High-concentration low-temperature methanol washing waste gas adsorption purification and combined incineration treatment device and process

Abstract

The application discloses a high-concentration low-temperature methanol washing waste gas adsorption purification and combined incineration treatment device, which comprises a first incineration module, an adsorption module and a mixing pipeline, the first incineration module comprises a combustion chamber and a plurality of heat storage chambers connected with the combustion chamber; the heat storage chambers are provided with heat storage bodies; the waste gas flows to the heat storage chambers through the mixing pipeline to form a first gas inlet path, and the mixing pipeline is provided with a flow adjusting device; the waste gas flows to a heat accumulator after passing through the adsorption module to form a second gas inlet path; the waste gas exchanges heat with the heat storage bodies in the heat storage chambers to increase the inlet gas temperature; the waste gas is combusted in the combustion chamber to form purified waste gas, the purified waste gas is discharged through the heat storage chambers and stores heat in the heat storage bodies in the heat storage chambers. Through the cooperation of adsorption and dynamic mixing, the application not only avoids the problem of insufficient purification rate caused by the direct entry of high-concentration waste gas into the combustion chamber, but also avoids the problem of energy waste caused by the need for additional auxiliary fuel to maintain the combustion state under the low-concentration working condition.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of waste gas treatment, in particular to a high-concentration low-temperature methanol wash waste gas adsorption purification and combined incineration treatment device and process. BACKGROUND

[0002] VOCs refers to organic compounds with high vapor pressure, easy to volatilize at room temperature and pressure. VOCs emissions are common in industrial production, especially in printing, chemical industry, building materials, health care and food processing industries. Direct emission of VOCs will cause great harm to the environment and even human health.

[0003] Regenerative combustion method is one of the common environmental protection technologies for treating VOCs. This technology uses a regenerative thermal oxidation furnace to absorb and store the heat of high-temperature gas oxidized by using high-temperature ceramic regenerative material, and then releases the heat to heat the new incoming waste gas containing waste gas to approach the ignition point, and then absorbs part of the heat to oxidize VOCs. Regenerative combustion method is widely used due to its high removal rate, low operating cost, small footprint and low energy consumption.

[0004] The composition and concentration of waste gas produced by different chemical processes are different. Regenerative combustion method only provides a way for VOCs treatment, and there is no fixed regenerative combustion VOCs treatment method that can be applied to all waste gas treatment. When using regenerative combustion method to treat waste gas, the process route needs to be designed according to the composition and concentration characteristics of the waste gas itself, combined with other waste gas treatment methods.

[0005] Using regenerative combustion method to treat VOCs, the commonly applicable VOCs concentration is 8g / Nm 3 Below, the low-calorific-value VOCs concentration can be increased to 12g / Nm 3Because the purification efficiency of the regenerative combustion waste gas treatment technology cannot reach 100%, the higher the concentration of VOCs in the waste gas, the higher the non-methane total hydrocarbon and characteristic pollutants in the exhaust gas, which may exceed the limited value of the environmental protection standard. On the other hand, the RTO reversing valve needs to act frequently, and after a long time, the sealing performance becomes poor, and a small amount of untreated gas will always leak into the exhaust gas. Obviously, the higher the concentration of organic matter in the untreated waste gas, the more demanding the sealing performance of the reversing valve will be, otherwise the VOCs leaked from the reversing valve will increase the concentration of non-methane total hydrocarbon in the exhaust gas. In order to meet the requirements of the emission index, the destruction rate needs to be improved to more than 99.9%. According to relevant research, the higher the destruction rate of organic matter, the higher the required furnace operating temperature; at the same time, the heat released after the oxidation of VOCs with high concentration will increase the flue gas temperature. Therefore, the operating temperature of the RTO device after treating the waste gas with high concentration is obviously higher than that of the general RTO device. The higher operating temperature brings the problem of cost increase of the RTO furnace and the regenerator.

[0006] The low-temperature methanol washing waste gas has the characteristics of high heat value, high VOCs concentration and low oxygen concentration, and the traditional regenerative combustion waste gas treatment technology cannot effectively treat it, which has become one of the difficulties in the process route design of the regenerative combustion method.

[0007] For example, the invention patent with the publication number CN117722683A proposes a combined device and process for high-concentration organic waste gas incineration purification, which includes pipeline systems, RTO incineration furnaces, waste heat boilers, coal economizers and other components. However, the device and process have the following shortcomings: (1) there is a risk of incomplete oxidation and emission tail gas concentration exceeding the standard. When the concentration of VOCs fluctuates and increases, although most of the volatile organic compounds are completely oxidized, due to the large concentration base of VOCs, the residual volatile organic compounds still exceed the requirements of the emission standard in the national standard; (2) the temperature difference between the inlet and outlet is too large. The heat released during the oxidation of VOCs will increase the sensible heat of the exhaust gas, and the higher the concentration of VOCs in the exhaust gas, the higher the flue gas temperature in the exhaust gas. The high exhaust gas temperature of the RTO not only fails to meet the requirement in the Technical Code for Regenerative Combustion Industrial Organic Waste Gas Treatment Engineering (HJ1093-2020) that the temperature difference between the inlet and outlet of the regenerative combustion device should not be greater than 60℃, but also is a huge waste of energy.

[0008] In summary, the existing technology has the shortcomings of high treatment cost and low purification efficiency when treating low-temperature methanol washing waste gas. SUMMARY

[0009] The purpose of the present application is to solve the problems in the prior art, and to provide a high-concentration low-temperature methanol washing waste gas adsorption purification and combined incineration treatment device and process.

[0010] The purpose of the present application is achieved by the technical scheme that the high-concentration low-temperature methanol washing waste gas adsorption purification and combined incineration treatment device, including first incineration module, adsorption module, mixing pipeline, the first incineration module includes combustion chamber and the several regenerative chambers connected with combustion chamber;Regenerative chamber is provided with regenerator;Waste gas flows to regenerative chamber through mixing pipeline to form first inlet path, and flow regulating device is arranged on mixing pipeline;Waste gas flows to regenerative chamber through adsorption module to form second inlet path;Waste gas and regenerator in regenerative chamber carry out heat exchange to improve inlet temperature;Waste gas carries out combustion in combustion chamber and forms purified waste gas, and purified waste gas is discharged through regenerative chamber and regenerative chamber in regenerative chamber is heat stored.

[0011] As preferred, when the volatile organic compound concentration in the waste gas entering the regenerative chamber is lower than the first concentration threshold, then the opening of the flow regulating device is increased to increase the volatile organic compound concentration in the waste gas entering the regenerative chamber and maintain the combustion chamber within the set temperature range.

[0012] As preferred, the first incineration module contains three states of regenerative chambers in any one working cycle, respectively, the regenerative chamber in heat release state, the regenerative chamber in heat storage state and the regenerative chamber in purge state;Waste gas enters the combustion chamber through the regenerative chamber in heat release state, and purified waste gas is discharged through the regenerative chamber in heat storage state;Part of the purified waste gas is discharged through the purge channel into the regenerative chamber in purge state;Each regenerative chamber works in turn according to the order of heat storage state, heat release state and purge state.

[0013] As preferred, the regenerative chamber is provided with heat exchanger space and regenerator space, and the regenerator space is located above the heat exchanger space;The regenerator space is in communication with the internal space of the combustion chamber;The regenerator space is provided with regenerator, and the heat exchanger space is provided with first heat exchanger;The first heat exchanger includes shell and heat exchange pipe arranged in the shell, the upper end of the heat exchange pipe is in communication with the regenerator space, and the lower end of the heat exchange pipe is the waste gas inlet end;The space between the heat exchange pipe and the shell is the shell side space, and the first heat exchanger is provided with medium inlet and medium outlet outside;The medium inlet and the medium outlet are in communication with the shell side space;Waste gas enters the regenerator space through the heat exchange pipe and exchanges heat with the regenerator;When the waste gas flow entering the regenerative chamber exceeds the first flow threshold, the heat medium is introduced into the shell side space through the medium inlet to increase the temperature of the waste gas;The purified waste gas is discharged after passing through the regenerator space and the heat exchange pipe in turn;When the flow of purified waste gas exceeds the second flow threshold, the coolant is introduced into the shell side space through the medium inlet to cool the regenerator.

[0014] As preferred, the adsorption module comprises a first activated carbon tank group and a second activated carbon tank group, the first activated carbon tank group and the second activated carbon tank group are alternately operated between an adsorption state and a desorption state; the first activated carbon tank group and the second activated carbon tank group each consist of one or more activated carbon tanks; when the activated carbon tank is in the adsorption state, the waste gas enters the activated carbon tank through the waste gas inlet pipe and is adsorbed by the adsorption filler inside for treatment, and the treated waste gas is discharged through the waste gas outlet pipe and enters the regenerator; when the activated carbon tank is in the desorption state, the back flushing gas enters the activated carbon tank through the back flushing gas inlet pipe and is discharged through the back flushing gas outlet pipe; the adsorption filler inside is desorbed by the back flushing gas.

[0015] As preferred, the adsorption module further comprises an activated carbon tank in standby state, when the concentration of volatile organic compounds in the waste gas entering the regenerator is higher than the second concentration threshold, the standby activated carbon tank is activated for adsorption operation.

[0016] As preferred, the second incineration module is further comprised, the back flushing gas outlet pipe is connected with the second incineration module, the second incineration module is connected with the waste heat boiler; the back flushing gas forms rich hydrocarbon waste gas after passing through the activated carbon tank, the rich hydrocarbon waste gas is combusted in the second incineration module to generate high temperature tail gas, the high temperature tail gas provides heat for the waste heat boiler to generate steam, and the steam exchanges heat with the back flushing gas to increase the temperature of the back flushing gas.

[0017] As preferred, the second incineration module adopts a direct-fired thermal oxidation furnace.

[0018] The high concentration low temperature methanol washing waste gas adsorption purification and combined incineration treatment process is specifically as follows:

[0019] The waste gas flows to the regenerator in the heat releasing state through the second gas inlet path or the first gas inlet path and the second gas inlet path in a cooperative manner, the adsorption module adsorbs part of the volatile organic compounds in the waste gas when the waste gas passes through the adsorption module; the waste gas exchanges heat with the heat storage body in the regenerator to increase the inlet temperature of the waste gas; then the waste gas enters the combustion chamber for combustion; the purified waste gas after combustion passes through the combustion chamber in the heat storage state and is discharged outward, and the purified waste gas exchanges heat with the heat storage body in the combustion chamber to increase the temperature of the heat storage body; when the concentration of volatile organic compounds in the waste gas entering the regenerator is lower than the first concentration threshold, the opening of the flow regulating device is increased to increase the concentration of volatile organic compounds in the waste gas entering the regenerator and maintain the combustion chamber at a set temperature range.

[0020] As preferred, when the flow of the exhaust gas entering the heat storage chamber exceeds the first flow threshold, the heat medium is introduced into the shell side space of the first heat exchanger in the heat storage chamber to raise the temperature of the exhaust gas; the purified exhaust gas is discharged after sequentially passing through the heat storage body space and the heat exchange tube; when the flow of the purified exhaust gas exceeds the second flow threshold, the cold medium is introduced into the shell side space of the first heat exchanger in the heat storage chamber to cool the heat storage body.

[0021] The beneficial effects of the present application are:

[0022] 1. The present application avoids the problem of insufficient purification rate caused by directly entering the combustion chamber with high-concentration exhaust gas, and avoids the problem of energy waste caused by additional auxiliary fuel to maintain the combustion state under low-concentration conditions.

[0023] 2. The present application adopts the adsorption+combustion collaborative processing framework to construct a double-path processing mode, which realizes the precise matching of exhaust gas concentration and processing technology. The ideal concentration exhaust gas (2-5 g / Nm3) after adsorption enters the heat storage chamber, is preheated to above 760℃ by the heat storage body, stays in the combustion chamber for 1-2 seconds to complete the oxidation decomposition, and realizes a heat recovery rate of more than 95% by using the heat storage body; the rich-hydrocarbon exhaust gas generated by desorption after saturation is directly input into the second incineration module for incineration. The second incineration module adopts high-temperature air preheating+exhaust gas lance cyclone design. The preheater uses the waste heat of high-temperature exhaust gas to heat the combustion air to a high temperature state. In combination with the furnace temperature of 750-1100℃ and the residence time of 0.5-2 seconds in the second incineration module, the complete oxidation of volatile organic compounds is ensured, and the risk of deflagration in the traditional treatment of high-concentration exhaust gas is avoided. The second incineration module is heated to 850℃ by fuel gas in the starting stage, and only relies on self-sustaining combustion of rich-hydrocarbon exhaust gas after normal operation, which significantly reduces the consumption of auxiliary fuel.

[0024] 3. The present application adds a first heat exchanger in the heat storage chamber. When the flow of the mixed exhaust gas is too large, the heat medium (steam) is introduced into the shell side space of the first heat exchanger to preheat the exhaust gas, so as to increase the inlet temperature of the exhaust gas and make the volatile organic compounds completely oxidize and burn in the combustion chamber; when the temperature of the heat storage body is too high, the cold medium (water) is introduced into the shell side space to reduce the temperature of the heat storage body, so as to avoid the melting or cracking of the heat storage body caused by the high temperature of the heat storage chamber, and ensure the safe operation of the system. BRIEF DESCRIPTION OF DRAWINGS

[0025] Figure 1 The figure is a schematic diagram of the pipeline connection of the present application.

[0026] Figure 2 The figure is a structural schematic diagram of the heat storage chamber.

[0027] BRIEF DESCRIPTION OF DRAWINGS: 1, exhaust gas inlet, 2, flow regulating device, 3, exhaust gas upper air pipe, 4, exhaust gas upper air pipe control valve, 5, back flushing lower air pipe, 6, back flushing lower air pipe control valve, 7, activated carbon tank, 8, adsorption filler, 9, exhaust gas outlet pipe, 10, exhaust gas outlet pipe control valve, 11, back flushing upper air pipe, 12, back flushing upper air pipe control valve, 13, exhaust gas inlet pipe, 14, exhaust gas inlet pipe control valve, 15, regenerator purging pipe, 16, regenerator purging pipe control valve, 17, purified exhaust gas outlet pipe, 18, purified exhaust gas outlet pipe control valve, 19, regenerator, 20, regenerator, 201, first regenerator, 202, second regenerator, 203, third regenerator, 204, fourth regenerator, 205, fifth regenerator, 21, combustion chamber, 22, burner, 23, direct-fired thermal oxidizer, 24, flame lances, 25, low NOx burner, 26, waste heat boiler, 27, first preheater, 28, economizer, 29, second preheater, 30, exhaust gas pipe, 31, desorption pipe, 32, second heat exchanger, 33, first heat exchanger, 34, mixing pipe, 35, shell, 36, heat exchange pipe, 37, regenerator space, 38, medium inlet, 39, medium outlet. DETAILED DESCRIPTION

[0028] The technical solutions in the embodiments of the present application will be clearly and completely described below with reference to the drawings in the embodiments of the present application. Obviously, the described embodiments are only part of the embodiments of the present application, rather than all the embodiments. All other embodiments obtained by those skilled in the art based on the embodiments in the present application belong to the scope of protection of the present application.

[0029] Those skilled in the art should understand that in the disclosure of the present application, the orientations or positional relationships indicated by the terms "longitudinal", "transverse", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer" and the like are based on the orientations or positional relationships shown in the drawings, which are only for the convenience of describing the present application and simplifying the description, and do not indicate or imply that the devices or elements referred to must have a particular orientation, be constructed and operated in a particular orientation, therefore the above terms cannot be understood as a limitation on the present application.

[0030] It can be understood that the term "one" should be understood as "at least one" or "one or more", that is, in one embodiment, the number of one element can be one, and in another embodiment, the number of the element can be multiple, and the term "one" cannot be understood as a limitation on the number.

[0031] As Figure 1As shown, the high-concentration low-temperature methanol washing waste gas adsorption purification and combined incineration treatment device includes a first incineration module, an adsorption module, and a mixing pipeline 34. The first incineration module includes a combustion chamber 21 and a plurality of heat storage chambers 20 connected to the combustion chamber 21. The heat storage chambers 20 are provided with heat storage bodies 19. The waste gas flows to the heat storage chambers 20 through the mixing pipeline 34 to form a first gas inlet path. The mixing pipeline 34 is provided with a flow regulating device 2. The waste gas flows to the heat storage chambers 20 through the adsorption module to form a second gas inlet path. The waste gas exchanges heat with the heat storage bodies 19 in the heat storage chambers 20 to increase the inlet gas temperature. The waste gas is combusted in the combustion chamber 21 to form purified waste gas, which is discharged through the heat storage chambers 20 and heats the heat storage bodies 19 in the heat storage chambers 20. The combustion chamber 21 is provided with a burner 22.

[0032] The waste gas enters from the waste gas inlet 1. When the waste gas enters the heat storage chambers 20 along the first gas inlet path, the waste gas has not been purified by the adsorption module, and therefore contains a high concentration of volatile organic compounds. When the waste gas enters the heat storage chambers 20 along the second gas inlet path, the adsorption module adsorbs part of the volatile organic compounds in the waste gas, thereby reducing the concentration of volatile organic compounds in the waste gas.

[0033] The flow regulating device 2 is a proportional regulating valve for controlling the gas flow in the mixing pipeline 34. Each heat storage chamber 20 is provided with a waste gas inlet pipeline 13, and each waste gas inlet pipeline 13 is provided with a waste gas inlet pipeline control valve 14 for controlling the on-off of the waste gas inlet pipeline 13. A volatile organic compound concentration monitor is provided on the waste gas inlet pipeline 13 for real-time detection of the concentration of volatile organic compounds in the waste gas. When the concentration of volatile organic compounds in the waste gas entering the heat storage chambers 20 is lower than the first concentration threshold, the opening of the flow regulating device 2 is increased to increase the concentration of volatile organic compounds in the waste gas entering the heat storage chambers 20 and maintain the combustion chamber 21 within the set temperature range. When the concentration is lower than the ideal combustion threshold, the opening of the flow regulating device 2 is dynamically adjusted based on the PID control algorithm, and part of the high-concentration waste gas that has not been adsorbed is mixed into the adsorbed waste gas, so that the concentration of the mixed gas is stably maintained in the optimal range of 2-5 g / Nm3.

[0034] Conversely, if the concentration of volatile organic compounds in the waste gas entering the heat storage chambers 20 is too high, it will easily lead to insufficient combustion and result in insufficient purification efficiency. At this time, the opening of the flow regulating device 2 is reduced or the flow regulating device 2 is closed, thereby reducing the proportion of high-concentration waste gas and the overall concentration of the mixed waste gas, thereby avoiding the problem of incomplete purification rate.

[0035] The present application avoids the problem of insufficient purification rate caused by directly entering the combustion chamber 21 by adsorption and dynamic mixing, and avoids the problem of energy waste caused by additional auxiliary fuel to maintain the combustion state under low concentration conditions.

[0036] The first incineration module contains three types of regenerator 20 in any one working cycle, which are regenerator 20 in heat releasing state, regenerator 20 in heat storage state and regenerator 20 in purging state; the exhaust gas enters the combustion chamber 21 through the regenerator 20 in heat releasing state, and the purified exhaust gas is discharged through the regenerator 20 in heat storage state; part of the purified exhaust gas is discharged into the regenerator 20 in purging state through the purging channel; each regenerator 20 works in the order of heat storage state, heat releasing state and purging state.

[0037] Each regenerator 20 is provided with a purified exhaust gas discharge pipeline 17, and the purified exhaust gas discharge pipeline 17 is provided with a purified exhaust gas discharge pipeline control valve 18. The purified exhaust gas discharge pipeline 17 is connected to the chimney. Each regenerator 20 is also connected with a regenerator purging pipeline 15, and the regenerator purging pipeline 15 is provided with a regenerator purging pipeline control valve 16.

[0038] In the present application, a total of five regenerators 20 are provided, which are first regenerator 201, second regenerator 202, third regenerator 203, fourth regenerator 204 and fifth regenerator 205.

[0039] When the adsorption module is actually running, it runs in the following five processes in turn:

[0040] The first process: the exhaust gas enters the first regenerator 201 and the second regenerator 202, at this time, the first regenerator 201 and the second regenerator 202 are in the heat releasing state, the exhaust gas exchanges heat with the high-temperature heat storage bodies 19 in the first regenerator 201 and the second regenerator 202, the temperature of the heat storage bodies 19 decreases to become cold-bed heat storage bodies 19, and the temperature of the exhaust gas increases and enters the combustion chamber 21, and the temperature continues to increase, when the temperature exceeds the self-ignition point of the volatile organic compounds, the volatile organic compound molecules in the exhaust gas are completely oxidized; after the exhaust gas is combusted, the purified exhaust gas is formed, the purified exhaust gas enters the third regenerator 203 and the fourth regenerator 204, at this time, the third regenerator 203 and the fourth regenerator 204 are in the heat storage state, and the fifth regenerator 205 is in the purging state, the purified exhaust gas exchanges heat with the heat storage bodies 19 in the third regenerator 203 and the fourth regenerator 204, the temperature of the heat storage bodies 19 in the third regenerator 203 and the fourth regenerator 204 increases to become hot-bed heat storage bodies 19, to prepare for preheating the exhaust gas in the next process, and the temperature of the purified exhaust gas decreases and is discharged through the regenerator 20, most of the purified exhaust gas is transported to the chimney for emission, and a small part of the purified exhaust gas enters the fifth regenerator 205 in the purging state through the regenerator purging pipeline 15, the heat storage bodies 19 of the fifth regenerator 205 have just released heat from the last cycle, and change from hot-bed heat storage bodies 19 to cold-bed heat storage bodies 19, the purified exhaust gas enters the fifth regenerator 205 to perform the purging function;

[0041] The second process: the second regenerator 202 and the third regenerator 203 are in the heat releasing state, the fourth regenerator 204 and the fifth regenerator 205 are in the heat storage state, and the first regenerator 201 is in the purging state, the exhaust gas enters the combustion chamber 21 from the second regenerator 202 and the third regenerator 203, the purified exhaust gas is discharged from the fourth regenerator 204 and the fifth regenerator 205, and the first regenerator 201 performs purging;

[0042] The third cycle: the third regenerator 203 and the fourth regenerator 204 are in the heat releasing state, the first regenerator 201 and the fifth regenerator 205 are in the heat storage state, and the second regenerator 202 is in the purging state, the exhaust gas enters the combustion chamber 21 from the third regenerator 203 and the fourth regenerator 204, the purified exhaust gas is discharged from the first regenerator 201 and the fifth regenerator 205, and the second regenerator 202 performs purging;

[0043] The fourth cycle: the fourth regenerator 204 and the fifth regenerator 205 are in the heat releasing state, the first regenerator 201 and the second regenerator 202 are in the heat storage state, and the third regenerator 203 is in the purging state, the exhaust gas enters the combustion chamber 21 from the fourth regenerator 204 and the fifth regenerator 205, the purified exhaust gas is discharged from the first regenerator 201 and the second regenerator 202, and the third regenerator 203 performs purging;

[0044] Cycle five: the first regenerator 201 and the fifth regenerator 205 are in heat releasing state, the second regenerator 202 and the third regenerator 203 are in heat storing state, the fourth regenerator 204 is in purging state, the exhaust gas enters the combustion chamber 21 from the first regenerator 201 and the fifth regenerator 205, the purified exhaust gas is discharged from the second regenerator 202 and the third regenerator 203, and the fourth regenerator 204 performs purging.

[0045] Further, the heat exchanger space and the heat storage body space 37 are arranged in the regenerator 20, the heat storage body space 37 is located above the heat exchanger space, the heat storage body space 37 is in communication with the internal space of the combustion chamber 21, the heat storage body 19 is arranged in the heat storage body space 37, and the first heat exchanger 33 is arranged in the heat exchanger space; the first heat exchanger 33 comprises a shell 35 and a heat exchange pipe 36 arranged in the shell 35, the upper end of the heat exchange pipe 36 is in communication with the heat storage body space 37, the lower end of the heat exchange pipe 36 is an exhaust gas inlet end, the space between the heat exchange pipe 36 and the shell 35 is a shell side space, the medium inlet 38 and the medium outlet 39 are arranged outside the first heat exchanger 33, the medium inlet 38 and the medium outlet 39 are in communication with the shell side space, the exhaust gas enters the heat storage body space 37 through the heat exchange pipe 36 and exchanges heat with the heat storage body 19, when the flow of the exhaust gas entering the regenerator 20 exceeds the first flow threshold value, the heat medium is introduced into the shell side space through the medium inlet 38 to increase the temperature of the exhaust gas, the purified exhaust gas is discharged after sequentially passing through the heat storage body space 37 and the heat exchange pipe 36, and when the flow of the purified exhaust gas exceeds the second flow threshold value, the coolant is introduced into the shell side space through the medium inlet 38 to cool the heat storage body 19.

[0046] In the application, the heat storage body 19 is a modular ceramic honeycomb unit (200*200*100mm, cordierite material), which is layered and stacked in the heat storage body space 37. The heat exchange pipe 36 is arranged in an array, penetrates through the whole heat exchanger space, and the pipe wall of the heat exchange pipe 36 is sprayed with an aluminum oxide coating. The spiral baffle (inclination angle 25°) is arranged in the shell side space to strengthen the heat transfer effect.

[0047] The application adds the first heat exchanger 33 in the regenerator 20, when the flow of the mixed exhaust gas is too large, the heat medium (steam) is introduced into the shell side space of the first heat exchanger 33 to preheat the exhaust gas, the inlet temperature of the exhaust gas is increased to make the volatile organic compounds completely oxidize and burn in the combustion chamber 21, when the temperature of the heat storage body 19 is too high, the coolant (water) is introduced into the shell side space to reduce the temperature of the heat storage body 19, so that the melting or cracking of the heat storage body 19 caused by the high temperature of the regenerator 20 is avoided, and the safe operation of the system is ensured.

[0048] The adsorption module comprises a first activated carbon tank group 7 and a second activated carbon tank group, the first activated carbon tank group and the second activated carbon tank group alternately operate between an adsorption state and a desorption state; the first activated carbon tank group and the second activated carbon tank group each comprise one or more activated carbon tanks 7; when the activated carbon tank 7 is in the adsorption state, the exhaust gas enters the activated carbon tank 7 through the exhaust gas inlet pipe 3 and is adsorbed by the internal adsorption filler 8, and the exhaust gas after the adsorption treatment is discharged through the exhaust gas outlet pipe 9 and enters the heat storage chamber 20; when the activated carbon tank 7 is in the desorption state, the back flushing gas enters the activated carbon tank through the back flushing gas inlet pipe 11 and is discharged through the back flushing gas outlet pipe 5; the internal adsorption filler 8 is back-flushed and desorbed by the back flushing gas.

[0049] In this embodiment, the first activated carbon tank group 7 comprises two activated carbon tanks, and the second activated carbon tank group comprises two activated carbon tanks 7. When the first activated carbon tank group 7 is in the adsorption state, the second activated carbon tank group is in the desorption regeneration state; conversely, when the second activated carbon tank group is in the adsorption state, the first activated carbon tank group is in the desorption regeneration state. Through the alternative operation of the two (one adsorption and one desorption regeneration), the continuous operation of the adsorption operation is ensured.

[0050] The adsorption filler 8 in the activated carbon tank 7 is activated carbon. The activated carbon tank 7 is provided with an exhaust gas inlet pipe 3, an exhaust gas outlet pipe 9, a back flushing gas inlet pipe 11 and a back flushing gas outlet pipe 5, the exhaust gas inlet pipe 3 is provided with an exhaust gas inlet pipe control valve 4, the exhaust gas outlet pipe 9 is provided with an exhaust gas outlet pipe control valve 10, the back flushing gas inlet pipe 11 is provided with a back flushing gas inlet pipe control valve 12, and the back flushing gas outlet pipe 5 is provided with a back flushing gas outlet pipe control valve 6. The back flushing gas inlet pipe 11 is connected with the desorption pipe 31, and the desorption pipe 31 is connected with the exhaust gas inlet 1.

[0051] When the activated carbon tank 7 is in the adsorption state, the exhaust gas enters from the exhaust gas inlet pipe 3, flows through the adsorption filler 8 and then flows out from the exhaust gas outlet pipe 9, and the volatile organic compounds in the exhaust gas are adsorbed by the adsorption filler 8. When the activated carbon tank 7 is in the desorption state, part of the exhaust gas from the exhaust gas inlet 1 is used as back flushing gas, the back flushing gas enters the activated carbon tank 7 through the desorption pipe 31 and the back flushing gas inlet pipe 11, and performs back flushing and desorption operation on the adsorption filler 8 in the activated carbon tank 7; the volatile organic compounds originally adsorbed in the adsorption filler 8 are desorbed and mixed into the back flushing gas to form rich hydrocarbon exhaust gas, and the rich hydrocarbon exhaust gas is discharged from the back flushing gas outlet pipe 5.

[0052] The adsorption module further comprises an activated carbon tank 7 in standby state, when the concentration of volatile organic compounds in the exhaust gas entering the heat storage chamber 20 is higher than the second concentration threshold, the standby activated carbon tank 7 is started to perform adsorption operation. Prevent the concentration of VOCs in the exhaust gas entering the combustion chamber 21 from being too high.

[0053] The present application also comprises a second incineration module, the back-blowing gas pipeline 5 is connected with the second incineration module, and the second incineration module is connected with a waste heat boiler 26; the back-blowing gas forms a hydrocarbon-rich waste gas after passing through the activated carbon tank 7, the hydrocarbon-rich waste gas is combusted in the second incineration module to generate high-temperature tail gas, the high-temperature tail gas provides heat for the waste heat boiler 26 and generates steam, and the steam exchanges heat with the back-blowing gas to increase the temperature of the back-blowing gas.

[0054] The second heat exchanger 32 is arranged on the desorption pipeline 31. The steam generated by the waste heat boiler 26 enters the second heat exchanger 32, and the steam with a high temperature exchanges heat with the back-blowing gas in the desorption pipeline 31 to increase the temperature of the back-blowing gas, thereby improving the desorption effect.

[0055] In the embodiment, the second incineration module adopts a direct-fired thermal oxidation furnace 23. The direct-fired thermal oxidation furnace 23 is provided with a flame spraying gun 24 and a low-nitrogen combustor 25. The high-temperature tail gas generated by the combustion of the hydrocarbon-rich waste gas enters the waste heat boiler 26, and heats and evaporates water in the waste heat boiler 26 to generate steam.

[0056] The steam generated by the waste heat boiler 26 can also be used as a heat medium that enters the first heat exchanger 33 to preheat the waste gas that enters the heat storage chamber 20.

[0057] The high-temperature tail gas after the combustion of the hydrocarbon-rich waste gas passes through the waste heat boiler 26 and is discharged outward through the smoke exhaust pipeline 30, the smoke exhaust pipeline 30 is connected with a smokestack, and the tail gas after the combustion of the hydrocarbon-rich waste gas is finally discharged from the smokestack. The smoke exhaust pipeline 30 is provided with a first preheater 27, a second preheater 29 and an economizer 28. Since air needs to be introduced into the second incineration module during combustion, the air exchanges heat with the high-temperature tail gas in the smoke exhaust pipeline 30 through the first preheater 27 and the second preheater 29 before being introduced into the second incineration module to increase the temperature of the air, thereby improving the incineration effect. When water is supplied to the preheating boiler, the water first passes through the economizer 28, and the economizer 28 is essentially a heat exchanger. The water exchanges heat with the high-temperature tail gas in the smoke exhaust pipeline 30 through the economizer 28 to increase the temperature of the water, thereby promoting the generation of steam.

[0058] The application adopts adsorption+combustion cooperative treatment framework, constructs a double-path treatment mode, and realizes precise matching of waste gas concentration and treatment process. Among them, the ideal concentration waste gas (2-5g / Nm3) after adsorption enters the heat storage chamber 20, is preheated to above 760 DEG C by the heat storage body 19, stays in the combustion chamber 21 for 1-2 seconds to complete oxidative decomposition, and realizes heat recovery rate of more than 95% by using the heat storage body 19. The rich hydrocarbon waste gas (concentration is greater than 8g / Nm3) generated after adsorption saturation is directly input into the second incineration module for incineration. The second incineration module adopts high-temperature air preheating+waste gas lance cyclone design. The preheater uses the waste heat of high-temperature tail gas to heat the combustion air to a high temperature state. Cooperate with the furnace temperature of 750-1100 DEG C in the second incineration module and the residence time of 0.5-2 seconds, ensure that the volatile organic compounds are completely oxidized, avoid the risk of deflagration when treating high-concentration waste gas in the traditional way, and the second incineration module is started by fuel gas heating to 850 DEG C. After normal operation, it only relies on self-sustaining combustion of rich hydrocarbon waste gas, which significantly reduces auxiliary fuel consumption.

[0059] A high-concentration low-temperature methanol washing waste gas adsorption purification and combined incineration treatment process, the specific method is as follows:

[0060] The waste gas flows to the heat storage chamber 20 in the heat release state through the second gas inlet path or the first gas inlet path and the second gas inlet path cooperatively. When the waste gas passes through the adsorption module, the adsorption module adsorbs part of the volatile organic compounds in the waste gas. The waste gas exchanges heat with the heat storage body 19 in the heat storage chamber 20 to increase the inlet temperature of the waste gas. Then the waste gas enters the combustion chamber 21 for combustion. The purified waste gas after combustion passes through the combustion chamber 21 in the heat storage state and is discharged outward. The purified waste gas exchanges heat with the heat storage body 19 in the combustion chamber 21 to increase the temperature of the heat storage body 19. When the concentration of volatile organic compounds in the waste gas entering the heat storage chamber 20 is lower than the first concentration threshold, the opening of the flow regulating device 2 is increased to increase the concentration of volatile organic compounds in the waste gas entering the heat storage chamber 20 and maintain the combustion chamber 21 within the set temperature range. When the flow of waste gas entering the heat storage chamber 20 exceeds the first flow threshold, the heat medium is introduced into the shell space of the first heat exchanger 33 in the heat storage chamber 20 to increase the temperature of the waste gas. When the purified waste gas successively passes through the heat storage body space 37 and the heat exchange pipe 36, it is discharged. When the flow of purified waste gas exceeds the second flow threshold, the coolant is introduced into the shell space of the first heat exchanger 33 in the heat storage chamber to cool the heat storage body 19.

[0061] The present application is not limited to the above best mode of implementation, and anyone can derive other various forms of products under the inspiration of the present application, but regardless of any changes in shape or structure, any technical solution with the same or similar to the present application falls within the scope of the present application.

Claims

1. A device for adsorption purification and combined incineration treatment of high-concentration low-temperature methanol wash waste gas, characterized in that, The application relates to a waste gas treatment device, which comprises a first incineration module, an adsorption module and a mixing pipeline, the first incineration module comprises a combustion chamber and a plurality of heat storage chambers connected with the combustion chamber; heat storage bodies are arranged in the heat storage chambers; waste gas flows to the heat storage chambers through the mixing pipeline to form a first air inlet path, a flow adjusting device is arranged on the mixing pipeline; waste gas flows to a heat accumulator through the adsorption module to form a second air inlet path; waste gas exchanges heat with the heat storage bodies in the heat storage chambers to increase the temperature of inlet air; waste gas is combusted in the combustion chamber to form purified waste gas, the purified waste gas is discharged through the heat storage chambers and stores heat in the heat storage bodies in the heat storage chambers; The adsorption module comprises a first activated carbon tank group and a second activated carbon tank group, the first activated carbon tank group and the second activated carbon tank group alternately operate between adsorption states and desorption states; the first activated carbon tank group and the second activated carbon tank group are each composed of one or more activated carbon tanks; when the activated carbon tank is in the adsorption state, waste gas enters the activated carbon tank through a waste gas inlet pipeline and is adsorbed by internal adsorption fillers, the waste gas after the adsorption treatment is discharged through a waste gas outlet pipeline and reaches the heat storage chamber; when the activated carbon tank is in the desorption state, back-blowing gas enters the activated carbon tank through a back-blowing gas inlet pipeline and is discharged through a back-blowing gas outlet pipeline; the internal adsorption fillers are back-blowing desorption treated by the back-blowing gas; The application further comprises a second incineration module, the back-blowing gas outlet pipeline is connected with the second incineration module, the second incineration module is connected with a waste heat boiler; the back-blowing gas after passing through the activated carbon tank forms hydrocarbon-rich waste gas, the hydrocarbon-rich waste gas is combusted in the second incineration module to generate high-temperature tail gas, the high-temperature tail gas provides heat for the waste heat boiler and generates steam, the steam exchanges heat with the back-blowing gas to increase the temperature of the back-blowing gas.

2. The device according to claim 1, wherein the device is characterized by: When the concentration of volatile organic compounds in the waste gas entering the heat storage chamber is lower than a first concentration threshold, the opening degree of the flow adjusting device is increased to increase the concentration of volatile organic compounds in the waste gas entering the heat storage chamber and maintain the combustion chamber in a set temperature range.

3. The device according to claim 1, wherein the device is characterized by: The first incineration module contains three states of heat storage chambers in any working cycle, which are heat releasing state heat storage chambers, heat storage state heat storage chambers and purging state heat storage chambers; waste gas enters the combustion chamber through the heat releasing state heat storage chambers, and purified waste gas is discharged through the heat storage state heat storage chambers; part of the purified waste gas is discharged and enters the purging state heat storage chambers through the purging channel; each heat storage chamber works in the order of heat storage state, heat releasing state and purging state.

4. The device according to claim 1, wherein the device is characterized by: The heat storage chamber is provided with a heat exchanger space and a heat storage body space, the heat storage body space is located above the heat exchanger space; the heat storage body space is in communication with the internal space of the combustion chamber; the heat storage body space is provided with heat storage bodies, and the heat exchanger space is provided with a first heat exchanger; the first heat exchanger comprises a shell and heat exchange pipes arranged in the shell, the upper end of the heat exchange pipe is in communication with the heat storage body space, and the lower end of the heat exchange pipe is a waste gas inlet end; the space between the heat exchange pipe and the shell is a shell side space, the first heat exchanger is provided with a medium inlet and a medium outlet outside; the medium inlet and the medium outlet are in communication with the shell side space; waste gas enters the heat storage body space through the heat exchange pipe and exchanges heat with the heat storage bodies; When the flow of the exhaust gas into the heat storage chamber exceeds the first flow threshold, the heat medium is introduced into the shell side space through the medium inlet to increase the temperature of the exhaust gas; the purified exhaust gas is discharged after sequentially passing through the heat storage body space and the heat exchange tube; when the flow of the purified exhaust gas exceeds the second flow threshold, the cold medium is introduced into the shell side space through the medium inlet to cool the heat storage body.

5. The device according to claim 1, wherein the device is characterized by: The adsorption module further includes an activated carbon tank in a standby state, and when the concentration of volatile organic compounds in the exhaust gas entering the heat storage chamber is higher than the second concentration threshold, the standby activated carbon tank is activated to perform adsorption work.

6. The device according to claim 1, wherein the device is characterized by: The second incineration module adopts a direct-fired thermal oxidation furnace.

7. The high concentration rectisol off-gas adsorptive purification and combined incineration disposal process according to claim 1, the high concentration rectisol off-gas adsorptive purification and combined incineration disposal device based on claim 1, characterized in that, The specific method is as follows: The exhaust gas flows to the heat storage chamber in the heat release state through the second gas inlet path or the first gas inlet path and the second gas inlet path in cooperation, the adsorption module adsorbs part of the volatile organic compounds in the exhaust gas when the exhaust gas passes through the adsorption module, the exhaust gas exchanges heat with the heat storage body in the heat storage chamber to increase the inlet temperature of the exhaust gas, and then the exhaust gas enters the combustion chamber for combustion; the purified exhaust gas after combustion passes through the combustion chamber in the heat storage state and is discharged outward, and the purified exhaust gas exchanges heat with the heat storage body in the combustion chamber to increase the temperature of the heat storage body; when the concentration of volatile organic compounds in the exhaust gas entering the heat storage chamber is lower than the first concentration threshold, the opening of the flow regulating device is increased to increase the concentration of volatile organic compounds in the exhaust gas entering the heat storage chamber and maintain the combustion chamber at a set temperature range.

8. The high concentration rectisol off-gas adsorptive purification and combined incineration disposal process according to claim 7, characterized in that, When the flow of the exhaust gas into the heat storage chamber exceeds the first flow threshold, the heat medium is introduced into the shell side space of the first heat exchanger in the heat storage chamber to increase the temperature of the exhaust gas; the purified exhaust gas is discharged after sequentially passing through the heat storage body space and the heat exchange tube; when the flow of the purified exhaust gas exceeds the second flow threshold, the cold medium is introduced into the shell side space of the first heat exchanger in the heat storage chamber to cool the heat storage body.

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