is the diameter of the baffle orifices and a is the baffle free open area.
  • the hydraulic diameter is a parameter which is often used to predict the performance of baffles with respect to gas-liquid mass transfer rates.
  • a value of d h within this range provides for the optimal production of an increased number of very small diameter microbubbles, leading to a high efficiency gas-liquid reaction.
  • the baffles within the OBR may be equally spaced along the reactor tube.
  • the baffles may be spaced according to a non-regular sequence.
  • the baffles may also be randomly spaced along the reactor tube.
  • the multi-orifice oscillatory baffled reactor may have a spacing between two consecutive baffles (the inter-baffle spacing, L) of between d h and 3d h .
  • An inter-baffle spacing within this range provides the optimal inter-baffle region size to achieve the necessary trapping of the microbubbles produced, leading to an increased gas hold-up, increased time of bubble residence within the reactor tube and therefore enhanced gas utilisation efficiency.
  • the average number of orifices per baffle may be from 2 to 1500 e.g. from 5 to 1000, or from 5 to 750 or from 5 to 500 e.g. from 5 to 250. More preferably, the average number of orifices per baffle may be between 10 and 100, more preferably 15 and 80, more preferably 20 and 60, more preferably 25 and 35.
  • the skilled person will be aware that the selection of the average number of orifices per baffle depends upon dh for the reactor and hence the total cross sectional area A of the baffle. Using a set of baffles having an average number of orifices within this range enhances the generation of microbubbles. The diameter of observed microbubbles also decreases for orifice numbers within this range.
  • the baffles may be manufactured from any suitable rigid material. Examples of suitable materials include stainless steel, acrylic polypropylene and PVC.
  • the baffles may have a laminate structure comprising a plurality of layers sandwiched together.
  • a baffle may be constructed by sandwiching a suitable rigid polymer between two stainless steel layers.
  • the central rigid polymer layer may be polypropylene.
  • the baffles may be produced by any suitable method, including machining from sheet material, lamination or 3D printing.
  • the baffles may be supported within the OBR by suitable supporting means which may fix the position of the baffles relative to the reactor tube.
  • the supporting means may fix the position of the baffles relative to one another.
  • the supporting means may connect all baffles together and to the oscillatory means, such that all the baffles may be oscillated simultaneously.
  • the supporting means may be a connecting member which connect all baffles together.
  • the connecting member may also be connected to the reactor tube, or the oscillatory means.
  • the connecting member may be a rod fixed within the reactor tube, passing through and connected to each baffle.
  • the rod may be made from any suitable rigid material. Suitable materials include stainless steel.
  • the baffles may be designed so as to provide a close fit with the internal wall of the reactor tube.
  • the diameter of the baffles may be substantially equal to the internal diameter of the reactor tube such that little or no fluid may pass between the outer perimeter of the baffle and the internal wall of the reactor tube.
  • All baffles within the OBR may be of identical design. That is, all baffles may have the same baffle free open area a and the same number, size and distribution of orifices. Furthermore, the baffles may all be manufactured from identical material with identical physical properties. Alternatively, the design of an individual baffle may differ from the design of other baffles within the reactor tube. For example, the distribution of orifices in the baffle may be different, although a and other parameters may be the same.
  • the OBR may be of the "pulsed" type.
  • the oscillatory means may comprise an axially movable fluid displacement member within the reactor tube at one end, movable to vary the total internal volume of the reactor tube and therefore effect an oscillation of fluid within the reactor tube. The fluid within the reactor is thereby “pulsed” back and forth through the baffle.
  • the fluid displacement member may be a piston.
  • the fluid displacement member may be any suitable means for providing displacement of the fluid, such as a diaphragm pump.
  • the OBR may be of the "reciprocating plate” type.
  • the oscillatory means may be connected to one or more baffles to provide reciprocation of the baffle relative to the reactor tube (and relative to any fluid present in the reactor tube). In this case the oscillatory means may be located either inside or outside the reactor tube.
  • This setup equally provides the strong radial mixing within the reactor tube necessary to produce microbubbles from a gas introduced to the OBR. Whether the OBR is of "pulsed" or "reciprocating plate” type, the net result is similar. The key concern is that there is flow of fluid relative to the baffles (through the baffle orifices), which creates the strong radial mixing and a large number of microbubbles.
  • the oscillatory means may be connected to a servo-hydraulic system which imparts the oscillatory motion.
  • any suitable means for providing oscillatory motion may be provided, such as a combustion, wind or solar powered motor.
  • the oscillatory means may be capable of providing sinusoidal oscillatory motion.
  • the oscillatory means can be controlled to produce a desired frequency and amplitude of fluid oscillation and/or baffle oscillation. The result is movement of fluid relative to the baffle through the baffle orifices, which creates the strong radial mixing in the reactor tube, particularly in the inter-baffle region when a plurality of baffles is present.
  • the combination of oscillation and the specific baffle design in the OBR lead to the production and trapping of microbubbles within the reactor tube.
  • the reactor tube may be made from any suitable material. Suitable materials include rigid plastics materials such as acrylic, PVC or polypropylene, or metallic materials such as steel, or glass.
  • the reactor tube may be made from a transparent material to provide for ease of visual monitoring, which is important to allow the user to ensure that an adequate number and distribution of microbubbles is produced and maintained within the reactor tube during use.
  • the reactor tube may be sealed at both ends to prevent the unwanted leakage of fluid during operation of the OBR.
  • the reactor tube may define an opening which acts as a fluid inlet.
  • the opening may be sealable my means of a valve.
  • the reactor tube may define an opening which acts as a fluid outlet.
  • the opening may be sealable my means of a valve.
  • the reactor tube may be of a wide range of dimensions depending on the intended application.
  • the size of the reactor tube may range from a size suitable for small scale (e.g. laboratory) use, up to sizes suitable for large scale (e.g. industrial water treatment) use.
  • the dimensions of all other components of the reactor will also vary accordingly to correspond with the dimensions of the reactor tube.
  • a suitable size of baffle will be selected depending on the size of the reactor tube.
  • the multi-orifice oscillatory baffled reactor may include a reactor tube with an internal diameter (d c ) of at least 50 mm and up to 1 m.
  • the reactor tube may have an internal diameter (d c ) of less than 300 mm. More preferably the reactor tube has an internal diameter of less than 250 mm, less than 200 mm or less than 150 mm.
  • the total volume of the reactor tube may be less than 15 L, less than 14 L, less than 13 L, less than 12 L or less than 11 L.
  • the height of the reactor tube may be less than 2 m.
  • the reactor tube may have an internal diameter of up to 1 m.
  • the height of the reactor tube may be less than 2 m.
  • the OBR may be a compact modular reactor unit. Such compact modular units are suitable for household use or application in small water and wastewater treatment plants. They could also be used in small industrial units, hospitals, water purification systems in small to medium sized businesses and car washing stations. They can therefore provide affordable and efficient water decontamination systems for a wide variety of users.
  • the OBR could also find application in countries where clean and safe drinking water sources are rare.
  • the efficiency of the gas-liquid reaction means that the OBR can provide an affordable source of clean water to supply small communities in such countries.
  • the multi-orifice oscillatory baffled reactor may be suitable for small to medium scale fluid throughputs, for example up to 10 Us.
  • the OBR may be capable of a fluid throughput of at least 1 Us.
  • the reactor tube of the multi-orifice oscillatory baffled reactor may contain between 8 and 10 baffles, each baffle having a free open area of up to 20% and the inter-baffle spacing being between 35 mm and 45 mm, wherein the hydraulic diameter dh is between 25 mm and 30 mm, the hydraulic diameter being defined as above.
  • the OBR may be connected to a central processing unit (CPU).
  • the CPU may control various functions of the OBR.
  • the CPU may control the frequency and/or amplitude of oscillation provided by the oscillatory means.
  • the CPU may be connected to a servo-hydraulic unit which is in turn connected to the oscillatory means.
  • the CPU will provide the servo- hydraulic unit with the necessary signal as to the frequency and/or amplitude, and the duration of oscillation.
  • the CPU may provide a means for monitoring the size and distribution of microbubbles generated within the OBR.
  • the CPU may be connected to a CCD camera or similar device which may record images or video footage of the OBR interior.
  • the CCD camera may be located either internally or externally of the reactor tube.
  • a means for reducing optical distortion may be provided between the reactor tube and the CCD camera.
  • This may be a vessel filled with a distortion reducing medium, such as glycerol.
  • the CPU may be programmed to adjust the frequency and/or oscillation of the oscillatory means in response to data gathered from the CCD camera in order to attain optimal size and/or distribution of microbubbles.
  • the CPU may provide a means for monitoring the level of dissolved reactant gas and/or the level of contaminants present within a fluid in the reactor tube.
  • the CPU may be connected to a sensor located within the reactor tube.
  • the sensor may monitor the concentration of dissolved gas, such as dissolved ozone or chlorine, present within the reaction fluid.
  • the sensor may monitor the concentration of one or more dissolved contaminants within the reaction fluid. If the OBR is operating in batch mode, such monitoring will be useful in assessing the extent of decontamination and reaction completion. In continuous mode, the effectiveness of the decontamination may be assessed and the throughput or other conditions such as oscillation or gas superficial velocity adjusted accordingly.
  • the CPU may be connected to a user interface to allow monitoring of the OBR conditions, such as the oscillation frequency and amplitude, the concentration of dissolved reactant gas and/or contaminants, the quantity and distribution of microbubbles etc.
  • the interface may include means for manual adjustment of one or more of these parameters.
  • the interface may be a display monitor.
  • the OBR may be adapted for the treatment of water.
  • the OBR may be adapted for the treatment of wastewater.
  • the OBR may be adapted for the removal of organic contaminants from a fluid.
  • the OBR may be adapted to carry out a method selected from sanitation treatment of mineral bottled water by ozonation; tertiary treatment to remove micro-contaminants of concern from wastewater; disinfection of drinking water; sanitation of recreational water; decontamination of water used in pulp and paper processing; decontamination of water used in food and beverage production; decontamination of water used in semiconductor manufacture; decontamination of cooling water for antibacterial control; colour removal from textile wastewater; treatment of metal working fluids; decontamination of underground water and decontamination of ballast water for reuse.
  • the OBR may be adapted to remove Pharmaceuticals and Personal Care Products (PPCPs) from a fluid.
  • PPCPs Pharmaceuticals and Personal Care Products
  • PCPPs are an area of particular importance as these are difficult to remove by existing decontamination methods and can find their way into natural water sources after inefficient treatment of municipal wastewater.
  • the present device is an effective means to remove such contaminants, presenting a major environmental benefit.
  • the OBR may be adapted to further subject the fluid to one or more additional processes selected from H2O2 treatment, UV exposure, photo-Fenton processes and sulphate treatment. Including other known decontamination means in the OBR will ensure effective decontamination of the fluid.
  • the oscillatory means may be adapted to oscillate at a frequency of up to 20 Hz.
  • the oscillatory means may be adapted to oscillate at a frequency of up to 10 Hz.
  • the oscillatory means may be adapted to oscillate at a frequency of up to 19, 18, 17, 16, 15, 14, 13, 12, 11 , 10, 9 or 8 Hz.
  • the oscillatory means may be adapted to oscillate at a frequency of at least 0.5 Hz, for example at least 1 Hz, 1.5 Hz, 2 Hz, 2.5 Hz, 3 Hz, 3.5 Hz, 4 Hz, 4.5 Hz or 5 Hz.
  • Oscillation within this frequency range provides optimal conditions to establish the strong radial mixing which supports the presence of a large quantity of microbubbles throughout the fluid.
  • the oscillatory means may be adapted to oscillate with a centre-to-peak amplitude of up to 20 mm.
  • the oscillatory means may be adapted to oscillate with a centre-to-peak amplitude of up to 10 mm.
  • the oscillatory means may be adapted to oscillate with a centre-to-peak amplitude of up to 19, 18, 17, 16, 15, 14, 13, 12, 11 or 10 mm.
  • the oscillatory means may be adapted to oscillate with a centre-to-peak amplitude of at least 2.5 mm, for example at least 3 mm, 3.5 mm, 4 mm, 4.5 mm, 5 mm, 5.5 mm or 6 mm.
  • the OBR may be adapted to decontaminate fluid in continuous or batch mode.
  • the gas source may be adapted to provide a gas superficial velocity of between 0.001 and 10 mm s _1 .
  • the OBR may be adapted to decontaminate fluid in continuous mode with a throughput of between 0.1 and 10 Ls _ .
  • the OBR may be adapted to carry out decontamination at pH 7 or above.
  • the OBR may be adapted to carry out decontamination at pH 8, 9, 10 or above.
  • decontamination at pH 8, 9, 10 or above.
  • the enhancement in ozone utilisation efficiency is not as complete as when the reaction is carried out at higher pH values.
  • up to 100% ozone use may be achieved.
  • the OBR may be adapted to carry out decontamination at atmospheric temperature and pressure. This makes the running of the OBR more cost-efficient.
  • the OBR may be adapted such that the level of the fluid in the reactor tube during use is kept above the level of the uppermost baffle. This avoids any air from the headspace above the fluid becoming trapped during operation of the OBR.
  • a second aspect of the invention is a method of removing contaminants from a fluid by contacting the fluid with an oxidising gas, the method comprising the steps of: introducing the fluid into the multi-orifice oscillatory baffled reactor according to the first aspect; introducing the oxidising gas into the fluid through the gas source; and oscillating the fluid and/or the one or more baffles with the oscillatory means to provide a dispersion of micro- bubbles within the fluid.
  • the term “removal” or “removing” refers to the elimination or degradation of one or more contaminants from the fluid, which includes the chemical degradation of contaminants resulting in products which are less harmful to humans, animals and/or the environment than the original contaminants present.
  • the reaction which degrades the contaminants may be oxidation.
  • the combination of the OBR design (in particular the baffle design) and the fluid and/or baffle oscillation provides strong radial mixing within the inter- baffle region of the reactor tube. This results in the production of a great quantity of microbubbles which provides a highly efficient gas-liquid reaction, as described above. Furthermore, the microbubbles are trapped within the inter-baffle region rather than passing through the length of the reactor tube in the direction of net fluid flow, for a period of time sufficient to provide up to 100% use of the oxidising gas, with very little or no wastage.
  • the fluid may be water.
  • the fluid may be wastewater.
  • the oxidising gas may be ozone or chlorine.
  • ozonation using standard bubble columns is already employed in the treatment of water and wastewater to remove organic contaminants.
  • the use of ozone in the present method can provide a highly efficient ozonation reactor and reaction process to supplement or replace the existing inferior reactors in order to provide a cost efficient water treatment solution in waste water treatment plants and other similar locations.
  • chlorine gas could be employed in the disinfection of water supplies.
  • the method and device are fully compatible with existent ozonation and chlorination technologies.
  • the oxidising gas may be ozone, such that the reaction occurring in the reactor is ozonation.
  • Ozonation is a particularly important process in the treatment of water and wastewater, as described above.
  • the use of the ozonation method to decontaminate water and wastewater will make it possible to reuse water and reduce the level of discharge of recalcitrant chemicals into the environment, therefore presenting simultaneously major economic and environmental benefit for local communities and wildlife.
  • the method may be a method of removing organic contaminants from the fluid.
  • the method may be selected from sanitation treatment of mineral bottled water by ozonation; tertiary treatment to remove micro-contaminants of concern from wastewater; disinfection of drinking water; sanitation of recreational water; decontamination of water used in pulp and paper processing; decontamination of water used in food and beverage production; decontamination of water used in semiconductor manufacture; decontamination of cooling water for antibacterial control; colour removal from textile wastewater; treatment of metal working fluids; decontamination of underground water and decontamination of ballast water for reuse.
  • the contaminants may be Pharmaceuticals and Personal Care Products (PCPPs).
  • PCPPs Pharmaceuticals and Personal Care Products
  • the present method is an effective means to remove such contaminants, presenting a major environmental benefit.
  • the method may also subject the fluid to one or more additional processes selected from H2O2 treatment, UV exposure, photo-Fenton processes and sulphate treatment. These additional processes may occur before decontamination with the oxidising gas, after decontamination with the oxidising gas, or simultaneously with decontamination with the oxidising gas. Combining the method with other known decontamination processes will ensure effective decontamination of the fluid.
  • the fluid may be decontaminated in continuous or batch mode.
  • the selection of either continuous or batch mode of operation allows the throughput of the method to be adapted to suit the particular application.
  • the fluid may be decontaminated in continuous mode with a throughput of between 0.001 and 10 Ls " .
  • 100% of the oxidising gas introduced to the reactor tube may be consumed by the reaction with contaminants.
  • up to 100% of the oxidising gas introduced to the reactor tube may be consumed by the reaction, for example at least 90% of the oxidising gas.
  • the reaction may consume up to 99%, 98%, 97%, 96% or 95% of the oxidising gas.
  • the reaction may consume at least 90% of the oxidising gas, for example at least 91 %, 92%, 93%, 94%, 95%, 96%, 97%, 98% or 99%.
  • the method may be carried out at pH 7 or above.
  • the method is carried out at pH 8, 9, 10 or above.
  • the enhancement in ozone utilisation efficiency is not as complete as when the reaction is carried out at higher pH values.
  • up to 100% ozone use may be achieved.
  • the method may be carried out at atmospheric pressure and room temperature. This ensures a cost-efficient decontamination method.
  • a third aspect of the invention is a method of CO 2 sequestration comprising the steps of introducing a fluid into the multi-orifice oscillatory baffled reactor according to the first aspect;
  • a fourth aspect of the present invention is a method of manufacturing bioproduct using syngas bioconversion comprising the steps of
  • the bioconversion medium may be a biomass culture.
  • the bioproduct may be a biofuel.
  • the bioproduct may be a bioplastic.
  • the bioproduct may be a compound selected from ethanol, butanol, acetic acid, butyric acid and methane.
  • the oscillatory means may be used to oscillate the fluid directly.
  • the oscillatory means may be used to oscillate the baffles directly. In either case the desired result is the oscillatory movement of fluid relative to the baffles, such that fluid passes through the baffle orifices.
  • the oscillatory means may be oscillated in a sinusoidal motion.
  • Sinusoidal oscillation favours dissipation of eddy rings or vortices within the reactor tube.
  • the oscillatory means may be oscillated at a frequency of up to 20 Hz.
  • the oscillatory means may be oscillated at a frequency of up to 10 Hz.
  • the oscillations may be at a frequency of up to 19, 18, 17, 16, 15, 14, 13, 12, 1 1 , 10, 9 or 8 Hz.
  • the oscillations may be at a frequency of at least 0.5 Hz, for example at least 1 Hz, 1.5 Hz, 2 Hz, 2.5 Hz, 3 Hz, 3.5 Hz, 4 Hz, 4.5 Hz or 5 Hz.
  • Oscillation within this frequency range provides optimal conditions to establish the strong radial mixing which supports the presence of a large quantity of microbubbles throughout the fluid.
  • the oscillatory means may be oscillated with a centre-to- peak amplitude of up to 20 mm.
  • the oscillatory means may be oscillated with a centre-to- peak amplitude of up to 10 mm.
  • the centre-to-peak amplitude may be up to 19, 18, 17, 16, 15, 14, 13, 12, 1 1 or 10 mm.
  • the centre-to-peak amplitude may be at least 2.5 mm, for example at least 3 mm, 3.5 mm, 4 mm, 4.5 mm, 5 mm, 5.5 mm or 6 mm.
  • the oxidising gas may be introduced through a sparged gas source having an outlet within the reactor tube.
  • the level of fluid in the reactor tube may be kept above the level of the uppermost baffle. This avoids any air from the headspace above the fluid becoming trapped.
  • a fifth aspect of the invention is the use of the multi-orifice oscillatory baffled reactor according to the first aspect in decontamination of water by ozonation, sequestration of CO2, or bioconversion of syngas into a bioproduct.
  • the use may be in the decontamination of wastewater by ozonation.
  • the OBR described herein provides particular advantages with respect to ozonation reactions, where ozone is an expensive reactant and the reduction of its wastage is desirable. These advantages have been described in detail above.
  • Figure 1 is a longitudinal cross-section through a reactor according to the present invention.
  • Figure 2 is a simplified representation of a batch mode ozonation reactor according to the present invention.
  • Figure 3 shows plan views of three different baffle designs.
  • Figure 4 shows six photographs from the optical observation of air bubbles rising in the inter-baffle region in a multi-orifice baffled column in different configurations.
  • Figure 5 shows bubble size distributions for baffle designs 1 and 2 in different oscillatory conditions.
  • Figure 6 shows the bubble size distribution within the OBR of the present invention using baffle design 3, in comparison to the equivalent distribution in an un-baffled reactor tube.
  • Figure 7 shows time-tracking plots of (a) (x,y) position and (b) instantaneous vertical velocity (V y ) for four bubbles randomly selected in the inter-baffle region during one oscillatory cycle of the OBR of the present invention.
  • Figure 8 shows time-tracking plots of (a) (x,y) position and (b) instantaneous vertical velocity (V y ) for four bubbles randomly selected in the inter-baffle region during one oscillatory cycle of the OBR of the present invention.
  • Figure 9 shows time-tracking plots of (a) (x,y) position and (b) instantaneous vertical velocity (V y ) for four bubbles randomly selected in the inter-baffle region during one oscillatory cycle of the OBR of the present invention.
  • Figure 10 shows time-tracking plots of (a) (x,y) position and (b) instantaneous vertical velocity (V y ) for four bubbles randomly selected in the inter-baffle region during four oscillatory cycles of the OBR of the present invention.
  • Figure 11 shows flow visualisation of liquid mixing in the OBR of the present invention using tracing polyamide particles. Images (1), (2) and (3) were respectively taken at three different points on the oscillation cycle.
  • Figure 12 shows flow visualisation of liquid mixing in the OBR of the present invention using tracing polyamide particles.
  • Columns (1), (2) and (3) indicate images taken at different points on the oscillation cycle and rows (a), (b) and (c) indicate different fluid oscillation conditions.
  • Figure 13 shows (a) plots of dissolved para-hydroxybenzoic acid (p-HBA) concentration and ozone concentration against time, and (b) a plot of dissolved p-HBA concentration and ozone utilisation efficiency against time.
  • p-HBA dissolved para-hydroxybenzoic acid
  • Figure 14 shows (a) a plot of the amount of p-HBA degraded against cumulative O3 injected, and (b) a plot of dissolved p-HBA concentration and ozone utilisation efficiency against time.
  • Figure 15 shows (a) plots of dissolved ozone concentration against time for different oscillation conditions, and (b) plots of dissolved p-HBA concentration and ozone utilisation efficiency against time at pH 4 and pH 10.
  • Figure 16 shows (a) plots of In (C/Co) against time for two different Ug as values, and (b) plots of the amount of p-HBA degraded against the amount of cumulative O3 injected at two different U ga s values.
  • Figure 17 shows (a) a plot of Q syn gas n) and Q syn gas (out) against time, and (b) plots of instantaneous methane yield from CO and instantaneous methane production rate against time.
  • Figure 18 shows the effect of specific CO loading rates on (a) the specific reaction rates for CO, H2 and CH4, and (b) the removal efficiency of CO and H2, during continuous syngas fermentation in the OBR.
  • Figure 19 shows CO and H 2 concentration profiles as measured in the OBR headspace.
  • Figure 20 shows the OBR setup used in continuous syngas fermentation experiments using anaerobic bacteria.
  • Figure 21 shows (a) the rate of ozone consumption, (b) rate of degradation of p-HBA and (c) TOC reduction in a continuous bubble column (BC) and a continuous mulit-orifice baffled column (MOBC with a mean liquid contacting time of 2.25 minutes.
  • Figure 22 shows (a) the rate of ozone consumption, (b) rate of degradation of p-HBA and (c) TOC reduction in a continuous bubble column (BC) and a continuous mulit-orifice baffled column (MOBC with a mean liquid contacting time of 1 1.2 minutes.
  • Figure 23 shows ozone utilisation efficiency at different ozone dosages.
  • Figure 24 shows a simplified representation of a continuous mode ozonation reactor according to the present invention.
  • Multi-Orifice Oscillatory Baffled Reactor Figure 1 shows a longitudinal cross-section of a multi-orifice oscillatory baffled reactor 30 according to one embodiment of the present invention, configured to carry out batch processes.
  • the OBR includes a transparent cylindrical reactor tube 301 made from glass.
  • the reactor tube has a maximum internal diameter of 150 mm. At the base of the reactor tube the internal surface extends inwards into an annular lip 302 with an internal diameter of 125 mm.
  • the total reactor tube height (h) is 540 mm.
  • the total volume of the reactor tube is 10.6 L and the working volume ( VL) is 9.6 L.
  • the reactor base 306 includes an inner base flange 307 which abuts the planar annular surface at the end of the tube 301 .
  • the reactor tube includes an external lower annular flange 303a close to the lower end of the tube.
  • a series of screws 304 pass through the annular flange 303a and into the base 306. The tightening of these screws seals the annular flange 307 of the base 306 against the reactor tube 301 .
  • the tube opening is sealed by a cap 308.
  • An external upper annular flange 303b is located close to the upper end of the tube.
  • a series of screws 305 pass through the flange 303b and the cap 308. The tightening of these screws seals the opening at the upper end of the tube.
  • the upper end of the tube is not entirely sealed, due to the presence of gas vent 325 which allows for the escape of gas from the headspace within the tube.
  • Each baffle 309 is fixed at a certain position along a stainless steel connecting rod 310 of 6 mm diameter.
  • the baffles are spaced along the rod at equal intervals of 40 mm. The precise interval may be varied by sliding the baffles along the rod before fixing them in place.
  • Two rods are shown in Figure 1 , and a third rod is also used which is not visible.
  • Each baffle 309 is of circular geometry having a diameter of 150 mm such that it fits snugly within the reactor tube 301.
  • Each baffle includes a plurality of orifices (not shown) each orifice being circular with a diameter of 10.5 mm. The orifices are distributed in a regular hexagonal array.
  • Each baffle 309 is made from acrylic material and is 3.0 mm thick.
  • each baffle 309 Between each baffle 309 is an inter-baffle region 312 defined by the internal surface of the reactor tube 301 and the surface of two neighbouring baffles 309.
  • the reactor tube contains a series of equally spaced baffles 302, with 10 baffles in the series.
  • the baffles are connected in series with stainless steel rods 303 of 6 mm diameter.
  • Inter-baffle region 304 is established between neighbouring baffles inside the tube.
  • the inter-baffle spacing is variable by movement of the baffles along the stainless steel rods.
  • Each baffle is of circular geometry and fits snugly within the reactor tube.
  • rods 310 are secured to the floor of the reactor tube, and plastic spacers (not shown) are placed on the rods between two adjacent baffles to maintain the inter-baffle separation.
  • a piston 313 seals the annular opening at the bottom of the tube 301 defined by the internal surface of the lip 302 and the internal surface of the inner base flange 307.
  • the piston is of 125 mm diameter and therefore fits snugly against the internal surface of the base, sealing the internal volume of the tube 301.
  • the piston 313 is axially slidable within the base 306 and the tube 301 , as shown by the double-headed arrow in Figure 1.
  • the piston is connected by drive shaft 314 to a motor 315 which is part of a servo-hydraulic unit 316.
  • This servo-hydraulic unit 316 is controlled by a CPU 317 which is in turn connected to a user interface 318 which in this case is a display monitor.
  • the servo- hydraulic unit can be adjusted to vary the amplitude and frequency of the piston motion.
  • the gas sparger 323 is an elongate cylindrical PVC tube extending laterally within the reactor tube, with 0.6 mm diameter perforation to allow gas to be sparged into the reactor tube.
  • a dissolved gas sensor 326 passes through the cap 308 and into the internal volume of the tube 301.
  • the sensor is also connected to and controlled by the CPU 317.
  • a CCD camera 319 is positioned outside the tube 301 , with a view into the transparent tube.
  • a Perspex optical box 324 is positioned around one portion of the tube and filled with glycerol. This reduces optical distortion and allows the internal volume of the tube to be clearly monitored by the CCD camera.
  • the reactor shown in Figure 1 may be used in the treatment of a fluid to remove contaminants, for example for ozonation of water, such as wastewater, to remove organic contaminants.
  • the reactor may also be used in CO2 sequestration.
  • the OBR shown in Figure 1 is a batch mode OBR, and fluid (not shown) is added to the OBR in batches for treatment.
  • the OBR could easily be modified with fluid inlets and outlets to provide a continuous mode OBR for continuous treatment.
  • the fluid is introduced to the reactor tube 301 up to a level (not shown) just above the uppermost baffle 309, to prevent any trapping of air from the headspace during oscillation.
  • the height of the liquid phase (hi_) is 450 mm.
  • Ozone gas is introduced from an ozone source 320 through the needle valve 213 and the gas line 322 and passes out of the sparger 323 into the water contained within the reactor tube.
  • the piston 313 is oscillated by the servo-hydraulic unit 316.
  • the fluid contained within the tube oscillates in an axial direction, passing back and forth through the series of baffles 309.
  • the baffles have the correct free open area a, as the fluid oscillates through the baffles a large number of microbubbles are generated within the fluid. The size and distribution of these may be monitored by the CCD camera 319.
  • the microbubbles are trapped within the inter-baffle region 312 by the strong radial mixing arising from the oscillatory motion of the fluid.
  • the microbubbles are trapped for a number of oscillatory cycles of the piston.
  • a consequence of the trapped microbubbles is that up to 100% of the ozone introduced into the reactor can be used in the ozonation reaction. Gaseous ozonation reaction products can be removed through the gas vent 325. The user can easily adjust the amplitude and frequency of oscillation of the piston to achieve the optimal generation of microbubbles in the reactor.
  • FIG. 2 shows the setup used for batch ozonation processes. It shows a longitudinal cross section of OBR 50 according to one embodiment of the present invention.
  • the OBR 50 includes a reactor tube 501 within which is situated a series of equally spaced baffles 502. At the base of the reactor tube is a piston 503 configured to oscillate in the manner shown by the double-headed arrow in Figure 2.
  • An oxygen cylinder 504 delivers oxygen to an ozone generator 505.
  • Ozone produced by the generator passes through a gas flow meter 506 and into an ozone inlet line 507.
  • the ozone then passes via a gas flow controller 508 to the OBR ozone inlet 509.
  • Ozone passes through the water 510 contained within the reactor tube 501.
  • the water can be recirculated within the reactor tube by means of the water recirculation line 51 1 , which includes a pump 512.
  • the water recirculation line has a flow capacity of 1 L/min.
  • Product gases which may include ozone pass out of gas outlet 513 and where recirculation is required (e.g. before any reaction has occurred and the gas passing out of the outlet is ozone) the gas passes into the ozone recirculation line 514.
  • the ozone recirculation line has a flow capacity of 10 L/min.
  • the outlet gases pass through the outlet line 515 which includes a damper 516.
  • the line also includes mass flow control 517.
  • the gases then pass along the gas line to the ozone analyser 518 via gas flow controller 519, before finally passing along another gas line to an ozone destroyer 520.
  • FIG 20 shows the OBR setup 60 used for continuous syngas bioconversion processes using anaerobic baceria.
  • the setup is very similar to that shown in Figure 1 , and the main parts of the OBR and its operation are identical and are therefore not relabelled and not discussed again here.
  • the OBR has however been adapted to be able to perform syngas bioconversion.
  • Syngas cylinder 601 supplies syngas consisting of 60 % CO, 30% H 2 and 10 % CO 2 .
  • the syngas passes through the inlet gas flow controller 602 and through a ball valve 614 before being sparged into the reactor tube of the OBR as described above in relation to Figure 1.
  • the reactor tube is surrounded by a water jacket 604 through which water is circulated from the water bath 605 in order to keep the reaction medium within the reactor at the correct temperature for syngas bioconversion.
  • Liquid from the reaction medium is recirculated through the liquid recirculation line 606 which feeds liquid back into the top of the OBR through the fluid inlet 603. Furthermore, a gas recirculation line 607 is able to feed gas which passes out of the OBR gas outlet 608 back to the gas inlet line. This is useful for example to ensure no waste of syngas which flows through the reactor before any reaction is in progress and is therefore not used up.
  • Gas exhaust line 609 carries exhaust gases from the gas outlet 608 via a non-return valve 610 and moisture trap 61 1 to outlet gas flow meter 612 before leaving through gas exhaust 613.
  • the setup includes various ball valves 614 to provide control over gas flow.
  • the setup also includes two diaphragm pumps 615 and a peristaltic pump 616.
  • the setup includes two gas sampling ports 617 and a liquid sampling port 618.
  • pressure gauge 619 and temperature probe 620 provide means for monitoring gas pressure and water temperature within the system.
  • the system also includes a Dreschel bottle 621 at the OBR gas outlet.
  • d c is the internal diameter of the column (m)
  • f the fluid oscillation frequency
  • ⁇ is kinematic fluid viscosity (kg nr s _ )
  • p is the specific mass of the fluid (kg nr 3 )
  • xo is the centre-to-peak fluid oscillation amplitude (m).
  • the Re 0 in the equation above was described in analogy to net flow Reynolds number where the product (2n-xo-f) represents the peak fluid velocity (m s _ ) during an oscillation cycle which occurs halfway the piston full stroke.
  • Both Reo and St have been modified to accurately represent the state of mixing in the multi-orifice baffled column and to support scale-up from single-orifice to multi-orifice OBRs.
  • d 0 s the "equivalent" diameter of the baffle area surrounding each open orifice
  • d c the main geometrical parameter controlling the flow separation and eddy formation, as opposed to do
  • d c which govern the properties of single-orifice OBRs.
  • This can be defined as: where, d c is the internal diameter of the column, a is the fraction of open area of the baffle, and n is the number of orifices in the baffle.
  • the Strouhal number St in the equation above has been modified to represent the actual ratio of diameter of column to fluid amplitude in the region around each individual orifice on the baffles in a multi-orifice baffled column.
  • the modified Strouhal number St' can therefore be written as:
  • Figure 13 shows the results of an experiment into ozone utilisation efficiency in the OBR according to the present invention.
  • the batch column was filled with 9 L of distilled water and spiked with 500 mg of p- hydroxybenzoic acid (p-HBA) yielding a molar concentration of 0.40 mM.
  • the concentration of p-HBA in the liquid was monitored along the ozonation time using chromatography, and the concentration of ozone was also monitored in the gas phase at both inlet and outlet points from the column.
  • the results shown in Figure 13 show 100% ozone utilization efficiency at very low superficial gas velocity during p-HBA degradation.
  • Ozone utilization efficiency was calculated based on: where E is ozone utilisation efficiency, C, is the ozone concentration at the ozone inlet and C 0 is the ozone concentration at the ozone outlet.
  • Ozone diluted in oxygen at a concentration of 0.48 mmol/L was injected with a superficial gas velocity of 0.46 mm/s in a batch column containing degassed distilled water with pH adjusted to 4.
  • the dissolved ozone concentration was monitored using a colorimetric assay.
  • the saturation ozone concentration was determined as 0.133 mM at 20°C.
  • the column showed similar performance for different amplitude and frequency combinations as shown in Figure 15(a).
  • a 150 mm internal diameter column with 9.6L of degassed distilled water and a total height of 540 mm was sparged with 5% v/v CO2 in air at atmospheric pressure and room temperature (20°C), at a superficial gas velocity of 0.81 mm/s. Dissolved CO 2 concentration was measured using a dissolved CO2 probe.
  • Table 1 below provides details of the three different baffle designs tested. Baffle designs 1-3 are depicted in Figure 3 (a)-(c) respectively.
  • Table 2 shows the effect of baffle geometry on volumetric mass transfer coefficient, kia for CO2 in water.
  • the inventive baffle design 3 (having a baffle open area of 15% i.e. less than 30%) allowed around 3-fold improvement in ki_a compared to unbaffled column or other baffle geometries.
  • Figure 4 shows six photographs from the optical observation of air bubbles rising in the inter-baffle region in the multi-orifice baffled column.
  • the scale bar corresponds to 10 mm.
  • the top row (a) includes photos taken of stagnant fluid, i.e. with no oscillations.
  • the bottom row (b) includes photos taken of oscillating fluid.
  • Columns (1)-(3) represent baffle designs 1-3 respectively (as shown in Figure 3). Table 3 below describes the aeration rates Qair and oscillation conditions used.
  • FIG. 5 shows bubble size distributions for the OBR including baffle design 1 ( Figure 5(a)-(b)) and baffle design 2 ( Figure 5(c)-(d)).
  • Each plot includes a distribution corresponding to bubbles generated in the OBR without oscillation (solid line) and one or more distributions corresponding to various oscillation conditions.
  • Figure 6 shows a bubble size distribution for inventive baffle design 3 where the OBR is oscillated at 2 Hz with an amplitude of 10 mm, alongside the corresponding distribution for the unbaffled column without oscillation.
  • Example 8
  • Figures 7-10 include plots of time tracking of (x,y) bubble position and instantaneous vertical bubble velocity (V y ) for bubbles in the inter-baffle region using the OBR configured with inventive baffle design 3, in each case the bubbles being selected at random.
  • the column conditions used in each case are given in Table 4 below.
  • FIG 11 shows flow visualisation of liquid mixing in the OBR configured with baffle design 2, using tracing polyamide particles.
  • Figure 12 shows flow visualisation of liquid mixing in the OBR configured instead with baffle design 3, using tracing polyamide particles.
  • Rows (a)-(c) represent three different fluid oscillation conditions as shown in Table 5 below.
  • Columns (1)-(3) represent three different time points in the oscillation cycle, as shown in the graph at the top right of Figure 12.
  • the horizontal lines which appear white in the photographs are adjacent baffles within the column.
  • the multi-orifice oscillatory baffled bioreactor (MOBB) used to perform syngas bioconversion experiments is shown in Figure 20.
  • the total volume of the column was 10.6 L, with a working volume of 9.1 L, and a total column height of 540 mm.
  • the inlet gas stream (syngas) consisted of synthetic syngas mixture with the following composition (v/v): 60 % CO, 30 % H 2 , and 10 % C0 2 .
  • the gas was fed directly from a pressured cylinder and sparged from the bottom of the MOBB, with flow rates continuously measured and controlled. At the outlet, gas flow rate was also continuously measured.
  • Gas mixture inside column was continuously recirculated from the headspace at a constant gas flow rate of 600 ml_ min- , in order to enhance gas-liquid contacting and make the syngas continuously available to the anaerobic microorganisms.
  • Figure 17 shows the syngas fermentation performance in the MOBB during continuous operation: (a) inlet and outlet syngas flow rate (Q syn gas (in), Qsyngas (out)) ' , (b) instantaneous methane yield from CO (YCHVCO), expressed as mmol of CH 4 produced per mmol of CO consumed (averaged by straight fitting), and instantaneous methane production rate (Fm,cH4), expressed in mmol CH 4 produced per gVSS in the liquid medium per day (averaged by exponential line).
  • Five different syngas flow rates were tested: (i) 5, (ii) 10, (iii) 20, (iv) 40, and (v) 100 ml_ mirr 1 .
  • Figure 17 shows a high molar yield of conversion of CO to methane, CH 4 , at a range of syngas flow rates.
  • Figure 18 shows the effect of specific CO loading rates: (a) on the specific reaction rates (r x ,/) for CO, H2 and CH 4 , and (b) on the removal efficiency of CO and H2, during the continuous syngas fermentations, in the MOBB.
  • Lines in graph (a) represent the fitting of data to typical Monod's model (R 2 > 0.99), while in graph (b) represent linear regression fitting (R 2 > 0.98). Vertical bars represent standard deviation.
  • Figure 18 shows up to 100% dissolution and conversion of CO and H2 to CH 4 at low gas inflow rates (the range tested was 0.03-0.63 mm S " ) .
  • Figure 19 shows carbon monoxide and hydrogen concentration profiles as measured in the headspace, during the dynamic gassing-out experiment performed in the MOBB.
  • the inlet superficial syngas velocity was 0.63 mm/s in phase (i) and (iii), and 0 mm/s in phase (ii), and fluid oscillation conditions were 2 Hz and 5 mm.
  • Baffle design 3 was used. Vertical dashed lines represent the time at which syngas flow was stopped and resumed.
  • a multi-orifice baffled column comprising a cylindrical glass column with maximum internal volume of 10L and internal diameter of 0.150m equipped with multi- orifice baffles having an average of 31 holes per baffle with an open orifice diameter of 10.5 mm and free baffle open area of 15% was set up for continuous ozontation.
  • a suitable system is shown in Figure 24. The setup is very similar to that shown in Figure 2, and the main parts of the OBR are identical and are therefore not discussed again here. Instead of recirculating the within the MOBC, clean water is continuously drawn off from the MOBC.
  • Baffles were spaced at 40mm, and the column continuously injected with water at pH 10+0.1 (adjusted with NaOH) containing 50 mg/L of a phenolic contaminant, p- hydroxybenzoic acid (p-HBA) and ozone diluted in pure oxygen at a concentration of 23 g/m 3 .
  • the working volume of the column was kept constant at 9L.
  • the ozone flow rate was varied from 2.1 to 4.7 L/min (corresponding to mean superficial gas velocities of 2.0 to 4.4 mm/s) and p-HBA flow rate set at 0.8 or 4.0 L/min (corresponding to mean hydraulic time of 2.25 and 1 1.25 min, respectively; the mean hydraulic time is defined as the ratio of internal working volume of the column divided by the liquid flow rate).
  • the fluid was oscillated with a 125mm outer diameter piston controlled by a PC and driven by a servo-hydraulic system at a frequency of 2 Hz and amplitude of 10 mm centre-to-peak.
  • the ozone content in both the inlet and outlet gas stream was monitored with an Anseros Ozomat GM-BWA ozone analyser. Liquid samples were collected at appropriate time intervals and filtered through 0.22 ⁇ , 33 mm Sterile Millex® Syringe Driven Filters (Millipore) for high performance liquid chromatography (HPLC) and total organic carbon (TOC) analysis.
  • HPLC high performance liquid chromatography
  • TOC total organic carbon
  • the inventors have compared the cumulative ozone supply and cumulative ozone need for p-HBA removal experiments (the last being a performance parameter for ozonation equipment), and the MOBC required 0.6-1.7 moles of ozone to fully degrade 1 mole of p- HBA, whereas the BC required 1.2-2.0 moles of ozone. Also surprisingly, the ozone cumulative need in the MOBC remains very similar for batch operation (estimated as 1.4 moles ozone per mole of p-HBA degraded as shown in Figure 16) and continuous operation.
  • the inventors have estimated the required energy input for producing fluid oscillations in the MOBC, based on equations available from literature for sparged oscillatory baffled columns (Baird and Carstang, Chemical Engineering Science, 1972, vol 27, pp 823-833). Considering a discharge coefficient, Cd equal to 0.7, the estimated power dissipation in the MOBC in Example 1 1 operating at a frequency of 2 Hz, 10 mm centre-to-peak amplitude and 9L working volume is approximately 8.4W. This demonstrates insignificant energy input required for producing the required fluid pulsations and achieve full ozone utilisation in the MOBC shown in the experimental data.

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Abstract

La présente invention concerne un réacteur à déflecteur oscillatoire à orifices multiples qui comprend un tube de réacteur, un déflecteur à l'intérieur du tube de réacteur, le déflecteur définissant une pluralité d'orifices, une source de gaz comprenant une évacuation à l'intérieur du tube de réacteur; et des moyen oscillatoires, lesquels, lors de l'utilisation, fournissent un écoulement oscillatoire d'un fluide par rapport au déflecteur. Le déflecteur présente une zone ouverte libre pouvant atteindre 30%.
PCT/GB2015/051975 2014-07-17 2015-07-08 Réacteur à déflecteur oscillatoire et procédé de réaction gaz/liquide WO2016009177A1 (fr)

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Cited By (4)

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Publication number Priority date Publication date Assignee Title
CN109550445A (zh) * 2018-12-12 2019-04-02 厉鼎 印染液搅均装置
WO2019126654A1 (fr) * 2017-12-22 2019-06-27 Cuello Joel L Bioréacteur à dispersion axiale (adbr) pour la production de microalgues et autres micro-organismes
EP3771489A1 (fr) * 2019-08-01 2021-02-03 Kraton Polymers Research B.V. Processus pour une réaction continue avec des matières premières dérivées de ressources bio-renouvelables
WO2023031391A1 (fr) 2021-09-03 2023-03-09 Stoli Catalysts Ltd. Réacteur à flux continu à insert amovible avec déflecteurs

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US4133714A (en) * 1975-10-03 1979-01-09 Vorobiev Jury P Reaction vessel with pulsating means for producing lignocellulose product from crushed vegetable raw materials
US6512131B1 (en) * 1999-10-29 2003-01-28 Dr. Frische Gmbh Process for carrying out multi-phase reactions according to the counter current principle of a liquid and gaseous phase and apparatus for carrying out the process

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2019126654A1 (fr) * 2017-12-22 2019-06-27 Cuello Joel L Bioréacteur à dispersion axiale (adbr) pour la production de microalgues et autres micro-organismes
CN109550445A (zh) * 2018-12-12 2019-04-02 厉鼎 印染液搅均装置
EP3771489A1 (fr) * 2019-08-01 2021-02-03 Kraton Polymers Research B.V. Processus pour une réaction continue avec des matières premières dérivées de ressources bio-renouvelables
US11608450B2 (en) 2019-08-01 2023-03-21 Kraton Corporation Process for a continuous reaction with feedstocks derived from Bio-Renewable resources
WO2023031391A1 (fr) 2021-09-03 2023-03-09 Stoli Catalysts Ltd. Réacteur à flux continu à insert amovible avec déflecteurs

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