KR101855040B1 - Method for manufacturing of pressable polymer-bonded explosives using water-based polymer emulsion and pressable polymer-bonded explosives by the same - Google Patents

Abstract

The present invention relates to compressive composite gunpowder and, more specifically, to a method for manufacturing compressive composite gunpowder using a polymer emulsion and compressive composite gunpowder manufactured through the same, capable of maximizing the efficiency of processes by using a polymer emulsion. The method includes: a polymer emulsion manufacturing step of manufacturing a polymer emulsion through polymerization by mixing a monomer and an emulsifier of a polymer binder with processing water and then adding an initiator; a slurry manufacturing step of manufacturing slurry by mixing a material including gunpowder and an emulsion breaker with other processing water; a flocculated particle forming step of forming flocculated particles covered with the polymer binder on the surface of the material by adding the polymer emulsion to the slurry; and a flocculated particle obtaining step of collecting and drying the flocculated particles through filtering.

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention [0001] The present invention relates to a method for producing a compression-type complex powder using a polymer emulsion, and a compression-

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a compression type compounding powder, and more particularly, to a process for producing a compression type compounding powder using a polymer emulsion to maximize the efficiency of the process and a compression type compounding powder produced thereby.

Gunpowder explosions cause a lot of casualties and massive property damage once they happen because there is no time to evacuate. For this reason, there has been a need for a desensitizing agent, which is an explosive that does not cause an explosion reaction due to unexpected external stimuli such as heat, shock, and the like, and the demand for the explosive agent has also increased. Therefore, studies have been made on the preparation of compound gunpowder which depresses the raw powder itself or coating the gunpowder particles with a polymer binder to lower sensitivity.

Of the various types of compound gunpowder, press polymer-bonded explosives (hereinafter also referred to as Press-PBXs or P-PBXs) are generally prepared by adding a solvent in which a polymer binder is dissolved to a suspension in which gunpowder particles are dispersed in water Which is produced by agglomerating explosive particles and polymer binder, and is compressed and molded into granular powder, which is used as an assisting or auxiliary charge for an inorganic system. Furthermore, these compressive compound explosives are mainly applied to ammunition warheads which require the performance of the debris and the jet performance of the molding agent because of the highest content ratio of the explosive particles.

Such compression type compounding powders are generally manufactured by applying a water-slurry (hereinafter, also referred to as WS) process. Here, the WS process is a process in which a coating solution in which a plasticizer and a polymer binder are dissolved is added to an organic solvent in a suspension in which a raw material containing powdered particles is dispersed and stirred in water at a temperature of about 60 ° C, And then removing the organic solvent through distillation at a high temperature to finally obtain a molding powder of the compression type compounding powder.

However, such a WS process is disadvantageous in that a distillation process at a temperature of 100 ° C or more is inevitable to remove the organic solvent after covering and coagulating the raw material, and further there is a danger in terms of handling safety of the organic solvent, There is also a harmful problem.

The matters described in the background art are intended to aid understanding of the background of the invention and may include matters which are not known to the person skilled in the art.

Korean Patent Registration No. 10-1276675

In order to solve the above-mentioned problems, the present invention provides a process for producing a compression type compound gasket which maximizes the efficiency of a process by using a polymer emulsion to replace an organic solvent, and a process for producing a compression type compound gasket .

In order to accomplish the above object, the present invention provides a method for producing a compression-type composite explosive using a polymer emulsion, the method comprising mixing a monomer and an emulsifier of a polymer binder in a process water and then adding an initiator to the polymer to prepare a polymer emulsion Emulsion manufacturing step S110; A slurry producing step (S120) of preparing a slurry by mixing a raw material containing an explosive in another process water and an emulsion breaker; An aggregated particle forming step (S130) of injecting the polymer emulsion prepared in the slurry into the slurry to form aggregated particles coated with a polymeric binder on the surface of the raw material; And a step (S140) of collecting the aggregated particles by filtration and drying the aggregated particles.

In the polymer emulsion preparation step (S110), the monomer is polymerized through a polymerization reaction such as styrene butadiene rubber (SBR), neoprene, nitrile butadiene rubber (NBR), acrylic rubber ), A fluorine-based rubber, and a polyisobutylene.

The emulsifier may be selected from the group consisting of sodium dodecyl sulfate (SDS), sodium dodecyl benzene sulfonate (SDBS), sodium dioctylsulfosinate dioctyl sulfosuccinate, acetyl dimethyl benzyl ammonium chloride, and hexadecyl trimethyl ammonium bromide.

In the polymer emulsion preparation step (S110), the emulsifier is added in an amount of 0.1 to 5% by weight based on the weight of the process water.

In the slurry production step (S120), the gunpowder is at least one of RDX, HMX, HNW and HNIW. By weight to 5 to 30% by weight.

In the slurry preparation step (S120), the emulsion breaker may be an inorganic salt such as calcium dichloride, sodium chloride, potassium chloride, magnesium chloride, sodium nitrate, Sodium carbonate, sodium iodide, and potassium iodide. In the present invention, it is preferable to use at least one of sodium carbonate, sodium iodide, and potassium iodide.

Also, in the slurry preparation step (S120), the raw material may further include at least one of aluminum, magnesium and boron.

In addition, a step water exchange step (S131) of recovering the aggregated particles through filtration after the aggregated particle formation step (S130) and re-introducing the recovered aggregated particles into new process water; And injecting a plasticizer to flocculate the plasticizer on the aggregated particles (S132).

Also, in the step of injecting the plasticizer (S132), the plasticizer may be dioctyl adipate (DOA), dioctyl sebacate, dioctyl phthalate (DOP), and isododecyl pelagneate isododecyl pelargonate, IDP).

The compression type compounding powder of the present invention produced by such a production method comprises 50 to 98% by weight of an explosive; 0 to 40% by weight of metal; 0.5 to 5% by weight of a polymeric binder; And 0 to 10% by weight of a plasticizer.

The present invention replaces an organic solvent and does not require a distillation step at a temperature of 100 ° C or higher by using a polymer emulsion. Therefore, the manufacturing time is shortened, and the cost is shortened, thereby maximizing the efficiency of the process.

In addition, since the step of distilling the organic solvent is not required, there is no need for an extra volume of about 1/2 volume of the total reactor for preventing the slurry from overflowing when the organic solvent is distilled, and the production amount per reactor is increased by about 200% It is effective. As a result, there is an effect that the production per unit time and per reactor is increased by about 1000%.

Further, by not using an organic solvent, safety and eco-friendliness of the process are high.

In addition, energy metal particles (aluminum, magnesium, boron, etc.) which can not be used as the composition of the composite explosive can be used as a reason for hydration reaction with water at a high temperature distillation temperature. Therefore, Can be greatly improved.

FIG. 1 is a schematic view of a conventional method for producing a compression type composite powder.
2 is a flow chart of a method for producing a compression type composite explosive of the present invention.
3 is a schematic view of a method for producing a compression-type composite explosive of the present invention.
FIGS. 4- (A) and (B) show SEM results of the agglomerated particles produced by the conventional compression type composite explosive manufacturing method.
FIGS. 4- (C) and (D) show SEM results of the agglomerated particles prepared by the method of the present invention.

Technical terms used herein should be interpreted in a sense that is generally understood by a person skilled in the art to which the present invention belongs, And shall not be construed as an oversimplified meaning. In addition, the general terms used in the present invention should be construed in accordance with the predefined or prior context.

Also, the singular forms "as used herein include plural referents unless the context clearly dictates otherwise. That is, the terms 'consisting of', 'consisting of', or 'comprising', as used herein, should not be construed as necessarily including the various elements or steps described in the specification, Some of the elements or some of the steps may not be included, or may be interpreted to include additional elements or steps.

FIG. 1 is a schematic view of a conventional method for producing a compression type composite powder. As shown in FIG. 1, a coating solution prepared by mixing a polymer binder and a plasticizer in an organic solvent is used to produce a compressed composite powder in a WS (water-slurry) . However, such a WS process is disadvantageous in that a distillation process at a temperature of 100 ° C or more is inevitable to remove the organic solvent after covering and coagulating the raw material, and further there is a danger in terms of handling safety of the organic solvent, There is also a harmful problem. In addition, the use of metal particles, which contribute to the explosion energy of the composite explosive, has been limited due to the hydration reaction of the metal accelerated at high temperatures.

Accordingly, the present invention is directed to a method of manufacturing a compression type composite powder in which the efficiency of a process is maximized by using a polymer emulsion to replace an organic solvent to solve the above problems, and a compression type composite powder produced by the method.

FIG. 2 is a flowchart of a method for producing a compression type compounding powder of the present invention, and FIG. 3 is a schematic view of a method for producing a compression type compounding powder of the present invention. Hereinafter, the present invention will be described with reference to Figs. 2 and 3. Fig.

As shown in FIG. 2, the present invention is characterized in that a polymer emulsion is prepared (S110) in which a monomer and an emulsifier of a polymer binder are added to and mixed with a process water and then an initiator is added to produce a polymer emulsion through polymerization, (S120) for preparing a slurry by dispersing the raw material and the emulsion breaker in the slurry, and adding the polymer emulsion to the slurry to form agglomerated particles coated with a polymeric binder on the surface of the raw material Forming step (S130), collecting the aggregated particles through filtration, and obtaining a coagulated particle (S140) for drying.

After the flocculating particle forming step (S130), a slurry having aggregated particles formed is filtered to recover aggregated particles, a process water exchange step (S131) in which the collected aggregated particles are redispersed in new process water, and a plasticizer is added and mixed (S132). ≪ / RTI >

Hereinafter, each step will be described in more detail.

The polymer emulsion preparation step (S110) is a step of preparing a water-based polymer emulsion in which polymer binders are surrounded by emulsifiers in the process water. First, the critical micelle concentration (critical micelle concentration (CMC) or higher emulsifier and a monomer of a polymer binder are added and mixed to arrange the emulsifier in a micellar structure. At this time, the monomer of the polymer binder is present in the micelle.

Thereafter, an initiator is added to cause a polymerization reaction of the monomer, and a polymer binder is formed through the polymerization reaction. Finally, an aqueous polymer emulsion is prepared in which the polymer binder is surrounded by an emulsifier in the process water.

Here, the polymeric binder is coated on the surface of the agglomerated particles in the aggregated particle formation step (S130), and is formed through the polymerization reaction of the monomers as described above, and includes styrene butadiene rubber (SBR), neoprene, It is preferably at least one of nitrile butadiene rubber (NBR), acrylic rubber, fluorine rubber, and polyisobutylene.

As a result, the monomer of the polymer binder may be polymerized through polymerization reaction using styrene butadiene rubber (SBR), neoprene, nitrile butadiene rubber (NBR), acrylic rubber, Polyisobutylene, and the monomer of the polymer binder is preferably added in an amount of 10 to 50 wt% based on the weight of the process water.

The emulsifier is added to prepare a polymer emulsion in which the polymer binder is surrounded by the polymer. The emulsion is composed of sodium dodecyl sulfate (SDS), sodium dodecyl benzene sulfonate (SDBS) An anionic emulsifier containing sodium dioctyl sulfosuccinate and a cation emulsifier containing acetyl dimethyl benzyl ammonium chloride and hexadecyl trimethyl ammonium bromide, .

It is preferable that the emulsifier is added in an amount of 0.1 to 5 wt% based on the weight of the process water. If the emulsifier is less than 0.1 wt%, the monomer of the polymer binder can not polymerize As a result, there is a problem that a polymer emulsion is not produced. When the amount is more than 5% by weight, the emulsifier is not a micellar structure but a complex nanostructure, which hinders formation of a spherical polymer emulsion.

The initiator is added to initiate polymerization of the monomer and is preferably at least one of potassium persulfate, sodium persulfate, ammonium persulfate, and hydrogen peroxide, But is not limited thereto.

In addition to such an initiator, a chain transfer agent such as a cross-linking agent such as divinyl benzene (DVB) or tert-dodecylmercaptan may be further added during the polymerization reaction And the amount thereof is preferably less than 1% of the molar ratio of the monomer of the polymer binder.

The slurry preparation step (S120) is a step of preparing a slurry in which powdered powders are dispersed, and is prepared by adding a raw material containing gunpowder to the process water and sufficiently dispersing it.

It is preferable that the explosive is at least one of the following: RDX, HMX, HNIW, and 5 to 30 wt% Is preferably added.

If the spraying agent is less than 5% by weight, there is a problem that the efficiency of the process is deteriorated because the amount (yield) of the aggregated particles finally obtained is too small. When the spraying agent is more than 30% by weight, And agglomeration of the agglomerates of the agglomerates may occur considerably.

Meanwhile, the raw material may further include a metal in powder form together with the explosive, wherein the metal is selected from the group consisting of aluminum, magnesium, and the like, which are energy metals capable of improving the explosion performance of the compression- And boron. [0031]

The slurry is prepared by mixing an emulsion breaker or a demulsifier together with a raw material (a powder or a powder and a metal), and the emulsion breaker is prepared by mixing the emulsion with an emulsifier in a polymer emulsion, And to precipitate the polymer binder.

The emulsion breaker is an inorganic salt such as calcium dichloride (CaCl ₂ ), sodium chloride (NaCl), potassium chloride (KCl), magnesium chloride (MgCl ₂ ), sodium nitrate ₃ ), sodium carbonate (NaCO ₃ ), sodium iodide (NaI), and potassium iodide (KI).

The emulsion breaker is preferably added in such an amount as to be able to deposit the entire amount of the polymer binder emulsified in the polymer emulsion introduced in the aggregated particle forming step (S130), and more specifically, May be added in an amount equal to or greater than the weight of the polymer binder contained in the emulsion.

This is because when a large amount of the polymeric binder that can not be precipitated is present, there may be a raw material (powder or powder and metal) which is not coated with the polymeric binder thereafter. In addition, the emulsion breaker is irrelevant to the manufacturing process since it can be removed through the subsequent step water exchange step (S131) even if a large amount of emulsion breaker is added.

Meanwhile, the slurry preparation step (S120) may further include adding a dispersant such as IPA (iso propyl alcohol) or a sonicator such as an ultrasonic disperser or the like so that the raw material (powder, powder, and metal) Can be used for a certain period of time.

In addition, the slurry preparation step (S120) is preferably performed at room temperature in consideration of the characteristics of the metal which accelerates hydration reaction at high temperature with heat-sensitive gunpowder, more specifically, at a temperature of 20 to 40 ° C.

The aggregated particle forming step S130 is a step of forming coagulated particles in which a polymer binder is coated and aggregated on the surface of a raw material, that is, a gunpowder or a gunpowder and a metal. In the slurry prepared in the slurry preparing step S120, a polymer emulsion preparing step S110 ) Is preferably added at a temperature of 20 to 40 DEG C in consideration of the characteristics of a heat-sensitive gunpowder and a metal accelerating the hydration reaction at a high temperature. More preferably, the polymer emulsion is stirred at a temperature of 20 to 40 DEG C desirable.

When the polymer emulsion containing the polymer-binding agent emulsified by the emulsifier is introduced into the slurry containing the raw material (powder or powder and metal) and the emulsion breaker, the polymer binder emulsified by the emulsifier by the emulsion breaker And the precipitated polymer binder coagulates and coagulates on the surface of the powder or the powder and the metal to form aggregated particles.

The weight of the polymer emulsion introduced into the slurry is preferably adjusted according to the chemical composition of the aggregated particles finally obtained through the step of obtaining aggregated particles (S140). More specifically, the weight of the polymer emulsion to be added to the slurry It is preferable that the amount is determined depending on the weight percentage of the polymer binder.

In the present invention, it is preferable that the aggregated particles produced by the production method of the present invention comprise 50 to 98% by weight of the total amount of agglomerated particles, 0 to 40% by weight of metal and 0.5 to 5% by weight of a polymer binder Do.

If the amount of the polymeric binder is less than 0.5% by weight, a large amount of powdery particles which are not coagulated by the polymer binder may be present, thereby being susceptible to external stimuli such as unexpected heat and shock. There is a problem that can be done.

Therefore, the weight of the polymer emulsion to be added to the slurry in the aggregated particle forming step (S130) is determined by considering the weight of the powder and metal used in the slurry preparation (S120) and the weight of the polymer binder precipitated by the emulsion breaker The aggregated particles are calculated and added so as to include 0.5 to 5% by weight of the polymer binder relative to the total weight of the aggregated particles.

On the other hand, in the aggregated particle formation step (S130), the aggregated particles are formed, and the slurry is aged for a predetermined time to adjust the size and shape of the aggregated particles. In this aging process, the aggregated particles gradually grow as the polymer binder coagulates. Here, the aging time may be about 10 minutes or more, but is not limited thereto and can be adjusted depending on the size and shape of the desired aggregated particles.

On the other hand, after the aggregated particle forming step (S130), a process water exchanging step (S131) in which the slurry having the aggregated particles formed therein is filtered through a filtration device to recover the aggregated particles and the thus collected aggregated particles are re- It proceeds.

The emulsifier remaining in the slurry and the residues such as inorganic salts due to the emulsion breaker are then removed to allow the aggregated particles finally obtained through the step of obtaining aggregated particles (S140) to contain no impurities.

On the other hand, after the step water exchange step (S131), a step of applying a plasticizer (S132) is carried out in which the plasticizer is added to the process water into which the coagulated particles have been reintroduced and dissolved so that the plasticizer coagulates to the aggregated particles. It is preferably at least one of dioctyl adipate (DOA) and dioctyl sebacate, dioctyl phthalate (DOP), and isododecyl pelargonate (IDP).

The weight of the injected plasticizer is preferably adjusted according to the chemical composition of the aggregate particles to be finally obtained through the step of obtaining the aggregate particles (S140). More specifically, the plasticizer is added to the total weight of the aggregate particles to be finally obtained It is preferable that the input amount is determined depending on whether it should be included in weight%.

In this connection, in the present invention, the aggregated particles produced by the production method of the present invention contain 50 to 98% by weight, 0 to 40% by weight of metal, 0.5 to 5% by weight of polymer binder and 0 to 10% by weight of plasticizer %. This is because if the plasticizer is more than 10% by weight, there is a problem that the physical properties of the composite explosive can be lowered.

Therefore, the weight of the plasticizer injected in the step of injecting the plasticizer (S132) is preferably 0 to 10% by weight based on the total weight of the aggregated particles of the finally obtained aggregate particles in consideration of the weight of the powder and metal used in the slurry preparation (S120) As shown in FIG.

On the other hand, after the step of injecting the plasticizer (S132), the coagulated particles are recovered by filtration using a filtration apparatus, and the recovered coagulated particles are placed in an oven capable of circulating air and dried to have a water content of about 0.5% (S140).

The finally obtained aggregated particles comprise from 50 to 98% by weight of the total weight of the agglomerated particles, from 0 to 40% by weight of the metal, from 0.5 to 5% by weight of the polymer binder and from 0 to 10% by weight of the plasticizer, The particles are compression molded to produce a compression type composite powder. The compressed composite powder of the present invention thus produced also has the same chemical composition as the chemical composition of the aggregated particles.

Hereinafter, the present invention will be described in more detail with reference to Comparative Examples and Examples. However, the following Comparative Examples and Examples are for illustrative purposes only, and the scope of the present invention is not limited thereto.

Comparative Example

26 g of acrylic rubber (HYTEMP) as a commercial polymer binder and 78 g of dioctyl adipate (DOA) as a plasticizer were added to 520 g of ethyl acetate as an organic solvent, and the mixture was stirred at 60 ° C. for about 2 to 8 hours To prepare a coating solution. On the other hand, 1196 g of RDX (Hanwha Co., Ltd.) was added to a 25-liter reactor and the mixture was stirred and dispersed at 60 ° C for 10 minutes to prepare a slurry. Then, the coating solution prepared was added to the slurry to form agglomerated particles, followed by aging for about 10 minutes to grow agglomerated particles. Thereafter, 3120 g of process water was added to terminate the growth of the agglomerated particles. After heating at a temperature of about 100 ° C., the organic solvent was distilled off by keeping it for about 30 to 50 minutes. Thereafter, 1300 g of aggregated particles were finally obtained through filtration and drying processes.

Example

(0.0043 mol) of sodium dodecyl sulfate, 156 g (1.217 mol) of butyl acrylate monomer as a monomer of a polymeric binder, 1 g of ethyl acrylate 52 g (0.52 mol) of ethyl acrylate was added, and the mixture was stirred for 1 hour. Thereafter, 0.52 g (0.0019 mol) of potassium persulfate, which is an initiator, was added at a temperature of about 80 to 90 ° C., and then polymerized at a temperature of 75 ° C. for 5 to 10 hours to prepare a polymer emulsion (S110). Then, on the other hand, 3600 g of RDX (Hanhwa) and 80 g of calcium chloride (CaCl ₂ ) as an emulsion breaker were added to 20000 g of the process water in a 25-liter reactor and stirred at 25 ° C for 10 minutes to prepare a slurry. Then, 400 g of the prepared polymer emulsion (80 g of the polymer binder) was added to the prepared slurry to form agglomerated particles, followed by aging for about 10 minutes to grow agglomerated particles. Then, the aggregated particles were recovered by filtration, and the recovered aggregated particles were reintroduced into the new process water to remove the residue. Then, 240 g of dioctyl adipate (DOA) as a plasticizer was added and stirred. Thereafter, 4000 g of aggregated particles were finally obtained through a filtration and drying process.

Gunpowder (RDX) Polymer binder Plasticizer (DOA) Composition ratio (% by weight) 92.10 wt% 1.96 wt% 5.94 wt%

Table 1 above shows that the aggregated particles prepared in the examples are dissolved in hexane as a solvent in which dioctyl adipate as a plasticizer is dissolved and in acetone as a solvent in which RDX is dissolved, It is the result of confirming composition ratio through. Here, the final residue after the extraction of dioctyl adipate and RDX is the composition ratio of the polymer binder.

Manufacturing method Sensitivity Shock [J] Friction [Kg · f] Static electricity [J] Shock [Kbar] Comparative Example 40.18 26.80 > 25 38.16 (150.38 kbar) Example 38.73 26.92 > 25 37.90 (151.88 kbar)

Table 2 shows the results of sensitivity tests of shock, friction, static electricity and shock of the agglomerated particles prepared in the comparative examples and the examples. Figs. 4- (A) and (B) FIGS. 4- (C) and (D) are SEM results of the agglomerated particles prepared by the method of the present invention.

Here, the impact sensitivity test was performed to determine the energy when the explosion reaction occurred at a 50% probability of the sample falling freely while changing the weight and height of the weight. The friction sensitivity test was performed by measuring the weight of the weight The energy of the explosion reaction occurred at 50% probability of the sample placed on the front side of the long lever while changing the position of the equidistance groove. The electrostatic sensitivity test was performed to measure the reactivity of the sample by applying electric energy, The thickness of the attenuator was measured when the explosion reaction occurred with a probability of 50% by injecting a shock pressure source with an attenuator between the donor explosive and the sample.

Table 2 and FIG. 4 show that the agglomerated particles prepared by the manufacturing method of the present invention exhibit excellent impact sensitivity, frictional sensitivity, electrostatic sensitivity, shock sensitivity and shape of the aggregated particles prepared by the conventional manufacturing method using organic solvents Which results in the production process of the present invention being more efficient in terms of time, cost and yield (yielding about 3 times more weight of agglomerated particles on the basis of 25 liters of the same capacity) It has been found that although the efficiency of the process is excellent, the aggregated particles having the same characteristics can be produced.

The method of producing a compression type complex powder using the polymer emulsion according to the present invention and the compression type complex powder produced by the method of the present invention replaces an organic solvent by using a polymer emulsion, thereby maximizing the efficiency of the process in terms of time, do. Further, by not using an organic solvent, safety and eco-friendliness of the process can be secured.

The method of producing a compression type complex powder using the polymer emulsion of the present invention and the compression type composite powder produced by the method of the present invention can be applied to a The present invention is not limited to the embodiments and the accompanying drawings, and thus the scope of the present invention is not limited thereto. Accordingly, the true scope of the present invention should be determined by the technical idea of the appended claims. It will be apparent to those skilled in the art that various substitutions, modifications and variations are possible within the scope of the present invention, and it is obvious that the parts easily changeable by those skilled in the art are included in the scope of the present invention .

S110: Polymer emulsion preparation step
S120: Slurry preparation step
S130: Step of forming aggregated particles
S131: Process water exchange step
S132: Step of injecting plasticizer
S140: Step of obtaining aggregated particles

Claims (10)

Preparing a polymer emulsion by mixing a monomer of a polymer binder and an emulsifier in the process water and then adding an initiator to produce a polymer emulsion through polymerization;
A slurry producing step of preparing a slurry by mixing a raw material containing an explosive in another process water and an emulsion breaker;
Forming an aggregated particle on the surface of the raw material by adding the polymer emulsion prepared in the slurry to form aggregated particles coated with a polymeric binder;
A step water exchange step of recovering the aggregated particles through filtration after the aggregated particle formation step and re-introducing the recovered aggregated particles into new process water;
Injecting a plasticizer into the process water into which the aggregated particles have been reintroduced to flocculate the plasticizer on the aggregated particles; And
Collecting the aggregated particles by filtration after the step of injecting the plasticizer, and drying the aggregated particles,
In the polymer emulsion preparation step,
The monomers can be polymerized by polymerization through the use of styrene butadiene rubber (SBR), neoprene, nitrile butadiene rubber (NBR), acrylic rubber, fluorocarbon rubber and polyisobutylene Wherein the polymeric emulsifier is a polymeric emulsion. delete The method according to claim 1,
In the polymer emulsion preparation step,
The emulsifier may be selected from the group consisting of sodium dodecyl sulfate (SDS), sodium dodecyl benzene sulfonate (SDBS), sodium dioctyl sulfosuccinate, acetyl dimethylbenzyl ammonium chloride dimethyl benzyl ammonium chloride, and hexadecyl trimethyl ammonium bromide. 2. The method of claim 1, wherein the polymer emulsion is at least one selected from the group consisting of dimethyl benzyl ammonium chloride and hexadecyl trimethyl ammonium bromide. The method according to claim 1,
In the polymer emulsion preparation step,
Wherein the emulsifier is added in an amount of 0.1 to 5 wt% based on the weight of the process water. The method according to claim 1,
In the slurry production step,
The gunpowder is at least one of RDX, HMX and HNIW and is dispersed in an amount of 5 to 30 wt% based on the weight of the process water Wherein the polymer emulsion is a mixture of at least two kinds of polymeric emulsions. The method according to claim 1,
In the slurry production step,
The emulsion breaker is an inorganic salt such as calcium dichloride, sodium chloride, potassium chloride, magnesium chloride, sodium nitrate, sodium carbonate, sodium iodide sodium iodide, and potassium iodide. 2. The method of claim 1, wherein the polymer emulsion is at least one of sodium iodide and potassium iodide. The method according to claim 1,
In the slurry production step,
Wherein the raw material further comprises at least one metal selected from the group consisting of aluminum, magnesium and boron. delete The method according to claim 1,
The plasticizer may be one or more of dioctyl adipate (DOA), dioctyl sebacate, dioctyl phthalate (DOP), and isododecyl pelargonate (IDP) A method for producing a compression type composite powder using a polymer emulsion. The compression type compounding powder produced by the production method of any one of claims 1, 3, 4, 5, 6, 7, and 9,
50 to 98% by weight of an explosive;
0 to 40% by weight of metal;
0.5 to 5% by weight of a polymeric binder; And
And 0 to 10% by weight of a plasticizer.

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