CN220618446U

CN220618446U - System for preparing oxygen by recycling high-temperature flue gas of glass kiln

Info

Publication number: CN220618446U
Application number: CN202322159925.8U
Authority: CN
Inventors: 冯海涛
Original assignee: Qingdao Ronghe New Material Technology Co Ltd
Current assignee: Qingdao Ronghe New Material Technology Co Ltd
Priority date: 2023-08-11
Filing date: 2023-08-11
Publication date: 2024-03-19
Anticipated expiration: 2033-08-11

Abstract

The utility model discloses an oxygen production system for recycling high-temperature flue gas of a glass kiln, which comprises a reactor, wherein the reactor is provided with a potassium chlorate feed inlet, a catalyst feed inlet, a solid material discharge outlet and a gas product discharge outlet, a heating interlayer is arranged outside the reactor, and the heating interlayer is provided with a high-temperature flue gas inlet and a high-temperature flue gas outlet; the gas product discharge port is connected with a gas purification unit, an inclined belt conveyor I is arranged below the solid material discharge port, the solid material discharge port is positioned above the lower end of the belt conveyor I, a water pipe I is arranged above the higher end of the belt conveyor I, and a spray header is arranged on the water pipe I; a potassium chloride solution collecting tank is arranged below the lower end of the belt conveyor and is connected with an evaporator; and a second belt conveyor is arranged below the higher end of the first belt conveyor. The utility model takes the high-temperature flue gas of the glass kiln as a heat source for preparing oxygen by potassium chlorate, thereby realizing the recovery and utilization of the waste heat of the high-temperature flue gas.

Description

System for preparing oxygen by recycling high-temperature flue gas of glass kiln

Technical Field

The utility model relates to the technical field of waste heat utilization of high-temperature flue gas of a glass kiln, in particular to an oxygen generation system for recycling high-temperature flue gas of the glass kiln.

Background

With the rapid development of the global chemical industry, more and more chemical enterprises are built in various places, and as is well known, the chemical enterprises are large energy-consuming enterprises, and a large amount of energy is required to be input when various products are processed and produced, so that the required products are obtained; at the same time, production facilities, cooling facilities, exhaust facilities, etc. output a large amount of dissipated energy. For example, kiln tail gas of glass processing enterprises is discharged, and a large amount of high-temperature smoke above 300 ℃ is discharged into the environment, so that a large amount of energy waste is caused. Therefore, how to recycle the waste heat of high-temperature flue gas in a flue of a glass kiln is a problem to be solved.

Chinese patent No. CN208786128U discloses a glass kiln flue gas waste heat comprehensive utilization device, comprising: the high-temperature section module type waste heat boiler, the SCR denitrification device, the low-temperature Duan Mokuai type waste heat boiler and the desulfurization device, wherein the input end of the high-temperature section module type waste heat boiler is communicated with the output end of the glass kiln, the input end of the SCR denitrification device is communicated with the output end of the high-temperature section module type waste heat boiler, the input end of the low-temperature Duan Mokuai type waste heat boiler is communicated with the output end of the SCR denitrification device, the input end of the desulfurization device is communicated with the output end of the low-temperature Duan Mokuai type waste heat boiler, and the high-temperature section module type waste heat boiler, the SCR denitrification device, the low-temperature Duan Mokuai type waste heat boiler and the desulfurization device are all in modular communication. The on-site installation is carried out by adopting an assembling and combining mode, the waste heat boiler can realize standardization and universalization in a factory, and the installation is quick and the replacement is convenient.

The utility model patent CN212645399U discloses a high-efficiency waste heat recycling system for glass kiln smoke, which comprises a pre-dedusting device, a heat exchange device, a pulse soot blower, an induced draft fan, a softened water preparation device, an evaporator and a steam collecting drum, wherein the output end of the pre-dedusting device is connected with the input end of the heat exchange device, the output end of the heat exchange device is connected with the input end of the induced draft fan, the output end of the pulse soot blower is connected with the input end of the heat exchange device, the output ends of the heat exchange device and the softened water preparation device are connected with the input end of the evaporator, and the output end of the evaporator is connected with the input end of the steam collecting drum. The high-efficiency waste heat recycling system for the glass kiln flue gas can effectively solve the problems of waste heat utilization rate of the kiln flue gas and atmospheric pollution, and periodically pulse soot blowing is performed through the pulse soot blowing device, so that the heat exchange efficiency of the heat exchange tube in the heat exchange device is improved.

The two patents provide two recycling modes of high-temperature flue gas of the glass kiln, the utility model aims at researching a new recycling way of the high-temperature flue gas of the glass kiln, and the reaction type that potassium chlorate can react to generate potassium chloride and oxygen under the high-temperature catalysis of a manganese dioxide catalyst is utilized, and the high-temperature flue gas of the glass kiln is used as a heat source to pass through heat for the reaction to prepare oxygen.

Disclosure of Invention

The utility model aims to solve the technical problems that: the oxygen production system for recycling the high-temperature flue gas of the glass kiln is provided, the high-temperature flue gas in the flue of the glass kiln is used as a heat source, potassium chlorate is reacted to generate oxygen under the catalysis of a manganese dioxide catalyst, and the oxygen is purified to obtain the oxygen for a production line, so that the waste heat recovery and utilization of the high-temperature flue gas of the glass kiln are realized.

The technical scheme of the utility model is as follows:

the oxygen production system for recycling the high-temperature flue gas of the glass kiln comprises a reactor, wherein the reactor is provided with a potassium chlorate feed inlet, a catalyst feed inlet, a solid material discharge outlet and a gas product discharge outlet, a heating interlayer is arranged outside the reactor, and the heating interlayer is provided with a high-temperature flue gas inlet and a high-temperature flue gas outlet; the gas product discharge port is connected with a gas purification unit, an inclined belt conveyor I is arranged below the solid material discharge port, the solid material discharge port is positioned above the lower end of the belt conveyor I, a water pipe I is arranged above the higher end of the belt conveyor I, and a spray header is arranged on the water pipe I; a potassium chloride solution collecting tank is arranged below the lower end of the belt conveyor and is connected with an evaporator; the belt conveyor II is arranged below the higher end of the belt conveyor I, a drying mechanism is arranged above the transmission rear end of the belt conveyor II, and a material conveying vehicle is arranged at the transmission tail end of the belt conveyor II.

Preferably, the potassium chlorate feeding port is connected with a potassium chlorate storage bin, the catalyst feeding port is connected with a catalyst storage bin, lifting mechanisms are respectively arranged on one side of the potassium chlorate storage bin and one side of the catalyst storage bin, a supporting table is arranged on the lifting mechanisms, a feeding hopper is arranged on the supporting table, an electric gate valve is respectively arranged at the feeding port and the discharging port of the feeding hopper, and the feeding hopper is connected with an output shaft of a first motor; the top of the potassium chlorate bin and the top of the catalyst bin are respectively provided with a feeding hole at one side of the feeding hopper, an electric gate valve is arranged at the feeding hole, and the motor drives the feeding hopper to topple over in the feeding hole direction of the potassium chlorate bin and the catalyst bin, so that the potassium chlorate and the catalyst are poured into the potassium chlorate bin and the catalyst bin.

Preferably, the lifting mechanism comprises a motor II, an output shaft of the motor II is connected with a driving gear, driven gears are further arranged on the potassium chlorate bin and the catalyst bin, chains are arranged on the driving gear and the driven gears, a supporting table is arranged on the chains, and the supporting table moves up and down along the height direction of the potassium chlorate bin and the catalyst bin under the driving of the chains.

Preferably, the feeding hopper is connected with a vacuum pump.

Preferably, the potassium chlorate bin and the catalyst bin are respectively connected with an oxygen pipe, the oxygen pipe is provided with an oxygen valve, and the oxygen pipe is connected with an oxygen outlet of the gas purification unit.

Preferably, a dust removing mechanism is further arranged between the gas product discharge port and the gas purifying unit of the reactor.

Preferably, the gas purification unit comprises a gas storage tank, a gas inlet of the gas storage tank is connected with a gas product discharge port through a pipeline, the pipeline stretches into the gas storage tank, and a plurality of aeration discs are arranged on the pipeline; the air storage tank is connected with a water pipe II and an oxygen conveying pipe, and the bottom is connected with a wastewater discharge pipe.

Preferably, a compressor is arranged on a pipeline between the air inlet of the air storage tank and the gas product discharge port, and a pressure regulating valve is arranged on the oxygen conveying pipe.

Preferably, the drying mechanism comprises an outer cover covered on the transmission rear end of the second belt conveyor, a high-temperature flue gas pipeline is arranged in the outer cover, and the high-temperature flue gas pipeline is positioned above the second belt conveyor and has a gap with the second belt conveyor.

Preferably, a rubber brush I is arranged below the belt conveyor I and contacts with the belt of the belt conveyor I, and the rubber brush I is arranged above the belt conveyor II; the rubber brush II is arranged below the belt conveyor II and contacts with the belt of the belt conveyor II, and the rubber brush II is arranged above the material conveying vehicle.

Compared with the prior art, the utility model has the following beneficial effects:

the system takes the high-temperature flue gas in the flue of the glass kiln as a heat source, so that potassium chlorate reacts under the catalysis of the manganese dioxide catalyst to generate oxygen, and the oxygen can be obtained for a production line after purification treatment, thereby realizing the waste heat recycling of the high-temperature flue gas of the glass kiln and reducing energy waste. Meanwhile, the utility model can also realize the recovery of the reaction product potassium chloride and the catalyst, and can be sold as a product.

Drawings

FIG. 1 is a schematic diagram of the connection of a glass kiln, flue, desulfurization and denitrification equipment and chimney of the present utility model.

FIG. 2 is a schematic structural view of the reactor of the present utility model.

Fig. 3 is a schematic diagram of the structures of the potassium chlorate silo and the catalyst silo of the utility model.

FIG. 4 is a schematic diagram of the structure of a gas purification unit of the present utility model.

Fig. 5 is a schematic structural view of the material recovery unit of the present utility model.

Figure 6 is a schematic structural view of a rubber gland according to the present utility model.

In the figure, 1, a glass kiln; 2. a flue; 3. a reaction zone; 4. desulfurization and denitrification equipment; 5. an induced draft fan; 6. a chimney; 7. a reactor; 701. potassium chlorate feed inlet; 702. a catalyst feed port; 703. a gas product discharge port; 704. a solid material discharging pipe; 705. heating the interlayer; 7051. a high temperature flue gas inlet; 7052. a high temperature flue gas outlet; 706. a rubber sealing sleeve; 8. a dust removing mechanism; 901. a potassium chlorate bin; 902. a catalyst bin; 903. a support table; 904. feeding a hopper; 905. an electric gate valve; 906. a first motor; 907. a feeding port; 908. a chain; 909. a vacuum pump; 910. an oxygen pipe; 911. an oxygen valve; 912. a discharge pipe; 913. an air pipe; 914. a stirring rod; 915. a paddle; 916. a third motor; 10. a gas purification unit; 1001. a gas storage tank; 1002. an aeration disc; 1003. a second water pipe; 1004. an oxygen delivery tube; 1005. a waste water discharge pipe; 1006. a compressor; 1007. a pressure regulating valve; 1101. a first belt conveyor; 1102. a first water pipe; 1103. a spray header; 1104. a potassium chloride solution collection tank; 1105. a belt conveyor II; 1106. a material transporting vehicle; 1107. a first rubber brush; 1108. a second rubber brush; 1201. an outer cover; 1202. a high temperature flue gas pipeline; 1203. brushing a plate; 13. a regulating valve; 14. a solenoid valve.

Detailed Description

In order to enable those skilled in the art to better understand the technical solution of the present utility model, the technical solution of the present utility model will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present utility model.

Example 1

As shown in fig. 1-2, this embodiment provides an oxygen generation system for recycling high-temperature flue gas of a glass kiln 1, which comprises a reaction zone 3, wherein a plurality of reactors 7 are arranged in the reaction zone 3 side by side, the reactors 7 are provided with a potassium chlorate feed inlet 701, a catalyst feed inlet 702, a solid material discharge outlet and a gas product discharge outlet 703, a heating interlayer 705 is arranged outside the reactors 7 (the plurality of reactors 7 share one heating interlayer 705), the heating interlayer 705 can be built by refractory bricks, and a concrete heat insulation layer is further arranged outside the refractory bricks, and the heating interlayer 705 is provided with a high-temperature flue gas inlet 7051 and a high-temperature flue gas outlet 7052. Wherein, the reactor 7 can adopt a screw conveyor which is inclined by 30 degrees, the potassium chlorate feed inlet 701, the catalyst feed inlet 702 and the high temperature flue gas inlet 7051 are positioned at the lower end, the solid material discharge outlet, the gas product discharge outlet 703 and the high temperature flue gas outlet 7052 are positioned at the higher end, and the conveying direction is from low to high. The high-temperature flue gas (about 450 ℃) from the glass kiln 1 enters a heating interlayer 705 to heat potassium chlorate and catalyst in a reactor 7, the conveying speed of a screw conveyor is controlled to react to generate solid potassium chloride and oxygen, and then the high-temperature flue gas is discharged from a high-temperature flue gas outlet 7052 to desulfurization and denitrification equipment 4 for treatment under the action of a draught fan 5 and is discharged through a chimney 6.

In order to utilize the waste heat of the high-temperature flue gas of the glass kiln 1 and reduce the occupied area, the reactor 7 in the system of the embodiment can be placed in the flue 2 of the glass kiln 1; of course, if the required reactor 7 is also larger to obtain more oxygen production, it may be placed outside the flue 2 (as shown in fig. 1), and the high temperature flue gas may be introduced into the reactor 7.

The gas product discharge port 703 is connected to a gas purification unit 10 to purify the oxygen generated by the reaction and improve the oxygen quality. Specifically, as shown in fig. 4, the gas purifying unit 10 includes a gas tank 1001, an air inlet at the bottom of the gas tank 1001 is connected to a gas product discharge port 703 through a pipeline, the pipeline extends into the gas tank 1001, and a plurality of aeration discs 1002 are arranged on the pipeline; the gas holder 1001 is connected with water pipe two 1003 and oxygen conveyer pipe 1004, and the bottom is connected with waste water discharge pipe 1005, is provided with solenoid valve 14 on water pipe two 1003 and the waste water discharge pipe 1005. A certain amount of pure water is introduced into the gas storage tank 1001 through the water pipe II 1003 to form a water filtering layer, oxygen generated by the reaction enters the gas storage tank 1001 through a pipeline, tiny bubbles are formed under the action of the aeration disc 1002 and then enter the pure water, and tiny particles, grease and the like in the bubbles are trapped in the pure water, so that the gas in the gas storage tank 1001 has higher quality. The solenoid valve 14 on the waste water discharge pipe 1005 can be periodically opened to discharge the purified waste water, and fresh purified water can be supplied through the second water pipe 1003.

In order to increase the gas storage amount of the gas tank 1001, as shown in fig. 4, a compressor 1006 may be provided in a line between the gas inlet of the gas tank 1001 and the gas product outlet 703, and the generated oxygen may be pressurized and stored in the gas tank 1001, thereby increasing the gas storage amount of the gas tank 1001. Meanwhile, the oxygen delivery pipe 1004 is provided with a pressure regulating valve 1007, and after the air pressure in the air storage tank 1001 reaches a certain limit value, the pressure regulating valve 1007 is opened to deliver oxygen with stable pressure to the production line.

The reaction product potassium chloride and catalyst output by the solid material outlet enter a material recovery unit, as shown in fig. 5, specifically: the solid material discharging hole is connected with a solid material discharging pipe 704, an inclined belt conveyor I1101 is arranged below the solid material discharging pipe 704, the solid material discharging hole is positioned above the lower end of the belt conveyor I1101, a water pipe I1102 is arranged above the higher end of the belt conveyor I1101, and a spray header 1103 and a regulating valve 13 are arranged on the water pipe I1102; a potassium chloride solution collecting tank 1104 is arranged below the lower end of the first belt conveyor 1101, and the potassium chloride solution collecting tank 1104 is connected with an evaporator. The evaporator is an existing conventional evaporator, and the specific structure thereof is not described herein. The mixture of potassium chloride solid and catalyst generated by the reaction in the reactor 7 is discharged to the lower end of the first 1101 belt conveyor through a solid material discharge hole, then is conveyed upwards to the upper end, in the conveying process, the regulating valve 13 is opened, water is sprayed onto the first 1101 belt conveyor from the upper end through the spray header 1103, as potassium chloride is easily dissolved in water and manganese dioxide is insoluble in water, the water flows downwards in the upward conveying process of the first 1101 belt conveyor, so that potassium chloride in the mixture is dissolved to form a potassium chloride solution, and as the concentration of the potassium chloride solution increases, a high-concentration potassium chloride solution is finally formed and flows into the potassium chloride solution collecting tank 1104 below the first 1101 belt conveyor to be collected, and then is pumped into the evaporator to be evaporated, so that solid potassium chloride crystals are obtained and can be sold as products.

In addition, the heat required by the evaporator can be provided by high-temperature flue gas of the glass kiln 1, and condensed water obtained by evaporation can be sprayed on the first 1101 belt conveyor in a recycling way. Meanwhile, in order to prevent the external air from entering the reactor 7 from the solid material discharging pipe 704 from affecting the purity of the gas product, as shown in fig. 2 and 6, a rubber sealing sleeve 706 may be disposed on the solid material discharging pipe 704, the rubber sealing sleeve 706 is integrally tapered, an inlet and an outlet are disposed up and down respectively, and the inlet is in an open state, and the outlet is in a flat shape that is adsorbed together when no solid material passes through. When the material in the solid material discharging pipe 704 is accumulated to a certain amount, the outlet of the rubber sealing sleeve 706 is opened under the action of pressure, so that the material falls, after the material falls, the pressure of the material on the outlet is reduced, and the outlet is automatically contracted and closed, so that external air is prevented from entering.

As shown in fig. 5, a second belt conveyor 1105 is disposed below the higher end of the first belt conveyor 1101, a drying mechanism is disposed above the rear end of the second belt conveyor 1105 (i.e., the rear end of the second belt conveyor 1105 in the conveying direction), and a transporting carriage 1106 is disposed at the conveying end of the second belt conveyor 1105. Undissolved manganese dioxide catalyst on the first belt conveyor 1101 falls onto the second belt conveyor 1105 and is dried by the drying mechanism and then collected into the transporting carriage 1106 for transport. In order to prevent the undissolved wet catalyst from adhering to the first belt conveyor 1101 and failing to smoothly drop to the second belt conveyor 1105 below, a rubber brush 1107 may be disposed below the first belt conveyor 1101, where the rubber brush 1107 contacts the belt of the first belt conveyor 1101 and is located above the second belt conveyor 1105. Thus, even if a part of the wet catalyst material sticks to the first belt conveyor 1101, the wet catalyst material is brushed down onto the second belt conveyor 1105 below by the first rubber brush 1107.

Specifically, in this embodiment, as shown in fig. 5, the drying mechanism includes a housing 1201 covering the rear end of the second belt conveyor 1105, and a high-temperature flue gas pipe 1202 is disposed in the housing 1201, where the high-temperature flue gas pipe 1202 is located above the second belt conveyor 1105 and has a gap with the second belt conveyor 1105. High-temperature flue gas (which can also be introduced from the glass kiln 1) is introduced into the high-temperature flue gas pipeline 1202 and flows under the action of the induced draft fan 5, so that the catalyst on the second belt conveyor 1105 is heated and dried.

In order to prevent the catalyst stack height falling onto the second belt conveyor 1105 from exceeding the gap between the high-temperature flue gas pipeline 1202 and the second belt conveyor 1105, so that the catalyst is heated unevenly and the drying effect is affected, as shown in fig. 5, a brush plate 1203 with the same width as the second belt conveyor 1105 can be arranged at the front end of the outer cover 1201, so that the catalyst with too high stack height can be flattened on the second belt conveyor 1105, the uniform heating of the catalyst is ensured, and the drying effect is improved.

Similarly, to prevent a portion of the catalyst from sticking to the second belt conveyor 1105 and failing to fall down into the truck 1106, a second rubber brush 1108 may be disposed below the second belt conveyor 1105, as shown in fig. 5, where the second rubber brush 1108 contacts the belt of the second belt conveyor 1105 and is located above the truck 1106. In this way, catalyst stuck to the second belt conveyor 1105 may be brushed down into the truck 1106 for transport by the second rubber brush 1108.

Working principle:

the flue 2 of the glass kiln 1 can be connected with three branch flues, so that the high-temperature flue gas is divided into three paths, and one path enters the heating interlayer 705 of the reactor 7 to be used as a reaction heat source; the second path is used as an evaporation heat source of the evaporator; and the third path is used as a heat source of the drying mechanism to dry and recycle the wet catalyst. And after the high-temperature flue gas is recycled, the flue gas enters the subsequent desulfurization and denitrification equipment 4 for desulfurization and denitrification treatment, and finally is discharged through a chimney 6 under the action of a draught fan 5. The three high-temperature flue gas recycling pipelines of the embodiment all take energy recycling as guiding, so that the production cost is reduced while the recycling of the heat source is realized, and a larger economic value is created.

By adding potassium chlorate and manganese dioxide catalyst into the reactor 7, the catalyst reacts under the heating action of high-temperature flue gas in the heating interlayer 705, and the reaction process is as follows:

4KClO4＝KCl+3KClO4

3KClO4＝3KCl+6O2↑

because the above reactions are chain reactions, the combination is the following reaction:

2KClO3＝2KCl+3O2↑

the oxygen generated by the reaction enters the gas purification unit 10 from the gas product discharge port 703, fine particles, grease and other impurities in the oxygen are filtered by the pure water filter layer, and the purified oxygen is stored in the gas storage tank 1001 and can be conveyed to a production line for use.

The solid product potassium chloride and catalyst manganese dioxide generated by the reaction can fall onto a first 1101 belt conveyor through a solid material discharging pipe 704, wherein the potassium chloride is dissolved in spray water to form a potassium chloride solution, the potassium chloride solution is collected into a potassium chloride solution collecting tank 1104, and finally the potassium chloride solution is pumped into an evaporator to be evaporated into a potassium chloride solid product; the undissolved catalyst is transported to the second belt conveyor 1105 below by the first belt conveyor 1101, dried from wet material to dry material under the heating effect of the high-temperature flue gas in the drying mechanism, and finally transported away by the transporting carriage 1106.

Example 2

On the basis of example 1, as shown in fig. 3, a potassium chlorate feed inlet 701 of the reactor 7 is connected with a potassium chlorate storage bin 901, a catalyst feed inlet 702 is connected with a catalyst storage bin 902, potassium chlorate is filled in the potassium chlorate storage bin 901, and a manganese dioxide catalyst is filled in the catalyst storage bin 902. The potassium chlorate bin 901 and the catalyst bin 902 are respectively provided with a lifting mechanism, a supporting table 903 is arranged on the lifting mechanism, a feeding hopper 904 is arranged on the supporting table 903, an electric gate valve 905 is respectively arranged at a feed inlet and a discharge outlet of the feeding hopper 904, and the feeding hopper 904 is connected with an output shaft of a motor 906; the tops of the potassium chlorate bin 901 and the catalyst bin 902 are respectively provided with a feeding hole 907 at one side of the feeding hopper 904, an electric gate valve 905 is arranged at the feeding hole 907, the first motor 906 drives the feeding hopper 904 to topple over towards the feeding holes 907 of the potassium chlorate bin 901 and the catalyst bin 902, and potassium chlorate and catalyst are poured into the potassium chlorate bin 901 and the catalyst bin 902. Specifically, as shown in fig. 3, the lifting mechanism includes a second motor, an output shaft of the second motor is connected with a driving gear, driven gears are further arranged on the potassium chlorate storage bin 901 and the catalyst storage bin 902, chains 908 are arranged on the driving gear and the driven gears, a supporting table 903 is arranged on the chains 908, and the supporting table 903 is driven by the chains 908 to move up and down along the height direction of the potassium chlorate storage bin 901 and the catalyst storage bin 902.

When raw materials need to be filled into the potassium chlorate bin 901 and the catalyst bin 902, an electric gate valve 905 at a feed inlet of a feeding hopper 904 is opened, a worker loads potassium chlorate and manganese dioxide catalyst into the feeding hopper 904 on the ground, then the electric gate valve 905 is closed, a motor II is started, and the motor II drives a driving gear to rotate, so that a chain 908 is driven on the driving gear and a driven gear, and the feeding hopper 904 on a supporting table 903 is lifted to a top feed inlet 907 of the potassium chlorate bin 901 and the catalyst bin 902 from the ground. Then, starting a first motor 906 to drive the feeding hopper 904 to incline towards the feeding hole 907 on the supporting table 903, and finally butting with the feeding hole 907; after the butt joint is finished, an electric gate valve 905 at a discharge hole of the feeding hopper 904 and a discharge hole 907 of the storage bin is simultaneously opened, so that raw materials in the feeding hopper 904 enter the storage bin. After the blanking is finished, the electric gate valve 905 at the discharge port of the upper hopper 904 and the feed port 907 of the storage bin is closed, and then the upper hopper 904 is lowered to the ground by reverse operation, and the next feeding is waited.

As shown in fig. 3, the bottoms of the potassium chlorate bin 901 and the catalytic fines bin are respectively provided with a discharge pipe 912, and potassium chlorate and catalyst are transferred to the reactor 7 through the discharge pipe 912. The raw materials can be conveyed in a pneumatic conveying mode, namely, a horizontal section is arranged on the discharging pipe 912, an air pipe 913 is connected to the levelness of the discharging pipe, a fan and a regulating valve 13 are arranged on the air pipe 913, and the quantity of conveying raw materials conveyed into the reactor 7 by conveying pneumatic is regulated and controlled by regulating the air quantity of the fan and the regulating valve 13. During pneumatic conveying, a part of purified oxygen product can be conveyed to the gas pipes 913 at the discharge pipes 912 of the potassium chlorate bin 901 and the catalyst bin 902 to be used as a pneumatic conveying gas source.

Meanwhile, to ensure the purity of the oxygen product in the reactor 7, as shown in fig. 3, a loading hopper 904 may be connected to a vacuum pump 909. After the raw materials are filled in the upper hopper 904, an electric gate valve 905 at a feed port is closed, and then a vacuum pump 909 is started in a linked manner to suck the inside of the upper hopper 904 to vacuum. In addition, when the upper hopper 904 is in butt joint with the storage bin for discharging, in order to ensure the air pressure in the storage bin to be stable, as shown in fig. 3, an oxygen pipe 910 can be respectively connected to the potassium chlorate storage bin 901 and the catalyst storage bin 902, an oxygen valve 911 is arranged on the oxygen pipe 910, and the oxygen pipe 910 is connected with an oxygen outlet of the gas purification unit 10. When the feeding hopper 904 is in butt joint with the bin for discharging, oxygen is supplemented into the bin through the oxygen valve 911, so that the feeding hopper 904 in a vacuum state is prevented from affecting the air pressure of the bin. Wherein the oxygen introduced into the oxygen line 910 may be from purified oxygen.

Meanwhile, in order to prevent materials in a material bin from caking or being extruded into blocks and blocking blanking, as shown in fig. 3, a stirring rod 914 can be additionally arranged in the material bin, a paddle 915 is arranged on the stirring rod 914, the stirring rod 914 is driven to rotate by a motor III 916, the paddle 915 can uniformly and slowly stir the materials, and smooth blanking is ensured.

Example 3

On the basis of embodiment 1, as shown in fig. 2, a dust removing mechanism 8 (such as a glass fiber bag type dust collector) is further disposed between the gas product outlet 703 of the reactor 7 and the gas purifying unit 10, and the dust removing mechanism 8 can prevent dust materials from entering the gas purifying unit 10 along with the reaction gas, so that the burden of the gas purifying unit 10 is reduced, and the gas purifying effect is ensured.

Although the present utility model has been described in detail by way of preferred embodiments with reference to the accompanying drawings, the present utility model is not limited thereto. Various equivalent modifications and substitutions may be made in the embodiments of the present utility model by those skilled in the art without departing from the spirit and scope of the present utility model, and it is intended that all such modifications and substitutions be within the scope of the present utility model/be within the scope of the present utility model as defined by the appended claims. Therefore, the protection scope of the present utility model shall be subject to the protection scope of the claims.

Claims

1. The oxygen generation system for recycling high-temperature flue gas of the glass kiln is characterized by comprising a reactor (7), wherein the reactor (7) is provided with a potassium chlorate feed inlet (701), a catalyst feed inlet (702), a solid material discharge outlet and a gas product discharge outlet (703), a heating interlayer (705) is arranged outside the reactor (7), and the heating interlayer (705) is provided with a high-temperature flue gas inlet (7051) and a high-temperature flue gas outlet (7052); the gas product discharging port (703) is connected with the gas purifying unit (10), an inclined first belt conveyor (1101) is arranged below the solid material discharging port, the solid material discharging port is positioned above the lower end of the first belt conveyor (1101), a first water pipe is arranged above the higher end of the first belt conveyor (1101), and a spray header (1103) is arranged on the first water pipe; a potassium chloride solution collecting tank (1104) is arranged below the lower end of the first belt conveyor (1101), and the potassium chloride solution collecting tank (1104) is connected with an evaporator; the lower part of the higher end of the first belt conveyor (1101) is provided with a second belt conveyor (1105), the upper part of the transmission rear end of the second belt conveyor (1105) is provided with a drying mechanism, and the transmission tail end of the second belt conveyor (1105) is provided with a material transporting vehicle (1106).

2. The oxygen generation system for recycling high-temperature flue gas of a glass kiln according to claim 1, wherein the potassium chlorate feed inlet (701) is connected with a potassium chlorate feed bin (901), the catalyst feed inlet (702) is connected with a catalyst feed bin (902), lifting mechanisms are respectively arranged on one side of the potassium chlorate feed bin (901) and one side of the catalyst feed bin (902), a supporting table (903) is arranged on the lifting mechanisms, a feeding hopper (904) is arranged on the supporting table (903), an electric gate valve (905) is respectively arranged at the feed inlet and the discharge outlet of the feeding hopper (904), and the feeding hopper (904) is connected with an output shaft of a motor I (906); the potassium chlorate feed bin (901) and catalyst feed bin (902) top are located feed hopper (904) one side and are provided with feed opening (907) respectively, and feed opening (907) department is provided with electronic gate valve (905), and motor one (906) drives feed hopper (904) to empty to feed opening (907) direction of potassium chlorate feed bin (901) and catalyst feed bin (902), pours potassium chlorate and catalyst into potassium chlorate feed bin (901) and catalyst feed bin (902).

3. The oxygen generation system for recycling high-temperature flue gas of glass kiln according to claim 2, wherein the lifting mechanism comprises a second motor, an output shaft of the second motor is connected with a driving gear, driven gears are further arranged on the potassium chlorate bin (901) and the catalyst bin (902), a chain (908) is arranged on the driving gear and the driven gear, a supporting table (903) is arranged on the chain (908), and the supporting table (903) moves up and down along the height direction of the potassium chlorate bin (901) and the catalyst bin (902) under the driving of the chain (908).

4. The oxygen generation system for recycling high temperature flue gas of glass kiln according to claim 2, wherein the feeding hopper (904) is connected with a vacuum pump (909).

5. The oxygen generation system for recycling high-temperature flue gas of glass kiln according to claim 2, wherein the potassium chlorate bin (901) and the catalyst bin (902) are respectively connected with an oxygen pipe (910), the oxygen pipe (910) is provided with an oxygen valve (911), and the oxygen pipe (910) is connected with an oxygen outlet of the gas purification unit (10).

6. The oxygen generation system for recycling high-temperature flue gas of glass kiln according to claim 1, characterized in that a dust removal mechanism (8) is further arranged between the gas product discharge port (703) of the reactor (7) and the gas purification unit (10).

7. The oxygen generation system for recycling high-temperature flue gas of a glass kiln according to claim 1, wherein the gas purification unit (10) comprises a gas storage tank (1001), a gas inlet of the gas storage tank (1001) is connected with a gas product discharge port (703) through a pipeline, the pipeline extends into the gas storage tank (1001) and a plurality of aeration discs (1002) are arranged on the pipeline; the gas storage tank (1001) is connected with a water pipe II (1003) and an oxygen conveying pipe (1004), and the bottom is connected with a wastewater discharge pipe (1005).

8. The oxygen generation system for recycling high-temperature flue gas of glass kiln according to claim 7, wherein a compressor (1006) is arranged on a pipeline between an air inlet of the air storage tank (1001) and a gas product discharge port (703), and a pressure regulating valve (1007) is arranged on the oxygen conveying pipe (1004).

9. The oxygen generation system for recycling high-temperature flue gas of a glass kiln according to claim 1, wherein the drying mechanism comprises an outer cover (1201) covered on the transmission rear end of the second belt conveyor (1105), a high-temperature flue gas pipeline (1202) is arranged in the outer cover (1201), and the high-temperature flue gas pipeline (1202) is located above the second belt conveyor (1105) and has a gap with the second belt conveyor (1105).

10. The oxygen generation system for recycling high-temperature flue gas of a glass kiln according to claim 1, wherein a rubber brush I (1107) is arranged below the belt conveyor I (1101), the rubber brush I (1107) contacts a belt of the belt conveyor I (1101), and the rubber brush I (1107) is arranged above the belt conveyor II (1105); the rubber brush II (1108) is arranged below the belt conveyor II (1105), the rubber brush II (1108) is in contact with the belt of the belt conveyor II (1105), and the rubber brush II (1108) is arranged above the material conveying vehicle (1106).