JPS59501590A - Apparatus and method for continuous production of polymer aqueous solution - Google Patents

Abstract

(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.

Description

[Detailed description of the invention] Apparatus and method for continuous production of 41Jmer aqueous solution (technical field) This invention relates to an apparatus and method for the production of aqueous polymer solutions, particularly in underground oil-containing formations. Continuous in-situ preparation of solution for use in secondary and 6th grade oils relates to an apparatus and method for manufacturing.

(Background technology) Apparatus and methods for the continuous polymerization of water-bathable polymers are the subject of numerous U.S. patents. be. For example, U.S. Patent No. 2.820.777-@ polymerizes acrylamide, A continuous method for hydrolysis is disclosed. The patent implements the method It does not teach anything about the equipment for this purpose. U.S. Patent No. 3.732.193 No. 1 is a method for heating and continuously heating an aqueous solution of a water-soluble unsaturated monomer such as acrylamide. Polymer is polymerized and dried on a continuously moving belt to produce a thin, film-like polymer. A continuous polymerization process is disclosed. U.S. Patent No. 4,110.5 No. 21 discloses an apparatus for continuous polymerization of water-soluble polymers. There is. Its equipment is static fluid mixer, same (jacket with static fluid mixer) reactor after attaching, and static fluid mixer for mixing polymer and water raw materials Consists of a diluter with. To hold the reactants to be added to the later reactor A tank with a jacket is provided. According to the patent, from the diluter 2 The final product can be sent to bulk storage or used directly.

The device disclosed in U.S. Pat. No. 3,732.196 is suitable for all practical purposes. point, the type of pot used in the secondary and tertiary recovery of oil from underground oil-bearing formations. It will not be useful for in situ production of aqueous remer solutions. U.S. Patent No. 4,110 , 521 for use in -2nd and 6th order oil recovery operations. The preparation of aqueous d-rimer solutions is described in U.S. Pat. No. 3,732,196. However, the in situ preparation of such solutions has a clear advantage over It has many drawbacks that reduce its application to In particular, the device of this patent is applicable to a wide range of static fluid mixers. It is characterized by a wide range of uses. Static fluid mixers are expensive and therefore Its use on the intended scale is such that the device is sufficiently severe to cease its use. It's a risk. Moreover, the device of the patent includes not only a reactor but also a reactant. Each tank or vessel used for It is necessary to use it. For cooling or heating of the size and type contemplated by the patent. The use of shag adds further complexity and increases the cost of the equipment. be.

Yet another significant shortcoming of the device of the patent, and no mention is made in the patent. There are no drawbacks produced using said equipment. d Related to the characteristics of the remer solution Ru. For example, the patent states that one of its objectives is to provide uniform molecular weight and provides an apparatus adapted to produce a polymer that seals the distribution; However, at the same time, the patent also requires that the polymers made of bath liquid be prevented from deteriorating or does not disclose a means of producing a polymer bath solution in such a way that it is reduced to a novel level. stomach. Degradation or dilution of the polymer is caused by injection and mobility of the polymer bath. properties) and thereby satisfy the performance requirements of the oil-containing layer. This reduces its ability to a considerable extent.

(Disclosure of invention) The uninvented apparatus and method provides for secondary or sixth generation of oil from underground oil-containing formations or oil reservoirs. Polymers for use as driving fluids and/or mobility buffers in storage in situ of aqueous polymer solutions, especially partially hydrolyzed polyacrylamide aqueous solutions. It is very well suited for continuous preparation. The device is expensive to build. It is easy to install and operate. Moreover, importantly The equipment is suitable for use with virtually any oil-bearing formation or reservoir in view of its capabilities. to provide a final product with predictable properties that also meet the performance requirements of 7. Forms of limmer liquors that should be strictly controlled at all stages in their preparation It makes it possible to achieve success.

Additionally, the device of the invention requires a pump to manipulate the concentrated polymer solution. If not, and if used, the pump is advantageously located only on the inlet feed stream side of the licker. It is characterized by placing The apparatus in a preferred embodiment of the invention includes a polymerization reactor, a hydrolysis reactor and a diluter. It consists of The polymerization and hydrolysis reactors each preferably operate at a predetermined flow rate. The residence time of the reaction mixture in the tube or pipe is a strip of length and cross-sectional area such that it can be produced and completed at It has the shape of a long tube or pipe. Reactor dimensions are determined to ensure completion of the desired reaction. fluid in the reactor to reduce the flow rate of the reaction mixture in such a way as to can be optimally sized by incorporating flow control or delay means. I can do it. The diluter used in the device is a polymer@liquid, e.g. The dilution of the hydrolyzed polyacrylamide bath solution is completely free of the polymer consisting of the solution. be able to reach a predetermined concentration without having any adverse effects on defects; Become a special feature.

The above and other features and advantages of the invention will be apparent from the following description based on the accompanying drawings. It will become even clearer.

(Brief explanation of the drawing) FIG. 1 is a schematic diagram of an embodiment of the inventive apparatus; FIG. 2 is a diagram of the fluid flow arranged in the reactor; Schematic cross-sectional views showing aspects of the adjustment or delay means, Figures 6 and 4 are shown at 3-6 in Figure 2. A schematic cross-sectional view taken along line 4--4, FIG. 5 shows the grid plate and plate of FIG. It is a sectional view showing a rotated bad ball.

(Best mode for carrying out the invention) The embodiment of the apparatus shown in FIG. 1 includes a polymerization reactor 10, a hydrolysis reactor 12, and a diluter. It consists of 14 parts. Reactors 10 and 12 and diluter 14 are preferably made of stainless steel. They are made from steel tubes or pipes, each having an inlet and an outlet.

The tips of reactors 10 and 12 define the flow pattern of fluids entering and exiting the reactors. It is preferably rounded or cup-shaped to modify the turn.

Reactor 10 and 12 and diluter 140 dimensions may vary; and in the case of reactors 10 and 12, to terminate the reaction taking place in the reactor. determined by the residence time at the preselected flow rate required for the diluter 14. in some cases at a preselected flow rate necessary to provide a polymer solution of the desired concentration. Determined by residence time. For example, partially hydrolyzed polyacrylamide When using the apparatus of this invention for continuous preparation of dilute aqueous solutions, the polymerization reactor 10 advantageously has a length to diameter ratio of about 6:1 to about 10:1, while Hydrolysis reactor 12 can have a length-to-diameter ratio ranging from about 4:1 to about 6:1. It's advantageous.

On the other hand, diluter 14 can have a length to diameter ratio of fJ30:1 to about 10:1. can.

As mentioned above, the dimensions, sometimes the volumes of reactors 10 and 12, allow for flow control within the reactors. Alternatively, it can be reduced to an optimal capacity by providing delay means.

Mo 6 Such means include screens placed substantially perpendicular to the fluid flow in the reactor; plates parallel to the flow, grid-like plates parallel to the flow t, or flow It consists of rods parallel to . 2 to 5, a grid plate 1 is placed inside the reactor 10. An array of 8-shaped plates 16 is shown. One or more as shown The upper grid plates are used, each at a different angle with respect to the other grid plates in the reactor. It may be placed at a predetermined position. Arrange the trap grid plates at intervals like this, and The plates of each lattice plate are placed in different planes with respect to the plates of the slack lattice plate. An even more comprehensive flow pattern can be obtained by rotating the Ru. In those instances, if control of the temperature of the reaction mixture in the reactor is desired, , place the coil to heat or cool the reaction mixture parallel to the fluid flow in the reactor. Alternatively, a drag generating means such as a rod may be incorporated into the reactor.

The diluter 14 of the apparatus shown in FIG. 1 has a plurality of polymer solution dispersion stations inside. It is desirable to have a 14cL version. This station is a perforated plate. consisting of a plate or screen, or a combination of a perforated plate and a screen. You can leave it there. A unit suitable for use as a diluter 14 is also disclosed in the U.S. application No. 279.027, filing date June 60, 1981, title of invention: Dilution device and and methods. Dilutor 14 prevents any concomitant degradation or dilution of the polymer. Polymers such as aqueous solutions of partially hydrolyzed polyacrylamide - Dilution of the solution can be achieved, thereby improving the performance of the oil-bearing formation or oil reservoir. Preparation of the final product with the necessary injection and mobility characteristics to meet the demands can be made possible.

Now, to explain in more detail with reference to Figure 1 of the drawings, the illustrated device is a secondary oil source. or for continuous in-situ preparation of polymer solutions for use in 6th recovery. Particularly suitable for cold weather. For this purpose, injection into injection wells of oil-bearing formations or oil reservoirs Upstream reactor 10 and 12 tanks and supplements necessary for the preparation of suitable polymer solutions. Auxiliary equipment will be installed. As shown, a water tank 20 connected to a water source; Storage tanks to hold supplies of aqueous solutions of monomers such as acrylamide and acrylamide. 22 is provided.

Prior to absorbing the monomer bath from tank 22 into the water stream, the polymerization reactor is to remove metal ions such as L-ijTrl that may interfere with the reaction. The monomer solution may be passed through an ion exchanger 24. The flow of water itself is a polymerization reaction. The water is passed through a heater 26 to raise the temperature of the water sufficient to facilitate the initiation of the reaction. You may let them. After the 7mer solution is absorbed into the water light from the water source, the reaction mixture in the static fluid mixer 28 to achieve complete distribution of the monomer solution in the compound. It is desirable to let it pass. The water bath liquid is oxygenated from the mixer 28) IJ tube 6 Pass it to 0. The oxygen stripper is in communication with a source of nitrogen gas filter 2. nitrogen gas into the monomer bath liquid in the stripper 60 to remove dissolved oxygen from the solution. Nomi pulled.

As shown, the first catalyst from tank 64 is drained from the monomer bath. - added to the hepatumer solution as it exits the filter O. The catalyst is used for the polymerization of seven polymers. It may be selected from any of the many organic and inorganic compounds used. So Mixtures of catalysts such as They may be added separately to the liquid. The monomer bath liquid, in the presence of the first catalyst, may optionally be It may be kept in a small tank or large diameter pipe 66 for a short period of time. then The monomer/catalyst bath is drained from tank 66 and transferred to a second reactor from tank 68. A medium is added. The pumps 40, 42, 44, 46 and the devices shown in the drawings are water tanks. tank 20, monomer storage tank 22, and catalyst tanks 64 and 68, respectively. tied together. After addition of the second catalyst, the monomer solution containing the catalyst is then statically It passes through a fluid mixer 48 and into the polymerization reactor 10 .

The residence time of the reaction mixture in reactor 10 may vary from about 7 to about 10 hours. The resulting polymer solution is then discharged from the reactor 10 and stored in the storage tank 5. 0 into the polymer solution by pump 52. Sent. The reaction mixture thus formed is then advantageously transferred to a static fluid mixer 54. and from there to the hydrolysis reactor 12.

The residence time of the reaction mixture in reactor 12 can vary from about 4 to about 6. , the hydrolyzed polymer solution is then sent to diluter 14 and water from the wax water source is reacted. It is supplied to the diluter 14 together with the hydrolyzed 4.1 J mer bath liquid from the reactor 12. . The diluted bath liquid flows out of the diluter and then additional water from the water source is added. The fluid is then sent to a static fluid mixer 56, which is located in a static fluid mixer 56. The diluted solution flowing out of the mixer 56 The fluid can be sent directly to the injection well or, for example, to a storage area where it can be used. It may be further diluted prior to.

Example Unique equipment for producing dilute water bath solutions of partially hydrolyzed polyacrylamide To illustrate particular utility, a monomer bath consisting of 50% by weight acrylamide The liquid is passed through an ion exchanger at a rate of approximately 0.7 lb/min to remove all present in the solution. removes copper ions. This solution was then preheated to a temperature of about 110"F. Introduced into the water stream. The immediately heated solution is passed through a static fluid mixer and then oxygenated. Pass through a stripper where nitrogen gas is used to purge the dissolved oxygen. purge When the solution leaves the stripper, a 25% by weight aqueous solution of sodium bisulfite is added to the bath at a rate of about 0.00025 pounds 9/min. The catalyst-containing bath liquid is then and into a small (6 gallon) holding tank where it is held for about 15 minutes. The melt When the liquid exits the retention tank, 25% ammonium persulfate 10 A second catalyst stone solution consisting of an aqueous solution is added to the monomer solution at a rate of about 0.0005 lb/min. Boil it. The monomer/catalyst solution is then passed through a static fluid mixer for an additional approximately 5. Polymerization at a rate of 7 h/min, at a temperature of 105'F, and under a pressure of 100 pS. feed into the reactor. The reactor is approximately 16 feet long and 2 feet in diameter; It has a capacity of approximately 675 gallons. Polymerization of the monomers in the reactor takes approximately 9 hours. Stand up and proceed. , f +) mer solution becomes about 1557 due to the increase in temperature in the reactor. rises to the height of 6% by weight polyacrylamide solution formed in the reactor exits at a rate of about 5.7 kg/min under a pressure of about 90 psi. Sodium hydroxide Approximately 0.11 lbs of 50 wt% thorium water bath solution was pumped into the polymer solution. speed of de/min and 90 p, ? Place it on the side with the pressure of iy. Temperature of the hydroxide solution is approximately 75')F. The polymer caustic bath is first discharged into a static fluid mixer, and then Pass through a hydrolysis reactor. The reactor is approximately 10 feet long and approximately 2 feet in diameter. , has a capacity of approximately 235 gallons.

Hydrolysis of the polymer in the reactor proceeds over a period of about 6 hours. polyacrylica The % hydrolysis of Mido is approximately 60%. Partially hydrolyzed polyacrylic in solution The concentration of amide is approximately 6.6% by weight. The hydrolyzed polymer bath solution is approximately 135' It has a temperature of F. The solution is then pumped at a rate of about 5.79 lb/min and about 60 p. siy pressure and consists of a tube approximately 4 inches in diameter and approximately 10 feet long. Feed into a continuous screen diluter. The diluter preferably contains 6 polymer dispersions. screens with stations, each of them having different mensch dimensions The mesh size of the screen rotates from the inlet end of the diluter to its outlet end. is continuously decreasing. 62.4 bonds/min of water at a temperature of about 70°F At high speed and under a pressure of 75 s Supply to the extractor. Partially hydrolyzed polyacrylic acid is obtained by diluting the bath solution in a diluter. Make a solution containing about 1% by weight of Mid. The residence time of the solution in the diluter is approximately 2 minutes. Ru. This 1% solution (!d from the diluter at a rate of about 38 lbs/min, about 20 psiy Additional water at a temperature of about 70" F. is added to the solution at a pressure of about 80 F. and a temperature of about 80 F. delivered to a location where it is being supplied at a rate of 5 lb/min and a pressure of approximately 35 pgig. Ru.

This solution with additional water is then passed through a static fluid mixer to partially hydrolyze it. Prepare a 0.1% solution of polyacrylamide. The diluted bath solution has mobility ( Ready to inject into injection wells as a control buffer or as a driving fluid in a state.

Preparation of partially hydrolyzed polyacrylamide melt using the apparatus and method of the invention Although we have described their specific uses in are described as illustrations and examples, and are described as limiting the present invention. and that the apparatus and method are not used for the preparation of other polymer baths. Adapted to 2 It should be understood that this can happen.

international search report AIJhJEX To THi INTERNATIONAL 5EARCH EPORT　0NINTERNATIONAL　APPLrCATION　No , PCT/US 83101046 (SA 5565) US-A-4110 52129108/78 NoneFR-A-1383924None GB-ni-1139917None

Claims (1)

[Claims] (1) Provide a JIJ mamer formation reaction mixture containing at least one monomer. means for receiving the reaction mixture; formed from an inlet end for receiving the reaction mixture; Reactor means having an outlet end for discharging the polymer solution, the reactor means comprising: The four residence times at a predetermined flow rate of the reaction mixture in the J reactor are a length and cross-sectional area that is sufficient to substantially completely polymerize one monomer. control the flow rate of the reaction mixture from the inlet to the outlet of the reactor means; reactor means and associated fluid flow control means for controlling the reaction mixture; is reacted for a period of time sufficient to substantially completely polymerize one monomer. held in the reactor means, An apparatus for preparing a dilute solution of a water-bathable polymer consisting of: (2) the reactor means is cylindrical in shape and the length to diameter ratio of the reactor means is about 6: 1 to about 10:1. (3) the outlet of the reactor means is connected to the second reactor means, and the outlet of the reactor means is connected to the second reactor means; The stage has an inlet at one end and an outlet at all other ends, and the polymer is supplied at a continuous flow rate. - the residence time of the solution in the second reactor means of the polymer bath from said first reactor means; The special feature is that the length and cross-sectional area are sufficient to modify the , the device described in the preceding section (1). (The second reactor means is cylindrical in shape and has a length to diameter ratio of about 4:1. 6:1. (5) the reactor means has a flow delay for controlling the flow of the reaction mixture through the reactor means; The device according to the preceding item il+, comprising a spreading means. (6) Consisting of a grid plate made of plates, which plate is used for the reaction in the reactor means. The device according to the preceding item (5), which is arranged transversely to the flow direction of the mixture. (7) The flight delay means consists of at least two grid plates made of plates, and the grid plates are spaced apart from each other and the plates are spaced apart from each other; consisting of one of the lattice plates placed in a different plane than one of the plates consisting of The device described in the preceding paragraph (5). (8) the flow retardation means are substantially relative to the longitudinal axis of the reactor means with respect to their longitudinal axes; The device according to item (5) above, which comprises a plurality of central tubes arranged in parallel. (9) The hollow tube provides a flow for heating or cooling the reaction mixture within the reactor means. The device according to the preceding paragraph (8), which contains a body. (lα) the second reactor means is connected to the polymer solution dilution means, said dilution a plurality of device means arranged at intervals from each other along the long axis of the device means; The apparatus according to the preceding item (3), comprising a polymer dispersion station. +n+ J　IJ Mama-san Station, polymer passes through the screen described below. The number of surface species on the polymer increases when Apparatus according to the previous paragraph (101) having a screen loading the mesh size as follows. To remove metal ions that interfere with polymerization from the reaction mixture forming O3 polymers The apparatus according to the preceding clause (11), wherein the apparatus is equipped with an ion exchange means. Floor 0: Equipped with dissolved oxygen removal means to remove oxygen from the reaction mixture. The device described in the preceding paragraph (1). O4) A second reactor means for controlling the flow rate of the polymer bath passing therethrough. The device according to item (3) above, comprising a flow delaying means. (151 Polymer-forming reaction mixture containing at least one polymerizable monomer) a closed system containing means for providing the reaction mixture; a first reactor means connected to the first means, the first reactor means having a predetermined The residence time of the reaction mixture at a flow rate of The length and cross-sectional area are sufficient for complete polymerization; the first reaction a second reaction coupled to the first reactor means for modifying the reaction product from the reactor means; reactor means, the second reactor means having a residence time of the reaction mixture therein which is longer than the first reactor means. a length that is sufficient to modify the reaction products from the stage in a predetermined manner and a cross-sectional area of the chemical reactant in the reaction product from the first reactor means; means for introducing to modify the reaction product; and a predetermined amount of diluent; a second reactor means for introducing into the reaction product from the two reactor means; Apparatus for the continuous preparation of dilute solutions of water-soluble polymers, comprising diluter means. (16) to increase the residence time of the reaction mixture in the reactor means; The apparatus according to item u9 above, wherein the reactor means is provided with flow retardation means. (1η the diluter means consists of a first diluter means and a second diluter means, and the first diluter means a dispersion means having a plurality of spaced apart homer dispersion stations therein; It consists of an elongated cylindrical member with a hollow chamber and at least some of the stations. the second dilution comprising a screen having a preselected mesh size; diluter means is disposed in a downward flow from said first diluter means and is configured to provide additional diluent. a first diluter means serving to disperse the diluted reaction product from the first diluter means; The device described in item a. (1 to 8 polymers containing at least one polymerizable monomer in a closed system) - forming a reaction mixture; passing the reaction mixture into a first reactor at a predetermined flow rate; passing the reaction mixture through a stage; retaining the chemical modifier in the first reactor means for a period of time; introducing the reaction product and the resulting reaction mixture at a predetermined flow rate. passing the reaction product from the first reactor means through a chemical modifier; and retaining the resulting reaction mixture in a ninth reactor means. 7 transferring the modified reaction product from the second reactor means to a plurality of dispersion stations; ? and dilution of the denatured reaction product. The modified reaction products are introduced into each dispersion station of the diluter means at a predetermined flow rate. A method for the continuous preparation of dilute solutions of water-soluble polymers consisting of transferring. The method described in Q8) above, wherein the O9 polymer forming reaction mixture contains acrylamide. . ■ The preceding item α in which the residence time of the reaction mixture in the first reactor means is about 7 to about 12 hours. (to) the method described. (21) The preceding clause, wherein the residence time of the reaction mixture in the second reactor means is about 4 to about 6 hours. The method described in Oa. The chemical modifier hydrolyzes the polymer formed in the first reactor means. an alkali metal hydroxide which can be used as The method according to the preceding item α9, wherein the method is present in an amount sufficient to perform 45% hydrolysis. (c) The polymer-forming reaction mixture is placed in a mixer before it enters the first reactor means. and before the reaction product from the first reactor means enters the second reactor means. The method described in the preceding paragraph aυ in which mixing is performed.