CA1186152A - Continuous method for the preparation of explosives emulsion precursor - Google Patents

Continuous method for the preparation of explosives emulsion precursor

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Publication number
CA1186152A
CA1186152A CA000400386A CA400386A CA1186152A CA 1186152 A CA1186152 A CA 1186152A CA 000400386 A CA000400386 A CA 000400386A CA 400386 A CA400386 A CA 400386A CA 1186152 A CA1186152 A CA 1186152A
Authority
CA
Canada
Prior art keywords
fuel
mixer
phase
emulsion
salt solution
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired
Application number
CA000400386A
Other languages
French (fr)
Inventor
Rejean Binet
Ming C. Lee
Roland Picard
Chang-Hwa Chin
Anthony C.F. Edmonds
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
PPG Architectural Coatings Canada Inc
Original Assignee
Rejean Binet
Ming C. Lee
Roland Picard
Chang-Hwa Chin
Anthony C.F. Edmonds
C-I-L Inc.
Ici Canada Inc.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Rejean Binet, Ming C. Lee, Roland Picard, Chang-Hwa Chin, Anthony C.F. Edmonds, C-I-L Inc., Ici Canada Inc. filed Critical Rejean Binet
Priority to CA000400386A priority Critical patent/CA1186152A/en
Priority to NZ203653A priority patent/NZ203653A/en
Priority to US06/478,292 priority patent/US4472215A/en
Priority to AU13106/83A priority patent/AU549820B2/en
Application granted granted Critical
Publication of CA1186152A publication Critical patent/CA1186152A/en
Expired legal-status Critical Current

Links

Classifications

    • CCHEMISTRY; METALLURGY
    • C06EXPLOSIVES; MATCHES
    • C06BEXPLOSIVES OR THERMIC COMPOSITIONS; MANUFACTURE THEREOF; USE OF SINGLE SUBSTANCES AS EXPLOSIVES
    • C06B21/00Apparatus or methods for working-up explosives, e.g. forming, cutting, drying
    • C06B21/0008Compounding the ingredient
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01FMIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/50Circulation mixers, e.g. wherein at least part of the mixture is discharged from and reintroduced into a receptacle
    • B01F25/51Circulation mixers, e.g. wherein at least part of the mixture is discharged from and reintroduced into a receptacle in which the mixture is circulated through a set of tubes, e.g. with gradual introduction of a component into the circulating flow
    • CCHEMISTRY; METALLURGY
    • C06EXPLOSIVES; MATCHES
    • C06BEXPLOSIVES OR THERMIC COMPOSITIONS; MANUFACTURE THEREOF; USE OF SINGLE SUBSTANCES AS EXPLOSIVES
    • C06B47/00Compositions in which the components are separately stored until the moment of burning or explosion, e.g. "Sprengel"-type explosives; Suspensions of solid component in a normally non-explosive liquid phase, including a thickened aqueous phase
    • C06B47/14Compositions in which the components are separately stored until the moment of burning or explosion, e.g. "Sprengel"-type explosives; Suspensions of solid component in a normally non-explosive liquid phase, including a thickened aqueous phase comprising a solid component and an aqueous phase
    • C06B47/145Water in oil emulsion type explosives in which a carbonaceous fuel forms the continuous phase

Abstract

Abstract Continuous Method for the Preparation of Explosive Emulsion Precursor A process and apparatus is provided for the con-tinuous manufacture of a water-in-oil explosive emulsion precursor. Separate streams of the water phase component and the oil phase component are introduced into an in-line motionless mixer. A chosen portion of the output from the mixer is recirculated and returned to the motionless mixer for further emulsification. The process allows for the production of a very high phase ratio water-to-oil emulsion (up to 95% water phase) without phase inversion after long storage. The precursor is simply converted to a sensitive explosive by means of known density lower-ing techniques.

Description

~ 36~S~

The present invention relates to a method and apparatus for the continuous manufacture o~ an emulsified water-in-oil precursor for emulsion explosives. In particular, the invention relates to the continuous production of an emulsified precursor for emulsion explosives employing a mixing zone containing a mokionless mixer. By explosive emulsion precursor is meant a com-position ~hich is substantially insensitive to initiation 10 except by strong boostering but which can be converted into a useful and often cap-sensitive explosive by the lowering of its density by, for example, the inclusion therein of minute gas bubbles or ~articulate void-containing material such as glass or resin microspheres.
Water-in-oil emulsion explosives are now well known in the explosives art and have been demonstrated to be safe, economic and simple to manufacture and to yield excellent blasting results. Bluhm, in United States Patent No. 3,447,978, disclosed an emulsion explosive composition 20 comprising an aqueous discontinous phase containing dis-solved oxygen-supplying salts, a carbonaceous fuel continuous ph~se, an occluded gas and an emulsifierO Since Bluhm, further disclosures have described improvements and variations in water in-oil explosives compositions.

~86~
- 2 - C-I-L 647 These include United States patent No. 3,674,578, Cattermole et al., United States patent No. 3,770,522, Tomic, United States patent No. 3,715,247, Wade, United States patent No. 3,675,964, Wade, United States patent No. 4,110,134, Wade, United States patent No. 4,149,916, Wade, United States patent No. 4,141,917, Wade, United States patent No. 4,141,767, Sudweeks & Jessup, Canadian patent No. 1,096,173, Binet & Set:o, United States patent 10 No. 4,111,727, Clay, United States patent No. 4,10~,092, Mullay, United States patent No. 4,~31,821, Sudweeks &
Lawrence, United States patent No. 4,218,272, Brockington, United States pa-tent No. 4,138,281, Olney & Wade, United States patent No. 4,216,040, Sudweeks & Jessup.
Emulslon explosive compositions have, in most instances, been manufactured in commercial quantities by means of batch processes employing conventional high-shear mixing apparatus. Generally, the prior art has not been speci~ic in suggesting an~ particular mixing or 20 emulsifying apparatus or techniques, references usually being made merely to "agitation" or "mixing" or "blending"
of the aqueous phase and the oil phase in the presence of an emulsifier. Cattermole et al, in U.S. Reg. No.
28060, refer to the use of a turbine mixer. Chrisp, in 25 U.S. patent No. 4008108, refers to a high shear mixer, that is, a shear pump. Olney, in U.S. patent No. 4138281, suggests the possible use of a continuous recycle mixer, for example, the VOTATOR (Reg TM) mixer, an in-line mixer, for example, the TURBON (Reg TM) and a colloid type 30 mixer, for example, the OAKES (Reg TM). In recent Canadian patent No. 1,106,835, Aanonsen et al refer to the potential utility and advantages of an in-line motion-less or "static" mixer for emulsion explosives manufacture, but the inventors note that such a mixer is deficient 35 since it does not generally achieve adequate dispersion of the fuel phase liquid in the aqueous oxidizer salt 36~5~
- 3 - C-I-L 647 phase, esp~cially where the fuels are viscous or where the emulsified composition has a relatively high viscosity.
~anonsen et al state that, to date, it has been necessary to employ mechanically driven mixing means to produce adequate emulsion compositions.
It is self-evident that in the manufacture of any sensitive explosive material, the use of mechanical mixers with the ever-present risk of breakdown and impact 10 should be avoided. In addition, the generation o~ heat by any high shear mechanical mixing device produces additional hazard. Furthermore, with mechanical mixers production rates are limited and, often, capital invest-ment is high.
Notwithstanding the commonly held belief that an in-line, static or motionless mixer is an inappropriate apparatus for the manufacture of high phase ratio wa-ter-in-oil emulsion explosives, applicants have now found that a conventional in-line static mixer can be adapted 20 for the efficient production of a highly viscous and stable high phase ratio explosive emulsion precursor which is superior to emulsions prepared with high shear mechanical mixers, and without the attendant risks.
By "in~line static mixer" is meant a hollow, 25 generally tubular element containing one or more stationary, perforated or slotted elements which achieve mixing by dividing and sub-dividing a fluid flow passing therethrough. Typical of such static mixers is, for example~ the SULZER mixer manufactured by Sulzer Brothers 30 Limited of Switzerland. By high phase ratio water-in-oil emulsion is meant an emulsion composition wherein the amount of the dispersed aqueous phase comprises at least 90% by weight of the total compositions and may comprise as much as 95% by weight or more of the total composition.
For purposes of an explosive composition, intimate s~
4 - C-I-L 647 contact between the oxygen-rich oxidizer salt phase and the carbonaceous fuel phase is required and a very small droplet size and distribution is particularly desirable.
Such a finely homogenized composition tends to be quite viscous, especially where the fuel phase comprises as little as 5~ by weight of the total composition. Standard colloid mills and blenders are not normally capable of forming such high phase-ratio, small droplet emulsions 10 and recourse has been taken to the use of high shear, high power consumption mixing devices with their attendant high operating cost,relatively low productivity and potential hazard.
By employing a mixing zone comprising a conventional 15 in-line static or motionless mixer having a recirculation loop through which a chosen proportion of the mixed and emulsified product may be passed again through the static mixer, applicants have found that continuous production of high phase ratio emulsions can be achieved without any 20 of the inherent disadvantages of prior art methods.
In order to provide a better understanding of the invention, reference is made to the accompanying drawing, which shows a schematic representation of the process of the invention.
Referring to the drawing, there is shown a mixing zone~ generally designated by 1. Zone 1 consists of horizontal pipe or tube 2 containing an in-line static mi~er 3. Leading into pipe 2 is aqueous phase inlet 4 and oil phase inlet 5. Connected to oil inlet 5 is 30 emulsifier inlet 6. Direction of ~low in all piping is indicated by the arrows. A pipe loop 7 containing pump 3 is shown on each side of static mixer 3. A second, optional static mixer in pipe 2 beyond loop 7 is shown at 9. A pressure or flow gauge is shown at 10.
The preparation of a high phase ratio water-in-oil 86~S;~
5 - ~-I-L 647 emulsion explosive precursor composition will be described with reference to the drawing. The oil or fuel component of the composition may comprise, for example, a variety of saturated or unsaturated hydrocarbons including petroleum oils, vegetable oils, mineral oils, dinitrotoluene or mixtures of these. Optionally, an amount of a wax may be incorporated in the fuel component. Such a fuel component is stored in a holding tank (not shown) which tank is often 10 heated to maintain fluidity of the fuel component. The fuel is introduced into mixing zone 1 through inlet conduit 5 by means of a metering type pump (not shown) or similar means.
~n emulsifier, such as for example sorbitan mono-oleate, sorbitan ~esqui-oleate or Alkaterge T (Reg TM~ is propor-15 tionally added to the fuel component in conduit 5 via conduit6. Alternatively, the emulsifier may be incorporated into the fuel component in the fuel reservoir (not shown). The amount of emulsifier added generally comprises from about .4 to 4% by weight of the total composition. An aqueous 20 solution of oxidizer salt containing 70% or more by weight of salts selected from ammonium nitrate, alkali and alkaline eabrth metal nitrates and perchlorates, amine nitrates or mixtures thereof, is delivered from a heated tank or reservoir (not shown) by means of metering pump (not shown) to mixing 25 zone l through conduit inlet 4. The oxidizer salt solution is maintained in a supersaturated state. The rate of flow of the fuel/emulsifier component and the oxidizer salt solution component can be adjusted so that the resultant mixture is in a desired high phase ratio typically, for 30 example, 94% by weight of the oxidizer phase to 6% by weight of the fuel/emulsifier phase. In actual operation, recircu-lation pump 8 in recirculation loop 7 is first activated and the fuel/emulsifier component is introduced into pipe 2, passed through static mixer 3 and recirculated through 35 loop 7. When substantially all of the volume of loop 7 has
6:~5~

been filled with the fuel/emulsifier component, the aqueous oxidizer component is then metered into pipe 2 where it forms a crude mixture with the fuel/emulsifier component.
The crude mixture then passes through static mixer 3 where it is converted into a coarse water-in-oil emulsion. A
proportion, at least 80% and up to 95% by volume of the coarse emulsion is drawn through recirculation loop 7 by pump 8 and returned to the crude stream in pipe 2 and 10 passed again through static mixer 3. Thus a large pro-portion is thus repeatedly recirculated through loop 7.
By first substantially filling the mixing zone 1 with a stream of fuel/emulsifier component and thereafter adding a metered amount of the aqueous salt component to this 15 fuel stream, dominance of the fuel/emulsifier component as the continuous phase of the resultant emulsion is accomplished at the outset of the production run. By recirculating a large portion of the coarse emulsion through loop 7, a continuous fuel phase dominance in the 20 emulsion product is maintained. The amount of recirculated product drawn through loop 7, essential to maintain dominance of the fuel phase, will vary depending on such factors as, for example, the phase ratio of the emulsion itself, the amount and effectiveness of the emulsifier 25 employed and the type of fuel selected. The actual value for the recirculation quantity is simply determined in operation by reducing the flow rate of pump 8 and observing the state of the final product. If phase inversion occurs, the quantity of recirculating coarse emulsion in increased 30 until the dominance of the oil phase is again achieved.
To produce a sensitive explosive emulsion containing very small droplet size, the product from mixing zone 1, which consists of a mix of a minor amount of coarse one-pass product and a major amount of finer multiple-pass produc~t, 5 is directed through an additional in-line static mixer 9
- 7 - C-I-L 647 and the density of the final product adjusted to a sensitive range by, for example, the addition of gas bubbles or particulate void-containing material.
The in-line static mixer employed in the process of the invention achieves emulsification of the two phases by continuous splitting and layer generation and the rearrangement and reunification of the incoming phase streams. In optimum performance, the mixers are operated 10 under turbulent flow range condltions. Suitable static mixers are the SULZER containing some SMV type mixing elements (Koch Engineering Co. Inc. of New York, U.S.A.) or the ROSS containing some ISG mixing elements (Charles Ross and Son Co. of Hauppauge, New York, U.S.A.) which 15 static mixing units comprise a number of these stationary elements housed in a pipe. The number and size of the elements can be selected to achieve the desired final produc-t emulsification.
The recirculation pump employed will be of the 20 positive displacement type, and preferably with variable speed. The pump size or capacity selected will depend on ratio of recirculated material to the total production flow.
The following examples describe the invention 25 but are not to be interpreted as a limitation in the scope thereof.

A precursor for a water-in-oil emulsion explosive of -the type described in applicant's pending Canadian Application 30 Serial No. 342,098 filed December 14, 1979 was prepared using the arrangement shown in the drawing. The chemical composition of this emulsion is shown in TABLE I below.

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- 8 - C-I~L 647 TABLE l . . . ___ _ __ __ , w/o Fmulsion Composition Parts Ingredients by Weight Oil Phase Emulsifier l 1.7 Paraffin Oil 2.5 Paraffin Wax 1.7 Aqueous Phase Ammonium Nitrate 61.1 Sodium Nitrate 14.7 Calcium Nitrate 3.6 Water 12.2 Dispersed phase/continuous phase weight ratio = 15.5 to 1.0 or 94%
. _ _ _ lEmulsifier comprising 0.7 parts Soya Lecithin, 0.7 parts Sorbitan Sesqui-oleate and 0.3 parts of a Polymeric emulsifying agent.
20 The production (total) flow rate was about 4.7 kg/min and the recirculation ratio was about 8 to l or 89~,well above the minimum recirculation ratio of about 5 to l below which emulsion does not form, or at which emulsion inver-sion occurred. A low pressure-drop motionless mixer unit 25 was used in the recirculation loop and consisted of 14 Sulzer SMV Type CY mixing elements housed in a 25.1 mm diameter schedule 40 stainless steel pipe, (Ex. 1) Also, three different high pressure-drop motionless mixer units were used in combination with the low-pressure-drop mixer.
30 These high pressure-drop units were:
Example 2 -A unit consisting of 10 Sulzer SMV Type DY
mixing elements housed in a 9.4 mm diameter schedule 40 stainless steel pipe, ~8~i~S~
9 - C-I-L 647 Example 3 -A unit consisting of lO Sulzer SMV Type DY
mixing elements housed in a 9.4 mm diameter schedule 80 stainless steel pipe, and Example 4 -A unit consisting of lO ISG Ross mixing elements housed in a 12.5 mm diameter stainless steel pipe.
The emulsions obtained were examined for droplet lO size distribution by either optical microscopy at 1,200 magnification or by freeze-fracture electron micrography at 10,000 and 50,000 magnification. The result of this analysis is presented in TABLE II as follows:
TABLE II

Droplet_Size Analysis of Emulsions-Recirculation Motionless Mixers Combination Exam~leUnit 34 Unit 34 125 mm Sulzer 225 mm Sulzer9.4 mm Sulzer-Sch. 40 20 325 mm Sulzer9.4 mm Sulzer-Sch. 80 425 mm Sulzer12.5 mm Ross ISG
, .. . . _ .
TABLE II cont'd Droplet Size Analysis of EmuIsions-Recirculation Total Pressure Drop dl 25 Example (~
1 50 - 75 2.762 3 650 - 700 1.322 4 750 - 800 1.232 30 1 Number average droplets size.
Analyzed by freeze-fracture electron micrography.
3 Analyzed by optical microscopy.
4 As shown in the drawing~

~36:~5~
- 10 - C-I-L 647 From the results presented in TABLE II it can be seen that the emulsification process and apparatus of the present invention as represented by Ex. 1 to 4 is particularly useEul in forming high-phase ratio emulsions with very small drople-t size distributions.

In order to compare the effectiveness of the process of Examples 1 - 4 with a process using identical 10 motionless mixer elements but without any recirculation of product, the emulsion composition of Table 1 was straight-passed through the mixers without recirculation.
The results are shown in Table III below:
TABLE III
. _ ~ , ~otionless Mixers Combination Example Unit 3Unit 3 25 mm Sulzer 6 25 mm 5ulzer 9.4 mm Sulzer-Sch. 40 7 25 mm Sulzer 9.4 mm Sulzer-Sch. 80 8 25 mm Sulzer 12.5 mm Ross ISG
-TABLE III cont'd . _ Droplet Size Analysis of Emulsions - Straight Pass Total Pressure Drop -dnl 25 Example (psig) (~) 10 ~ 20 no emulsion 6 30 - 50 no emulsion 7 200 - 400 no emulsion 8 300 - 500 no emulsion . . ~
* As shown in the drawing.
As can be seen by comparing the results in Tables II and III, in order to form an emulsion it was necessary to employ a recirculation loop.

5'~
~ C-I-L 647 A comparison of average droplet size between the emulsion compositions of Table II and emulsions produced using a selection of common homogenizing and/or emulsifying devices was made. The results using common devices are shown in Table IV below.
TABLE IV
, ~
Droplet Sizes with Various Emulsifying Devices Device Pr~ssure Drop dn (E~) (,~) Votatorl (Reg TM) 50 - 60 1.754 Colloid Mill 35 - 40 1.314 Sonolator3 (Reg TM) 575 - 600 0.80 A 5 H.P. 6" Model Votator CR mixer from Chemetron Process Equipment of Louisvilie, KentuckyO The emulsion of dn = 2.76 pm of TABLE II was fed at a rate o~ 4.7 kg/min to the ~otator running at 1,800 rpm.

20 2 A 3 H.P. Model 3 Colby Colloid Mill from Canadian Thermopower Industries of Islington, Ontario. A coarse emulsion of dn of about 5 ~m was fed at a rate of 4.6 kg/min to the Colloid Mill running at 5,000 rpm with the gap between 25 the rotor and the stator set at 0.075 mm (3 mils).

A Model 3 Sonolator from Sonic Corporation of Stratford, Connecticut. The emulsion of dn =

2.76 ~m of TABLE II was fed at a rate of 4.7 kg/min through a nozzle of 0.002 inch2.

30 4 Number average droplet sizes analyzed by freeze-fracture electron micrography at 10,000 and 50,000 magnification.

36~

The dispersed phase of an emulsion explosive is typically composed of a highly concentrated nitrate salt solution as exemplified by the composition of TABLE I.
It has been observed that a substantial proportion of the individual emulsion droplets can in fact remain in a super-saturated state once the emulsion is cooled below the saturation temperature. For optimum blasting perfor-10 mance and long-term storage stability as an explosive emulsion composition, it is most important to preserve this super~saturation and minimize crystal growth of the emulsion droplets. Two factors appear to have an influence on this phenomenon:
15 1) The amount and effectiveness of the emulsifying agent used, and 2) the emulsification process.
In order to further exemplify the merit and utility of the emulsification process and apparatus of 20 the present invention, the stability and sensitivity of emulsions prepared by this process were compared to emulsions prepared by the devices of TABLE IV. To make these emulsions sensitive to cap-initiation in 25 mm diameter charges, 2.5 parts by weight of glass 25 microbubbles were admixed to bring their density to about 1.12 + 0.02 g/cc in every case. Results are presented in TABLE V below.

5~

TABLE V

Sensitivity/Stability of Explosive Emulsions EX. 10 EX. 11 9.4 mm Sulzer- ~onolator Properties Sch. 80 _ .. . .
dn (~m) 1.32 1.75 M. In. (fresh) R-73 R-93 M. In. after 2 months R-7 E.B.
10 storage at 35C
M. In. after 4 R-83 E.B.4 cycles2 + 35~C
M. In.2 after 12 R-113 F. 2EB
cycl~s + 35C
_ . .
TABLE V cont'd Sensitivlty/Stabillty of Explosive Emulsions _ _.
EX. 12 EX. 13 Properties Colloid Mill Sonolator dn (~m) 1.31 0.80 20 M. In. (fresh) R-9 R-9 M~ In. after 2 months E.B. F.E.B.
storage at 35C
M. In. after 4 cycles2 _ 35C E.B. F.E.B.
25 M. In.2 after 12 F. 2EB
cycles + 35C

1 Minimum initiator to detonate the explosive in 25 mm diameter charges at 5C in all cases.
2 One cycle consisted of 2-3 days storage at 35C followed by 2-3 days of storage at - 35C.
3 R-series of detonators are charged with increasing amounts of GAM/PETN. R-7(0.1g GAM ~ 0.2g PETN),R-8(0.1g GAM + 0.-25g PETN
R-9(0.lg GAM + 0.3g PETN),R-11(0.lg GAM + 0.4g PET~
4 Electric Blasting detonator containing 0.78 g PETN.

5 Failed initiation with 2 Electric Blasting detonators.

L5;~
- 14 - C,I-L 647 From results presented in TABLE V, it can be seen that the explosive emulsions prepared by the emulsification process and apparatus of the present invention (EX. lO~
possess outstanding stabilities and sensitivities when compared to compositions prepared by the other emulsifying devices.

Claims

(1) A continuous method for the manufacture of a water-in-oil explosive emulsion precursor wherein the ratio of dis-continuous aqueous phase to continuous oil phase is at least 8 to 1 by weight, comprising the steps of:
(a) forming an aqueous salt solution containing at least 75%
by weight of oxygen-supplying salt, (b) forming a liquid mixture comprising a hydrocarbon fuel and an emulsifier, (c) passing a stream of said liquid fuel-emulsifier mixture into the inlet of a motionless in-line mixer, collecting said stream from the outlet of said mixer and reintroducing same through a recirculation loop into the said mixer inlet until the said recirculation loop is substantially filled with said fuel/emulsifier mixture, (d) introducing and continuously adding a stream of said aqueous salt solution to the said recirculating fuel/
emulsifier mixture stream, the weight ratio of said salt solution to said fuel/emulsifier mixture being at least 8:1, and passing said salt and fuel streams through the said in-line mixer, (e) collecting at least 80% by volume of the mixed streams from the said in-line mixer outlet and reintroducing same through said recirculation loop to the said in-line mixer inlet for further mixing, and (f) withdrawing the mixed unrecirculated and recirculated streams from the said in-line mixer outlet in the form of a stable water-in-oil emulsion explosive precursor while adding an amount of liquid fuel/emulsifier mixture and an a-queous salt solution to the said in-line mixer inlet in an amount equal to the amount of emulsion withdrawn.
(2) A method as claimed in Claim 1, wherein the said salt solution is maintained at a temperature above the crystallization temperature.
(3) A method as claimed in Claim 1, wherein the said fuel/emulsifier mixture is formed from converging streams of fuel and emulsifier.

(4) A method as claimed in Claim 1, wherein the quantity of recirculating material is variable.
(5) An apparatus for the continuous production of a water-in oil explosive emulsion precursor, said apparatus comprising:
(a) a tubular conduit having an entry end and an exit end, (b) means associated with the said entry end for the delivery therein of separate streams of an aqueous salt solution phase and a liquid hydrocarbon fuel phase, (c) an in-line motionless mixer located in said conduit between the said entry and exit ends for the mixing and emulsification of said separate salt solution and liquid fuel phases, (d) a recirculating duct loop connected into said tubular conduit on either side of said motionless mixer, and (e) pump means in said recirculating duct loop adapted to recirculate a portion of said mixed salt solution and liquid fuel phases from an outlet of said motionless mixer to an inlet of said motionless mixer.
(6) An apparatus as claimed in Claim 5 also containing means whereby an emulsifier may be continuously added to the said liquid hydrocarbon fuel phase.
CA000400386A 1982-04-02 1982-04-02 Continuous method for the preparation of explosives emulsion precursor Expired CA1186152A (en)

Priority Applications (4)

Application Number Priority Date Filing Date Title
CA000400386A CA1186152A (en) 1982-04-02 1982-04-02 Continuous method for the preparation of explosives emulsion precursor
NZ203653A NZ203653A (en) 1982-04-02 1983-03-22 A continuous method for the manufacture of a precursor of a water-in-oil emulsion explosive
US06/478,292 US4472215A (en) 1982-04-02 1983-03-24 Continuous method and apparatus for the preparation of explosives emulsion precursor
AU13106/83A AU549820B2 (en) 1982-04-02 1983-03-31 Forming explosive emulsion precursor

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CA000400386A CA1186152A (en) 1982-04-02 1982-04-02 Continuous method for the preparation of explosives emulsion precursor

Publications (1)

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CA1186152A true CA1186152A (en) 1985-04-30

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