阅读说明：本技术 一种膨化硝铵***的生产方法 (Production method of expanded ammonium nitrate explosive ) 是由 武永 李志雄 刘振茂 张健 黄嵩 邓云云 陈池钦 陆海东 杨明 刘�东 程健 于 2019-10-21 设计创作，主要内容包括：本发明涉及一种膨化硝铵炸药的生产方法,属于炸药生产技术领域。本膨化硝铵炸药的生产方法包括以下步骤：将硝酸铵破碎后,通入蒸汽溶解,得到液态硝酸铵溶液,将液态硝酸铵溶液输送到水相储存罐中保温储存,再计量膨化剂加入到水相储存罐中；复合油经熔化后输送到油相储存罐中保温储存；将水相与油相混合,得到预混合液；预混合液经真空膨化后,得到炸药预产物,多级放料到储存罐中；将敏化剂加入到储存罐中,经螺旋混合输送,并经悬挂凉药输送到料仓后,得到半成品；分装,得到膨化硝铵炸药成品。本发明的效果是能够有效的提高油相和水相的混合均匀程度,同时能够提高膨化过程的膨化均匀度,使得制备的成品膨化硝铵炸药品质稳定。(The invention relates to a production method of an expanded ammonium nitrate explosive, belonging to the technical field of explosive production. The production method of the expanded ammonium nitrate explosive comprises the following steps: after ammonium nitrate is crushed, introducing steam to dissolve the ammonium nitrate to obtain a liquid ammonium nitrate solution, conveying the liquid ammonium nitrate solution to a water phase storage tank for heat preservation and storage, and then metering a swelling agent and adding the swelling agent into the water phase storage tank; the composite oil is melted and then is conveyed into an oil phase storage tank for heat preservation and storage; mixing the water phase and the oil phase to obtain a premix; performing vacuum expansion on the premix to obtain an explosive pre-product, and discharging the explosive pre-product into a storage tank in multiple stages; adding a sensitizer into a storage tank, carrying out spiral mixing and conveying, and carrying out hanging cooling to a storage bin to obtain a semi-finished product; and (5) subpackaging to obtain the finished expanded ammonium nitrate explosive. The invention has the effects of effectively improving the mixing uniformity of the oil phase and the water phase and simultaneously improving the puffing uniformity in the puffing process, so that the prepared finished product puffed ammonium nitrate explosive has stable quality.)

1. A production method of expanded ammonium nitrate explosive is characterized by comprising the following steps:

s1, preparing a water phase: after ammonium nitrate is crushed, steam is introduced to dissolve the ammonium nitrate to obtain liquid ammonium nitrate solution, the liquid ammonium nitrate solution is conveyed into a water phase storage tank and stored at the temperature of 120-130 ℃, and then a swelling agent accounting for 0.2-0.3% of the mass of the liquid ammonium nitrate solution in the water phase storage tank is added to obtain water phase liquid;

s2, oil phase preparation: melting the composite oil, transferring to an oil phase storage tank, and storing at 90-105 deg.C to obtain oil phase liquid;

s3, premixing water and oil: respectively filtering the water phase liquid in the water phase storage tank in the step S1 and the oil phase liquid in the oil phase storage tank in the step S2, and respectively conveying 90-93 parts by weight of the filtered water phase liquid and 3-5 parts by weight of the filtered oil phase liquid into a mixing tank for mixing to obtain a premix;

s4, vacuum puffing: performing vacuum expansion on the premix obtained in the step S3 to obtain an explosive pre-product, and then performing multi-stage discharge and entering a storage tank;

s5, preparing a semi-finished product: weighing 3-5 parts by weight of a sensitizer, adding the sensitizer into the storage tank in the step S4, mixing the sensitizer with the explosive pre-product, conveying the mixture to a hanging conveying herbal medicine cooling machine through a screw conveyor, and conveying the mixture to a storage bin to obtain a semi-finished product;

s6, packaging: and (5) naturally cooling the semi-finished product obtained in the step (S5), metering, and subpackaging into bags to obtain the finished product of the expanded ammonium nitrate explosive.

2. The method for producing an expanded ammonium nitrate explosive according to claim 1, wherein the specific gravity of the aqueous liquid is 1.35 to 1.47g/cm in step S1³。

3. The method for producing an expanded ammonium nitrate explosive according to claim 1, wherein in step S2, the specific gravity of the oil phase liquid is 0.8 to 0.85g/cm³。

4. The method for producing an expanded ammonium nitrate explosive according to claim 1, wherein in step S3, the temperature of the water phase liquid is maintained at 115 ℃ to 125 ℃ and the temperature of the oil phase liquid is maintained at 90 ℃ to 100 ℃ during the transportation to the mixing tank.

5. The method for producing an expanded ammonium nitrate explosive according to claim 1, wherein in the step S4, the vacuum expansion is performed by pumping the premixed solution obtained in the step S3 into a single-effect vacuum crystallizer, performing primary expansion at a vacuum degree of-0.08 MPa and a temperature of 45-55 ℃ to obtain a pre-expanded product, and then putting the pre-expanded product into a double-effect vacuum crystallizer to perform secondary expansion at a vacuum degree of-0.09 MPa and a temperature of 40-45 ℃.

6. The method for producing an expanded ammonium nitrate explosive according to claim 1, wherein in step S4, the multi-stage discharge means that the explosive pre-product falls into a first-stage discharge tank, the explosive pre-product falls into a second-stage discharge tank after a discharge port of the two-effect vacuum crystallizer is closed, the explosive pre-product falls into a third-stage discharge tank after the discharge port of the first-stage discharge tank is closed, and the explosive pre-product finally falls into a storage tank after the discharge port of the second-stage discharge tank is closed.

7. The method for producing an expanded ammonium nitrate explosive according to claim 1, wherein in step S5, the sensitizing agent is wood flour or rice bran flour, the moisture content is less than 6.0 wt%, and the mesh number is more than or equal to 40 meshes.

8. The method for producing an expanded ammonium nitrate explosive according to claim 1, wherein the conveying pressure of the screw conveyor is 0.6Mpa and the temperature is 40-45 ℃ in step S5.

9. A method for producing an expanded ammonium nitrate explosive according to any one of the claims 1 to 8, wherein in step S5, the cooling temperature of the hanging delivery cool drug machine is 44-52 ℃.

10. A method for the production of an expanded ammonium nitrate explosive according to any one of claims 1 to 8 wherein the temperature after natural cooling is less than 50 ℃ in step S6.

Technical Field

The invention belongs to the technical field of explosive production, and particularly relates to a production method of an expanded ammonium nitrate explosive.

Background

Ammonium nitrate explosives are powdery explosive mechanical mixtures, are one of the most widely used industrial explosive varieties, and have moderate power and certain sensitivity.

At present, the existing preparation process of expanded ammonium nitrate explosive comprises the preparation of ammonium nitrate water phase and the preparation of expanding agent oil phase, and the finished ammonium nitrate explosive is prepared after the prepared water phase and the prepared oil phase are mixed and expanded.

However, the water phase and the oil phase produced in the existing production method of the expanded ammonium nitrate explosive are very easy to be mixed unevenly during mixing, so that the quality of the expanded product is unstable. Meanwhile, incomplete puffing is easy to occur in the mixed puffing process, so that the detonation velocity and the brisance of the explosive do not reach the standard, and the quality of the prepared finished explosive is influenced.

In view of the above, there is a need to provide a new method for producing expanded ammonium nitrate explosive, so as to solve the deficiencies of the prior art.

Disclosure of Invention

The invention provides a production method of expanded ammonium nitrate explosive for solving the technical problems, which can effectively improve the mixing uniformity of an oil phase and a water phase, and can improve the expansion uniformity in the expansion process, so that the prepared finished expanded ammonium nitrate explosive has stable quality.

The technical scheme for solving the technical problems is as follows: a production method of expanded ammonium nitrate explosive comprises the following steps:

s1, preparing a water phase: after ammonium nitrate is crushed, steam is introduced to dissolve the ammonium nitrate to obtain liquid ammonium nitrate solution, the liquid ammonium nitrate solution is conveyed into a water phase storage tank and stored at the temperature of 120-130 ℃, and then a swelling agent accounting for 0.2-0.3% of the mass of the liquid ammonium nitrate solution in the water phase storage tank is added to obtain water phase liquid;

s2, oil phase preparation: melting the composite oil, transferring to an oil phase storage tank, and storing at 90-105 deg.C to obtain oil phase liquid;

s3, premixing water and oil: respectively filtering the water phase liquid in the water phase storage tank in the step S1 and the oil phase liquid in the oil phase storage tank in the step S2, and respectively conveying 90-93 parts by weight of the filtered water phase liquid and 3-5 parts by weight of the filtered oil phase liquid into a mixing tank for mixing to obtain a premix;

s4, vacuum puffing: performing vacuum expansion on the premix obtained in the step S3 to obtain an explosive pre-product, and then performing multi-stage discharge and entering a storage tank;

s5, preparing a semi-finished product: weighing 3-5 parts by weight of a sensitizer, adding the sensitizer into the storage tank in the step S4, mixing the sensitizer with the explosive pre-product, conveying the mixture to a hanging conveying herbal medicine cooling machine through a screw conveyor, and conveying the mixture to a storage bin to obtain a semi-finished product;

s6, packaging: and (5) naturally cooling the semi-finished product obtained in the step (S5), metering, and subpackaging into bags to obtain the finished product of the expanded ammonium nitrate explosive.

The invention has the beneficial effects that: through the water phase storage step and the oil phase storage step, the water phase and the oil phase which are prefabricated can be formed firstly, and the heat preservation operation is carried out, so that the mobility of the water phase and the oil phase can be ensured. Meanwhile, the oil-water phase-mixing agent can be taken at any time when in production, and is beneficial to mixing of a water phase and an oil phase. The mixed liquid of the oil phase and the water phase prepared after the storage step is mixed more uniformly, so that the quality of the prepared expanded ammonium nitrate explosive is more uniform. In addition, through the multi-stage discharging step, the prepared explosive pre-product is discharged step by step, the phenomenon that the expansion crystallization effect of the pre-mixed liquid is influenced due to the fact that the degree of vacuum fluctuates greatly during expansion can be effectively avoided, and the stable quality of the expanded ammonium nitrate explosive prepared by production can be improved.

On the basis of the technical scheme, the invention can be further improved as follows.

Further, in step S1, the specific gravity of the aqueous liquid is 1.35 to 1.47g/cm³。

The beneficial effect of adopting the further scheme is that: the influence of water evaporation on the concentration of liquid ammonium nitrate can be avoided, and the conveying amount of the water phase is convenient to meter and control.

Further, in step S2, the specific gravity of the oil phase liquid is 0.8 to 0.85g/cm³。

The beneficial effect of adopting the further scheme is that: to facilitate control of the oil phase delivery.

Further, in step S3, the temperature of the water phase liquid is maintained at 115-125 ℃ and the temperature of the oil phase liquid is maintained at 90-100 ℃ during the transportation to the mixing tank.

The beneficial effect of adopting the further scheme is that: so that the water phase is used to have a temperature during transportation, thereby facilitating mixing of the water phase with the oil phase.

Further, in step S4, the vacuum puffing is to pump the premix of step S3 into a single-effect vacuum crystallizer, perform primary puffing at a vacuum degree of-0.08 MPa and a temperature of 45 to 55 ℃ to obtain a pre-puffed material, and then put the pre-puffed material into a double-effect vacuum crystallizer to perform secondary puffing at a vacuum degree of-0.09 MPa and a temperature of 40 to 45 ℃.

The beneficial effect of adopting the further scheme is that: through setting up two-stage vacuum bulking for mixed liquid bulking effect is better.

Further, in step S4, the multi-stage discharging means that the explosive pre-product falls into a first-stage discharging tank, falls into a second-stage discharging tank after a discharge port of the two-effect vacuum crystallizer is closed, falls into a third-stage discharging tank after the discharge port of the first-stage discharging tank is closed, and finally falls into a storage tank after the discharge port of the second-stage discharging tank is closed.

The beneficial effect of adopting the further scheme is that: the situation that the expansion is affected by the large fluctuation of the vacuum degree in the first-effect vacuum crystallizer and the second-effect vacuum crystallizer is effectively avoided.

Further, in step S5, the sensitizer is wood flour or rice bran flour, the moisture content is less than 6.0 wt%, and the mesh number is more than or equal to 40 meshes.

The beneficial effect of adopting the further scheme is that: the added wood powder needs to be kept dry, so that the explosive blasting effect is prevented from being influenced.

Further, in step S5, the conveying pressure of the screw conveyor is 0.6MPa, and the temperature is 40-45 ℃.

The beneficial effect of adopting the further scheme is that: the spiral mixing plus cooling in the conveying can reduce separate mixing and cooling steps.

Further, in step S5, the cooling temperature of the hanging conveying herbal medicine cooling machine is 44-52 ℃.

The beneficial effect of adopting the further scheme is that: the explosive pre-product and the wood powder which are uniformly mixed are conveyed to a storage bin through a hanging conveying explosive cooling machine, and meanwhile, the explosive pre-product and the wood powder are further cooled in the conveying process, so that the special cooling steps are reduced.

Further, in step S6, the temperature after natural cooling is less than 50 ℃.

The beneficial effect of adopting the further scheme is that: the potential safety hazard caused by the high temperature can be avoided.

Drawings

FIG. 1 is a schematic flow diagram of a process for producing an expanded ammonium nitrate explosive according to the present invention.

Detailed Description

The principles and features of this invention are described below in conjunction with the following drawings, which are set forth by way of illustration only and are not intended to limit the scope of the invention.