Energy-containing material production route and production process based on gas-liquid dual-circulation system

Abstract

The invention discloses an energetic material production route and production process based on a gas-liquid dual-circulation system, and belongs to the technical field of energetic material production. The production system is used for forming and processing energetic materials, and the carrier gas conveying system provides carrier gas power for the production system; solvent-rich mixed gas discharged by the production system is subjected to graded dust removal through the dry-wet mixed dust removal system, large-particle dust and part of solvent steam are removed through wet condensation dust removal, fine dust is further filtered through the dry filter dust remover, output solvent carrier gas enters the solvent recovery system to be subjected to condensation and adsorption treatment, and the solvent-rich mixed gas is discharged through the dry-wet mixed dust removal system. The efficient recovery of the solvent is realized. The recovered regenerated carrier gas is re-introduced into the carrier gas conveying system to form single-input and multi-cycle closed flow, and through gas-liquid double-cycle cooperative operation, the synchronous recovery and cyclic utilization of the carrier gas and the solvent are realized, the energy consumption and the material loss are obviously reduced, and the benefits of the energetic material production process are improved.

Description

Technical Field

[0001] This invention relates to the field of energetic materials production technology, specifically to an energetic materials production route and process based on a gas-liquid dual circulation system. Background Technology

[0002] The production of energetic materials requires the participation of solvents and carrier gases to drive material movement and achieve uniform dispersion and safe production. Solvent recovery is a common method to improve the overall economics and environmental friendliness of the production line. In contrast, carrier gas has lower costs and safety risks, and its recovery and recycling systems are relatively rare. However, the amount of carrier gas used is large in production, solvent dispersing, and other processes, and the cost of continuously introducing nitrogen from the outside cannot be ignored.

[0003] Furthermore, energetic materials are prone to forming fine energetic dust particles under the purging of carrier gas, which then accumulate inside the pipeline, posing a potential hazard to the production process. Considering the small particle size (micro-nano scale) of energetic dust, the removal efficiency of traditional filtration-based dust removal equipment is limited. While water curtain dust removal is effective, it inevitably introduces impurities such as water vapor, leading to a decrease in product quality stability. This necessitates the introduction of targeted impurity removal equipment, increasing production costs and complexity, and creating difficulties for subsequent maintenance. Therefore, a safe, simple, and maintenance-free safe drying and dissolving process route needs to be developed.

[0004] In view of the above, the present invention designs an energetic material production route and process based on a gas-liquid dual circulation system, which solves the above-mentioned technical problems. Summary of the Invention

[0005] The technical objective of this invention is to provide a production route and process for energetic materials based on a gas-liquid dual circulation system, thereby solving the problems of unrecyclable carrier gas and solvent, resource waste, and pollution emissions during the production of energetic materials.

[0006] To achieve the above-mentioned technical objectives, the present invention provides the following technical solution: This invention provides a production route for energetic materials based on a gas-liquid dual-circulation system, comprising a production system for producing and molding energetic materials. The production system has an input end connected to a carrier gas delivery system for introducing the required carrier gas. The system also includes a wet-dry mixing dust removal system and a solvent recovery system. The input end of the wet-dry mixing dust removal system is connected to the output end of the production system. The input end of the solvent recovery system is connected to the output end of the wet-dry mixing dust removal system, and is used to recover the solvent carried in the carrier gas through condensation and adsorption. The carrier gas output end of the solvent recovery system is connected to the carrier gas delivery system to form a single-input carrier gas circulation flow. The solvent output end of the solvent recovery system is connected to the wet-dry dust removal system to replenish the solvent in the wet-dry dust removal system.

[0007] Furthermore, the wet-dry mixed dust removal system includes a wet condensation dust removal system and a dry filtration dust removal system. The input end of the wet condensation dust removal system is connected to the output end of the production system, the output end of the wet condensation dust removal system is connected to the input end of the dry filtration dust removal system, and the output end of the dry filtration dust removal system is connected to the input end of the solvent recovery system.

[0008] Furthermore, the wet condensation dust removal system includes a dust collector, an exhaust pipe, a liquid collection tank, a level gauge, and an auxiliary fan. The dust collector removes dust using a water curtain dust removal method. The exhaust pipe is connected to the output end of the production system and is used to introduce carrier gas into the dust collector. The liquid collection tank is connected to the solvent liquid inside the dust collector. The level gauge is installed inside the dust collector to monitor the volume of the solvent liquid inside the dust collector. The auxiliary fan is located at the top of the dust collector and is used to discharge the carrier gas that has undergone dust removal treatment inside the dust collector. A drain port is also provided at the bottom of the dust collector. The dry filtration dust removal system filters dust from the carrier gas through a dry dust filter.

[0009] When the level gauge detects that the solvent capacity in the dust collector is lower than a set threshold, the solvent output end of the solvent recovery system replenishes the dust collector by introducing solvent through a pipeline; when the solvent capacity in the dust collector is higher than the set threshold, the solvent in the dust collector flows into the collection tank.

[0010] Preferably, the solvent liquid in the dust collector is further provided with a heat exchanger, which is connected to an external refrigeration system through a heat exchange pipeline for cooling the solvent liquid in the dust collector.

[0011] The solvent recovery system includes a condensation recovery system and an adsorption system. The condensation recovery system includes an air condenser and a liquid storage tank. The air condenser condenses the incoming carrier gas by connecting to a refrigeration system. The liquid storage tank is used to store the solvent liquid condensed from the carrier gas. The liquid storage tank is connected to the dust collector in the wet condensation dust removal system via a diaphragm pump.

[0012] Preferably, the adsorption system includes multiple adsorption tanks for adsorbing solvents in the carrier gas. The multiple adsorption tanks are connected in series to form a closed circulation pipeline. The input ends of the multiple adsorption tanks are connected in parallel to the carrier gas output end of the condensation recovery system, and the output ends of the multiple adsorption tanks are connected in parallel to the carrier gas delivery system.

[0013] Furthermore, the carrier gas delivery system is also connected to a secondary compression circulation system. The secondary compression circulation system includes a booster system, a check valve, a gas storage tank, a carrier gas heater, a carrier gas cooler, and a carrier gas output pipeline. The booster system and the check valve are located at the input end of the secondary compression circulation system. The input end of the gas storage tank is connected to the output end of the booster system through the check valve. The input ends of the carrier gas heater and the carrier gas cooler are connected in parallel to the output end of the gas storage tank. The output ends of the carrier gas heater and carrier gas cooler are connected in reverse to the output ends of the multiple adsorption tanks through the regeneration gas inlet pipe, and the adsorption tanks are further connected in reverse to the input end of the condensation recovery system through the regeneration gas outlet pipe. The output end of the gas storage tank is also connected to the dry dust filter in the production system and the dry dust removal system. The dry dust filter is also equipped with a differential pressure sensor and a backflush valve. The backflush valve is located on the pipeline between the output end of the gas storage tank and the dry dust filter. After the backflush valve is opened, it is used to reverse the flow of carrier gas into the dry dust filter. The differential pressure sensor is used to monitor the positive and negative air pressure difference inside the dry dust filter.

[0014] Based on the above, preferably, the carrier gas delivery system includes a liquid content monitoring system, an oxygen concentration monitoring system, an vent valve, a main circuit isolation valve, a carrier gas inlet valve, an air inlet valve, a pressure sensor, a main fan, an air heater, and a temperature sensor; the liquid content monitoring system and the oxygen concentration monitoring system are connected to the carrier gas output end of the solvent recovery system to monitor the output data of the carrier gas; the input end of the vent valve is connected to the carrier gas output end of the solvent recovery system, and the output end of the vent valve is connected to a discharge pipe, which is used to discharge carrier gas with compliant output data; the main circuit isolation valve, pressure sensor, main fan, air heater, and temperature sensor are connected in series between the output end of the solvent recovery system and the input end of the production system to form a carrier gas circulation pipeline; the carrier gas inlet valve is used to connect the pipeline for carrier gas to enter the production system; the air inlet valve is used to connect the pipeline for air to enter the production system.

[0015] This invention also provides a process for producing energetic materials based on a gas-liquid dual circulation system, applicable to the aforementioned production route for energetic materials based on a gas-liquid dual circulation system, specifically including the following steps: S1. Close the air intake valve, open the carrier air intake valve and the vent valve, and introduce carrier air into the production system. S2. The gas parameters in the pipeline are continuously monitored by the oxygen concentration monitoring system, liquid content monitoring system and pressure sensor. The carrier gas is automatically replenished and the waste gas is discharged in the production system according to the preset carrier gas index requirements until the purity of the carrier gas in the production line meets the process requirements. S3. Close the vent valve, start the secondary compression circulation system, and when the carrier gas pressure meets the requirements, close the carrier gas inlet valve, turn on the air heater, and preheat the carrier gas in the production line to 65°C. S4. After the carrier gas condition remains stable for 1 hour, start the production system to begin production. S5. After the initial carrier gas flows through the production system, it forms a mixed carrier gas rich in solvent and dust, which is then introduced into a wet condensation dust removal system for preliminary dust removal. S6. The mixed carrier gas that has undergone preliminary dust removal is then introduced into the dry filtration dust removal system for secondary dust removal, and outputs solvent-rich carrier gas. S7. The solvent carrier gas is introduced into the condensation recovery system for condensation treatment, and part of the solvent in the solvent carrier gas is condensed and recovered and stored in the liquid storage tank. When the solvent liquid in the wet condensation dust removal system is insufficient, the diaphragm pump draws the solvent from the liquid storage tank into the dust collector. S8. The solvent carrier gas is then introduced into the adsorption system. The adsorption tank adsorbs and recovers the remaining solvent in the solvent carrier gas and retains it in the adsorption tank, thereby outputting the regenerated carrier gas. The carrier gas output from the adsorption system is output under the detection of the solvent concentration sensor. If the concentration meets the standard, regenerated carrier gas is output; if the concentration does not meet the standard, it continues to be fed into the condensation recovery system for solvent recovery. S9. Regenerated carrier gas is introduced into the carrier gas delivery system and then reintroduced into the production route to form a cycle.

[0016] The process of regenerated carrier gas being introduced into the carrier gas delivery system and then re-entering the production route to form a cycle includes the following steps: S9.1 A portion of the regenerated carrier gas is introduced into the secondary compression cycle system, and the regenerated carrier gas is pressurized by the pressurization system to obtain pressurized carrier gas; S9.2 A portion of the pressurized carrier gas is introduced into the carrier gas heater and the carrier gas cooler to obtain heated carrier gas and cooled carrier gas, respectively; S9.3. The heated carrier gas, heated to 90°C, is introduced into the adsorption tank after saturation adsorption to desorb the saturated adsorption medium in the adsorption tank. S9.4 After desorption is completed, cooling carrier gas is introduced into the adsorption tank to cool down the adsorption medium inside the tank, so that the adsorption medium can regain its adsorption function. S9.5, and another part of the pressurized carrier gas is sent to the production system through the carrier gas output pipeline to participate in production and the dry filtration dust removal system for reverse blowing. In this process, pressurized carrier gas is reversed and introduced into the dry dust filter for cleaning.

[0017] The beneficial effects of this invention are as follows: 1. This invention constructs a gas-liquid dual-circulation system in the production route of energetic materials, realizing the coordinated operation of carrier gas circulation and solvent circulation. The production route of this invention uses a dry-wet mixed dust removal system to classify and remove dust from the mixed gas carrying dust and solvent during the production process. Then, the solvent recovery system performs dual treatment of condensation and adsorption, enabling efficient recovery and reuse of carrier gas and solvent. This forms a closed system with single input and multiple circulations, which significantly reduces the consumption of carrier gas and solvent, avoids the direct emission of organic solvents in the production tail gas, realizes the greening and low emission of the energetic material production process, and improves the system resource utilization rate and production safety.

[0018] 2. This invention establishes a dynamically adjustable dust removal process by cascading a wet condensation dust removal system and a dry filtration dust removal system, and automatically monitoring the solvent capacity using a level gauge. The wet system removes large dust particles and solvent vapors through water curtain condensation, while the dry system uses a high-efficiency filter to further remove fine dust. Through the interaction of staged dust removal and automatic solvent replenishment, dual stable control of dust removal efficiency and solvent concentration is achieved, avoiding the risk of static electricity or explosion caused by dust accumulation, and significantly improving the safety and continuity of energetic material production processes.

[0019] 3. In the further optimized production process, a circuit design with a secondary compression circulation system and adsorption regeneration function is set up. By pressurizing, heating and cooling the regeneration carrier gas, the online desorption and cooling regeneration of the adsorption tank are realized, so that the adsorption medium can be recycled. The circulation process provided by the present invention not only maintains the long-term stability of the carrier gas purity, but also maintains the dust removal efficiency and system flow by backflushing the dry filter.

[0020] In summary, this invention achieves a synergistic effect of carrier gas purification, adsorption medium regeneration, and filtration system self-cleaning, thereby reducing the frequency of manual maintenance, extending equipment lifespan, and improving the automation level and system reliability of the entire production line. Attached Figure Description

[0021] To more clearly illustrate the specific embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the specific embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of the present invention. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.

[0022] The above and other aspects of the invention will now be described by way of example only, with reference to the accompanying drawings, in which: Figure 1 This is a schematic diagram of the overall production line of the present invention; Figure 2This is a schematic diagram of the dry and wet mixed dust removal system of the present invention; Figure 3 This is a schematic diagram of the solvent recovery system of the present invention; Figure 4 This is a schematic diagram of the secondary compression cycle system of the present invention; Figure 5 This is a process flow diagram of the production process of this invention; Figure 6 This is a flowchart illustrating the specific steps of the production process of this invention.

[0023] In the diagram: 1. Exhaust pipe; 2. Liquid collection tank; 3. Liquid level gauge; 4. Auxiliary fan; 5. Dry dust filter; 6. Differential pressure sensor; 7. Backflush valve; 8. Air condenser; 9. Liquid storage tank; 10. Diaphragm pump; 11. Adsorption tank; 12. Regeneration gas inlet pipe; 13. Regeneration gas outlet pipe; 14. Liquid content monitoring system; 15. Oxygen concentration monitoring system; 16. Vent valve; 17. Main circuit isolation valve; 18. Carrier gas inlet valve; 19. Air intake valve; 20. Pressure sensor; 21. Main fan; 22. Air heater; 23. Temperature sensor; 24. Pressurization system; 25. Check valve; 26. Air tank; 27. Carrier gas heater; 28. Carrier gas cooler; 29. ​​Carrier gas output pipe; 30. Heat exchanger; 31. Discharge pipe; 32. One-way intake valve; 33. Production equipment; 34. Upper pneumatic clamp valve; 35. Lower pneumatic clamp valve; 36. Material inlet. Detailed Implementation

[0024] To better understand the above technical solutions, the following will provide a detailed explanation of the technical solutions in conjunction with the accompanying drawings and specific implementation methods.

[0025] Example 1: As Figure 1-4 As shown, this embodiment provides a production route for energetic materials based on a gas-liquid dual circulation system. This embodiment includes a production system, a carrier gas conveying system, a dry-wet mixing dust removal system, and a solvent recovery system. The production system is an energetic material production and molding device, specifically including a one-way inlet valve 32, a production device 33, an upper pneumatic clamp valve 34, a lower pneumatic clamp valve 35, and a material inlet 36. Nitrogen is pre-filled between the upper and lower pneumatic clamp valves 35. After material production is completed, the upper pneumatic clamp valve 34 is opened; after material discharge is completed, the upper pneumatic clamp valve 34 is closed; the lower pneumatic clamp valve 35 is opened; after material discharge is completed, the lower pneumatic clamp valve 35 is closed, thus achieving a fully enclosed internal structure for the production machine and reducing the impact of the carrier gas on production.

[0026] like Figure 1As shown, the output of the production system is connected to the input of the wet-dry dust collection system, and the output of the wet-dry dust collection system is connected to the input of the solvent recovery system. The carrier gas output of the solvent recovery system is connected to the carrier gas delivery system to form a single-input carrier gas circulation flow. The solvent output of the solvent recovery system is connected to the wet-dry dust collection system to replenish the solvent in the wet-dry dust collection system. The carrier gas delivery system is used to supply the carrier gas required for production to the production system and maintain circulation. The carrier gas flows in a closed loop between the production system, the wet-dry dust collection system, and the solvent recovery system. Only a small amount of carrier gas is added from the outside when there is a slight leakage or valve switching, thereby realizing the coordinated recovery and recycling of carrier gas and solvent, ensuring that the system operates stably for a long time under the conditions of meeting production parameters (such as carrier gas purity and pressure).

[0027] Example 2: Figure 1 and Figure 2 As shown, this embodiment specifically implements a wet-dry mixed dust removal system and its control and heat exchange measures. The wet-dry mixed dust removal system consists of a wet condensation dust removal system (using a water curtain or solvent curtain condensation dust removal) and a dry filtration dust removal system connected in series. The wet condensation dust removal system includes an exhaust pipe 1 for introducing carrier gas, a dust collector containing solvent liquid and passing through a water curtain for dust removal, a liquid collection tank 2 connected to the dust collector, a level gauge 3 for monitoring the solvent capacity in the dust collector, and an auxiliary fan 4 installed at the top of the dust collector for pumping out the treated carrier gas. A drain port is provided at the bottom of the dust collector. When the level gauge 3 detects that the solvent capacity in the dust collector is lower than a preset threshold (the example threshold can be set to 10% to 20% of the total volume of the dust collector or an absolute liquid level such as 50 mm), the liquid storage tank 9 replenishes the dust collector with solvent through the diaphragm pump 10 according to the controller's instructions.

[0028] When the liquid level exceeds a preset threshold, excess solvent flows from the dust collector into the collection tank 2 for temporary storage, and impurities are periodically or as needed discharged through the drain outlet. To control the solvent temperature inside the dust collector, in this embodiment, a heat exchanger 30 is arranged in the solvent liquid of the dust collector and connected to an external refrigeration system through a heat exchange pipeline. A commonly used cooling temperature range is 0-15 ℃, which improves the solvent's ability to condense solvent vapor and reduces the carrier gas temperature, thereby improving the primary recovery efficiency.

[0029] like Figure 2 As shown, the dry filtration dust removal system in this embodiment uses a dry dust filter 5 to intercept the fine dust remaining after wet dust removal. The dry dust filter 5 is equipped with a differential pressure sensor 6 to monitor the forward and reverse pressure difference. When the pressure difference exceeds the set upper limit (the upper limit can be set to 200-500 Pa in the example), the controller triggers the backflush valve 7 to open and perform reverse purging. Carrier gas is introduced into the pipeline between the air tank 26 and the backflush valve 7 for a short time to perform reverse purging, so as to maintain the filtration efficiency and avoid the long-term accumulation of dust in the pipeline, which may lead to safety hazards.

[0030] Example 3: Figure 1 , Figure 3 and Figure 4 As shown, this embodiment describes a specific implementation of the solvent recovery system, adsorption regeneration, and secondary compression circulation system. The solvent recovery system consists of a condensation recovery system and an adsorption system. The condensation recovery system includes an air condenser 8 (which condenses the incoming carrier gas by connecting to a refrigeration system; in this example, the condenser outlet temperature is controlled at 0-10 °C to facilitate the condensation of volatile solvents) and a liquid storage tank 9. The liquid storage tank 9 is used to temporarily store the solvent recovered from condensation and supplies it to the wet condensation dust removal system via a diaphragm pump 10. The adsorption system consists of multiple adsorption tanks 11, which are connected in series according to process requirements to form a circulation pipeline. Their input ends are connected in parallel to the carrier gas output end of the condensation recovery system, and their output ends are connected in parallel to the carrier gas delivery system to output regenerated carrier gas.

[0031] like Figure 4 As shown, in this embodiment, a secondary compression circulation system is set up to regenerate the adsorption function of the adsorption tank 11. This system includes a pressurization system 24, a one-way valve 25, a gas storage tank 26, a carrier gas heater 27, a carrier gas cooler 28, and a carrier gas output pipe 29. Part of the recovered carrier gas enters the secondary compression circulation system and is pressurized (e.g., the pressure after pressurization can be in the range of 0.2-1.0 MPa, adjusted according to the properties of the adsorption medium and the adsorbate). Heated carrier gas and cooled carrier gas are obtained through the parallel carrier gas heater 27 and carrier gas cooler 28. The heated carrier gas is heated to about 90 °C and introduced into the saturated adsorption tank 11 through the regeneration gas inlet pipe 12 to achieve desorption of the adsorption medium. The regenerated solvent vapor is connected to the condensation recovery system through the regeneration gas outlet pipe 13 for condensation recovery. After desorption, a cooling carrier gas of about 20 °C is introduced to cool the adsorption tank 11 to restore its adsorption capacity. The output end of the gas storage tank 26 is also connected to the backflushing passage of the production system and the dry dust filter 5. During backflushing, the pressurized carrier gas is reversed and introduced into the dry dust filter 5 through the one-way valve 25 and the backflushing valve 7 to clean the filter layer. The differential pressure sensor 6 monitors the filter condition to determine the timing and duration of backflushing.

[0032] In addition, such as Figure 1 As shown, the carrier gas delivery system integrates a liquid content monitoring system 14, an oxygen concentration monitoring system 15, an vent valve 16, a main circuit isolation valve 17, a carrier gas inlet valve 18, an air inlet valve 19, a pressure sensor 20, a main fan 21, an air heater 22, and a temperature sensor 23. The liquid content monitoring system 14 and the oxygen concentration monitoring system 15 are installed at the carrier gas output end of the solvent recovery system to determine online whether the carrier gas meets the recirculation index (e.g., solvent content ≤ 50 mg / m³ as the release threshold). When the monitoring index meets the standard, the qualified gas is discharged to the outside through the vent valve 16 and the discharge pipe 31, or the regenerated carrier gas is returned to the production system; in terms of production process.

[0033] The specific workflow of this embodiment is as follows: a portion of the regenerated carrier gas is pressurized and heated to 90°C for desorption in adsorption tank 11. After desorption, cooling carrier gas is introduced to cool the gas, which can then be reused in adsorption treatment. Another portion of the pressurized gas is directly supplied to the production system and the backflushing dry dust filter 5 to achieve carrier gas reuse and equipment self-cleaning. This ensures the coordinated operation of carrier gas purification, solvent recovery, adsorption medium regeneration, and filter backflushing cleaning, reducing the frequency of manual maintenance and improving system automation and reliability.

[0034] Example 4: Figure 1 - Figure 6 As shown, this embodiment is a specific implementation example of the production route based on the above embodiments one to four. In this embodiment, the production system can be replaced by granulation, drying or dissolution process modules. When the production route is started, the air inlet valve 19 is closed first, and the carrier gas inlet valve 18 and the vent valve 16 are opened to introduce carrier gas into the production system. The oxygen concentration monitoring system 15, the liquid content monitoring system 14 and the pressure sensor 20 continuously monitor the gas parameters in the pipeline and automatically replenish or discharge waste gas until the carrier gas parameters in the pipeline meet the process requirements (for example, the carrier gas pressure in the pipeline reaches about 30 kPa and the oxygen content is lower than the predetermined threshold). Then, the vent valve 16 is closed and the secondary compression circulation system is started. After the carrier gas pressure stabilizes, the carrier gas inlet valve 18 is closed and the air heater 22 is turned on to preheat the carrier gas in the pipeline to about 65 ℃. After maintaining the carrier gas stability for 1 hour, the production system is started.

[0035] Furthermore, the solvent-rich and dust-mixed carrier gas output from the production system first enters a wet condensation dust collector for preliminary dust removal and cooling, then enters a dry filtration dust collector for secondary dust removal, and subsequently enters a condensation recovery system and an adsorption system to recover the solvent, obtaining regenerated carrier gas, which is then returned to the carrier gas delivery system, forming a complete closed-loop production route from process materials to recycling and reuse. This is suitable for process route deployment in various production processes such as granulation, drying, and solvent displacement.

[0036] It should be noted that, for those skilled in the art, it is obvious that the present invention is not limited to the details of the above exemplary embodiments, and that the present invention can be implemented in other specific forms without departing from the spirit or essential characteristics of the invention. Therefore, the embodiments should be considered exemplary and non-limiting in all respects, and the scope of the invention is defined by the appended claims rather than the foregoing description. Thus, all variations falling within the meaning and scope of equivalents of the claims are intended to be included within the present invention, and no reference numerals in the claims should be construed as limiting the scope of the claims.

[0037] This specification uses specific examples to illustrate the principles and implementation methods of the present invention. The descriptions of the above embodiments are only for the purpose of helping to understand the method and core ideas of the present invention. Furthermore, those skilled in the art will recognize that, based on the ideas of the present invention, there will be changes in the specific implementation methods and application scope. Therefore, the content of this specification should not be construed as a limitation of the present invention.

Claims

1. An energetic material production route based on a gas-liquid dual circulation system, comprising a production system for the production and molding of energetic materials, an input end of the production system being connected with a carrier gas delivery system for the carrier gas required for the production system, characterized in that, Also included are, a dry-wet hybrid dust removal system, an input end of the dry-wet hybrid dust removal system being connected with an output end of the production system; a solvent recovery system, an input end of the solvent recovery system being connected with an output end of the dry-wet hybrid dust removal system, for recovering the solvent carried in the carrier gas by condensation and adsorption treatment; a carrier gas output end of the solvent recovery system being connected with a carrier gas conveying system, for forming a single-input carrier gas circulating flow; a solvent output end of the solvent recovery system being connected with the dry-wet hybrid dust removal system, for supplementing the solvent into the dry-wet hybrid dust removal system.

2. The energetic material production route based on gas-liquid dual circulation system according to claim 1, characterized in that: The dry-wet hybrid dust removal system comprises a wet condensation dust removal system and a dry filtration dust removal system, an input end of the wet condensation dust removal system being connected with an output end of the production system, an output end of the wet condensation dust removal system being connected with an input end of the dry filtration dust removal system, and an output end of the dry filtration dust removal system being connected with an input end of the solvent recovery system.

3. The energetic material production route based on gas-liquid dual circulation system according to claim 2, characterized in that: The wet condensation dust removal system comprises a dust remover, an exhaust pipe (1), a liquid collecting tank (2), a liquid level meter (3), and an auxiliary fan (4), the dust remover being used for dust removal by means of water curtain dust removal; the exhaust pipe (1) is connected with the output end of the production system, for inputting the carrier gas into the dust remover; the liquid collecting tank (2) is connected with the solvent liquid inside the dust remover; the liquid level meter (3) is arranged inside the dust remover, for monitoring the capacity of the solvent liquid inside the dust remover; the auxiliary fan (4) is arranged at the top of the dust remover, for discharging the carrier gas after dust removal treatment inside the dust remover; the bottom of the dust remover is further provided with a blowdown port; the dry filtration dust removal system filters the dust in the carrier gas by means of a dry dust filter (5) therein.

4. The energetic material production route based on gas-liquid dual circulation system according to claim 3, characterized in that: When the solvent capacity in the dust remover is monitored by the liquid level meter (3) to be lower than a set threshold, the solvent output end of the solvent recovery system inputs the solvent into the dust remover through a pipeline for supplement; when the solvent capacity in the dust remover is higher than the set threshold, the solvent in the dust remover flows into the liquid collecting tank (2).

5. The energetic material production route based on gas-liquid dual circulation system according to claim 3, characterized in that: A heat exchanger (30) is further arranged in the solvent liquid of the dust remover, the heat exchanger (30) is connected with an external refrigeration system through a heat exchange pipeline, for cooling the solvent liquid in the dust remover.

6. The energetic material production route based on gas-liquid dual circulation system according to claim 2, characterized in that: The solvent recovery system comprises a condensation recovery system and an adsorption system; The condensation recovery system comprises an air condenser (8) and a liquid storage tank (9), the air condenser (8) is connected with a refrigeration system, for condensing the input carrier gas, the liquid storage tank (9) is used for storing the solvent liquid condensed from the carrier gas; the liquid storage tank (9) is connected with the dust remover in the wet condensation dust removal system through a diaphragm pump (10); The adsorption system comprises a plurality of adsorption tanks (11), the adsorption tanks (11) are used for adsorbing the solvent in the carrier gas, the plurality of adsorption tanks (11) are connected in series to form a closed circulating pipeline, input ends of the plurality of adsorption tanks (11) are connected in parallel with the carrier gas output end of the condensation recovery system, and output ends of the plurality of adsorption tanks (11) are connected in parallel with the carrier gas conveying system.

7. The energetic material production route based on gas-liquid dual circulation system according to claim 6, characterized in that: The carrier gas delivery system is also connected with a secondary compression circulation system, the secondary compression circulation system comprises a booster system (24), a one-way valve (25), a gas storage tank (26), a carrier gas heater (27), a carrier gas cooler (28) and a carrier gas output pipeline (29), the booster system (24) and the one-way valve (25) are arranged at the input end of the secondary compression circulation system, the input end of the gas storage tank (26) is connected with the output end of the booster system (24) through the one-way valve (25); the input ends of the carrier gas heater (27) and the carrier gas cooler (28) are connected in parallel with the output end of the gas storage tank (26); The output ends of the carrier gas heater (27) and the carrier gas cooler (28) are reversely connected with the output ends of a plurality of the adsorption tanks (11) through a regenerative gas inlet pipe (12), and the adsorption tanks (11) are further reversely connected with the input end of the condensation recovery system through a regenerative gas outlet pipe (13); The output end of the gas storage tank (26) is also connected with a production system and a dry dust filter (5) in a dry filtration and dust removal system; wherein, a differential pressure sensor (6) and a back flushing valve (7) are further arranged on the dry dust filter (5), the back flushing valve (7) is arranged on the pipeline between the output end of the gas storage tank (26) and the dry dust filter (5), and the back flushing valve (7) is used for reversely inputting carrier gas into the dry dust filter (5) after being opened; the differential pressure sensor (6) is used for monitoring the positive and negative pressure difference inside the dry dust filter (5).

8. The energetic material production route based on gas-liquid dual circulation system according to any one of claims 1-7, characterized in that: The carrier gas delivery system comprises a liquid material content monitoring system (14), an oxygen concentration monitoring system (15), an emptying valve (16), a main loop isolation valve (17), a carrier gas inlet valve (18), an air inlet valve (19), a pressure sensor (20), a main air blower (21), an air heater (22) and a temperature sensor (23); The liquid material content monitoring system (14) and the oxygen concentration monitoring system (15) are connected at the carrier gas output end of the solvent recovery system, and are used for monitoring the output data of the carrier gas; The input end of the emptying valve (16) is connected with the carrier gas output end of the solvent recovery system, and the output end of the emptying valve (16) is connected with a discharge pipe (31), the discharge pipe (31) is used for discharging the carrier gas with up-to-standard output data; The main loop isolation valve (17), the pressure sensor (20), the main air blower (21), the air heater (22) and the temperature sensor (23) are sequentially connected in series between the carrier gas circulation pipeline formed between the output end of the solvent recovery system and the input end of the production system; The carrier gas inlet valve (18) is used for connecting the pipeline through which the carrier gas is input into the production system; and the air inlet valve (19) is used for connecting the pipeline through which the air is input into the production system.

9. An energetic material production process based on a gas-liquid dual circulation system, suitable for the energetic material production route based on a gas-liquid dual circulation system according to claim 8, characterized in that, The method comprises the following steps: S1, closing the air inlet valve (19), opening the carrier gas inlet valve (18) and the emptying valve (16), and inputting carrier gas into the production system; S2, continuously monitor the gas parameters in the pipeline through the oxygen concentration monitoring system (15), the liquid content monitoring system (14) and the pressure sensor (20), and automatically supplement the carrier gas and discharge the waste gas according to the preset carrier gas index requirements until the purity of the carrier gas in the production line meets the process requirements; S3, close the emptying valve (16) and open the secondary compression circulation system, and when the carrier gas pressure meets the requirements, close the carrier gas inlet valve (18) and open the air heater (22) to preheat the carrier gas in the production line to 65℃; S4, after the carrier gas state is stable for 1 hour, start the production system for production; S5, after the initial carrier gas flows through the production system, a mixed carrier gas rich in solvent and dust is formed and is introduced into a wet condensation dust removal system for preliminary dust removal; S6, the mixed carrier gas after preliminary dust removal is introduced into a dry filtration dust removal system for secondary dust removal, and a solvent-rich solvent carrier gas is output; S7, the solvent carrier gas is introduced into a condensation recovery system for condensation treatment, part of the solvent in the solvent carrier gas is condensed and recovered and stored in the liquid storage tank (9); Wherein, when the solvent liquid in the wet condensation dust removal system is insufficient, the diaphragm pump (10) extracts the solvent in the liquid storage tank (9) into the dust remover; S8, the solvent carrier gas is further introduced into the adsorption system, and the adsorption tank (11) adsorbs and recovers the remaining solvent in the solvent carrier gas and retains it in the adsorption tank (11), thereby outputting a regenerated carrier gas; Wherein, the carrier gas output from the adsorption system is output under the detection of the solvent concentration sensor, and the concentration meets the standard to output the regenerated carrier gas, and the concentration does not meet the standard to continue to be introduced into the condensation recovery system for solvent recovery treatment; S9, the regenerated carrier gas is introduced into the carrier gas delivery system and introduced into the production line again to form a cycle.

10. The production process according to claim 9, characterized in that: The regenerated carrier gas is introduced into the carrier gas delivery system and introduced into the production line again to form a cycle, including the following steps: S9.1, a part of the regenerated carrier gas is introduced into the secondary compression circulation system, and the regenerated carrier gas is pressurized through the booster system (24) to obtain pressurized carrier gas; S9.2, a part of the pressurized carrier gas is introduced into the carrier gas heater (27) and the carrier gas cooler (28) to obtain heated carrier gas and cooled carrier gas, respectively; S9.3, the heated carrier gas heated to 90℃ is introduced into the saturated adsorption adsorption tank (11) to desorb the saturated adsorption medium in the adsorption tank (11); S9.4, after desorption, cooled carrier gas is introduced into the adsorption tank (11) to cool the adsorption medium in the tank, so that the adsorption medium regains the adsorption function; S9.5, the other part of the pressurized carrier gas is introduced into the production system for production and the dry filtration dust removal system for reverse blowing through the carrier gas output pipeline (29); Wherein, the pressurized carrier gas is introduced into the dry dust filter (5) in reverse for cleaning.

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