System and method for using industrial waste gas and industrial waste brine to prepare soda ash

Abstract

Provided in the present invention are a system and method for using industrial waste gas and industrial waste brine to prepare soda ash. The system comprises a waste liquid pipe, a waste gas pipe, an ammonia gas pipe, a heat exchanger, an oxidation reaction tower, a dust removal tower, a preliminary carbonization reaction tower and a deep carbonization reaction tower; an outlet of the waste liquid pipe is connected to the oxidation reaction tower, the heat exchanger being arranged on the waste liquid pipe; an oxidation product generated in the waste liquid pipe is conveyed to the preliminary carbonization reaction tower by means of a first conveying pipe; the waste gas pipe is connected to the dust removal tower by means of the heat exchanger, a dust removal product obtained in the waste gas pipe being conveyed to the preliminary carbonization reaction tower by means of a second conveying pipe; the ammonia gas pipe is connected to the preliminary carbonization reaction tower; an outlet at the bottom of the preliminary carbonization reaction tower is connected to a third conveying pipe, an outlet of the third conveying pipe being connected to the deep carbonization reaction tower. The system realizes a carbon-negative, green, and low-energy-consumption environmentally-friendly soda ash production process, and meets the industrial production requirement for green and sustainable development.

Description

System and method for producing alkali by using industrial waste gas and industrial waste brine TECHNICAL FIELD The present application relates to the technical field of soda ash production, in particular to a system and method for producing alkali by using industrial waste gas and industrial waste brine. BACKGROUND Water pollution and air pollution caused by industrial production are currently the environmental problems that the world pays attention to. The waste brine and waste gas discharged by factories not only pollute the natural environment, but also further cause waste of resources. The development of human society inevitably brings changes to the natural environment. The policies such as "green sustainable development concept", "carbon peak and carbon neutralization", and "community of shared future for mankind" proposed by the country also show the importance of environmental protection. In order to ensure efficient production, it is necessary to minimize the damage to the ecological environment system, which is the only development direction for technological upgrading and reform of the industrial system. The chemical principle of "Hou's alkali production method 1.0" mainly includes the following three chemical reaction steps: (1) NH3+H2O+CO2=NH4HCO3 (2) NH4HCO3+NaCl=NH4Cl+NaHCO3↓ (3) 2NaHCO3=Na2CO3+CO2↑+H2O (thermal decomposition) In the above three reaction steps, steps (1) and (2) are carried out in a carbonization reactor (commonly known as a carbonization tower), and step (3) is carried out in a calcination furnace. Compared with "Solvay alkali production method", "Hou's alkali production method 1.0" is to build and produce jointly by ammonia plant and alkali plant. The ammonia plant provides ammonia and carbon dioxide raw materials required for the reaction to the alkali plant. The reaction not only produces the precursor compound NaHCO3 of the target product Na2CO3, but also produces ammonium chloride which can be recycled as a chemical product or fertilizer, instead of a large amount of solid waste CaCl2 produced in the "Solvay alkali production method" process, thereby improving the atom economy and greatly improving the value of the production process. However, in the current Hou's joint alkali production process, the raw materials such as NH3, CO2 and NaCl used for producing soda ash need to be purchased. The raw materials for synthesizing ammonia mainly come from coal-based synthetic ammonia, and various energy sources used in the production process are mostly fossil energy, rather than renewable green energy. The raw material CO2 in "Hou's alkali production method 1.0" is high-concentration CO2 (concentration 85%-90%) obtained from the synthesis of ammonia gas and shift section, rather than low-concentration flue gas CO2 released in other production processes. The former is used in the production process of "Hou's alkali production method 1.0", and the overall carbon balance of the whole process is still a high-carbon production process. In addition, the characteristics of joint alkali production require that the alkali production plant be built near the synthetic ammonia plant, which increases the production cost. In addition, in the current chemical industry, such as petroleum cracking, coal-to-methanol, etc. Petroleum chemical industry and coal chemical industry, there are a large amount of CO2 in the exhaust gas discharged by the factory, and the gas composition is simple and easy to separate. These CO2 are directly discharged without recovery, which causes environmental problems and resource waste. And in the industries such as pharmaceutical factories, pesticide factories and fertilizer factories, the industrial waste brine discharged contains a high concentration of NaCl, and the sewage treatment technology used by many factories currently has high cost, and is directly discharged after reaching the standard, without any economic value. Therefore, the present application is proposed. SUMMARY The first object of the present application is to provide a system for producing alkali from industrial waste gas and industrial waste brine. The method uses industrial waste brine and industrial waste gas as raw materials for alkali production, which can realize negative carbon, green, low energy consumption and environmental protection. The alkali production process can effectively improve the reaction efficiency and utilization rate of raw materials and improve the alkali production efficiency by combining the mass transfer reactor in the alkali production process section (i.e. the preliminary carbonization reaction tower and the deep carbonization reaction tower). The second object of the present application is to provide a method for producing alkali from industrial waste gas and industrial waste brine. The method uses industrial waste brine and industrial waste gas as raw materials for alkali production, which has the characteristics of negative carbon, green, low energy consumption and environmental protection, low production cost and high raw material utilization rate. In order to achieve the above object of the present application, the following technical scheme is adopted: The present application provides a system for producing alkali from industrial waste gas and industrial waste brine, comprising: a waste liquid pipeline, a waste gas pipeline, an ammonia gas pipeline, a heat exchanger, an oxidation reaction tower, a dust removal tower, a preliminary carbonization reaction tower and a deep carbonization reaction tower. The outlet of the waste liquid pipeline is connected to the oxidation reaction tower, and the heat exchanger is arranged on the waste liquid pipeline. The industrial waste brine in the waste liquid pipeline undergoes wet oxidation reaction in the oxidation reaction tower to generate oxidation products, which are transported to the preliminary carbonization reaction tower through a first conveying pipeline; The waste gas pipeline is connected to the dust removal tower through the heat exchanger. The industrial waste gas in the waste gas pipeline is dedusted in the dust removal tower, and the dedusted product is transported to the preliminary carbonization reaction tower through a second conveying pipeline; The ammonia gas pipeline is connected to the preliminary carbonization reaction tower, and the bottom outlet of the preliminary carbonization reaction tower is connected to a third conveying pipeline, and the outlet of the third conveying pipeline is connected to the deep carbonization reaction tower; The first and second enhanced mass transfer reactors are arranged on opposite side walls of the deep carbonization reaction tower, and the outlets of the first and second enhanced mass transfer reactors face each other, and the first and second enhanced mass transfer reactors are connected with the second conveying pipeline; the dedusting product is dispersed and broken into micron-sized micro-bubbles by the first and second enhanced mass transfer reactors, and then reacts with the material conveyed by the third conveying pipeline to realize the production of alkali by the negative carbon production process. In the above scheme, the industrial waste brine in the waste liquid pipeline is subjected to real-time oxidation reaction in the oxidation reaction tower, and a high-concentration brine (i.e. oxidation product) can be obtained; by using the dedusting tower to dedust the industrial waste gas, a high-purity CO2 gas (i.e. dedusting product) can be obtained; the oxidation product, the dedusting product and the ammonia water can be sequentially reacted in the preliminary carbonization reaction tower and the deep carbonization reaction tower to produce NaHCO3. At the same time, by arranging the first and second enhanced mass transfer reactors, the first and second enhanced mass transfer reactors can be used to disperse and break the CO2 gas into micron-sized micro-bubbles to increase the gas-liquid mass transfer area; by making the outlets of the first and second enhanced mass transfer reactors face each other, the two streams of micro-bubbles can be used for counterflow to further disperse and break the two streams of micro-bubbles, which helps to further increase the gas-liquid mass transfer area. It can be understood that the concentration of CO2 in the dedusting product after purification of the industrial waste gas is usually low (concentration less than 70%), and the present scheme combines the alkali production process with the enhanced mass transfer technology, and specifically arranges the position of the enhanced mass transfer reactor, which can still ensure good alkali production efficiency when the concentration of CO2 gas is low. The alkali production scheme has the characteristics of negative carbon, green, low energy consumption and environmental protection, and meets the needs of green and sustainable industrial production. In addition, since the enhanced mass transfer technology is used to increase the phase boundary mass transfer area of the gas-liquid two phases, the requirement for the conveying pressure of the conveyed gas phase raw material can be reduced, i.e. the CO2 gas can be conveyed at low pressure, which helps to further reduce the production energy consumption. Preferably, the system further comprises a stirrer, the stirrer comprising a stirring motor, a stirring shaft and a stirring wing, the stirring motor being connected with the stirring shaft, the stirring wing being arranged at one end of the stirring shaft away from the stirring motor; the one end of the stirring shaft away from the stirring motor penetrates into the inside of the deep carbonization reaction tower through the deep carbonization reaction tower; the stirring wing is located above the first and second reinforced mass transfer reactors in the vertical direction, and the stirring wing is located in the middle of the first and second reinforced mass transfer reactors in the horizontal direction. By arranging the stirrer, the micro-bubbles can be uniformly distributed by stirring. Meanwhile, by arranging the stirring wing above the first and second reinforced mass transfer reactors in the vertical direction, the influence of the stirring wing on the collision of the two micro-bubble flows can be reduced, so that the gas-liquid mass transfer area can be further increased, and the raw material utilization rate can be increased. In addition, this arrangement can also reduce the influence of the stirring of the stirring wing on the products reacted at the bottom of the tower, avoid the production of product backmixing, and ensure the stable output of the tower bottom product. Preferably, a distribution pipe is arranged between the outlet of the first reinforced mass transfer reactor and the outlet of the second reinforced mass transfer reactor; and a plurality of distribution holes are arranged on the pipe wall of the distribution pipe close to the side of the stirring wing. In this scheme, the distribution pipe can provide a relatively independent space for the collision of the two micro-bubble flows, avoiding the influence of the stirring of the stirrer on the collision effect. Meanwhile, by arranging a plurality of distribution holes close to the side of the stirring wing, the micro-bubbles further broken after the collision can be sent into the vicinity of the stirring wing from the distribution holes, and uniformly dispersed under the stirring of the stirring wing, which helps to further avoid bubble coalescence and improve the uniform dispersion degree of the micro-bubbles. Preferably, a third reinforced mass transfer reactor is further arranged in the deep carbonization reaction tower, the third reinforced mass transfer reactor being arranged above the liquid level of the deep carbonization reaction tower; an extension pipe is connected to the outlet of the third reinforced mass transfer reactor, the extension pipe penetrating into the liquid level of the deep carbonization reaction tower, and the outlet of the extension pipe being located above the first and second reinforced mass transfer reactors; and the outlet of the third conveying pipeline is connected with the third reinforced mass transfer reactor. In this scheme, the material in the third conveying pipeline can suck the unreacted gas at the top of the tower into the third reinforced mass transfer reactor for further dispersion and breaking, and return to the tower for further reaction, which helps to further improve the raw material conversion rate. Preferably, the deep carbonization reaction tower is provided with a circulation pipeline, the inlet of the circulation pipeline is connected to the sidewall of the deep carbonization reaction tower, and the outlet is connected to the third intensified mass transfer reactor; the inlet of the circulation pipeline is located between the first intensified mass transfer reactor and the liquid surface of the deep carbonization reaction tower in the vertical direction. On the one hand, the circulation pipeline can stir the liquid in the deep carbonization reaction tower, improving the reaction efficiency; on the other hand, the inlet of the circulation pipeline is arranged between the first intensified mass transfer reactor and the liquid surface of the deep carbonization reaction tower in the vertical direction, which can reduce the influence of the stirring of the circulation pipeline on the product at the bottom of the tower that has been reacted, avoid the production of product backmixing, and ensure the stable output of the product at the bottom of the tower. At the same time, the circulating materials in the circulation pipeline can be input into the third intensified mass transfer reactor together with the materials in the third conveying pipeline, that is, two streams of materials provide the power of dispersion and fragmentation at the same time, which helps to improve the fragmentation degree of micro-bubbles and reduce the size of micro-bubbles, thereby further improving the phase interface mass transfer area. Preferably, the preliminary carbonization reaction tower is provided with a fourth intensified mass transfer reactor and a fifth intensified mass transfer reactor, the fourth intensified mass transfer reactor is arranged below the liquid surface in the preliminary carbonization reaction tower, the fifth intensified mass transfer reactor is arranged above the liquid surface in the preliminary carbonization reaction tower, the outlet of the fifth intensified mass transfer reactor is connected with a first connecting pipe, and the outlet of the first connecting pipe is connected with the fourth intensified mass transfer reactor; the first conveying pipeline is connected with the fifth intensified mass transfer reactor; the ammonia gas pipeline and the second conveying pipeline are connected with the fourth intensified mass transfer reactor. This scheme can disperse and fragment the ammonia gas and CO2 in the second conveying pipeline into micro-bubbles of micron level, thereby improving the phase interface mass transfer area, by arranging the fourth intensified mass transfer reactor; the fifth intensified mass transfer reactor arranged above can suck the unreacted gas at the top of the tower and send it back into the tower after dispersion and fragmentation to participate in the reaction again, which helps to improve the conversion rate of raw materials; in addition, the micro-bubbles fragmented by the fifth intensified mass transfer reactor are sent into the fourth intensified mass transfer reactor along the first connecting pipe, which can be further dispersed and fragmented by the fourth intensified mass transfer reactor, and the stream of materials can collide with the micro-bubbles fragmented by the fourth intensified mass transfer reactor, which also helps to improve the dispersion and fragmentation degree of micro-bubbles. At the same time, the arrangement of the first connecting pipe can also support the fifth intensified mass transfer reactor, improving the overall structural strength. Preferably, the preliminary carbonization reactor is provided with a back-mixing pipeline, an inlet of the back-mixing pipeline is connected to a side wall of the preliminary carbonization reactor, and an outlet is connected to the fifth mass transfer intensifier reactor, and the inlet of the back-mixing pipeline is located between the fourth mass transfer intensifier reactor and the liquid level of the preliminary carbonization reactor in the vertical direction. This scheme can stir the material in the tower by providing the back-mixing pipeline, thereby improving the reaction efficiency and the uniformity of the micro-bubbles. Meanwhile, the material in the back-mixing pipeline and the material in the first conveying pipeline are input into the fifth mass transfer intensifier reactor at the same time, that is, the two materials provide the power for dispersion and fragmentation at the same time, which helps to improve the fragmentation degree of the micro-bubbles and reduce the size of the micro-bubbles, thereby further improving the phase interface mass transfer area. Preferably, a plurality of layers of baffles are staggered in the preliminary carbonization reactor, and the baffles are located below the fourth mass transfer intensifier reactor. The product of the preliminary carbonization reactor is output from the bottom of the tower, and the staggered arrangement of the plurality of layers of baffles below the fourth mass transfer intensifier reactor helps to avoid back-mixing of the product, so that the product is stably and orderly input into the next reaction tower (i.e., the deep carbonization reactor). Preferably, the dust removal tower is provided with a sixth mass transfer intensifier reactor and a seventh mass transfer intensifier reactor, the sixth mass transfer intensifier reactor and the seventh mass transfer intensifier reactor are both arranged below the liquid level in the dust removal tower, and the sixth mass transfer intensifier reactor and the seventh mass transfer intensifier reactor are arranged on opposite side walls in the dust removal tower, respectively; the sixth mass transfer intensifier reactor and the seventh mass transfer intensifier reactor are both connected to the waste gas pipeline. In this scheme, by arranging the sixth mass transfer intensifier reactor and the seventh mass transfer intensifier reactor, the industrial waste gas can be dispersed and fragmented into micron-level micro-bubbles, thereby increasing the gas-liquid mass transfer area to improve the dust removal effect of the industrial waste gas; by arranging the sixth mass transfer intensifier reactor and the seventh mass transfer intensifier reactor on opposite side walls in the dust removal tower, respectively, the outlets of the two mass transfer intensifiers face each other, so that the micro-bubbles output by the two mass transfer intensifiers can collide with each other, thereby further dispersing and fragmenting. Preferably, the dust removal tower is provided with a sprayer, the sprayer is connected to a dust removal liquid pipeline; the sprayer is located above the liquid level in the dust removal tower in the vertical direction, and the sprayer is arranged between the sixth mass transfer intensifier reactor and the seventh mass transfer intensifier reactor in the horizontal direction. This scheme sends the dust removal liquid into the dust removal tower through the sprayer. This way can increase the dust removal efficiency, and by arranging the sprayer between the sixth mass transfer intensifier reactor and the seventh mass transfer intensifier reactor in the horizontal direction, the sprayed dust removal liquid is more concentrated between the sixth mass transfer intensifier reactor and the seventh mass transfer intensifier reactor, thereby further improving the dust removal efficiency. Preferably, an auxiliary dust collector is arranged in the dust removal tower, and is located between the sprayer and the sixth intensified mass transfer reactor in the vertical direction; the auxiliary dust collector is tapered in the vertical direction, and the opening at the bottom of the auxiliary dust collector is located between the sixth intensified mass transfer reactor and the seventh intensified mass transfer reactor in the horizontal direction. In this way, the auxiliary dust collector can limit the upward movement of the gas from the position between the sixth intensified mass transfer reactor and the seventh intensified mass transfer reactor, and since the sprayer is arranged between the sixth intensified mass transfer reactor and the seventh intensified mass transfer reactor in the horizontal direction, the newly added spray liquid is concentrated between the sixth intensified mass transfer reactor and the seventh intensified mass transfer reactor, and in this case, the gas rises along the position where the spray liquid is concentrated, thereby further improving the dust removal efficiency. Preferably, a rotating motor is arranged outside the dust removal tower, and a rotating shaft is connected to the rotating motor, penetrates through the wall of the dust removal tower and extends into the dust removal tower, and a rotating fan blade is connected to the end of the rotating shaft away from the rotating motor; the rotating fan blade is located below the sixth intensified mass transfer reactor in the vertical direction, and is located between the sixth intensified mass transfer reactor and the seventh intensified mass transfer reactor in the horizontal direction. In this way, the rotating fan blade can improve the uniformity of the distribution of the micro-bubbles, thereby further improving the interfacial mass transfer area between the gas and liquid phases, which can further improve the dust removal effect. Preferably, an eighth intensified mass transfer reactor and a ninth intensified mass transfer reactor are arranged in the oxidation reaction tower, and the eighth intensified mass transfer reactor and the ninth intensified mass transfer reactor are both located below the liquid level in the oxidation reaction tower in the vertical direction; the eighth intensified mass transfer reactor is located above the ninth intensified mass transfer reactor in the vertical direction, and the outlets of the eighth intensified mass transfer reactor and the ninth intensified mass transfer reactor are opposite to each other; the eighth intensified mass transfer reactor and the ninth intensified mass transfer reactor are both connected to an oxidation gas pipeline; preferably, the outlet of the eighth intensified mass transfer reactor is connected to the outlet of the ninth intensified mass transfer reactor through a second connecting pipe, and a plurality of through holes are arranged in the wall of the second connecting pipe. In this way, the eighth intensified mass transfer reactor and the ninth intensified mass transfer reactor can disperse and break the oxidation gas (which can be oxygen or air) into micro-bubbles of micron level, increase the interfacial mass transfer area between the micro-bubbles and the industrial waste brine, thereby improving the wet oxidation efficiency, and since the outlets of the two intensified mass transfer reactors are opposite to each other, the two streams of micro-bubbles can be used for collision to achieve further dispersion and breaking. In a further scheme, the second connecting pipe can provide a place for the collision of the two streams of micro-bubbles, and the micro-bubbles after the collision can be uniformly diffused into the liquid material in the oxidation reaction tower through the through holes in the second connecting pipe, which can further improve the wet oxidation efficiency. Preferably, the heat exchanger comprises an inner tube and an outer shell, the inner tube is arranged inside the outer shell, and a heat exchange cavity is formed between the inner tube and the outer shell; the waste liquid pipeline is connected with the oxidation reaction tower via the inner tube, and the waste gas pipeline is connected with the dust removal tower via the heat exchange cavity; a plurality of baffles are arranged in the inner tube along the material flow direction, and adjacent two baffles are arranged staggeredly. In this scheme, by arranging the baffles, the flow path of the industrial waste brine can be prolonged, thereby prolonging the heat exchange time of the industrial waste brine and the industrial waste gas, so as to heat the industrial waste brine by using the high temperature carried by the industrial waste gas, thereby facilitating the subsequent wet oxidation reaction. It can be understood that the reaction temperature of the wet oxidation reaction is generally about 250℃, and the temperature of the industrial waste gas after dust removal is usually below 100℃. This scheme helps to greatly reduce energy consumption and further save production cost by heat coupling the industrial waste brine and the industrial waste gas. Preferably, the baffle is inclined to the outlet end of the inner tube, and the included angle between the baffle and the inner tube wall is within the range of [30°, 50°]. This scheme can further prolong the flow path of the industrial waste brine by arranging the inclination angle of the baffle, thereby facilitating further improvement of the heat exchange performance. Preferably, a temperature insulation plate is arranged in the heat exchange cavity, the temperature insulation plate divides the heat exchange cavity into a first heat exchange cavity and a second heat exchange cavity along the material flow direction; the waste gas pipeline is connected with the dust removal tower via the first heat exchange cavity; and the first conveying pipeline is connected with the preliminary carbonization reaction tower via the second heat exchange cavity. In this scheme, the heat carried by the industrial waste gas and the oxidation product can be fully utilized to heat the industrial waste brine, which can further reduce the energy required for subsequent heating of the industrial waste brine. At the same time, in this scheme, the industrial waste brine is first heat coupled with the industrial waste gas, and then heat coupled with the oxidation product, because the temperature of the industrial waste gas itself is usually above 300℃, and the initial temperature of the industrial waste brine is relatively low, the temperature difference between the two is large, and the heat exchange efficiency is high, so the temperature of the industrial waste brine can be quickly raised, and the temperature of the industrial waste gas can be reduced. Then, by heat exchanging the oxidation product and the industrial waste brine, the industrial waste brine can be heated twice, so that the temperature of the industrial waste brine is closer to the temperature requirement of the wet oxidation reaction, so as to ensure the efficient performance of the subsequent reaction. In short, this kind of staged heating mode can further improve the heat exchange efficiency and reduce the energy consumption. In the above scheme of the present application, the industrial waste gas and the industrial waste brine are heat-exchanged and then enter the dust removal process section (i.e., the dust removal tower) and the wet oxidation process section (i.e., the oxidation reaction tower), respectively. This heat coupling mode helps to reduce energy consumption and save production cost. At the same time, in the dust removal process section, by combining the enhanced mass transfer technology with the spray dust removal process, and by specifically setting the positions of the enhanced mass transfer reactor, the sprayer and the auxiliary dust remover, the industrial dust removal efficiency can be improved, thereby improving the concentration of CO2 in the dust removal product and ensuring the orderly progress of the subsequent alkali production process. In the wet oxidation process section, by combining the enhanced mass transfer technology with the wet oxidation reaction, the wet oxidation efficiency can be improved, thereby improving the purification efficiency of the industrial waste brine and reducing the COD value of the industrial waste brine, so that it can participate in the subsequent alkali production process. In the alkali production process section, by setting two-stage carbonization reaction towers, the conversion rate of the reaction raw materials can be improved. By combining the enhanced mass transfer technology, the phase interface contact area between the gas-phase raw materials and the liquid-phase raw materials can be improved, so that good alkali production efficiency can be ensured even when the concentration of CO2 is low, that is, CO2 in the industrial waste gas can be used for alkali production, thereby realizing a negative carbon type of alkali production mode. This production mode has the advantages of green environmental protection and low energy consumption. In summary, the scheme of the present application utilizes CO2 in the industrial waste gas and NaCl in the industrial waste brine to realize a green synthesis process of soda ash, which helps to reduce production cost. The scheme not only does not cause environmental pollution itself, but also consumes waste gas and waste brine from other industries, which helps to reduce the cost of waste gas and waste brine treatment and realizes a negative carbon type of production mode. The present application recycles industrial waste materials and further converts them into valuable industrial chemicals, realizing the cyclic conversion of industrial production. Not only does it not consume pure CO2 gas, but it also further purifies and utilizes industrial waste materials, forms a negative carbon industrial chain, and perfectly matches the concept of green and sustainable development. The skilled in the art can understand that the intensifying mass transfer reactor adopted by the present application has been embodied in the prior patents of the present inventors, such as the patents with the application numbers CN201610641119.6, CN201610641251.7, CN201710766435.0, CN106187660A, CN105903425A, CN205833127U and CN207581700U. The specific product structure and working principle of the micron bubble generator (i.e. bubble breaker) are introduced in detail in the prior patent CN201610641119.6. It is recorded in the application file that “the micron bubble generator comprises a body and a secondary breaking piece, the body has a cavity, the body is provided with an inlet communicating with the cavity, the opposite first end and the second end of the cavity are open, and the cross-sectional area of the cavity decreases from the middle of the cavity to the first end and the second end of the cavity; the secondary breaking piece is arranged at least one of the first end and the second end of the cavity, a part of the secondary breaking piece is arranged in the cavity, and an annular channel is formed between the secondary breaking piece and the open through hole at the two ends of the cavity. The micron bubble generator further comprises a gas inlet pipe and a liquid inlet pipe.” From the specific structure disclosed in the application file, it can be known that the specific working principle is that the liquid enters the micron bubble generator through the liquid inlet pipe tangentially, rotates at a high speed and cuts the gas, so that the gas bubbles are broken into micron-sized micro-bubbles, thereby increasing the mass transfer area between the liquid phase and the gas phase, and the micron bubble generator in the patent belongs to a pneumatic bubble breaker. In addition, it is recorded in the prior patent 201610641251.7 that the primary bubble breaker has a circulating liquid inlet, a circulating gas inlet and a gas-liquid mixture outlet, and the secondary bubble breaker is communicated with the feed inlet and the gas-liquid mixture outlet, which indicates that the gas-liquid mixture needs to be mixed into the bubble breaker, and in addition, it can be known from the subsequent drawings that the circulating liquid is mainly used as the power in the primary bubble breaker, so the primary bubble breaker actually belongs to a liquid-driven intensifying reactor, and the secondary bubble breaker is used for simultaneously introducing the gas-liquid mixture into the rotating ball in an elliptical shape to rotate, so as to realize bubble breaking in the process of rotation, and therefore the secondary bubble breaker actually belongs to a gas-liquid linkage type bubble breaker. Actually, whether it is a liquid-driven bubble breaker or a gas-liquid linkage type bubble breaker, it belongs to a specific form of bubble breaker, however, the intensifying mass transfer reactor adopted by the present application is not limited to the above-mentioned several forms, and the specific structure of the bubble breaker recorded in the prior patents is only one of the forms that can be adopted by the present application. In addition, it is recorded in the prior patent 201710766435.0 that “the principle of the bubble breaker is to achieve mutual collision of gas by high-speed jet flow”; and the specific structure of the bubble breaker is also recorded in the prior patent CN106187660A, and the specific description is as follows:

[0031] -

[0041] The section and the part of the drawing, which are detailed in the specific working principle of the bubble breaker S-2, the top of the bubble breaker is a liquid phase inlet, and the side is a gas phase inlet, the entrainment power is provided by the liquid phase from the top, so as to achieve the effect of smashing into superfine bubbles, and it can be seen from the drawing that the bubble breaker is conical, the diameter of the upper part is larger than that of the lower part, and the liquid phase can provide better entrainment power. Because the bubble breaker was just developed at the initial stage of the prior patent application, it was named micron bubble generator (CN201610641119.6) in the early stage, and with continuous technical improvement, it was renamed as a bubble breaker in the later stage, and the reinforced mass transfer reactor in the present application is equivalent to the previous micron bubble generator, micro-interface generator, etc., only the name is different. In summary, The reinforced mass transfer reactor of the present application belongs to the prior art. The present application also provides a method for producing alkali by using industrial waste gas and industrial waste brine. Compared with the prior art, the present application has the following advantages: 1. The present application uses CO2 in industrial waste gas and NaCl in industrial waste brine to realize green synthesis process of soda ash, reduces production cost, does not cause environmental pollution itself, consumes waste gas and waste brine from other industries, reduces waste gas and waste brine treatment cost, and realizes negative carbon production mode. 2. The present application can use low concentration CO2 to prepare soda ash in a low pressure environment, and the production efficiency is high. The reaction system combines the reinforced mass transfer technology into the soda ash preparation process, effectively improves the reaction efficiency of raw materials and the utilization rate of carbon dioxide, and reduces the input pressure of carbon dioxide and energy consumption. 3. The reaction raw material of the present application is low carbon and environmentally friendly, the ammonia raw material can use green ammonia or blue ammonia, CO2 can use 70% or lower concentration CO2 as raw material, or mix the recovered CO2 with a concentration of 75-80% from the calcining furnace with low concentration CO2 from flue gas to form 50-75% CO2 as carbon source. In this way, the production process of the present application becomes a negative carbon production process, which reduces the production cost. BRIEF DESCRIPTION OF DRAWINGS Various other advantages and benefits will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are for purposes of illustration only and are not considered a limitation of the present application. Moreover, like reference numerals are used to designate like parts throughout the specification and drawings. In the drawings: Fig. 1 shows a schematic diagram of an alkali production system according to one embodiment of the present application; Fig. 2 shows a structural schematic diagram of a heat exchanger according to one embodiment of the present application; Figure 3 shows a structural schematic diagram of an oxidation reaction tower according to one embodiment of the present application; Figure 4 shows a structural schematic diagram of a dust removal tower according to one embodiment of the present application; Figure 5 shows a structural schematic diagram of an auxiliary dust remover according to one embodiment of the present application; Figure 6 shows a structural schematic diagram of a preliminary carbonization reaction tower according to one embodiment of the present application; Figure 7 shows a structural schematic diagram of a deep carbonization reaction tower according to one embodiment of the present application; Figure 8 shows a flow chart of an alkali production process according to one embodiment of the present application. In the figures: 1, waste liquid pipeline; 2, heat exchanger; 201, inner tube; 202, outer shell; 203, thermal insulation plate; 204, baffle; 3, waste gas pipeline; 4, heater; 5, oxidation reaction tower; 501, eighth enhanced mass transfer reactor; 502, second connecting pipe; 503, ninth enhanced mass transfer reactor; 504, emptying port; 6, oxidation gas pipeline; 7, first conveying pipeline; 8, dust removal tower; 801, rotary motor; 802, rotary shaft; 803, rotary fan blade; 804, sixth enhanced mass transfer reactor; 805, seventh enhanced mass transfer reactor; 806, auxiliary dust remover; 807, sprayer; 9, dust removal liquid pipeline; 10, second conveying pipeline; 11, fourth conveying pipeline; 12, preliminary carbonization reaction tower; 1201, fourth enhanced mass transfer reactor; 1202, first connecting pipe; 1203, fifth enhanced mass transfer reactor; 1204, gas collecting pipe; 1205, suction pump; 1206, back mixing pipeline; 1207, partition plate; 13, deep carbonization reaction tower; 1301, stirring motor; 1302, stirring shaft; 1303, third enhanced mass transfer reactor; 1304, extension pipe; 1305, stirring wing; 1306, first enhanced mass transfer reactor; 1307, distribution pipe; 1308, second enhanced mass transfer reactor; 1309, conveying pump; 1310, circulation pipeline; 14, third conveying pipeline; 15, filtration tower; 16, calcination tower; 17, mother liquor storage tank; 18, product conveyor; 19, calcination gas pipeline; 20, product conveying pipeline; 21, fifth conveying pipeline; 22, ammonia gas pipeline; 23, gas-liquid separator. DETAILED DESCRIPTION The technical solutions of the present application will be clearly and completely described below in combination with the drawings and specific embodiments, but those skilled in the art will understand that the following described embodiments are part of the embodiments of the present application, rather than all the embodiments, and are only used to illustrate the present application, and should not be regarded as limiting the scope of the present application. Based on the embodiments in the present application, all other embodiments obtained by those skilled in the art without creative labor are within the scope of protection of the present application. If the specific conditions are not specified in the embodiments, the conventional conditions or the conditions recommended by the manufacturer are used. If the manufacturers of the reagents or instruments used are not specified, they are all conventional products that can be purchased on the market. In the description of the present application, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer" and the like indicate the orientation or positional relationship based on the orientation or positional relationship shown in the drawings, and are only for the convenience of describing the present application and simplifying the description, and therefore cannot be understood as limiting the indicated device or element to have a specific orientation, to be constructed and operated in a specific orientation, and therefore cannot be understood as limiting the present application. In addition, the terms "first", "second", "third" are only for descriptive purposes and cannot be understood as indicating or implying relative importance. In the description of the present application, it should be noted that unless otherwise explicitly specified and limited, the terms "mounting", "connecting", "connecting" should be understood broadly, for example, it can be fixedly connected, or it can be detachably connected, or integrally connected; it can be mechanically connected, or it can be electrically connected; it can be directly connected, or it can be indirectly connected through an intermediate medium; it can be the communication inside two elements. For those skilled in the art, the specific meaning of the above terms in the present application can be understood according to the specific circumstances. Referring to FIGS. 1-7, the embodiment of the present application provides a system for producing alkali by using industrial waste gas and industrial waste brine, comprising: a waste liquid pipeline 1, a waste gas pipeline 3, an ammonia gas pipeline 22, a heat exchanger 2, an oxidation reaction tower 5, a dust removal tower 8, a preliminary carbonization reaction tower 12 and a deep carbonization reaction tower 13. The outlet of the waste liquid pipeline 1 is connected to the oxidation reaction tower 5, and the heat exchanger 2 is arranged on the waste liquid pipeline 1; the industrial waste brine in the waste liquid pipeline 1 is subjected to wet oxidation reaction in the oxidation reaction tower 5, and the generated oxidation product is transported to the preliminary carbonization reaction tower 12 through the first conveying pipeline 7. The waste gas pipeline 3 is connected to the dust removal tower 8 through the heat exchanger 2, and the industrial waste gas in the waste gas pipeline 3 is subjected to dust removal in the dust removal tower 8, and the obtained dust removal product is transported to the preliminary carbonization reaction tower 12 through the second conveying pipeline 10. The ammonia gas pipeline 22 is connected to the preliminary carbonization reaction tower 12, and the preliminary carbonization reaction tower 12 is connected with the deep carbonization reaction tower 13 through the third conveying pipeline 14 at the bottom outlet. The deep carbonization reaction tower 13 is provided with a first enhanced mass transfer reactor 1306 and a second enhanced mass transfer reactor 1308. The first enhanced mass transfer reactor 1306 and the second enhanced mass transfer reactor 1308 are respectively arranged on opposite side walls in the deep carbonization reaction tower 13, and the outlets of the first enhanced mass transfer reactor 1306 and the second enhanced mass transfer reactor 1308 are opposite to each other. The first enhanced mass transfer reactor 1306 and the second enhanced mass transfer reactor 1308 are connected with the second conveying pipeline 10. The dedusting product is broken into micron-sized micro-bubbles by the first enhanced mass transfer reactor 1306 and the second enhanced mass transfer reactor 1308, and then reacts with the material conveyed through the third conveying pipeline 14, so as to realize the production of alkali by the negative carbon production process. In the scheme of the embodiment, the main component of the industrial waste gas is CO2, which mainly comes from the industries of petroleum cracking, coal methanol production, coal ethanol production, thermal power plant and new energy battery production. The waste gas is subjected to a dedusting process section (i.e. the dedusting tower 8) to remove excess gas impurities (such as SO2, H2S, NO2, etc.), and separate to obtain CO2 gas with high purity. The mixed gas can contain inert gases such as N2 and He. Due to the use of the enhanced mass transfer technology, the low concentration of CO2 does not affect the production efficiency of the pure alkali in the alkali production process. In the scheme of the embodiment, the industrial waste gas can be subjected to pre-treatment and then enter the waste gas pipeline 3. The pre-treatment can adopt any existing or future developed dedusting process, which is not described in detail. In the embodiment, the industrial waste gas is subjected to pre-treatment and dedusting in the dedusting tower 8, which can further improve the purity of CO2 in the gas. In the scheme of the embodiment, the main component of the industrial waste salt water is NaCl, which mainly comes from the wastewater in any one of the industrial productions of petroleum chemical industry, natural gas exploitation, papermaking and pharmaceutical production. In some embodiments, the industrial waste salt water can be subjected to pre-treatment and then enter the waste liquid pipeline 1. Specifically, the industrial waste salt water can be subjected to pre-treatment to reduce the COD value, and then subjected to the oxidation reaction tower 5 to remove trace organic waste that is difficult to oxidize, so as to reduce the COD value to less than 10 mg / L, thereby obtaining a raw material liquid (i.e. oxidation product) mainly containing inorganic salt NaCl. Referring to FIG. 1, the waste liquid pipeline 1 can also be provided with a heater 4. The heater 4 is arranged behind the heat exchanger 2 along the material flow direction, so as to further heat the industrial waste salt water after heat exchange, so that it can meet the reaction temperature requirement of the wet oxidation reaction. In some embodiments, the oxidation product can be separated. In the embodiment shown in Fig. 1, the system further comprises a gas-liquid separator 23. The oxidation product in the first conveying pipeline 7, after heat exchange with the industrial waste brine in the heat exchanger 2, enters the gas-liquid separator 23, and the liquid phase (mainly containing inorganic salt NaCl) therein is conveyed to the preliminary carbonization reaction tower 12, and the gas phase (mainly including unreacted oxygen) can be directly discharged into the air or conveyed to the oxidation reaction tower 5 via an air compressor to continue to participate in the wet oxidation of the industrial waste brine. It can be understood that, in this embodiment, the first conveying pipeline 7 can be regarded as comprising three pipeline sections, i.e., a first pipeline section between the outlet of the oxidation reaction tower 5 and the heat exchanger 2, a second pipeline section between the heat exchanger 2 and the gas-liquid separator 23, and a third pipeline section between the liquid phase outlet of the gas-liquid separator and the preliminary carbonization reaction tower 12. As shown in Fig. 2, the heat exchanger 2 comprises an inner tube 201 and an outer shell 202, the inner tube 201 is arranged inside the outer shell 202, and a heat exchange cavity is formed between the inner tube 201 and the outer shell 202; the waste liquid pipeline 1 is connected with the oxidation reaction tower 5 via the inner tube 201, and the waste gas pipeline 3 is connected with the dust removal tower 8 via the heat exchange cavity; a plurality of baffles 204 are arranged in the inner tube 201 along the material flow direction, and adjacent two baffles 204 are arranged staggered. Continuing to refer to Fig. 2, the baffles 204 are inclined to the outlet end of the inner tube 201, and the included angle between the baffle 204 and the tube wall of the inner tube 201 is within the range of [30°, 50°]. Continuing to refer to Fig. 2, a heat insulation plate 203 is arranged in the heat exchange cavity, the heat insulation plate 203 divides the heat exchange cavity into a first heat exchange cavity and a second heat exchange cavity along the material flow direction; the waste gas pipeline 3 is connected with the dust removal tower 8 via the first heat exchange cavity; and the first conveying pipeline 7 is connected with the preliminary carbonization reaction tower 12 via the second heat exchange cavity. As shown in Fig. 3, the oxidation reaction tower 5 is provided with an eighth enhanced mass transfer reactor 501 and a ninth enhanced mass transfer reactor 503, and the eighth enhanced mass transfer reactor 501 and the ninth enhanced mass transfer reactor 503 are both located below the liquid level in the oxidation reaction tower 5 along the vertical direction; the eighth enhanced mass transfer reactor 501 is located above the ninth enhanced mass transfer reactor 503 along the vertical direction, and the outlets of the eighth enhanced mass transfer reactor 501 and the ninth enhanced mass transfer reactor 503 are opposite to each other; and the eighth enhanced mass transfer reactor 501 and the ninth enhanced mass transfer reactor 503 are both connected with the oxidation gas pipeline 6. Continuing to refer to Fig. 3, the outlet of the eighth enhanced mass transfer reactor 501 is connected with the outlet of the ninth enhanced mass transfer reactor 503 via a second connecting pipe 502; and a plurality of through holes are arranged on the pipe wall of the second connecting pipe 502. Continuing to refer to Fig. 3, the bottom of the oxidation reaction tower 5 can be provided with a discharge port 504. The method for treating industrial waste brine by using the oxidation reaction tower 5 can be referred to as a micro-interface wet oxidation process. As shown in FIG. 4, the dust removal tower 8 is provided with a sixth enhanced mass transfer reactor 804 and a seventh enhanced mass transfer reactor 805, both of which are arranged below the liquid level in the dust removal tower 8 and are arranged on opposite side walls of the dust removal tower 8, respectively; the sixth enhanced mass transfer reactor 804 and the seventh enhanced mass transfer reactor 805 are connected with the waste gas pipeline 3. Continuing to refer to FIG. 4, the dust removal tower 8 is provided with a sprayer 807, which is connected with a dust removal liquid pipeline 9; the sprayer 807 is located above the liquid level in the dust removal tower 8 in the vertical direction, and is arranged between the sixth enhanced mass transfer reactor 804 and the seventh enhanced mass transfer reactor 805 in the horizontal direction. The dust removal liquid in the dust removal liquid pipeline 9 can be water. In combination with FIGS. 4-5, the dust removal tower 8 is further provided with an auxiliary dust remover 806, which is located between the sprayer 807 and the sixth enhanced mass transfer reactor 804 in the vertical direction; the auxiliary dust remover 806 is tapered in the vertical direction, gradually decreasing from top to bottom, and the opening at the bottom of the auxiliary dust remover 806 is located between the sixth enhanced mass transfer reactor 804 and the seventh enhanced mass transfer reactor 805 in the horizontal direction. As shown in FIG. 4, the dust removal tower 8 is provided with a rotary motor 801, which is connected with a rotary shaft 802 that penetrates the tower wall of the dust removal tower 8 and extends into the interior of the dust removal tower 8, and the end of the rotary shaft 802 away from the rotary motor 801 is connected with a rotary fan blade 803; the rotary fan blade 803 is located below the sixth enhanced mass transfer reactor 804 in the vertical direction, and is located between the sixth enhanced mass transfer reactor 804 and the seventh enhanced mass transfer reactor 805 in the horizontal direction. The dust removal process in the above embodiment can be referred to as a micro-interface purification and separation process. As shown in FIG. 6, the preliminary carbonization reaction tower 12 is provided with a fourth enhanced mass transfer reactor 1201 and a fifth enhanced mass transfer reactor 1203, the fourth enhanced mass transfer reactor 1201 is arranged below the liquid level in the preliminary carbonization reaction tower 12, and the fifth enhanced mass transfer reactor 1203 is arranged above the liquid level in the preliminary carbonization reaction tower 12; the outlet of the fifth enhanced mass transfer reactor 1203 is connected with a first connecting pipe 1202, and the outlet of the first connecting pipe 1202 is connected with the fourth enhanced mass transfer reactor 1201; the first conveying pipeline 7 is connected with the fifth enhanced mass transfer reactor 1203; the ammonia gas pipeline 22 and the second conveying pipeline 10 are both connected with the fourth enhanced mass transfer reactor 1201. Continuing to refer to FIG. 6, a gas collecting pipe 1204 can be arranged on the fifth intensified mass transfer reactor 1203 to facilitate the entrainment of the overhead gas into the fifth intensified mass transfer reactor 1203. Continuing to refer to FIG. 6, the preliminary carbonization reaction tower 12 is provided with a back-mixing pipe 1206 on one side, the inlet of the back-mixing pipe 1206 is connected to the sidewall of the preliminary carbonization reaction tower 12, and the outlet is connected to the fifth intensified mass transfer reactor 1203. The inlet of the back-mixing pipe 1206 is located between the fourth intensified mass transfer reactor 1201 and the liquid level of the preliminary carbonization reaction tower 12 in the vertical direction. In FIG. 6, a suction pump 1205 can be arranged on the back-mixing pipe 1206 to provide power for the flow of the material in the back-mixing pipe 1206. It should be understood that a pump can be arranged on each pipe in the present scheme to facilitate the flow of the material and meet the delivery pressure requirements of the corresponding material. The specific arrangement mode can be selected according to actual needs, and will not be described here. Continuing to refer to FIG. 6, a plurality of layers of baffles 1207 are arranged staggered in the preliminary carbonization reaction tower 12, and the baffles 1207 are located below the fourth intensified mass transfer reactor 1201. As shown in FIG. 7, the system further comprises a stirrer, the stirrer comprising a stirring motor 1301, a stirring shaft 1302, and stirring wings 1305, the stirring motor 1301 being connected to the stirring shaft 1302, and the stirring wings 1305 being arranged at the end of the stirring shaft 1302 away from the stirring motor 1301; the end of the stirring shaft 1302 away from the stirring motor 1301 penetrates into the deep carbonization reaction tower 13; the stirring wings 1305 are located above the first intensified mass transfer reactor 1306 and the second intensified mass transfer reactor 1308 in the vertical direction, and the stirring wings 1305 are located in the middle of the first intensified mass transfer reactor 1306 and the second intensified mass transfer reactor 1308 in the horizontal direction. Continuing to refer to FIG. 7, a distribution pipe 1307 is arranged between the outlet of the first intensified mass transfer reactor 1306 and the outlet of the second intensified mass transfer reactor 1308; a plurality of distribution holes are arranged on the pipe wall near the side of the distribution pipe 1307 close to the stirring wings 1305. Continuing to refer to FIG. 7, a third intensified mass transfer reactor 1303 is further arranged in the deep carbonization reaction tower 13, and the third intensified mass transfer reactor 1303 is arranged above the liquid level of the deep carbonization reaction tower 13; the outlet of the third intensified mass transfer reactor 1303 is connected to an extension pipe 1304, the extension pipe 1304 penetrates into the liquid level of the deep carbonization reaction tower 13, and the outlet of the extension pipe 1304 is located above the first intensified mass transfer reactor 1306 and the second intensified mass transfer reactor 1308; the outlet of the third delivery pipe 14 is connected to the third intensified mass transfer reactor 1303. Continuing to refer to FIG. 7, the deep carbonation reaction tower 13 is provided with a circulation pipeline 1310, the inlet of the circulation pipeline 1310 is connected to the sidewall of the deep carbonation reaction tower 13, and the outlet is connected to the third enhanced mass transfer reactor 1303; the inlet of the circulation pipeline 1310 is located between the first enhanced mass transfer reactor 1306 and the liquid level of the deep carbonation reaction tower 13 in the vertical direction. In this embodiment, a delivery pump 1309 is arranged on the circulation pipeline 1310, and a tail gas outlet can be arranged at the top of the deep carbonation reaction tower 13. The method for preparing soda ash by using the initial carbonation reaction tower and the deep carbonation reaction tower 13 in this embodiment can be referred to as "Hou's 2.0" soda ash production process. As shown in FIG. 1, the system can further include a fourth delivery pipeline 11 for delivering high-concentration CO2. In this scheme, low-concentration CO2 obtained from industrial waste gas can be purified by using high-concentration CO2 and mixed into the subsequent soda ash production process, which helps to further improve the soda ash production efficiency. In the scheme of this embodiment, the delivery pressure of CO2 can be 0.03-0.18 MPa. In the related art, the delivery pressure of CO2 in "Hou's Soda Ash Production Method 1.0" is usually 0.45 MPa, and the delivery pressure of CO2 in this embodiment is only 0.03-0.18 MPa, thereby helping to reduce the energy consumption of soda ash production. As shown in FIG. 1, the system further includes a filter tower 15, a calcination tower 16, a mother liquor tank 17, and a product delivery machine 18. The deep carbonation reaction tower 13 is connected with a fifth delivery pipeline 21, the outlet of the fifth delivery pipeline 21 is connected to the filter tower 15, the solid-phase product outlet of the filter tower 15 is connected to the calcination tower 16, and the liquid-phase product outlet is connected to the mother liquor tank 17. The product of the deep carbonation reaction tower 13 is filtered in the filter tower 15, the liquid is introduced into the mother liquor tank 17, and then the traditional separation is used to obtain the ammonium chloride product (specifically, sodium chloride is added to the mother liquor to precipitate ammonium chloride, and the remaining sodium chloride solution can be reused as a reaction raw material); the filter residue is introduced into the calcination tower 16, the sodium bicarbonate therein is decomposed by heat to obtain soda ash, and the soda ash is output from the product delivery pipeline 20 under the driving of the product delivery machine 18 arranged on the product delivery pipeline 20. The calcination tower 16 can be connected with a calcination gas pipeline 19, which can be used to provide high-temperature gas to the calcination tower 16. The embodiment also provides a method for producing soda ash by using industrial waste gas and industrial waste brine, which can use the system of any of the above embodiments to produce soda ash. Figure 8 shows a flow chart of a process for producing caustic soda according to one embodiment of the present application. As shown in Figure 8, after the industrial waste brine is pretreated and further removed of COD by the micro-interface wet oxidation process, the NaCl obtained after separation and filtration is sent to the process section of the Hou 2.0 caustic soda production process. After the industrial waste gas is pretreated and purified by the micro-interface purification separation process, a gas with high purity of CO2 is obtained, which is sent to the process section of the Hou 2.0 caustic soda production process. At the same time, ammonia gas and CO2 from the synthetic ammonia plant can be sent to the process section of the Hou 2.0 caustic soda production process. The above raw materials are subjected to the Hou 2.0 caustic soda production process to obtain pure caustic soda Na2CO3. In order to more clearly illustrate the technical solutions in the present application, the following will be described in the form of specific embodiments. Embodiment 1 In this embodiment, the system shown in Figure 1 is used to produce pure caustic soda. Embodiment 2 The difference between this embodiment and Embodiment 1 is that the stirring wing 1305 in the deep carbonation reaction tower is located below the first mass transfer intensifier reactor 1306. Embodiment 3 The difference between this embodiment and Embodiment 1 is that the distribution holes on the distribution pipe 1307 are located on the pipe wall away from the stirring wing 1305. Embodiment 4 The difference between this embodiment and Embodiment 1 is that the outlet of the extension pipe 1304 is located below the first mass transfer intensifier reactor. Embodiment 5 The difference between this embodiment and Embodiment 1 is that the partition plate 1207 is located above the fourth mass transfer intensifier reactor 1201. Experimental Example 1 The same industrial waste gas, industrial waste brine and ammonia gas are respectively introduced into the systems of Embodiments 1-5, and pure caustic soda is produced using the systems of Embodiments 1-5. The pure caustic soda yield in the product output by the product delivery pipeline, the purity, and the CO2 concentration in the tail gas discharged from the top of the deep carbonation reaction tower are tested, and the test results are as follows. Table 1 Test Results As shown in the above table, it can be seen that when the system of the present application is used to produce pure caustic soda from industrial waste gas and industrial waste brine, it can ensure a high yield and purity of pure caustic soda, and the CO2 conversion rate is high. Comparing Embodiment 1 with Embodiment 2, it can be found that the pure caustic soda yield in Embodiment 2 is lower and the CO2 concentration in the tail gas is higher. This may be due to the different positions of the stirring wings. Specifically, it may be due to the stirring wing being located lower, causing the product to backmix when stirring, affecting the stable output of the product. Comparing Example 1 with Example 3, it can be found that the soda yield in Example 3 is lower and the CO2 concentration in the tail gas is higher. This can be caused by the difference in the position of the distribution hole. Specifically, the scheme of Example 1 has the distribution hole located on the tube wall close to the side of the stirring wing, and the output micro-bubbles are directly dispersed into the liquid phase material in the tower by stirring with the stirring wing, so the distribution is more uniform, and thus the soda yield and the CO2 conversion rate are higher. Comparing Example 1 with Example 4, it can be found that the soda yield in Example 4 is lower and the CO2 concentration in the tail gas is higher. This can be caused by the fact that the material in the extension tube is directly transported to the lower side of the first enhanced mass transfer reactor, which on one hand causes the back mixing of part of the product due to the impact on the tower bottom product. On the other hand, the micro-bubbles directly input to the lower side can be coalesced, reducing the phase interface mass transfer area. Comparing Example 1 with Example 5, it can be found that the soda yield in Example 5 is lower and the CO2 concentration in the tail gas is higher. This can be caused by the fact that the partition plate located on the upper side affects the reaction of the raw material between the two enhanced mass transfer reactors, resulting in a decrease in the raw material conversion rate and the soda yield. In summary, it can be seen that the scheme of Example 1 improves the raw material conversion rate and the soda yield by specifically setting the positions of the first enhanced mass transfer reactor, the second enhanced mass transfer reactor, the extension tube, the stirring wing and the distribution tube. Based on this, Example 1 is a preferred embodiment of the present application. Experimental Example 2 The oxidation product and the dedusting product in Example 1 were collected, and the COD content in the oxidation product and the CO2 content in the dedusting product were detected. The results are shown in the following table: Table 2 detection results As shown in the above table, it can be seen that the present application can effectively reduce the COD concentration in the industrial waste brine, and can effectively increase the CO2 content in the industrial waste gas. Finally, it should be noted that: the above examples are only used to illustrate the technical solutions of the present application, and not to limit them; although the present application has been described in detail with reference to the foregoing examples, those skilled in the art should understand that they can still modify the technical solutions recorded in the foregoing examples, or make equivalent replacement for part or all of the technical features; and these modifications or replacements do not make the essence of the corresponding technical solutions deviate from the scope of the technical solutions of the embodiments of the present application.

Claims

1. A system for producing alkali using industrial waste gas and industrial waste brine, characterized by, The application relates to a negative-carbon production process and device. The waste liquid pipeline, the waste gas pipeline, the ammonia gas pipeline, the heat exchanger, the oxidation reaction tower, the dust removal tower, the preliminary carbonization reaction tower and the deep carbonization reaction tower are connected; the outlet of the waste liquid pipeline is connected with the oxidation reaction tower, the heat exchanger is arranged on the waste liquid pipeline; the industrial waste brine in the waste liquid pipeline is subjected to a wet oxidation reaction in the oxidation reaction tower, and the generated oxidation product is transported to the preliminary carbonization reaction tower through a first conveying pipeline; the waste gas pipeline is connected with the dust removal tower through the heat exchanger; after the industrial waste gas in the waste gas pipeline is subjected to dust removal in the dust removal tower, the obtained dust removal product is transported to the preliminary carbonization reaction tower through a second conveying pipeline; the ammonia gas pipeline is connected with the preliminary carbonization reaction tower; the bottom outlet of the preliminary carbonization reaction tower is connected with a third conveying pipeline; the outlet of the third conveying pipeline is connected with the deep carbonization reaction tower; the first reinforced mass transfer reactor and the second reinforced mass transfer reactor are arranged in the deep carbonization reaction tower; the first reinforced mass transfer reactor and the second reinforced mass transfer reactor are arranged on opposite side walls in the deep carbonization reaction tower respectively, and the outlets of the first reinforced mass transfer reactor and the second reinforced mass transfer reactor are opposite to each other; the first reinforced mass transfer reactor and the second reinforced mass transfer reactor are connected with the second conveying pipeline; the dust removal product is broken into micron-level micro-bubbles through the first reinforced mass transfer reactor and the second reinforced mass transfer reactor, and then reacts with the material transported through the third conveying pipeline, so that the negative-carbon production process is used to produce alkali. The device further comprises a stirrer, the stirrer comprises a stirring motor, a stirring shaft and a stirring wing, the stirring motor is connected with the stirring shaft, and the stirring wing is arranged at one end of the stirring shaft away from the stirring motor; the one end of the stirring shaft away from the stirring motor penetrates into the inside of the deep carbonization reaction tower through the deep carbonization reaction tower; the stirring wing is located above the first reinforced mass transfer reactor and the second reinforced mass transfer reactor in the vertical direction, and the stirring wing is located in the middle of the first reinforced mass transfer reactor and the second reinforced mass transfer reactor in the horizontal direction. A distribution pipe is arranged between the outlet of the first reinforced mass transfer reactor and the outlet of the second reinforced mass transfer reactor; a plurality of distribution holes are arranged on the pipe wall of the distribution pipe close to the stirring wing. A third reinforced mass transfer reactor is further arranged in the deep carbonization reaction tower; the third reinforced mass transfer reactor is arranged above the liquid surface of the deep carbonization reaction tower; the outlet of the third reinforced mass transfer reactor is connected with an extension pipe; the extension pipe penetrates into the liquid surface of the deep carbonization reaction tower, and the outlet of the extension pipe is located above the first reinforced mass transfer reactor and the second reinforced mass transfer reactor; the outlet of the third conveying pipeline is connected with the third reinforced mass transfer reactor. ​ 2. The system of claim 1, wherein, ​ 3. The system of claim 2, wherein, ​ 4. The system of claim 3, wherein, ​ Preferably, the deep carbonization reactor is provided with a circulation pipeline, the inlet of the circulation pipeline is connected to the sidewall of the deep carbonization reactor, and the outlet is connected to the third enhanced mass transfer reactor; the inlet of the circulation pipeline is located between the first enhanced mass transfer reactor and the liquid level of the deep carbonization reactor in the vertical direction.

5. The system of claim 1, wherein, The preliminary carbonization reactor is provided with a fourth enhanced mass transfer reactor and a fifth enhanced mass transfer reactor, the fourth enhanced mass transfer reactor is arranged below the liquid level in the preliminary carbonization reactor, the fifth enhanced mass transfer reactor is arranged above the liquid level in the preliminary carbonization reactor, the outlet of the fifth enhanced mass transfer reactor is connected to a first connecting pipe, the outlet of the first connecting pipe is connected to the fourth enhanced mass transfer reactor; the first conveying pipeline is connected to the fifth enhanced mass transfer reactor; the ammonia gas pipeline and the second conveying pipeline are connected to the fourth enhanced mass transfer reactor; Preferably, the preliminary carbonization reactor is provided with a back mixing pipeline, the inlet of the back mixing pipeline is connected to the sidewall of the preliminary carbonization reactor, and the outlet is connected to the fifth enhanced mass transfer reactor; the inlet of the back mixing pipeline is located between the fourth enhanced mass transfer reactor and the liquid level of the preliminary carbonization reactor in the vertical direction. Preferably, the preliminary carbonization reactor is provided with a back mixing pipeline, the inlet of the back mixing pipeline is connected to the sidewall of the preliminary carbonization reactor, and the outlet is connected to the fifth enhanced mass transfer reactor; the inlet of the back mixing pipeline is located between the fourth enhanced mass transfer reactor and the liquid level of the preliminary carbonization reactor in the vertical direction.

6. The system of claim 1, wherein, The preliminary carbonization reactor is provided with a plurality of layers of baffles arranged alternately, and the baffles are arranged below the fourth enhanced mass transfer reactor. The dust removal tower is provided with a sixth enhanced mass transfer reactor and a seventh enhanced mass transfer reactor, both of which are arranged below the liquid level in the dust removal tower, and the sixth enhanced mass transfer reactor and the seventh enhanced mass transfer reactor are arranged on opposite sidewalls in the dust removal tower, respectively; both the sixth enhanced mass transfer reactor and the seventh enhanced mass transfer reactor are connected to the waste gas pipeline; 7. The system of claim 6, wherein, Preferably, the dust removal tower is provided with a sprayer, and the sprayer is connected to a dust removal liquid pipeline; the sprayer is located above the liquid level in the dust removal tower in the vertical direction, and the sprayer is arranged between the sixth enhanced mass transfer reactor and the seventh enhanced mass transfer reactor in the horizontal direction. The dust removal tower is also provided with an auxiliary dust remover, which is located between the sprayer and the sixth enhanced mass transfer reactor in the vertical direction; the auxiliary dust remover is conical and gradually decreases from top to bottom in the vertical direction, and the opening at the bottom of the auxiliary dust remover is located between the sixth enhanced mass transfer reactor and the seventh enhanced mass transfer reactor in the horizontal direction; Preferably, the dust removal tower is provided with a rotating motor outside, the rotating motor is connected to a rotating shaft, the rotating shaft penetrates through the tower wall of the dust removal tower and extends into the interior of the dust removal tower, and the end of the rotating shaft away from the rotating motor is connected to a rotating fan blade; the rotating fan blade is located below the sixth enhanced mass transfer reactor in the vertical direction, and the rotating fan blade is located between the sixth enhanced mass transfer reactor and the seventh enhanced mass transfer reactor in the horizontal direction.

8. The system of claim 1, wherein, The oxidation reaction tower is provided with an eighth intensified mass transfer reactor and a ninth intensified mass transfer reactor, the eighth intensified mass transfer reactor and the ninth intensified mass transfer reactor are located below the liquid level in the oxidation reaction tower in the vertical direction; the eighth intensified mass transfer reactor is located above the ninth intensified mass transfer reactor in the vertical direction, and the eighth intensified mass transfer reactor and the ninth intensified mass transfer reactor are opposite to each other at the outlets; The eighth intensified mass transfer reactor and the ninth intensified mass transfer reactor are connected with an oxidation gas pipeline; Preferably, the outlet of the eighth intensified mass transfer reactor is connected with the outlet of the ninth intensified mass transfer reactor through a second connecting pipe, and a plurality of through holes are arranged on the wall of the second connecting pipe.

9. The system according to any of claims 1-8, characterized in that, The heat exchanger comprises an inner tube and an outer shell, the inner tube is arranged inside the outer shell, and a heat exchange cavity is formed between the inner tube and the outer shell; the waste liquid pipeline is connected with the oxidation reaction tower via the inner tube, and the waste gas pipeline is connected with the dust removal tower via the heat exchange cavity; a plurality of baffles are arranged in the inner tube along the material flow direction, and adjacent two baffles are arranged staggered; Preferably, the baffle is inclined to the outlet end of the inner tube, and the included angle between the baffle and the wall of the inner tube is in the range of [30°, 50°]; Preferably, a temperature insulation plate is arranged in the heat exchange cavity, the temperature insulation plate divides the heat exchange cavity into a first heat exchange cavity and a second heat exchange cavity along the material flow direction; the waste gas pipeline is connected with the dust removal tower via the first heat exchange cavity; and the first conveying pipeline is connected with the preliminary carbonization reaction tower via the second heat exchange cavity.

10. A method for producing alkali using industrial waste gas and industrial waste brine, characterized by, The system is applied to produce alkali.

Images