JPH01274835A - Method and apparatus for continuous reaction of gas and liquid - Google Patents

Abstract

PURPOSE: To continuously and effectively effect a gas-liquid reaction with a simple structure by tightly connecting a pressurized, liquid driven inline parallel flow stream mixing device, a regeneration turbine pump means and a product accepting tank. CONSTITUTION: The apparatus has a venturi jet mixer 14 as a main unit component, the multistage regeneration turbine pump 16 and the product accepting tank 18 and are continuously connected by fluid operating conduits 15, 17. A liquid reactant like a dilute caustic alkali soln. under an adequate pressure is introduced through a nozzle 12 into the venturi part 13 of a jet mixer 14, by which the gaseous chlorine of the lower pressure is supplied via a supply line 10 to its circumference. The chlorine bulk past the mixer 14 and the turbine pump 16 reacts to form hypochlorite. The remaining reaction product is drained into the product accepting tank 18 and the liquid product is accumulated in the lower part. The unreacted gas is recirculated and is returned to the beginning of the process.

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 a water container, such as a caustic sorter, which is carried out in turbulent parallel flow under sufficient overpressure in a very compact reactor device. Continuous combinatorial reactions.

Liquid bleaching solutions, such as aqueous solutions of hypochlorite or hypochlorous acid, are primarily intended products. 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 port of the mating stator element 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 of the vanes.

[Industrial application field]

The present invention relates to technology C that acts 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. In fact, the system and apparatus of the present invention allows gas-
Liquid reactions are carried out to produce desired gas or liquid products of consistent quality at controlled ratios that provide chemicals as needed for use, for example, in a continuous process. 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) Organic liquid with HCI, (,7!, ,Sol,O
(3) an aqueous solution of chlorite or chlorate material by reacting with a gas such as NOx or NO to produce the corresponding liquid organic derivative;
, , No2, Cl, , HCI or SO2 to obtain chlorine dioxide as a gas or in solution.

[Conventional technology]

Systems and devices that operate continuously on gas-liquid reactants have traditionally been biased toward retrograde 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 +41 that continuously produces fluid chemical reagents by reacting gases with liquids in a steady-state cocurrent flow system.
is described in U.S. Pat. Nos. 2,889,199 and 2,965,443 to Ofborn et al., in which chlorine gas is reacted with an aqueous slurry of calcium hydroxide to produce calcium hypochlorite bleach. Produce a solution. However, the actors used in these patents do not consist of longer lengths of conventional pipe or loops (reference numeral 16 in the drawings).

Other patents directed to gas-liquid mixing for the purpose of treating said liquids include U.S. 2.60 to Trube.
No. 6.150 and U.S. No. 3.997.6 by Sairiki Matsu et al.
Also disclosed are cocurrent flow devices and systems such as No. 31. These patents feature the use of liquid jet eductors or ejectors that mix ozone gas into the liquid being treated, such as water. Similar ejectors are disclosed, for example, in U.S. Pat.
, No. 020,850 (Michlen et al.), and No. 2,12
7.571 (Palday, Jr.), gas-
It was also used in various systems and devices that operate on liquid reactions. However, U.S. No. 4.483,826 and No.
The continuous reaction system taught by No. 50 and No. 2,127.571 relies on a retrograde integrated flow pattern between the gaseous and liquid reactants, and the parallel flow that occurs in the ejector apparatus shown in said patents is It's just localized.

Moreover, the devices and systems of the latter two references are inconvenient to operate, since they are both repeating 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 cocurrent 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; (2) a sealed regenerative turbine pump means comprising one or more mechanically driven multi-bladed impellers and a gas-liquid mixture during propulsion; - creating strong turbulence and interactions in the liquid mixture;
(3) a seal comprising adjacent cooperating stator elements arranged to simultaneously increase the pressure of said mixture by at least one atmosphere; and (3) pressure adjustment means and liquid level articulation means effective to maintain a substantial gas headspace. Product receiving and gas/liquid separation tanks.

Said tank (3) is preferably equipped with conduits to the gas/nod space and from its lower liquid space, connecting gas and liquid supply lines leading respectively to said flow mixing device and thus passing through said device. or allowing a portion of the liquid to be formed from circulating material. Similarly, specific ft. of in-line, flow mixing equipment (1 ft.) identified as most appropriate to initiate the desired gas-liquid reaction.
) is a Venturi jet mixer, while the regenerative turbine pumping means (2) found most effective in promoting the completion of the advanced stages of this type of reaction is a multi-stage turbine pump or liquid ring compressor; Turbine pumps are generally preferred unless the liquid flow is a very small fraction of the gas flow by volume.

JL (as described below), the present invention provides for rapidly achieving a chemical reaction between a reactant gas and a reactant liquid to (a) release the reactant liquid and/or the reactant liquid at a pressure substantially above atmospheric pressure; continuously supplying reactant gases to a fluid-driven, in-line cocurrent flow mixing zone to form a homogeneous gas/liquid reaction mixture, and transporting said mixture from said zone to a pressure not substantially below atmospheric pressure, but at least one of said reactants. at least one multi-bladed rotary impeller drives the gas/liquid reaction mixture to be drained at a pressure lower than the supply pressure of the body (bJ at the upstream end of a mechanically manipulated fluid propulsion zone to exert strong gas/liquid interactions and a high degree of turbulence of the reaction mixture through said zone, while simultaneously increasing the pressure of said mixture by at least 1 atm. (c) raising the mixture to an absolute pressure of at least about 2 atmospheres (bl) and draining the mixture therefrom at a pressure of at least about 2 atmospheres absolute;
A fluid product is produced on a continuous basis by a process consisting of introducing a sealed product-receiving and gas-liquid separation zone maintained at atmospheric pressure absolute and with a substantial gas headspace above.

Of course, for many gas-liquid reactions, some of the separated gas and/or gas from the gas/liquid separation zone of step (c) may be recycled to an in-line cocurrent mixing zone such as step (a). The desirability can be verified by going back to the beginning of the whole process. Thus, in addition to the potential to improve product yields and obtain better utilization of reactants, the simplified circulation feature of the present system allows for example adjustments to production rates while maintaining good quality control. The ability to provide fine-grained process flexibility.

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: +11 The fluid pressure-driven mixing device not only acts on the formation of a homogeneous gas-liquid mixture, but also supplies the same uniformly to the regenerative turbine pump at at least about atmospheric pressure and preferably under superpressure, (2) A regenerative turbine pump with multi-bladed impellers and side flow stator elements receives a uniform supply of mixed and easily reacting gases and liquids, effectively propelling their passage, while at least 1
(3) the product receiving separation tank is under a pressure of at least about 2 atmospheres; liquid level and pressure regulating means to allow gas/liquid separation to occur in a continuous manner, allowing for simple delivery of the product in a continuous manner as well as partial recycling of the liquid and/or gas components to whatever extent desired. become

From the basic equipment description and the brief functional analysis above, it can be seen that the mixture (1) and the pumping device (2) effectively act as reactors in the system, i.e. they achieve the desired gas-liquid reaction. It will also be understood that it actually provides a dominant band or stage. 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. The typical amount is about 1-5 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 or chlorine rather than hypochlorite). acid salts).

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 in the practice of the invention (
Suitable are aqueous solutions of compounds (e.g. salts or hydroxides) which give useful liquid and/or gaseous reaction products.
and a gas such as chlorine. 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, hypochlorous acid (HOI)
Solutions of can be prepared in a similar manner by adjusting the proportions of reacting caustic and chlorine. Alternatively, a HOCβ solution can be produced by reacting chlorine gas with carbonic acid or hypochlorite. Additionally, a gaseous product stream containing an active reagent such as chlorine dioxide can convert the aqueous chlorite solution into NO2 or 0. It could be obtained by reacting with a reactive gas such as

〔Example〕

Referring to the drawings, the main components of the installation F assembled herein include a Venturi Chef 1" mixer 14, a multi-stage regenerative turbine pump 16 and a product receiving tank 18, which are connected to fluid handling conduits 15 and 17. The prime mover of the pump 16 is an electric motor 24, which is capable of driving the shaft on which the turbine impeller of the pump 16 is mounted at a speed of at least about 1100 rpm. 18 is a pressure regulating valve 20 and vent 21 that maintains the desired level of overpressure pressure.
A liquid level controller 22 is provided to provide a substantial gas headspace. Vent 21 is equipped with a removal device or other sufficient cleaning device (not shown) to remove toxic gases.
Connect to.

A liquid reactant, e.g. dilute caustic solution, under suitable pressure is introduced axially via feed line 11 through an injection nozzle 12 into the venturi section 13 of jet mixer 14, and gaseous chlorine at a lower pressure is introduced into feed line 10. via a plenum chamber of a jet mixer 14 surrounding the inlet to the venturi section 13. Because chlorine has a low boiling point, it can also be supplied as a cold liquid so that it can be flash vaporized upon entering the plenum chamber. Supply lines 10 and 11 each have a chlorine source 5
and suitable control valves 7 and 9 connected to the caustic solution source 6 and articulating the feed rate and pressure of the reactants.
Equipped with.

Venturi jet mixer 14 and turbine pump 1
After passing through 6, the chlorine bulk reacts to form hypochlorite and the remaining reaction mixture drains via conduit 17 into a product receiving tank 18, in the lower part of which the liquid product accumulates. If automatic feedback regulation of the process is desired, a continuous monitor, such as a pH analyzer 32, may be installed in the bypass line from the product delivery conduit 17. The signal from this analyzer is then passed to a regulator 34 which has a preset pH reference point and compares said signal with it to ensure correct operation is effected through proportional adjustment of the chlorine feed rate control valve 9. Transfer continuously. This type of feedbank conditioning 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 between the gas headspace of the tank 18 and the gas supply line 10 to the venturi jet mixer 14 to allow unreacted gases to be recycled back to the beginning of the process. Provided for. Additionally, for maximum flexibility, a liquid recirculation line 27 is provided in the lower part of the gas headspace of the tank 18 which is optionally routed back to the liquid supply line of the venturi jet mixer 14 via a control valve 29. characteristics.

Finally, the tank 18 (in its liquid holding part) is connected to the controller 2
Also provided is a drain line 28 that delivers liquid product from the system through a control valve 30 as permitted by the liquid level joint imposed by 2.

As a result of the repressurization of the reaction mixture achieved with the regenerative turbine pump 16, the product receiving gas/liquid separation tank 1
It is very convenient to recirculate the remaining material from 8 at the beginning of the process.

Gas or liquid recycle streams (or both) can be used to obtain the most favorable results for maximum operational flexibility. 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 reacting chlorine with a dilute aqueous caustic soda solution to produce sodium hypochlorite bleach, the principle reaction involved proceeds as follows: 2NaOH(aq, ) + Cf!
2 (g)-NaOCl (aQ, )+NaCl(aq
. ) Stoichiometrically, this equation requires 1.13 pounds of NaOH for each pound of Cl reacted, which theoretically yields 1.05 bonds of Na OC
1 and 0.83 bonds of NaCl are obtained. Actually,
Chemistry? An unreasonably small excess of NaOH is necessary because high pH sodium hypochlorite solutions result in good stability (e.g., pH in the range of about 11-13 is about 5-15% (commonly obtained by using excess NaOH) is usually preferred. Therefore, when making sodium hypochlorite according to the present invention, it is recommended to use approximately 1.2 to 1.3 bonds of NaOH per bond of chlorine, which allows for better utilization of the chlorine reactant. Facilitate.

Liquid bleaches containing less than about 10% by weight Na0C6 are desirable because they are manufactured to avoid the need for unusual heat removal means or equipment in the system. Thus, the heat of reaction released is about 10 fI even though the starting caustic soda solution is precooled substantially all the way to about 0°C.
This is sufficient to bring the temperature of the liquid bleaching product containing fEf% Na0Cl to the maximum desired temperature (ie about 40°C). Therefore, approximately 1...approximately 6% by weight N; 30
Bleaching solutions containing Cβ represent an ideal product to produce with the present continuous production system and are fortunately generally in the range of initial interest in most industrial processing processes.

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. Thus, the first stage in-line flow mixer 14
The initial motive fluid pressure supplied to the regenerative turbine pump 16 is generally at least 2 atmospheres absolute and sufficient to pump the reaction mixture therefrom at a pressure not substantially less than atmospheric pressure, and the regenerative turbine pump 16 is at least 1 Atmospheric pressure is provided to increase the pressure of the reaction mixture. 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 significantly increased pressure is considered an advantageous factor in promoting the uniformity and performance of the desired reaction in the present system. In particular, mixer 14 and pump device 1
The propulsion of the gas/liquid reaction mixture through 6 becomes stabilized and remains very smooth and constant under conditions of significant overpressure of this type. The mass transfer and total reaction rate are
It generally increases 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 product receiving tank 18 is about 40 to about 80 psia.
However, the preferred pressure of the reaction mixture drained from mixer 14 and supplied to pump 16 is from about 20 to about 40 ps.
It is ia.

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 primary alternatives already specified, it will be apparent to those skilled in the art that many other minor variations and gastric perfusions are equally viable.

Thus, it is possible to operate either or both of the main actor equipment (eg jet mixer 14 and pump 16) in a non-horizontal plane. For example, if the pump 16 is provided with a top inlet inlet, it may be more advantageous to operate the jet mixer horizontally with an in-line conduit connecting said pump inlet. Similarly, other mechanisms for passing automatic feedback adjustments to the system may be used in the analyzer 3
2 and cooperating regulator 34. For example, similar devices based on measurements 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 operation and ideas involved in the successful practice of the invention;
■It should not be constructed as including any critical limitation.

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% Na0Cβ by weight.

Referring to the above drawing, 100 gallons per minute of 0.6 molar NaOH solution (24 grams NaOH per liter)
A pressure of 0 psig is supplied to the nozzle 12 of the venturi jet mixer 14 via a 21' pipe connection, which would otherwise have a 3 inch vibe connection;
11 gases for a total of 17.2 pounds per minute at approximately IQpsi
A pressure of g is applied to the plenum chamber surrounding the nozzle 12. The resulting chlorine-caustic reaction mixture is drained from the Venturi mixer via conduit 15 to
．． 7 and send it to the entrance of three stages at about X5 psig, but the low N
P S H turbine pump 16 has a turbine impeller in each stage, 20H,P.

Driven by a 1800 r p rn motor. Each turbine impeller has approximately 20 blades and is a tight fit between the channel ring stator elements.

(At least 60 blades per impeller are required for effective operation; any number of 10=30 blades per rotor is preferred.) The reaction mixture is drained from pump 16 at about 50 psig to 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 regulator set at about 45-5 Q psig. do.

The separated liquid and gaseous phases that form in the tank are such that the resulting liquid bleaching solution has a pH of about 12 and an N of about 1.9711%.
a OCI! unreacted chlorine accumulated there at a rate of about 1 bond per minute. These numbers are based on the chlorine that reacts, with approximately 94% of the supplied chlorine reacting! It shows that the yield of Na0ce with a value of 7 was about 98%.

Thereafter, the supply of fresh chlorine to mixer 14 is reduced by 0.9 bonds/min to a rate of 16.3 bonds/min and 0.9 bonds/min.
9 bonds/min of unreacted chlorine is recirculated from tank 16 via conduit 23 and sent to mixer 14 along with said fresh chlorine.
The quality of the 6-liquid bleach product and the rate of collection of unreacted chlorine were not affected by this modified operation, and the unreacted chlorine in this system was The ease of recirculating the reaction chlorine and obtaining its effective use was demonstrated.

Having described our invention, including the basic principles, illustrative embodiments and useful modifications of the species and variations thereof,
The scope of the claims as set forth is: 6 limited only by their own clear and specific terms, and does not include any inclusion or typicality of any gratuitous imposition or specific details set forth herein for illustrative purposes only. We do not intend to be limited by these conditions.

[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 floater-1 illustrates the main components of a given device, such as sodium hypochlorite bleach, dilute water, etc. It is shown how this type of apparatus can be operated in combination as a system for constant supply, long-term production via continuous reaction of liquid reagents such as g-liquid with chlorine gas and dilute caustic solution. 591. Chlorine source 600. Caustic solution source 78
0. Control valve 982. Control valve 10, supply line 11. ,, Supply line! 2. ．． ．． Injector nozzle 13, Venturi section 14, Venturi jet mixer 15, Fluid handling conduit 16, Multi-stage regeneration turbine pump 17, Fluid handling conduit 18, Product receiving tank 20, Pressure Control valve 21. ,,Bent 22,. , liquid level controller 23. , , fluid handling conduit 24 , .
, electric motor 25. ,,flow control valve 27. ,
, liquid recirculation line 28. ,,Drainage line 29,,,
Control valve 30. ,,control valve 32,,,p
H analyzer 33. ,,Transfer means 34,,, Articulating device patent applicant Quantum Technologies Incorporated Procedural amendment was filed on July 6, 1988 by the Commissioner of the Patent Office Yoshi 1) Wen Yi 1, Indication of the case 1988 Patent Application No. 104363 No. 2, Name of the invention Method and apparatus for continuous reaction between gas and liquid 3, Relationship with the case of the person making the amendment Patent publication name Quantum Chikunoroses Inc. Richard Jay Gear Latch (national elutriation)
(America's 4, agent

Claims (1)

Claims: (1) A compact assembly of devices for sequentially effecting chemical reactions between concurrently flowing gaseous and liquid reactants to form a desired liquid product, as specified The following units are closely connected in series in sequence: (a) separate inlets for gas and for liquid in close proximity to the inlet ends, plus means for continuously supplying said inlets with gas and liquid, respectively; a pressurized, fluid-driven, in-line co-current flow mixing device having an outlet for draining the resulting gas/liquid mixture; and (b) at least one mechanically driven multiplexer having an interference fit stator element. A sealed, regenerative turbine pump means having an impeller, 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. (c) a fluid transfer conduit between the outlet of the flow mixing device and the sealed inlet of the regenerative turbine pump means; and (d) ) a sealed, overpressure, pressure-sealed, product receiving tank comprising pressure regulating means and liquid level regulating means to maintain a desired overpressure pressure and substantial gas headspace, the side wall of said tank comprising: An inlet opening and a fluid transfer conduit located in (a) connect said inlet opening and said outlet from the regeneration pumping means of (b), and said tank connects a gas headspace and a lower liquid holding space to said fluid transfer conduit in (a). A compact assembly of equipment characterized in that it consists of a product receiving tank also comprising fluid circulation conduits connected to gas and liquid supply means for a cocurrent flow mixing device. 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 Venturi jet mixer. 4. The regenerative turbine pumping means of (b) having at least two stages with multi-blade impellers and having drive means adapted to rotate said impellers at speeds in excess of 1000 rpm. A small assembly of devices. 5. The apparatus assembly of claim 4, wherein each impeller has at least ten 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) at least for the desired reaction with the chlorine gas; A near-stoichiometric proportion of chlorine gas and a dilute aqueous solution of caustic soda are continuously fed 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. (b) draining the reaction mixture from the downstream end of the mixing zone at a pressure not substantially less than atmospheric pressure; Directly into the end, at least 1
Two multi-bladed rotary impellers are driven adjacent to the side flow stator to repressurize the pump zone to effect strong gas/liquid interactions and a high degree of turbulence of the reaction mixture through the pump zone. and simultaneously increasing the pressure of said mixture by at least about 1 atmosphere and draining said mixture at a pressure of at least about 2 atmospheres absolute; (c) bringing the drained mixture of (b) to a pressure of at least about 2 atmospheres absolute; (d) introducing the resulting liquid bleaching solution as a product into a receiving and gas-liquid separation zone; (e) collecting at least one of the unreacted chlorine gases in the headspace at the bottom of the separation zone;
recirculating some of the two fluids back to the upstream end of said cocurrent flow mixing zone of step (a). How to give. 8. The concentration of said dilute aqueous solution of caustic soda and the rate at which it reacts with said chlorine gas is adjusted to provide a liquid bleach solution containing from about 1 to about 6 weight percent sodium hypochlorite. the method of. 9. The method 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) The pressure maintained in the separation zone described in step (c) is about 40 to 80 psia and is greater than or equal to that of the superpressurized pressurized fluid serving to drive the cocurrent flow mixing zone of step (a). The method according to claim 7. (12) in effecting a chemical reaction between gaseous and liquid reactants in a continuous manner, (a) moving said reactants to an upstream end of a fluid pressure-driven, in-line, cocurrent flow mixing zone above substantially atmospheric pressure; (b) with at least one said reactant supplied at a pressure lower than the pressure supplied in (a), thereby forming a homogeneous gas-liquid reaction mixture; (c) draining the gas-liquid reaction mixture from the downstream end of the mixing zone at a pressure not substantially less than atmospheric pressure; A mechanically operated, regenerating, fluid-propelled and re-pressurizing pump driven at high speed adjacent to a side channel stator directs the powerful gas of the reaction mixture through the pump zone. /effecting liquid interaction and a high degree of turbulence, while simultaneously increasing the pressure of said mixture at least about 1 atmosphere and draining said mixture therefrom at a pressure of at least about 2 atmospheres absolute; (d) (c) a lower region with liquid level control means arranged to maintain a regulated pressure of at least about one atmosphere above atmospheric pressure and to maintain a substantial gas headspace in the drained and pressurized mixture; passing through an overpressure, pressure seal, product receiving and gas/liquid separation zone that also maintains a large liquid holding space; collecting a gaseous accumulation in said gas headspace; (f) some of either or both of the gas collecting in said headspace and (d) the liquid accumulating in said lower region of said separation zone; recirculating the cocurrent flow of the flow of water back to the upstream end of the mixing zone. (13) supplying the liquid reactant in (a) at about 40 psia or more;
13. The method of claim 12, wherein the regulated pressure is maintained at a higher pressure than the pressure supplied at. (14) Gaseous reactants are Cl_2, HCl, SO_3, O
13. The method of claim 12, wherein the liquid reactant is an organic liquid. 15. The method of claim 12, wherein the gaseous reactant is Cl_2 and the liquid reactant is an aqueous solution of an alkali metal salt or hydroxide. (16) in effecting a desired reaction between cocurrently flowing gas and liquid reactants to continuously produce a desired liquid product substantially free of solids, (a) said reactants are continuously feeding the upstream end of a fluid pressure-driven, in-line, co-current flow mixing zone at a rate providing a liquid to gas volume ratio greater than 0.1, introducing at least one of said reactants at overpressure pressure; (b) the resulting gas-liquid reaction mixture formed in (a) is supplied from the downstream end of said mixing zone with at least one fluid reactant at a pressure lower than but substantially greater than the pressure supplied in (a); (c) said reaction mixture drained in (b) is drained at a pressure not less than atmospheric pressure; directly to the upstream end of a regeneration, multi-stage fluid propulsion and repressurization pump zone operated to effect strong gas-liquid interactions and high turbulence of the reaction mixture through said pump zone, and at the same time Increase the pressure of the mixture by at least about 1 atmosphere, and increase the pressure by at least about 2 atmospheres.
(d) the mixture drained in (c) is maintained at a pressure of at least about 2 atmospheres absolute and has a substantial gas headspace retained above it; Stop product acceptance and gas-
(e) collecting unreacted gaseous accumulations in the gas headspace in the lower region of the gas-liquid separation zone; (f) at least one of the liquid products; and recirculating said unreacted gas from (e) back to the upstream end of said cocurrent flow mixing zone of said (a), continuous to the desired reaction between the gas and liquid reactants flowing in cocurrent flow. method of acting. 17. The method of claim 16, wherein the gaseous reactant is Cl_2 and the liquid reactant is a dilute aqueous solution of an alkali metal hydroxide.