JPH0542296B2 - - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION SUMMARY OF THE INVENTION Continuous systems, methods, and associated apparatus are disclosed for reacting gases and liquids to produce gaseous or liquid products. A preferred system consists of a reactive gas, such as chlorine, and an aqueous solution, such as caustic soda, which are combined continuously in turbulent parallel flow under sufficient overpressure in a very compact reactor apparatus. Make it react. Liquid bleaching solutions, such as aqueous solutions of hypochlorite or hypochlorous acid, are primarily among the products contemplated.
The main reactor system consists of a fluid pressure driven, in-line mixing system with a low slip (tight fit) regenerative turbine pump system connected in series. The fluid ports of the close-fit stator elements of the pump device should have a radial dimension at least equal to about half the vane.
In liquid ring compressors these ports are located adjacent to the lower part of the vanes, whereas in turbine pumps they are generally adjacent to the middle part of the vanes.

[Industrial application field]

TECHNICAL FIELD The present invention relates to technology that operates continuously on chemical reactions between gases and liquids. More particularly, it relates to improved systems, apparatus and methods for continuously producing fluid products from gas-liquid reactions of this type. Indeed, the systems and apparatus of the present invention perform gas-liquid reactions in a steady-state flow system to produce a desired gas of consistent quality in a controlled ratio to provide chemicals on demand for use in a continuous process, for example. or produce liquid products. A preferred system is one that produces a liquid product that does not contain significant amounts of insoluble solids. Examples of some particularly suitable gas-liquid reactions include: (1) obtaining a solution of hypochlorous acid and/or hypochlorite with chlorine gas and aqueous caustic solution; ( 2) Convert organic liquids into HCl, Cl ₂ , SO ₃ , O ₃ or NO ₂
(3) an aqueous solution of chlorite or chlorate material to form the corresponding liquid organic derivative by reacting with a gas such as
React with gases such as O ₃ , NO ₂ , Cl ₂ , HCl or SO ₂ to obtain chlorine dioxide as a gas or in solution.

[Conventional technology]

Systems and devices that operate on gas-liquid reactants in a continuous manner have traditionally been biased toward countercurrent flow of gas and liquid reactant streams. Examples of this dominant trend, which has been around for a long time and are worth noting, include the widespread use of operational equipment such as packed columns, bubble tray columns, spray towers, and the like.

A rare example of continuously producing fluid chemical reagents by reacting a gas with a liquid in a steady-state cocurrent flow system is described in U.S. Pat.
2889199 and 2965443, in which chlorine gas is reacted with an aqueous slurry of calcium hydroxide to produce a calcium hypochlorite bleaching solution. However, the reactors used in these patents do not consist of longer lengths or loops of conventional pipe (reference number 16 in the drawings). Other patents directed to gas-liquid mixing for the purpose of treating said liquids also disclose cocurrent flow devices and systems, such as U.S. No. 2,606,150 to Torp and U.S. No. 3,997,631 to Matsuoka et al. . These patents feature the use of a liquid jet eductor or ejector that mixes ozone gas into the liquid being treated, such as water. Similar ejectors are available, for example, in U.S. Pat.
No. 2,127,571 (Palday, Jr.), and in various systems and devices operating on gas-liquid reactions. However, U.S. Nos. 4,483,826 and 1,808,956 are directed only to batch or semi-batch operations, whereas the continuous reaction systems taught by U.S. Nos. 2,020,850 and 2,127,571 involve countercurrent flow between gaseous and liquid reactants. Due to the overall flow pattern, the parallel flow that occurs in the ejector device shown in the patent is only localized. Moreover, the devices and systems of the latter two references are inconvenient to operate, since they are both repeat complexes of all the various devices used therein, in particular ejectors, pumps, valves, separators, etc. extremely complex, expensive and difficult to use.

[Problem to be solved by the invention]

The primary object of the present invention is to provide a simple means to operate continuously on chemical reactions between reactant gases and reactant liquids under controlled conditions to produce gaseous or liquid products of consistent quality. It is to manufacture. The advantages and benefits associated with achieving this objective are particularly significant with regard to the economics and convenience of supplying products of this type for use in industrial manufacturing and processing where the products are difficult or expensive to transport or store. has. Another objective was to devise a simple, compact, in-line co-current flow device with strong agitation and turbulent gas-liquid internal mixing to promote the desired gas-liquid reactions and minimize the required residence time. It is to be. A further object is to provide a complete system for efficiently carrying out gas-liquid reactions of this type on a continuous basis with reliable and constant results. Other objects and advantages of the present invention will become apparent from the detailed description and specific embodiments that follow.

[Means to solve the problem]

The foregoing objects and advantages are achieved by carrying out the desired gas-liquid reaction using a fully parallel flow, in-line flow system comprising three main parts of the apparatus connected in series in the following order: (1) Homogeneous. a fluid pressure-driven, in-line, flow mixing device arranged to form a gas-liquid mixture; - adjacent cooperating stator elements arranged to create strong turbulence and interaction in the liquid mixture and at the same time increase the pressure of said mixture by at least one atmosphere; and (3) to maintain a substantial gas headspace. Sealed product receiving and gas/liquid separation tank with effective pressure regulation means and liquid level regulation means.

Said tank 3 preferably comprises a gas headspace and a conduit from its lower liquid space;
Gas and liquid supply lines are connected and each lead to said flow mixing device, thus allowing a portion of the gas and/or liquid to be formed from the circulating material through said device. Similarly, the desired gas -
The particular type of in-line, flow mixing device 1 that has been found most appropriate for initiating liquid reactions is the ventilated mixer, while the type of in-line, flow mixing device 1 that has been found to be most suitable for initiating liquid reactions is the ventilated mixer, while the type of in-line, flow mixing device 1 that has been found to be most appropriate for initiating liquid reactions is the ventilator mixer. Accepted regenerative turbine pumping means 2 are multi-stage turpin pumps or liquid ring compressors, with turbine pumps generally being preferred unless the liquid flow is a very small fraction of the gas flow by volume.

As generally described below, the present invention provides for rapidly achieving a chemical reaction between a reactant gas and a reactant liquid to (a) reactant liquid and/or reactant gas at a pressure substantially in excess of atmospheric pressure; continuously feeding a fluid-driven, in-line co-current flow mixing zone to form a homogeneous gas/liquid reaction mixture, and supplying said mixture from said zone to substantially no less than atmospheric pressure of at least one said reactant. (b) the gas/liquid reaction mixture discharged in (a) is discharged at a pressure lower than the pressure;
Strong gas/liquid interaction and high turbulence of the reaction mixture through the zone by introducing into the upstream end of a mechanically operated fluid propulsion zone driven adjacent to two side channel stators. (c) simultaneously increasing the pressure of said mixture by at least 1 atmosphere and draining said mixture at an absolute pressure of at least about 2 atmospheres; Producing a fluid product on a continuous basis by a process consisting of receiving a sealed product maintained at an absolute pressure of 2 atmospheres and with a substantial gas headspace above and introducing it into a gas-liquid separation zone. .

Of course, for many gas-liquid reactions, step (c)
Verify that it is desirable to circulate the separated gas and/or some of the gas from the gas/liquid separation zone back to the initial stage of the overall process, such as the in-line cocurrent mixing zone of step (a). obtain. Thus, in addition to the potential to improve product yields and obtain better utilization of reactants, the simplified recirculation feature of the system allows for example adjustments to production rates while maintaining good quality control. granular process flexibility, such as the ability to

The close cooperation and critical interdependence of the three main parts of the equipment incorporated into the gas/liquid reaction system identified above can be better appreciated from the following brief analysis of the functions each performs individually. Thus: (1) A fluid pressure-driven mixing device not only acts to form a homogeneous gas-liquid mixture, but also supplies the same uniformly to a regenerative turbine pump at at least about atmospheric pressure and preferably under superpressure. 2) A regenerative turbine pump with multi-blade impellers and cooperating side passage stator elements smoothly receives a uniform supply of mixed and easily reacting gases and liquids and effectively propels their passage; At the same time, the pressure is increased by at least 1 atm and the product is at a pressure of at least about 2 atm.
(3) a product receiving separation tank containing at least about two
Provided with liquid level and pressure regulating means to allow gas/liquid separation to occur under atmospheric pressure, delivering not only the product in a continuous manner but also the portion of the liquid and/or gas component to whatever extent desired. simplifies recycling. From the description of the basic equipment and the brief functional analysis mentioned above,
It will also be appreciated that the mixture 1 and the pump device 2 effectively act as reactors in the system, ie they actually provide the predominant zone or stage that achieves the desired gas-liquid reaction.
Due to the compact nature of these two parts of the apparatus and the high throughput volumes in which they operate effectively, the total residence time of the gas/liquid reaction mixture during passage therethrough is only a very small number of seconds, i.e. Typically, the amount is about 1 to 5 seconds.

Despite these limited residence times, excellent results in conversion and yield of reactants and quality of the desired products have been obtained in conducting facile gas-liquid reactions with the present system and apparatus. Possibly due to strong gas-liquid interactions and a high degree of turbulence, conversions of >90% are often obtained, e.g., without any recirculation, yet a homogeneous mixed-phase fluid flow is maintained in the active reaction zone and apparatus of the system. achieved. Similarly, yields of the desired product based on converted reactants are generally greater than 90%, indicating that little or no by-products are formed (e.g., chlorite rather than hypochlorite). salt or chlorate).

The present systems and devices are most advantageous when operating with highly reactive gas-liquid combinations that are thermodynamically favorable even at ambient temperatures. Of particular interest and relevance in the practice of the present invention is the reaction between an aqueous solution of a compound (such as a salt or hydroxide) and a gas such as chlorine to give a useful liquid and/or gaseous reaction product. For example, chlorine gas can react with a caustic soda solution to form a sodium hypochlorite solution useful in various infection control and bleaching treatments. Similarly, solutions of hypochlorous acid (HOCl) can be prepared by adjusting the proportions of caustic and chlorine reacting in a similar manner. Alternatively, a HOCl solution can be produced by reacting chlorine gas with carbonic acid or hypochlorite. Furthermore, a gaseous product stream containing an active reagent such as chlorine dioxide could be obtained by reacting an aqueous chlorite solution with a reactive gas such as _NO2 or _O3 .

〔Example〕

Referring to the drawings, the main components of the apparatus assembled herein include a bench turret mixer 14, a multi-stage regeneration turbine pump 16 and a product receiving tank 18, which are connected to fluid handling conduits 15 and 17. Concatenate continuously. The prime mover for the pump 16 is an electric motor 24, which is capable of driving a shaft on which the turbine impeller of the pump 16 is mounted at a speed of at least about 1000 rpm. The tank 18 is equipped with a pressure regulating valve 20 and a vent 21 to maintain the desired level of overpressure pressure.
and a liquid level controller 22 to ensure substantial gas head space. Vent 21 connects to a removal device or other sufficient cleaning device (not shown) to remove toxic gases.

A liquid reactant, e.g., dilute caustic solution, under suitable pressure is introduced axially through the feed line 11 through the injector nozzle 12 into the bench section 13 of the jet mixer 14, and gaseous chlorine at a lower pressure is introduced through the feed line 10. via which a plenum chamber of a jet mixer 14 surrounding the inlet to the bench lily 13 is fed. Because chlorine has a low boiling point, it can also be supplied as a cold liquid so that it flashes as it enters the plenum chamber. Feed lines 10 and 11 are connected to a source of chlorine 5 and a source of caustic solution 6, respectively, and are equipped with appropriate control valves 7 and 9 to regulate the reactant feed rate and pressure.

After passing through the bench urethane mass 14 and the turbine pump 16, the chlorine bulk reacts to form hypochlorite and the remaining reaction mixture is passed through the conduit 17.
through which the liquid product is drained into the product receiving tank 18, in the lower part of which the liquid product accumulates. If automatic feedback adjustment of the process is desired, a continuous monitor, such as a PH analyzer 32, can be used in the product delivery conduit 17.
It can be installed in a bypass line from The signal from this analyzer is then passed to a regulator 34 which has a preset PH reference point and compares this with said signal to ensure correct operation is effected through proportional adjustment of the chlorine feed rate regulating valve 9. Transfer continuously. This type of feedback regulation system is ideally suited for use in the present system due to its exceptionally short residence time.

A fluid handling conduit 23 containing a flow control valve 25 is connected to the gas headspace of the tank 18 and the gas supply line 10 to the ventilator mixer 14 to allow unreacted gases to be recycled back to the beginning of the process. Provided between. Additionally, for maximum flexibility, a liquid recirculation line is provided in the lower portion of the gas headspace of the tank 18 which is optionally routed through a control valve 29 and back to the liquid supply line of the ventilator mixer 14. It can have 27 characteristics. Finally, the tank 18 (to its liquid holding portion) has a drain line 28 that delivers liquid product from the system via a control valve 30 as permitted by the liquid level adjustments imposed by the controller 22. Also equipped.

As a result of the repressurization of the reaction mixture achieved with the regenerative turbine pump 16, it is very convenient to recirculate the remaining material from the product receiving gas/liquid separation tank 18 at the beginning of the process. Optimum results for maximum operational flexibility can be obtained using gas or liquid recycle streams (or both). Of course, the advantages realized by direct recirculation of gaseous reactants from gas/liquid separation tanks are usually greater when producing liquid products, but if the initial product is a gas, direct liquid recirculation is generally deserves priority consideration.

When producing sodium hypochlorite bleach by reacting chlorine with a dilute caustic soda aqueous solution,
The principle reaction involved proceeds as follows: 2NaOH (aq.) + Cl ₂ (g) → NaOCl (aq.) + NaCl (aq.) Stoichiometrically, this equation means that each pound of reacting 1.13 pounds of NaOH is required for _Cl2 , which theoretically yields 1.05 pounds of NaOCl and
0.83 lb of NaCl is obtained. In practice, a small excess of NaOH over the stoichiometry will result in a high pH sodium hypochlorite solution with good stability (e.g. a pH in the range of about 11 to 13 will result in a pH of about 5 to (commonly obtained by using a 15% excess of NaOH) is usually preferred. Thus, when making sodium hypochlorite in accordance with the present invention, approximately 1.2 to 1.3 pounds of chlorine is used per pound of chlorine.
The use of NaOH is recommended, as this facilitates better utilization of the chlorine reactant.

Liquid bleaches containing less than about 10% by weight NaOCl are desirable and are manufactured to avoid the need for unusual heat removal means or equipment in the system. Thus, the heat of reaction released will raise the temperature of the liquid bleach product containing about 10% by weight NaOCl to a maximum, even if the starting caustic soda solution is precooled to about 0°C by substantially Sufficient to achieve the desired temperature (ie about 40°C). Thus, a bleaching solution containing from about 1 to about 6% by weight NaOCl represents an ideal product to produce with the present continuous production system and, fortunately, is generally of initial interest in most industrial processing processes. in range.

Suitable reaction temperatures for the present system are very mild, generally similar to normal climatic temperatures, and the gas-liquid mixture formed here is maintained at a largely supraatmospheric pressure. Therefore, the first
The initial motive fluid pressure supplied to the staged in-line flow mixer 14 is generally at least 2 atmospheres absolute and is sufficient to drain the reaction mixture therefrom at a pressure not substantially less than atmospheric pressure, and the regenerative turbine pump 16 is provided to increase the pressure of the reaction mixture by at least one tenth of an atmosphere. Preferably, the turbine pump will have the ability to repressurize the reaction mixture drained into the product receiving tank 18 to a pressure at least as high as the initial motive fluid pressure supplied to the mixer 14.

Such use of this type of significant pressurizing pressure is
It is believed to be a beneficial factor that promotes the uniformity and performance of the desired reactions in this system. In particular, mixer 1
The propulsion of the gas/liquid reaction mixture through 4 and the pump device 16 becomes stabilized and remains very smooth and constant under conditions of significant overpressure of this kind. Mass transfer and overall reaction rates generally increase through compression, for example as a result of increased solubility of gases in liquids and other similar effects. Thus, the preferred pressure for the initial motive fluid as well as the contents of the product receiving tank 18 is approximately
The preferred pressure of the reaction mixture drained from mixer 14 and supplied to pump 16 is from about 20 to about 40 psia, although it may be from about 40 to about 80 psia.

As set forth in the foregoing description and discussion thereof, the flow sheet illustrations illustrated in the accompanying drawings more particularly illustrate the principles of operation of the present invention and illustrate specific embodiments of a sufficient apparatus for successfully putting it into practice. It is shown for identification. In addition to these major alternatives already specified, it will be apparent to those skilled in the art that many other minor variations and substitutions are equally possible.

Thus, it is possible to operate either or both of the main reactor devices (eg, jet mixer 14 and pump 16) in a non-horizontal position.
For example, if the pump 16 is provided with a top inlet,
It may be more advantageous to operate the jet mixer horizontally with an in-line conduit connecting to the pump inlet. Similarly, other mechanisms that apply automatic feedback adjustments to the system may be used in place of the PH analyzer 32 and associated regulator 34. For example, similar equipment based on the measurement of other product properties (eg redox potential) can often be used instead, eg when producing solutions of hypochlorite, hypochlorous acid, etc.

The following specific operational examples are included herein to further illustrate the details of the operation and ideas involved in the successful practice of the invention, but the foregoing examples do not imply any critical limitations to the useful scope of the invention. should not be configured as

EXAMPLE OF OPERATION This example illustrates the use of a system essentially similar to that shown in the accompanying drawings to produce an aqueous bleaching solution containing approximately 2% by weight NaOCl.

With reference to the drawing above, 100 gallons per minute of 0.6 molar NaOH solution (24 grams NaOH per liter)
is fed at a pressure of 40 psig through a 2-inch pipe connection to the nozzle 12 of the bench urethane mixer 14, which would otherwise have a 3-inch pipe connection, delivering a total of 17.2 pounds of chlorine gas per minute. A pressure of approximately 10 psig is supplied to the plenum chamber surrounding the nozzle 12. The resulting chlorine-caustic reaction mixture is drained from the bench lily mixer and sent via conduit 15 to the inlets of the three stages at approximately 15 psig, while the low NPSH turbine pump 1
6 has a turbine impeller in each stage,
Driven by 20H.P.1800rpm motor. Each turbine impeller has approximately 20 blades and is a tight fit between the channel ring stator elements. (At least 6 blades per impeller are required for effective operation, with anywhere from 10 to 30 blades being preferred depending on the rotor diameter.) The reaction mixture is drained from pump 16 at about 50 psig, discharging 20 gallons. tank 18 with a liquid level regulator set to maintain the liquid/gas interface at about 30-70% of the tank height and a pressure controller set at about 45-50 psig.

The separated liquid and gaseous phases forming in said tank were evaluated such that the resulting liquid bleaching solution was found to have a pH of about 12 and a strength of about 1.97% NaOCl by weight, but unreacted chlorine per minute. It accumulated there at the rate of a pound. These numbers indicate that about 94% of the chlorine fed was reacted and the yield of NaOCl based on the reacted chlorine was about 98%.

Then, supply fresh chlorine to mixer 14.
0.9 lb/min to a rate of 16.3 lb/min, except that 0.9 lb/min of unreacted chlorine is recirculated from tank 16 via conduit 23 and introduced into mixer 14 with said fresh chlorine. Operation resumed on the same system. Neither the quality of the liquid bleaching product nor the rate of collection of unreacted chlorine was affected by this modified operation, demonstrating the ease of recycling unreacted chlorine and obtaining its effective utilization in the present system. Ta.

Having described our invention, including its basic principles, illustrative embodiments, and various useful modifications and variations thereof, it is intended that the scope of the appended claims be limited only by their own clear and specific terms. ,
We do not intend to be limited by any inclusion of gratuitous charges or specific details or exemplary terms set forth herein for illustrative purposes only.

[Brief explanation of the drawing]

Attached FIG. 1 is a simplified diagram representing a typical flow sheet of a continuous process for carrying out gas-liquid reactions in accordance with the present invention. This flowsheet diagrammatically shows the main units of a given device,
How can this type of equipment be combined and operated as a system for constant-feed, long-term production of liquid reagents, such as dilute aqueous sodium hypochlorite bleach solutions, through the continuous reaction of chlorine gas with dilute caustic solution? Show what you get. 5...Chlorine source, 6...Caustic alkaline solution source, 7
... Control valve, 9 ... Control valve, 10 ... Supply line, 11 ... Supply line, 12 ... Injector nozzle, 13 ... Bench lily part, 14 ...
Bench ridge mixer, 15...Fluid handling conduit, 16...Multi-stage regeneration turbine pump, 17...
Fluid handling conduit, 18...product receiving tank, 2
0...Pressure control valve, 21...Vent, 22...
...Liquid level controller, 23...Fluid operation conduit, 2
4...Electric motor, 25...Flow control valve, 2
7...Liquid recirculation line, 28...Drainage line,
29...control valve, 30...control valve, 32
... PH analyzer, 33 ... transfer means, 34 ... regulator.

Claims (1)

Claims: 1. A compact assembly of devices for sequentially effecting a chemical reaction between concurrently flowing gaseous and liquid reactants to form a desired liquid product, in the order specified. The following units are closely connected in series: (a) Separate inlets for gas and for liquid in close proximity to the inlet ends, plus means and consequent means for continuously supplying gas and liquid to said inlets, respectively; (b) at least one mechanically driven multi-blade vane with an interference fit stator element; a sealed, regenerative turbine pump means having a wheel, said pump means constantly propelling a gas/liquid mixture through said pump means to an outlet thereof, and simultaneously increasing the pressure of said gas/liquid mixture by at least 1. (c) regenerative turbine pump means adapted to increase air pressure; (c) an outlet of said flow mixing device and said sealed;
a fluid transfer conduit to and from the inlet of the regenerative turbine pump means; and (d) a seal comprising pressure regulating means and liquid level regulating means to maintain a desired overpressure pressure and substantial gas headspace; an overpressure, pressure-tight, product receiving tank, wherein an inlet opening disposed in a side wall of said tank and a fluid transfer conduit connect said inlet opening and said outlet from the regeneration pumping means of (b); characterized in that the tank comprises a product receiving tank also comprising a fluid circulation conduit connecting the gas head space and the lower liquid holding space to the gas and liquid supply means for said cocurrent flow mixing device of (a). A small assembly of devices for 2. The compact assembly of apparatus of claim 1, wherein the means for continuously supplying liquid to the liquid inlet of the flow mixing apparatus of (a) is capable of supplying liquid at a pressure of at least about 40 psia. 3. The apparatus of claim 2, wherein said mixing device comprises a ventilator mixer. 4. The apparatus of claim 1, wherein the regenerative turbine pump means of (b) has at least two stages comprising a multi-blade impeller and has drive means adapted to rotate said impeller at a speed in excess of 1000 rpm. A small collection of. 5. A device assembly according to claim 4, wherein each impeller has at least 10 blades. 6. The apparatus assembly of claim 4, wherein said pumping means is a self-charging regenerative turbine pump. 7. In providing a continuous supply of a dilute aqueous hypochlorite bleaching solution of consistent quality by reacting chlorine gas with a dilute aqueous caustic solution, (a) continuously feeding stoichiometric proportions of chlorine gas and a dilute aqueous solution of caustic soda to the upstream end of a superpressurized, pressurized, fluid-driven, in-line, co-current flow mixing zone to form a homogeneous gas-liquid reaction mixture; draining said mixture from the downstream end of said mixing zone at a pressure not substantially less than atmospheric; (b) transferring the reaction mixture drained in (a) to the upstream end of a mechanically operated regeneration, fluid propulsion direct introduction and repressurization of a pump zone in which at least one multi-blade rotary impeller is driven adjacent to the side flow stator to direct strong gas/liquid interaction and transfer of the reaction mixture through said pump zone. (c) imparting a high degree of turbulence and simultaneously increasing the pressure of said mixture by at least about 1 atmosphere and draining said mixture at a pressure of at least 2 atmospheres absolute; introducing the sealed product into a receiving and gas-liquid separation zone maintained at an absolute pressure of 2 atmospheres and with a substantial gas headspace provided above; (d) the resulting liquid; (e) collecting at least one of the bleaching solutions as product in the lower part of said separation zone and unreacted chlorine gas in said headspace;
recirculating some of the two fluids back to the upstream end of said cocurrent flow mixing zone of step (a), continuously supplying a constant supply of dilute aqueous hypochlorite bleaching solution of consistent quality; How to give. 8 The concentration of the dilute aqueous solution of caustic alkali soda and the ratio at which it reacts with the chlorine gas are adjusted to about 1
8. The method of claim 7, wherein the method is adjusted to provide a liquid bleaching solution containing ~6% by weight of sodium hypochlorite. 9. The process of claim 7, wherein unreacted chlorine gas and liquid bleach solution collected in the separation zone of (d) are recycled to the upstream end of the cocurrent flow mixing zone of (a). 10. The method of claim 7, wherein steps (a) and (b) are carried out in only a few seconds. 11. Claim in which the pressure maintained in the separation zone described in step (c) is about 40 to 80 psia and greater than that of the superpressurized pressurized fluid serving to drive the cocurrent flow mixing zone of step (a). 7. The method described in 7. 12. In effecting a chemical reaction between gaseous and liquid reactants in a continuous manner, (b) continuously supplying at least one said reactant, thereby forming a homogeneous gas-liquid reaction mixture; (c) draining said gas-liquid reaction mixture from the downstream end of said mixing zone at a pressure not less than atmospheric pressure; Mechanically operated, regeneration, driven at high speed adjacent to the flow path stator
Direct fluid propulsion and repressurization to a pump zone to effect strong gas/liquid interactions and high turbulence of the reaction mixture through the pump zone, while simultaneously increasing the pressure of the mixture by at least about 1 atmosphere. elevating and draining said mixture therefrom at a pressure of at least about 2 atmospheres absolute; and (d) subjecting the mixture drained in (c) and thus pressurized to a regulated pressure of at least about 1 atmosphere above atmospheric pressure. overpressure, pressure sealing, product receiving and gas/liquid separation zone with liquid level control means provided to maintain a significant amount of gas head space and also maintain a large liquid holding space in the lower region. (e) the desired liquid product is collected in the lower region of said gas-liquid separation zone and unreacted gaseous accumulations are collected in said gas headspace; (f) the gas collected in said headspace; and (d) recycling some of the liquid that accumulates in the lower region of the separation zone of (a) back to the upstream end of the cocurrent flow mixing zone of (a). A continuous method of action of chemical reactions between bodies. 13. wherein said liquid reactant is provided in (a) at about 40 psia or more and said zone (d) is maintained at a regulated pressure greater than the pressure at which said liquid reactant is provided in (a).
The method described in 2. 14 Gaseous reactants include Cl ₂ , HCl, SO ₃ , O ₃ and
13. The method of claim 12, wherein the liquid reactant is an organic liquid selected from the group consisting of _NO2 . 15. The method of claim 12, wherein the gaseous reactant is _Cl2 and the liquid reactant is an aqueous solution of an alkali metal salt or hydroxide. 16. In effecting a desired reaction between gaseous and liquid reactants flowing in parallel streams to continuously produce a desired liquid product substantially free of solids, (a) said reactants are mixed with 0.1 (b) continuously feeding the upstream end of a fluid pressure-driven, in-line, co-current flow mixing zone at a rate that provides a volume ratio of liquid to gas that exceeds, and introducing at least one said reactant at an overpressure pressure; the resulting gas-liquid reaction mixture formed in a) from the downstream end of said mixing zone at a pressure less than the pressure at which the at least one fluid reactant is supplied in (a) but not substantially less than atmospheric pressure; (c) said reaction mixture drained in (b) is removed by at least one multi-blade rotating impeller adjacent to a side flow path stator driven at high speed mechanically operated. ,
Regeneration, multi-stage fluid propulsion and repressurization directly to the upstream end of the pumping zone to effect strong gas-liquid interactions and high turbulence of the reaction mixture through the pumping zone, while at the same time at least about 1 atm. (d) increasing the pressure of the mixture and draining the mixture therefrom at a pressure of at least about 2 atmospheres absolute, and (d) retaining the mixture drained in (c) above at a pressure of at least about 2 atmospheres absolute; (e) passing the desired liquid product to a sealed product receiving and gas-liquid separation zone having a substantially large gas headspace; (f) recycling the at least one liquid product and the unreacted gas from (e) back to the upstream end of the cocurrent flow mixing zone of (a); A method of continuously acting on a desired reaction between gas and liquid reactants flowing in cocurrent flow. 17. The method of claim 16, wherein the gaseous reactant is _Cl2 and the liquid reactant is a dilute aqueous solution of an alkali metal hydroxide.