System for preparing alkali by using industrial waste gas and industrial waste brine

Abstract

The utility model provides a system for preparing alkali by utilizing industrial waste gas and industrial waste brine. The system comprises a waste liquid pipeline, a waste gas pipeline, an ammonia gas pipeline, a heat exchanger, an oxidation reaction tower, a dust removal tower, a primary carbonization reaction tower and a deep carbonization reaction tower, the outlet of the waste liquid pipeline is connected with the oxidation reaction tower; an oxidation product generated by the waste liquid pipeline is conveyed into the primary carbonization reaction tower through a first conveying pipeline; the waste gas pipeline is connected with the dust removal tower through the heat exchanger, and a dust removal product obtained in the waste gas pipeline is conveyed into the primary carbonization reaction tower through a second conveying pipeline; the ammonia gas pipeline is connected with the primary carbonization reaction tower, a bottom outlet of the primary carbonization reaction tower is connected with a third conveying pipeline, and an outlet of the third conveying pipeline is connected with the deep carbonization reaction tower. According to the system, a negative carbon type, green and low-energy-consumption environment-friendly alkali production process is realized, and the industrial production requirements of green and sustainable development are met.

Description

Technical Field

[0001] The utility model relates to the technical field of soda ash preparation, and in particular, to a system for producing alkali by using industrial waste gas and industrial waste brine. Background Art

[0002] The chemical principle of "Hou's Soda-making Method 1.0" mainly includes the following three chemical reaction steps:

[0003] (1) NH3 + H2O + CO2 = NH4HCO3

[0004] (2) NH4HCO3 + NaCl = NH4Cl + NaHCO3↓

[0005] (3) 2NaHCO3 = Na2CO3 + CO2↑ + H2O (thermal decomposition)

[0006] In the above three reaction steps, the first two reaction steps (1) and (2) are carried out in a carbonation reactor (commonly known as a carbonation tower), while step (3) is carried out in a calciner. Compared with the "Solvay Soda-making Method", "Hou's Soda-making Method 1.0" combines and co-produces an ammonia plant and a soda plant. The ammonia plant provides the ammonia and carbon dioxide raw materials required for the reaction to the soda 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, rather than the large amount of solid waste CaCl2 produced in the "Solvay Soda-making Method" process. Therefore, the atom economy is improved and the value of the production process is greatly enhanced.

[0007] However, in the current Hou's combined soda-making process, raw materials such as NH3, CO2, and NaCl used for producing soda ash need to be purchased. The synthetic ammonia raw materials mainly come from coal-based synthetic ammonia, and most of the various energies used in its production process are also fossil energies, rather than renewable green energies. The raw material CO2 in "Hou's Soda-making Method 1.0" comes from the high-concentration CO2 (concentration 85%-90%) obtained from the synthetic ammonia gas-making and conversion sections, rather than the low-concentration flue gas CO2 released from other production processes. When the former is used in the production process of "Hou's Soda-making Method 1.0", the overall carbon balance of the whole process is still a high-carbon production process. Moreover, the characteristics of combined soda-making also require that the soda-making factory needs to be built near the synthetic ammonia plant, which increases the production cost.

[0008] In addition, in the current chemical industry, in petrochemical and coal chemical industries such as petroleum cracking and coal-to-methanol, a large amount of CO2 exists in the waste gas discharged from factories, and the gas composition is simple, which is convenient for separation. These CO2 are directly discharged without being recovered, causing environmental problems and wasting resources. In industries such as pharmaceutical factories, pesticide factories, and fertilizer factories, the industrial waste salt water discharged contains a high concentration of NaCl, and the current sewage treatment technologies used by many factories are costly. After reaching the standard, they are directly discharged without generating any economic value.

[0009] In view of this, the present utility model is specifically proposed. Summary of the Utility Model

[0010] The first object of the present utility model is to provide a system for producing alkali by using industrial waste gas and industrial waste salt water. This method uses industrial waste salt water and industrial waste gas as reaction raw materials to produce alkali, which can realize a negative-carbon, green, and low-energy-consumption environmental protection alkali production process. At the same time, by combining a mass transfer intensifier in the alkali production process section (i.e., the preliminary carbonation reaction tower and the deep carbonation reaction tower), the reaction efficiency and utilization rate of the raw materials can be effectively improved, and the alkali production efficiency can be increased.

[0011] The second object of the present utility model is to provide a method for producing alkali by using industrial waste gas and industrial waste salt water. This method uses industrial waste salt water and industrial waste gas as reaction raw materials to produce alkali, which has the characteristics of negative carbon, green, low energy consumption, and environmental protection, with low production costs and high raw material utilization rates.

[0012] In order to achieve the above objects of the present utility model, the following technical solutions are specifically adopted:

[0013] The present utility model provides a system for producing alkali by using industrial waste gas and industrial waste salt water, including: a waste liquid pipeline, a waste gas pipeline, an ammonia pipeline, a heat exchanger, an oxidation reaction tower, a dust removal tower, a preliminary carbonation reaction tower, and a deep carbonation reaction tower;

[0014] 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 salt water in the waste liquid pipeline undergoes a wet oxidation reaction in the oxidation reaction tower, and the generated oxidation product is transported to the preliminary carbonation reaction tower through the first pipeline;

[0015] The waste gas pipeline is connected to the dust removal tower via the heat exchanger. After the industrial waste gas in the waste gas pipeline is dust-removed in the dust removal tower, the obtained dust-removed product is transported to the preliminary carbonation reaction tower through the second pipeline;

[0016] The ammonia pipeline is connected to the preliminary carbonation reaction tower. The bottom outlet of the preliminary carbonation reaction tower is connected with a third pipeline, and the outlet of the third pipeline is connected to the deep carbonation reaction tower;

[0017] A first enhanced mass transfer reactor and a second enhanced mass transfer reactor are arranged in the deep carbonization reaction tower. The first enhanced mass transfer reactor and the second enhanced mass transfer reactor are respectively arranged on opposite side walls in the deep carbonization reaction tower, and the outlets of the first enhanced mass transfer reactor and the second enhanced mass transfer reactor are opposite to each other. Both the first enhanced mass transfer reactor and the second enhanced mass transfer reactor are connected to the second conveying pipeline; after the dust removal product is dispersed and broken into microbubbles in the micron range by the first enhanced mass transfer reactor and the second enhanced mass transfer reactor, it reacts with the material conveyed through the third conveying pipeline to realize soda production by using a negative carbon production process.

[0018] In the above solution, the industrial waste brine in the waste liquid pipeline undergoes a real-time oxidation reaction in the oxidation reaction tower, and brine with a relatively high concentration (i.e., the oxidation product) can be obtained; by using a dust removal tower to remove dust from industrial waste gas, a CO2 gas with a relatively high purity (i.e., the dust removal product) can be obtained; the oxidation product, the dust removal product, and ammonia water can successively react in the preliminary carbonization reaction tower and the deep carbonization reaction tower to produce NaHCO3. At the same time, by arranging the first enhanced mass transfer reactor and the second enhanced mass transfer reactor, the CO2 gas can be dispersed and broken into microbubbles in the micron range by the first enhanced mass transfer reactor and the second enhanced mass transfer reactor, increasing the gas-liquid mass transfer area; by making the outlets of the first enhanced mass transfer reactor and the second enhanced mass transfer reactor opposite to each other, two microbubble flows can be used for counterflow, further dispersing and breaking the two microbubble flows, which helps to further increase the gas-liquid mass transfer area. It can be understood that the concentration of CO2 in the dust removal product after the industrial waste gas is purified is usually relatively low (the concentration is less than 70%). By combining the soda production process with the enhanced mass transfer technology and specifically arranging the positions of the enhanced mass transfer reactors in this solution, good soda production efficiency can still be ensured when the concentration of the CO2 gas is relatively low, and this soda production solution has the characteristics of being negative carbon, green, low energy consumption, and environmentally friendly, meeting the industrial production requirements of green and sustainable development. In addition, since this solution increases the phase boundary mass transfer area between the gas and liquid phases by applying the enhanced mass transfer technology, the requirement for the conveying pressure of the gaseous raw material to be conveyed can be reduced, that is, the CO2 gas can be conveyed at a low pressure, which helps to further reduce the production energy consumption.

[0019] Preferably, the system further includes a stirrer, which includes a stirring motor, a stirring shaft, and stirring blades. The stirring motor is connected to the stirring shaft, and the stirring blades are provided at one end of the stirring shaft away from the stirring motor. One end of the stirring shaft away from the stirring motor passes through the deep carbonization reaction tower and extends into the interior of the deep carbonization reaction tower. The stirring blades are located above the first enhanced mass transfer reactor and the second enhanced mass transfer reactor in the vertical direction, and the stirring blades are located in the middle of the first enhanced mass transfer reactor and the second enhanced mass transfer reactor in the horizontal direction. By setting the stirrer in this solution, the microbubbles can be evenly distributed through stirring. At the same time, setting the stirring blades above the first enhanced mass transfer reactor and the second enhanced mass transfer reactor in the vertical direction can reduce the impact of the stirring of the stirring blades on the counterflow of the two microbubble streams, thereby further increasing the gas-liquid mass transfer area and improving the raw material utilization rate. In addition, this setting method can also reduce the impact of the stirring of the stirring blades on the products that have been reacted at the bottom of the tower, avoid product backmixing, and ensure the stable output of the bottom products of the tower.

[0020] Preferably, a distribution pipe is provided between the outlet of the first enhanced mass transfer reactor and the outlet of the second enhanced mass transfer reactor. A plurality of distribution holes are provided on the pipe wall of the distribution pipe on the side close to the stirring blades. In this solution, the distribution pipe can provide a relatively independent space for the counterflow of the two microbubble streams and prevent the stirring of the stirrer from affecting the counterflow effect. At the same time, by providing a plurality of distribution holes on the side close to the stirring blades, the further broken microbubbles after the counterflow can be sent from the distribution holes to the vicinity of the stirring blades and evenly dispersed under the stirring of the stirring blades, which helps to further prevent bubble coalescence and improve the uniform dispersion degree of the microbubbles.

[0021] Preferably, a third enhanced mass transfer reactor is further provided in the deep carbonization reaction tower. The third enhanced mass transfer reactor is provided above the liquid level of the deep carbonization reaction tower. The outlet of the third enhanced mass transfer reactor is connected with an extension pipe, and the extension pipe extends into the liquid level of the deep carbonization reaction tower, and the outlet of the extension pipe is located above the first enhanced mass transfer reactor and the second enhanced mass transfer reactor. The outlet of the third conveying pipeline is connected with the third enhanced mass transfer reactor. In this solution, the material in the third conveying pipeline can entrain the unreacted gas at the top of the tower into the third enhanced mass transfer reactor for further dispersion and crushing during the flow, and then return to the tower to continue to participate in the reaction, which helps to further improve the raw material conversion rate.

[0022] Preferably, a circulation pipeline is arranged on one side of the deep carbonization reaction tower. The inlet of the circulation pipeline is connected to the side wall of the deep carbonization reaction tower, and the outlet is connected to the third mass transfer intensifier reactor. The inlet of the circulation pipeline is located vertically between the first mass transfer intensifier reactor and the liquid level of the deep carbonization reaction tower. 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, setting the inlet of the circulation pipeline vertically between the first mass transfer intensifier reactor and the liquid level of the deep carbonization reaction tower can reduce the impact of the stirring of the circulation pipeline on the products that have completed the reaction at the bottom of the tower, avoid product backmixing, and ensure the stable output of the bottom products. At the same time, the circulating material in the circulation pipeline can be input into the third mass transfer intensifier reactor together with the material in the third conveying pipeline, that is, the two materials provide the power for dispersion and fragmentation at the same time, which helps to improve the fragmentation degree of microbubbles, reduce the scale of microbubbles, and thus further increase the phase boundary mass transfer area.

[0023] Preferably, a fourth mass transfer intensifier reactor and a fifth mass transfer intensifier reactor are arranged in the preliminary carbonization reaction tower. The fourth mass transfer intensifier reactor is arranged below the liquid level in the preliminary carbonization reaction tower, and the fifth mass transfer intensifier reactor is arranged above the liquid level in the preliminary carbonization reaction tower. The outlet of the fifth mass transfer intensifier reactor is connected with a first connecting pipe, and the outlet of the first connecting pipe is connected to the fourth mass transfer intensifier reactor. The first conveying pipeline is connected to the fifth mass transfer intensifier reactor. The ammonia pipeline and the second conveying pipeline are both connected to the fourth mass transfer intensifier reactor. This solution can disperse and fragment ammonia gas and CO2 in the second conveying pipeline into microbubbles of micron size by setting the fourth mass transfer intensifier reactor, increasing the phase boundary mass transfer area. The fifth mass transfer intensifier reactor located above can entrain the unreacted gas at the top of the tower, and after dispersion and fragmentation, send it back into the tower to participate in the reaction again, which helps to improve the raw material conversion rate. In addition, the microbubbles after dispersion and fragmentation by the fifth mass transfer intensifier reactor are sent into the fourth mass transfer intensifier reactor along the first connecting pipe, and the fourth mass transfer intensifier reactor can be used for further dispersion and fragmentation, and this material flow can impact the microbubble flow dispersed and fragmented by the fourth mass transfer intensifier reactor itself, which also helps to improve the dispersion and fragmentation degree of microbubbles. At the same time, the setting of the first connecting pipe can also support the fifth mass transfer intensifier reactor, improving the overall structural strength.

[0024] Preferably, a backmixing pipeline is provided on one side of the preliminary carbonization reaction tower. The inlet of the backmixing pipeline is connected to the side wall of the preliminary carbonization reaction tower, and the outlet is connected to the fifth mass transfer intensifier reactor. The inlet of the backmixing pipeline is located vertically between the fourth mass transfer intensifier reactor and the liquid level of the preliminary carbonization reaction tower. By setting the backmixing pipeline, the materials in the tower can be stirred, improving the reaction efficiency and the uniformity of the distribution of microbubbles. At the same time, the materials in the backmixing pipeline and the materials in the first conveying pipeline are input into the fifth mass transfer intensifier reactor together, that is, the two streams of materials provide the power for dispersion and fragmentation at the same time, which helps to improve the fragmentation degree of microbubbles, reduce the scale of microbubbles, and thus further increase the phase boundary mass transfer area.

[0025] Preferably, multiple layers of partition plates are staggered in the preliminary carbonization reaction tower, and the partition plates are located below the fourth mass transfer intensifier reactor. The product of the preliminary carbonization reaction tower is output from the bottom of the tower. By staggering multiple layers of partition plates below the fourth mass transfer intensifier reactor, it helps to avoid backmixing of the product and enables the product to be stably and orderly input into the next reaction tower (i.e., the deep carbonization reaction tower).

[0026] Preferably, a sixth mass transfer intensifier reactor and a seventh mass transfer intensifier reactor are provided in the dust removal tower. Both the sixth mass transfer intensifier reactor and the seventh mass transfer intensifier reactor are 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 respectively arranged on the opposite side walls in the dust removal tower; both the sixth mass transfer intensifier reactor and the seventh mass transfer intensifier reactor are connected to the waste gas pipeline. In this solution, by setting the sixth mass transfer intensifier reactor and the seventh mass transfer intensifier reactor, industrial waste gas can be dispersed and fragmented into microbubbles in the micron range, thereby increasing the gas-liquid mass transfer area to improve the dust removal effect on industrial waste gas; by arranging the sixth mass transfer intensifier reactor and the seventh mass transfer intensifier reactor on the opposite side walls in the dust removal tower respectively, with the outlets of the two mass transfer intensifier reactors facing each other, the microbubbles output from the two mass transfer intensifier reactors can be used to impact each other, thus further dispersing and fragmenting.

[0027] Preferably, a sprayer is provided in the dust removal tower, and the sprayer is connected to a dust removal liquid pipeline; the sprayer is located vertically above the liquid level in the dust removal tower, and the sprayer is arranged horizontally between the sixth mass transfer intensifier reactor and the seventh mass transfer intensifier reactor. In this solution, the dust removal liquid is sent into the dust removal tower through the sprayer. This method can increase the dust removal efficiency, and by arranging the sprayer horizontally between the sixth mass transfer intensifier reactor and the seventh mass transfer intensifier reactor, the sprayed dust removal liquid is more concentrated between the sixth mass transfer intensifier reactor and the seventh mass transfer intensifier reactor, which helps to further improve the dust removal efficiency.

[0028] Preferably, an auxiliary dust collector is further arranged in the dust removal tower. The auxiliary dust collector is located vertically between the sprayer and the sixth enhanced mass transfer reactor. The auxiliary dust collector is in a conical shape that gradually decreases from top to bottom in the vertical direction, and the bottom opening of the auxiliary dust collector is horizontally located between the sixth enhanced mass transfer reactor and the seventh enhanced mass transfer reactor. By setting the auxiliary dust collector, this solution can restrict the upward movement of gas from the position between the sixth enhanced mass transfer reactor and the seventh enhanced mass transfer reactor. Since the sprayer is horizontally arranged between the sixth enhanced mass transfer reactor and the seventh enhanced mass transfer reactor, that is, the newly supplemented spray liquid is relatively concentrated between the sixth enhanced mass transfer reactor and the seventh enhanced mass transfer reactor. In this case, the gas rises along the position where the spray liquid is relatively concentrated. Thus, it helps to further improve the dust removal efficiency.

[0029] Preferably, a rotating motor is arranged outside the dust removal tower. The rotating motor is connected to a rotating shaft. The rotating shaft passes through the tower wall of the dust removal tower and extends deep into the interior of the dust removal tower. And one end of the rotating shaft away from the rotating motor is connected to a rotating fan blade. The rotating fan blade is vertically located below the sixth enhanced mass transfer reactor, and the rotating fan blade is horizontally located between the sixth enhanced mass transfer reactor and the seventh enhanced mass transfer reactor. By setting the rotating fan blade, this solution helps to improve the uniform distribution degree of microbubbles, and further helps to increase the phase boundary mass transfer area between the gas phase and the liquid phase, which helps to further improve the dust removal effect.

[0030] Preferably, an eighth mass transfer intensifier reactor and a ninth mass transfer intensifier reactor are arranged in the oxidation reaction tower. The eighth mass transfer intensifier reactor and the ninth mass transfer intensifier reactor are both located below the liquid level in the oxidation reaction tower in the vertical direction. The eighth mass transfer intensifier reactor is located above the ninth mass transfer intensifier reactor in the vertical direction, and the outlets of the eighth mass transfer intensifier reactor and the ninth mass transfer intensifier reactor are opposite to each other. The eighth mass transfer intensifier reactor and the ninth mass transfer intensifier reactor are both connected with oxidation gas pipelines. Preferably, the outlet of the eighth mass transfer intensifier reactor is connected to the outlet of the ninth mass transfer intensifier reactor through a second connecting pipe. A plurality of through holes are arranged on the wall of the second connecting pipe. In this solution, the eighth mass transfer intensifier reactor and the ninth mass transfer intensifier reactor can disperse and break the oxidation gas (which can be oxygen or air) into microbubbles in the micron range, increasing the phase boundary mass transfer area between it and the industrial waste brine, thereby improving the wet oxidation efficiency. In addition, by making the outlets of the two mass transfer intensifier reactors opposite to each other, the two microbubble flows can be used to collide with each other to achieve further dispersion and fragmentation. In a further solution, by arranging the second connecting pipe, a place can be provided for the two microbubble flows to collide with each other. The microbubbles after collision can be evenly diffused into the liquid phase material in the oxidation reaction tower along the through holes on the second connecting pipe, which helps to further improve the wet oxidation efficiency.

[0031] Preferably, the heat exchanger includes an inner pipe and an outer shell. The inner pipe is arranged inside the outer shell, and a heat exchange cavity is formed between the inner pipe and the outer shell. The waste liquid pipeline is connected to the oxidation reaction tower via the inner pipe, and the waste gas pipeline is connected to the dust removal tower via the heat exchange cavity. A plurality of baffle plates are arranged in the inner pipe along the material flow direction, and two adjacent baffle plates are arranged staggeredly. In this solution, by arranging the baffle plates, the flow path of the industrial waste brine can be extended, thereby prolonging the heat exchange time between the industrial waste brine and the industrial waste gas, and using the high temperature carried in the industrial waste gas to heat the industrial waste brine, so as to facilitate the wet oxidation reaction in the subsequent process. It can be understood that the reaction temperature of the wet oxidation reaction is generally about 250 °C, while the temperature of the industrial waste gas dust removal is usually below 100 °C. This solution helps to greatly reduce the energy consumption and further save the production cost by thermally coupling the industrial waste brine and the industrial waste gas.

[0032] Preferably, the baffle plate inclines towards the outlet end of the inner pipe, and the included angle between the baffle plate and the inner pipe wall is within the range of [30°, 50°]. This solution can further extend the flow path of the industrial waste brine by setting the inclination angle of the baffle plate, which is beneficial to further improving the heat exchange performance.

[0033] Preferably, a heat insulation plate is provided in the heat exchange chamber, and the heat insulation plate divides the heat exchange chamber into a first heat exchange chamber and a second heat exchange chamber along the material flow direction; the waste gas pipeline is connected to the dust removal tower via the first heat exchange chamber; the first conveying pipeline is connected to the preliminary carbonization reaction tower via the second heat exchange chamber. In this solution, 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 heating the industrial waste brine subsequently. At the same time, in this solution, the industrial waste brine is first thermally coupled with the industrial waste gas and then with the oxidation product. This is because the temperature of the industrial waste gas itself is usually relatively high (above 300 °C), while the temperature of the initial industrial waste brine is relatively low, and the temperature difference between the two is large, resulting in high heat exchange efficiency, which can quickly increase the temperature of the industrial waste brine and reduce the temperature of the industrial waste gas. Then, by exchanging heat between the oxidation product and the industrial waste brine, the industrial waste brine can be reheated, making the temperature of the industrial waste brine closer to the temperature requirement of the wet oxidation reaction to ensure the efficient progress of the subsequent reaction. In short, this staged heating method can further improve the heat exchange efficiency and reduce energy consumption.

[0034] In the above solution of the present utility model, after the industrial waste gas and the industrial waste brine undergo heat exchange, they respectively enter the dust removal process section (i.e., the dust removal tower) and the wet oxidation process section (i.e., the oxidation reaction tower). This heat coupling method helps to reduce energy consumption and save production costs. At the same time, in the dust removal process section, by combining the enhanced mass transfer technology with the spray dust removal process and specifically setting the positions of the enhanced mass transfer reactor, the sprayer, and the auxiliary dust collector, it helps to improve the industrial dust removal efficiency, thereby helping to increase the concentration of CO2 in the dust removal product and ensuring the orderly progress of the subsequent soda-making 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 increasing the purification efficiency of the industrial waste brine and reducing the COD value in the industrial waste brine, so that it can participate in the subsequent soda-making process. In the soda-making process section, by setting up two-stage carbonation reaction towers, the conversion rate of the reaction raw materials can be increased. By combining the enhanced mass transfer technology, the phase boundary contact area between the gas-phase raw material and the liquid-phase raw material can be increased, so that good soda-making efficiency can still be ensured even when the concentration of CO2 is low, that is, the CO2 in the industrial waste gas can be used for soda-making, thus realizing a negative-carbon soda-making method. This production method has the advantages of environmental protection and low energy consumption. In short, the solution of the present utility model utilizes the CO2 in the industrial waste gas and the NaCl in the industrial waste brine to realize the green synthesis process of soda ash, which helps to reduce production costs. This solution not only does not cause environmental pollution itself, but also consumes the waste gas and waste brine from other industries, which helps to reduce the treatment cost of waste gas and waste brine and realize the negative-carbon production method. The present utility model reuses industrial waste and further converts it into valuable industrial chemicals, realizing the circular conversion of industrial production. It not only does not consume pure CO2 gas, but also further purifies and utilizes industrial waste, forming a negative-carbon industrial chain, which perfectly matches the concept of green sustainable development.

[0035] Those skilled in the art can understand that the enhanced mass transfer reactor adopted in the present invention has been embodied in the inventor's prior patents, such as patents with application numbers CN201610641119.6, CN201610641251.7, CN201710766435.0, CN106187660A, CN105903425A, CN205833127U and CN207581700U. The prior patent CN201610641119.6 describes in detail the specific product structure and working principle of the micron bubble generator (i.e., bubble breaker). The application document states that "the micron bubble generator includes a main body and a secondary crushing member, a cavity is provided in the main body, an inlet connected to the cavity is provided on the main body, the first and second opposite ends of the cavity are open, wherein the cross-sectional area of ​​the cavity decreases from the middle of the cavity to the first and second ends of the cavity; the secondary crushing member is provided at at least one of the first and second ends of the cavity, a part of the secondary crushing member is provided in the cavity, and an annular channel is formed between the secondary crushing member and the through holes open at both ends of the cavity. The micron bubble generator also includes an air inlet pipe and a liquid inlet pipe." From the specific structure disclosed in the application document, it can be known that its specific working principle is: the liquid enters the micron bubble generator tangentially through the liquid inlet pipe, rotates at ultra-high speed and cuts the gas, so that the gas bubbles are broken into micron-level microbubbles, thereby increasing the mass transfer area between the liquid phase and the gas phase, and the micron bubble generator in the patent is a pneumatic bubble breaker.

[0036] In addition, the prior patent 201610641251.7 records 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 connects the feed port with the gas-liquid mixture outlet, indicating that the bubble breaker requires gas-liquid mixture to enter. In addition, it can be seen from the following figures that the primary bubble breaker mainly uses circulating liquid as power, so the primary bubble breaker actually belongs to a hydraulic enhanced reactor, and the secondary bubble breaker simultaneously passes the gas-liquid mixture into an elliptical rotating ball for rotation, thereby achieving bubble breaking during the rotation process, so the secondary bubble breaker actually belongs to a gas-liquid linkage type bubble breaker. In fact, whether it is a hydraulic bubble breaker or a gas-liquid linkage type bubble breaker, it is a specific form of a bubble breaker. However, the enhanced mass transfer reactor adopted by the utility model is not limited to the above-mentioned forms. The specific structure of the bubble breaker recorded in the prior patent is only one of the forms that can be adopted by the utility model.

[0037] In addition, the prior patent 201710766435.0 records that "the principle of the bubble breaker is to achieve gas collision through high-speed jet flow"; moreover, the prior patent CN106187660 also has relevant records on the specific structure of the bubble breaker. Specifically, see paragraphs

[0031] -

[0041] in the specification and the attached drawings. It elaborates in detail on the specific working principle of the bubble breaker S-2. The top of the bubble breaker is the liquid-phase inlet, and the side is the gas-phase inlet. The liquid phase entering from the top provides entrainment power, thereby achieving the effect of being pulverized into ultra-fine bubbles. It can also be seen from the attached drawings that the bubble breaker has a conical structure, and the diameter of the upper part is larger than that of the lower part, which is also to enable the liquid phase to better provide entrainment power.

[0038] Since the bubble breaker was just developed in the initial stage of the prior patent application, it was initially named the microbubble generator (CN201610641119.6), etc. With continuous technological improvement, it was later renamed the bubble breaker. Now, the enhanced mass transfer reactor in the present utility model is equivalent to the previous microbubble generator, microinterface generator, etc., just with different names. In summary, the enhanced mass transfer reactor of the present utility model belongs to the prior art.

[0039] The present utility model also provides a method for producing soda using industrial waste gas and industrial waste brine, and this method uses the system in any of the above-mentioned solutions to produce soda.

[0040] Compared with the prior art, the beneficial effects of the present utility model are as follows:

[0041] 1. The present utility model utilizes CO2 in industrial waste gas and NaCl in industrial waste brine to achieve a green synthesis process of soda ash, reducing production costs. It not only does not cause environmental pollution itself, but also consumes waste gas and waste brine from other industries, reducing the treatment cost of waste gas and waste brine, and realizing a negative-carbon production method.

[0042] 2. The present utility model can use low-concentration CO2 to produce soda ash under a low-pressure environment, and has high production efficiency. This reaction system combines the enhanced mass transfer technology into the soda ash preparation process, effectively improving the reaction efficiency of raw materials and the utilization rate of carbon dioxide, while reducing the input pressure of carbon dioxide and lowering energy consumption.

[0043] 3. The reaction raw materials of the present utility model are low-carbon and environmentally friendly. Among them, the ammonia raw material can use green ammonia or blue ammonia, and CO2 can use low-concentration CO2 of 70% or less as the raw material, or can mix the recovered CO2 with a concentration of 75-80% from the calciner and the low-concentration CO2 in the flue gas to form CO2 with a concentration of 50-75% as the carbon source. In this way, the production process of the present utility model becomes a negative-carbon production process, reducing production costs. Brief Description of the Drawings

[0044] Various other advantages and benefits will become apparent to those of ordinary skill in the art by reading the following detailed description of the preferred embodiments. The drawings are only for the purpose of showing the preferred embodiments and are not considered to be a limitation of the present utility model. Moreover, throughout the drawings, the same reference numerals are used to represent the same components. In the drawings:

[0045] Figure 1 Shows a schematic diagram of an alkali-making system according to an embodiment of the present application;

[0046] Figure 2 Shows a schematic structural diagram of a heat exchanger according to an embodiment of the present application;

[0047] Figure 3 Shows a schematic structural diagram of an oxidation reaction tower according to an embodiment of the present application;

[0048] Figure 4 Shows a schematic structural diagram of a dust removal tower according to an embodiment of the present application;

[0049] Figure 5 Shows a schematic structural diagram of an auxiliary dust collector according to an embodiment of the present application;

[0050] Figure 6 Shows a schematic structural diagram of a preliminary carbonation reaction tower according to an embodiment of the present application;

[0051] Figure 7 Shows a schematic structural diagram of a deep carbonation reaction tower according to an embodiment of the present application;

[0052] Figure 8 Shows a process flow diagram of an alkali-making process according to an embodiment of the present utility model.

[0053] In the figure:

[0054] 1. Waste liquid pipeline; 2. Heat exchanger; 201. Inner pipe; 202. Outer shell; 203. Thermal insulation plate; 204. Baffle plate; 3. Exhaust gas pipeline; 4. Heater; 5. Oxidation reaction tower; 501. Eighth mass transfer intensifier reactor; 502. Second connecting pipe; 503. Ninth mass transfer intensifier reactor; 504. Drain port; 6. Oxidation gas pipeline; 7. First conveying pipeline; 8. Dust removal tower; 801. Rotating motor; 802. Rotating shaft; 803. Rotating fan blade; 804. Sixth mass transfer intensifier reactor; 805. Seventh mass transfer intensifier 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 mass transfer intensifier reactor; 1202. First connecting pipe; 1203. Fifth mass transfer intensifier reactor; 1204. Gas collecting pipe; 1205. Suction pump; 1206. Backmixing pipeline; 1207. Baffle; 13. Deep carbonization reaction tower; 1301. Stirring motor; 1302. Stirring shaft; 1303. Third mass transfer intensifier reactor; 1304. Extension pipe; 1305. Stirring wing; 1306. First mass transfer intensifier reactor; 1307. Distribution pipe; 1308. Second mass transfer intensifier reactor; 1309. Delivery 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 pipeline; 23. Gas-liquid separator. Detailed implementation manners

[0055] The technical solutions of the present utility model will be clearly and completely described below in conjunction with the accompanying drawings and specific implementation manners. However, those skilled in the art will understand that the following described embodiments are some embodiments of the present utility model, rather than all embodiments, and are only used to illustrate the present utility model and should not be construed as limiting the scope of the present utility model. Based on the embodiments of the present utility model, all other embodiments obtained by those of ordinary skill in the art without creative efforts shall fall within the protection scope of the present utility model. For those conditions not specified in the embodiments, they shall be carried out according to the conventional conditions or the conditions recommended by the manufacturer. Those reagents or instruments not specified by the manufacturer can be obtained as conventional products through commercial purchase.

[0056] In the description of the present utility model, it should be noted that the orientation or positional relationship indicated by the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. is based on the orientation or positional relationship shown in the drawings. It is only for the convenience of describing the present utility model and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be construed as a limitation to the present utility model. In addition, the terms "first", "second", "third" are only used for descriptive purposes and cannot be construed as indicating or implying relative importance.

[0057] In the description of the present utility model, it should be noted that unless otherwise clearly specified and defined, the terms "installation", "connection", "coupling" should be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be directly connected or indirectly connected through an intermediate medium, and it can be the communication inside two elements. For those of ordinary skill in the art, the specific meanings of the above terms in the present utility model can be understood according to specific circumstances.

[0058] Refer to Figures 1-7 , an embodiment of the present utility model provides a system for producing alkali by using industrial waste gas and industrial waste brine, including: a waste liquid pipeline 1, a waste gas pipeline 3, an ammonia 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.

[0059] 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 undergoes a 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.

[0060] The waste gas pipeline 3 is connected to the dust removal tower 8 via the heat exchanger 2. After the industrial waste gas in the waste gas pipeline 3 is dust-removed in the dust removal tower 8, the obtained dust-removed product is transported to the preliminary carbonization reaction tower 12 through the second conveying pipeline 10.

[0061] The ammonia pipeline 22 is connected to the preliminary carbonization reaction tower 12. The bottom outlet of the preliminary carbonization reaction tower 12 is connected with a third conveying pipeline 14, and the outlet of the third conveying pipeline 14 is connected to the deep carbonization reaction tower 13.

[0062] The deep carbonization reaction tower 13 is provided with a first mass transfer intensifier reactor 1306 and a second mass transfer intensifier reactor 1308. The first mass transfer intensifier reactor 1306 and the second mass transfer intensifier reactor 1308 are respectively arranged on the opposite side walls inside the deep carbonization reaction tower 13, and the outlets of the first mass transfer intensifier reactor 1306 and the second mass transfer intensifier reactor 1308 are opposite to each other. Both the first mass transfer intensifier reactor 1306 and the second mass transfer intensifier reactor 1308 are connected to the second conveying pipeline 10. After the dust removal product is dispersed and broken into microbubbles in the micron level by the first mass transfer intensifier reactor 1306 and the second mass transfer intensifier reactor 1308, it reacts with the material conveyed through the third conveying pipeline 14 to realize soda production by using the negative carbon production process.

[0063] In the solution of this embodiment, the main component of the industrial waste gas should be CO2, which mainly comes from industries such as petroleum cracking, coal - to - methanol, coal - to - ethanol, thermal power plants, and new energy battery production. After passing through the dust removal process section (i.e., the dust removal tower 8), the waste gas can remove excess gas impurities (such as SO2, H2S, NO2, etc.) and separate to obtain a relatively high - purity CO2 gas. This mixed gas may contain inert gases such as N2, He, etc. Due to the adoption of the enhanced mass transfer technology, low - concentration CO2 does not affect the soda production efficiency of the soda - making process.

[0064] In the solution of this embodiment, the industrial waste gas can enter the waste gas pipeline 3 after pre - treatment. This pre - treatment can adopt any existing or future - developed dust removal process, which will not be elaborated. In this embodiment, the industrial waste gas passes through pre - treatment and then is dust - removed by the dust removal tower 8, which can further improve the purity of CO2 in the gas.

[0065] In the solution of this embodiment, the main component of the industrial waste brine is NaCl, and the industrial waste brine can mainly come from the sewage in any one of industrial productions such as petrochemical industry, natural gas exploitation, papermaking, and pharmaceutical industry.

[0066] In some embodiments, the industrial waste brine can enter the waste liquid pipeline 1 through a pre - treatment process. Specifically, the industrial waste brine can reduce the COD value through the pre - treatment process, and then remove trace organic wastes that are difficult to oxidize through the oxidation reaction tower 5, reducing the COD value to below 10 mg / L, so as to obtain a raw material liquid (i.e., the oxidation product) mainly containing inorganic salt NaCl.

[0067] Continue to refer to Figure 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 to further heat the heat - exchanged industrial waste brine so that it can meet the reaction temperature requirements of the wet oxidation reaction.

[0068] In some embodiments, the oxidation product can be separated and filtered. In Figure 1In the illustrated embodiment, the system further includes a gas-liquid separator 23. The oxidation products in the first transfer pipeline 7 are heat-exchanged with industrial waste brine in the heat exchanger 2 and then enter the gas-liquid separator 23. The liquid phase therein (mainly containing inorganic salt NaCl) is transported to the preliminary carbonization reaction tower 12, and the gas phase (mainly including unreacted oxygen) can be directly discharged into the air or can be transported to the oxidation reaction tower 5 via an air compressor to continue to participate in the wet oxidation of industrial waste brine. It can be understood that in this embodiment, the first transfer pipeline 7 can be regarded as including three pipeline segments, namely, the first pipeline segment between the outlet of the oxidation reaction tower 5 and the heat exchanger 2, the second pipeline segment between the heat exchanger 2 and the gas-liquid separator 23, and the third pipeline segment between the liquid outlet of the gas-liquid separator and the preliminary carbonization reaction tower 12.

[0069] As Figure 2 shown, the heat exchanger 2 includes an inner pipe 201 and a housing 202. The inner pipe 201 is arranged inside the housing 202, and a heat exchange cavity is formed between the inner pipe 201 and the housing 202. The waste liquid pipeline 1 is connected to the oxidation reaction tower 5 via the inner pipe 201, and the waste gas pipeline 3 is connected to the dust removal tower 8 via the heat exchange cavity. A plurality of baffle plates 204 are arranged in the inner pipe 201 along the material flow direction, and two adjacent baffle plates 204 are arranged staggeredly.

[0070] Continue to refer to Figure 2 , the baffle plate 204 inclines towards the outlet end of the inner pipe 201, and the included angle between the baffle plate 204 and the inner wall of the inner pipe 201 is within the range of [30°, 50°].

[0071] Continue to refer to Figure 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 to the dust removal tower 8 via the first heat exchange cavity. The first transfer pipeline 7 is connected to the preliminary carbonization reaction tower 12 via the second heat exchange cavity.

[0072] As Figure 3 shown, an eighth enhanced mass transfer reactor 501 and a ninth enhanced mass transfer reactor 503 are arranged in the oxidation reaction tower 5. 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. The eighth enhanced mass transfer reactor 501 and the ninth enhanced mass transfer reactor 503 are both connected to an oxidation gas pipeline 6.

[0073] Continue to refer to Figure 3, the outlet of the eighth mass transfer intensifying reactor 501 is connected to the outlet of the ninth mass transfer intensifying reactor 503 through the second connecting pipe 502; a plurality of through holes are provided on the wall of the second connecting pipe 502.

[0074] Continue to refer to Figure 3 , a drain port 504 can be provided at the bottom of the oxidation reaction tower 5.

[0075] The above method of treating industrial waste brine using the oxidation reaction tower 5 can be called the microinterface wet oxidation process.

[0076] As Figure 4 shown, a sixth mass transfer intensifying reactor 804 and a seventh mass transfer intensifying reactor 805 are provided in the dust removal tower 8. Both the sixth mass transfer intensifying reactor 804 and the seventh mass transfer intensifying reactor 805 are provided below the liquid level in the dust removal tower 8, and the sixth mass transfer intensifying reactor 804 and the seventh mass transfer intensifying reactor 805 are respectively provided on the opposite side walls in the dust removal tower 8; both the sixth mass transfer intensifying reactor 804 and the seventh mass transfer intensifying reactor 805 are connected to the waste gas pipeline 3.

[0077] Continue to refer to Figure 4 , a sprayer 807 is provided in the dust removal tower 8. The sprayer 807 is connected to 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 the sprayer 807 is arranged horizontally between the sixth mass transfer intensifying reactor 804 and the seventh mass transfer intensifying reactor 805. The dust removal liquid in the dust removal liquid pipeline 9 can be water.

[0078] Combined with reference to Figures 4-5 , an auxiliary dust remover 806 is also provided in the dust removal tower 8. The auxiliary dust remover 806 is located between the sprayer 807 and the sixth mass transfer intensifying reactor 804 in the vertical direction; the auxiliary dust remover 806 is in a conical shape that gradually decreases from top to bottom in the vertical direction, and the bottom opening of the auxiliary dust remover 806 is located horizontally between the sixth mass transfer intensifying reactor 804 and the seventh mass transfer intensifying reactor 805.

[0079] As Figure 4 shown, a rotating motor 801 is provided outside the dust removal tower 8. The rotating motor 801 is connected to a rotating shaft 802. The rotating shaft 802 passes through the tower wall of the dust removal tower 8 and extends into the interior of the dust removal tower 8, and one end of the rotating shaft 802 away from the rotating motor 801 is connected to a rotating fan blade 803; the rotating fan blade 803 is located below the sixth mass transfer intensifying reactor 804 in the vertical direction, and the rotating fan blade 803 is located horizontally between the sixth mass transfer intensifying reactor 804 and the seventh mass transfer intensifying reactor 805.

[0080] The dust removal process in the above embodiment can be called the microinterface purification and separation process.

[0081] AsFigure 6 As shown in the figure, a fourth mass transfer intensifier 1201 and a fifth mass transfer intensifier 1203 are arranged in the preliminary carbonization reaction tower 12. The fourth mass transfer intensifier 1201 is arranged below the liquid level in the preliminary carbonization reaction tower 12, and the fifth mass transfer intensifier 1203 is arranged above the liquid level in the preliminary carbonization reaction tower 12. The outlet of the fifth mass transfer intensifier 1203 is connected with a first connecting pipe 1202, and the outlet of the first connecting pipe 1202 is connected with the fourth mass transfer intensifier 1201; the first conveying pipeline 7 is connected with the fifth mass transfer intensifier 1203; the ammonia pipeline 22 and the second conveying pipeline 10 are both connected with the fourth mass transfer intensifier 1201.

[0082] Continue to refer to Figure 6 , a gas collecting pipe 1204 can be arranged on the fifth mass transfer intensifier 1203 to facilitate the entrainment of the tower top gas into the fifth mass transfer intensifier 1203.

[0083] Continue to refer to Figure 6 , a backmixing pipeline 1206 is arranged on one side of the preliminary carbonization reaction tower 12. The inlet of the backmixing pipeline 1206 is connected to the side wall of the preliminary carbonization reaction tower 12, and the outlet is connected to the fifth mass transfer intensifier 1203. The inlet of the backmixing pipeline 1206 is located vertically between the fourth mass transfer intensifier 1201 and the liquid level of the preliminary carbonization reaction tower 12. In Figure 6 , a suction pump 1205 can be arranged on the backmixing pipeline 1206 to provide power for the material flow in the backmixing pipeline 1206.

[0084] It should be understood that a pump can be respectively arranged on each pipeline in this solution to facilitate the material flow and meet the conveying pressure requirements of the corresponding materials. The specific setting method can be selected according to actual needs and will not be elaborated.

[0085] Continue to refer to Figure 6 , multiple layers of partition plates 1207 are arranged in a staggered manner in the preliminary carbonization reaction tower 12, and the partition plates 1207 are located below the fourth mass transfer intensifier 1201.

[0086] Such as Figure 7As shown, the system further includes a stirrer, which includes a stirring motor 1301, a stirring shaft 1302, and stirring blades 1305. The stirring motor 1301 is connected to the stirring shaft 1302, and the stirring blades 1305 are arranged at one end of the stirring shaft 1302 away from the stirring motor 1301; one end of the stirring shaft 1302 away from the stirring motor 1301 passes through the deep carbonization reaction tower 13 and extends into the interior of the deep carbonization reaction tower 13; the stirring blades 1305 are located above the first enhanced mass transfer reactor 1306 and the second enhanced mass transfer reactor 1308 in the vertical direction, and the stirring blades 1305 are located in the middle of the first enhanced mass transfer reactor 1306 and the second enhanced mass transfer reactor 1308 in the horizontal direction.

[0087] Continue to refer to Figure 7 , a distribution pipe 1307 is arranged between the outlet of the first enhanced mass transfer reactor 1306 and the outlet of the second enhanced mass transfer reactor 1308; a plurality of distribution holes are arranged on the pipe wall of the distribution pipe 1307 on the side close to the stirring blades 1305.

[0088] Continue to refer to Figure 7 , a third enhanced mass transfer reactor 1303 is further arranged in the deep carbonization reaction tower 13, and the third enhanced mass transfer reactor 1303 is arranged above the liquid level of the deep carbonization reaction tower 13; an extension pipe 1304 is connected to the outlet of the third enhanced mass transfer reactor 1303, and the extension pipe 1304 extends into the liquid level of the deep carbonization reaction tower 13, and the outlet of the extension pipe 1304 is located above the first enhanced mass transfer reactor 1306 and the second enhanced mass transfer reactor 1308; the outlet of the third delivery pipeline 14 is connected to the third enhanced mass transfer reactor 1303.

[0089] Continue to refer to Figure 7 , a circulation pipeline 1310 is arranged on one side of the deep carbonization reaction tower 13, the inlet of the circulation pipeline 1310 is connected to the side wall of the deep carbonization 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 carbonization reaction tower 13 in the vertical direction.

[0090] 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 carbonization reaction tower 13.

[0091] In this embodiment, the method of using the initial carbonization reaction tower and the deep carbonization reaction tower 13 to prepare soda ash can be called the "Hou's 2.0" soda-making process.

[0092] As Figure 1As shown, the system may further include a fourth delivery pipeline 11 for delivering high-concentration CO2. In this solution, high-concentration CO2 can be used to purify low-concentration CO2 obtained from industrial waste gas and then mixed into the subsequent soda-making process section, which helps to further improve the soda-making efficiency.

[0093] In the solution 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-making Method 1.0" is usually 0.45 MPa, while only 0.03 - 0.18 MPa of delivery pressure is required in this embodiment. Thus, it helps to reduce the energy consumption of soda-making.

[0094] As Figure 1 shown, the system further includes a filtration tower 15, a calcination tower 16, a mother liquor storage tank 17, and a product conveyor 18. A fifth delivery pipeline 21 is connected to the lower part of the deep carbonization reaction tower 13. The outlet of the fifth delivery pipeline 21 is connected to the filtration tower 15. The solid-phase product outlet of the filtration tower 15 is connected to the calcination tower 16, and the liquid-phase product outlet is connected to the mother liquor storage tank 17. The product of the deep carbonization reaction tower 13 enters the filtration tower 15 for filtration. The liquid enters the mother liquor storage tank 17, and then ammonium chloride products are obtained through traditional separation (specifically, by adding sodium chloride to the mother liquor, ammonium chloride can be precipitated, and the remaining sodium chloride solution can be reused as a reaction raw material); the filter residue enters the calcination tower 16, where sodium bicarbonate is thermally decomposed to obtain soda ash, and is output from the product delivery pipeline 20 driven by the product conveyor 18 provided on the product delivery pipeline 20. The calcination tower 16 can be connected to a calcination gas pipeline 19, and the calcination gas pipeline 19 can be used to supply high-temperature gas to the calcination tower 16.

[0095] This embodiment also provides a method for making soda using industrial waste gas and industrial waste brine, and this method can use the system in any of the above embodiments to make soda.

[0096] Figure 8 Show a flowchart of the soda-making process according to an embodiment of the present invention. As Figure 8 shown, after the industrial waste brine is pretreated and further removes COD through the microinterface wet oxidation process, the NaCl obtained after separation and filtration is sent to the process section of "Hou's 2.0" soda-making process. After the industrial waste gas is pretreated and passes through the microinterface purification and separation process to obtain a gas with a relatively high purity of CO2, this gas is sent to the process section of "Hou's 2.0" soda-making process. At the same time, ammonia gas and CO2 from the synthetic ammonia plant can be sent to the process section of "Hou's 2.0" soda-making process. The above raw materials go through the "Hou's 2.0" soda-making process to obtain soda ash Na2CO3.

[0097] In order to more clearly elaborate on the technical solutions in the present invention, the following will be described in the form of specific embodiments.

[0098] Example 1

[0099] In this example, soda ash is prepared using the Figure 1 system shown.

[0100] Example 2

[0101] The difference between this example and Example 1 is that the stirring wing 1305 in the deep carbonization reaction tower is located below the first enhanced mass transfer reactor 1306.

[0102] Example 3

[0103] The difference between this example and Example 1 is that the distribution holes on the distribution pipe 1307 are located on the pipe wall on the side away from the stirring wing 1305.

[0104] Example 4

[0105] The difference between this example and Example 1 is that the outlet of the extension pipe 1304 is located below the first enhanced mass transfer reactor.

[0106] Example 5

[0107] The difference between this example and Example 1 is that the partition plate 1207 is located above the fourth enhanced mass transfer reactor 1201.

[0108] Experimental Example 1

[0109] The same industrial waste gas, industrial waste brine, and ammonia are respectively introduced into the systems of Examples 1 - 5, and soda ash is produced using the systems of Examples 1 - 5 respectively.

[0110] The soda ash production, purity in the product output from the product delivery pipeline, and the CO2 concentration in the tail gas discharged from the top of the deep carbonization reaction tower are tested, and the test results are shown in the following table.

[0111] Table 1 Test Results

[0112]

[0113] As shown in the above table, it can be seen that when the system of the present utility model uses industrial waste gas and industrial waste brine to prepare soda ash, it can ensure a relatively high soda ash production and purity, and a relatively high CO2 conversion rate.

[0114] Comparing Example 1 with Example 2, it can be found that the soda ash production in Example 2 is lower and the tail gas CO2 concentration is higher. This may be due to the different positions of the stirring wings. Specifically, it may be because the position of the stirring wing is relatively low, resulting in backmixing of the product during stirring and affecting the stable output of the product.

[0115] Comparing Example 1 with Example 3, it can be found that the soda ash production in Example 3 is lower and the CO2 concentration in the tail gas is higher. This may be due to the different positions of the distribution holes. Specifically, in the solution of Example 1, by making the distribution holes located on the tube wall close to one side of the stirring wing, the output microbubbles are directly stirred and dispersed into the liquid phase material in the tower via the stirring wing, and the degree of uniform distribution is higher. Therefore, its soda ash production and CO2 conversion rate are higher.

[0116] Comparing Example 1 with Example 4, it can be found that the soda ash production in Example 4 is lower and the CO2 concentration in the tail gas is higher. This may be because the material in the extension tube is directly transported to the lower part of the first enhanced mass transfer reactor. On the one hand, it impacts the bottom product of the tower, causing some product backmixing. On the other hand, the microbubbles directly input to the lower part may coalesce, reducing the phase boundary mass transfer area.

[0117] Comparing Example 1 with Example 5, it can be found that the soda ash production in Example 5 is lower and the CO2 concentration in the tail gas is higher. This may be because the baffle located above affects the reaction of the raw materials between the two enhanced mass transfer reactors, resulting in a decrease in the raw material conversion rate and soda ash production.

[0118] In summary, it can be seen that the solution of Example 1 improves the raw material conversion rate and soda ash production 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 invention.

[0119] Experimental Example 2

[0120] Collect the oxidation product and dust removal product in Example 1, and detect the COD content in the oxidation product and the CO2 content in the dust removal product. The results are shown in the following table:

[0121] Table 2 Detection Results

[0122]

[0123] As shown in the above table, it can be seen that the present invention can effectively reduce the COD concentration in industrial waste salt water and can effectively increase the CO2 content in industrial waste gas.

[0124] Finally, it should be noted that: the above embodiments are only used to illustrate the technical solutions of the present invention, rather than to limit it; although the present invention has been described in detail with reference to the foregoing embodiments, those of ordinary skill in the art should understand that: they can still modify the technical solutions recorded in the foregoing embodiments, or perform equivalent replacements on some 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 invention.

Claims

1. A system for producing alkali using industrial waste gas and industrial waste brine, characterized in that: include: Waste liquid pipeline, waste gas pipeline, ammonia pipeline, heat exchanger, oxidation reaction tower, dust removal tower, preliminary carbonization reaction tower and 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 a wet oxidation reaction in the oxidation reaction tower, and the generated oxidation product is transported to the preliminary carbonization reaction tower via the first transport pipeline; The exhaust gas pipeline is connected to the dust removal tower via the heat exchanger, and the industrial waste gas in the exhaust gas pipeline is dusted in the dust removal tower, and the obtained dust removal product is transported to the preliminary carbonization reaction tower via the second transport pipeline; The ammonia pipeline is connected to the preliminary carbonization reaction tower, the bottom outlet of the preliminary carbonization reaction tower is connected to a third delivery pipeline, and the outlet of the third delivery pipeline is connected to the deep carbonization reaction tower; A first enhanced mass transfer reactor and a second enhanced mass transfer reactor are arranged in the deep carbonization reaction tower. The first enhanced mass transfer reactor and the second enhanced mass transfer reactor are respectively arranged on opposite side walls in the deep carbonization reaction tower, and the outlets of the first enhanced mass transfer reactor and the second enhanced mass transfer reactor are opposite to each other. The first enhanced mass transfer reactor and the second enhanced mass transfer reactor are both connected to the second conveying pipeline. After the dust removal product is dispersed and broken into micron-level microbubbles by the first enhanced mass transfer reactor and the second enhanced mass transfer reactor, it reacts with the material conveyed by the third conveying pipeline to realize alkali production using the negative carbon production process.

2. The system according to claim 1, characterized in that It also includes an agitator, which includes a stirring motor, a stirring shaft and a stirring wing, the stirring motor is connected to the stirring shaft, and the stirring wing is arranged at the end of the stirring shaft away from the stirring motor; the end of the stirring shaft away from the stirring motor passes through the deep carbonization reaction tower and extends into the deep carbonization reaction tower; the stirring wing is located above the first intensified mass transfer reactor and the second intensified mass transfer reactor in the vertical direction, and the stirring wing is located between the first intensified mass transfer reactor and the second intensified mass transfer reactor in the horizontal direction.

3. The system according to claim 2, characterized in that A distribution pipe is arranged between the outlet of the first enhanced mass transfer reactor and the outlet of the second enhanced mass transfer reactor; a plurality of distribution holes are arranged on the pipe wall of the distribution pipe close to the stirring wing.

4. The system according to claim 3, characterized in that A third enhanced mass transfer reactor is also arranged in the deep carbonization reaction tower, and the third enhanced mass transfer reactor is arranged above the liquid level of the deep carbonization reaction tower; the outlet of the third enhanced mass transfer reactor is connected with an extension pipe, and the extension pipe penetrates into the liquid level of the deep carbonization reaction tower, and the outlet of the extension pipe is located above the first enhanced mass transfer reactor and the second enhanced mass transfer reactor; the outlet of the third conveying pipeline is connected to the third enhanced mass transfer reactor.

5. The system according to claim 1, characterized in that A fourth enhanced mass transfer reactor and a fifth enhanced mass transfer reactor are arranged in the preliminary carbonization reaction tower. The fourth enhanced mass transfer reactor is arranged below the liquid level in the preliminary carbonization reaction tower, and the fifth enhanced mass transfer reactor is arranged above the liquid level in the preliminary carbonization reaction tower. The outlet of the fifth enhanced mass transfer reactor is connected with a first connecting pipe, and 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 pipeline and the second conveying pipeline are both connected to the fourth enhanced mass transfer reactor.

6. The system according to claim 1, characterized in that The dust removal tower is provided with a sixth enhanced mass transfer reactor and a seventh enhanced mass transfer reactor, the sixth enhanced mass transfer reactor and the seventh enhanced mass transfer reactor are both 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 respectively arranged on opposite side walls in the dust removal tower; the sixth enhanced mass transfer reactor and the seventh enhanced mass transfer reactor are both connected to the exhaust gas pipeline; A sprayer is arranged in the dust removal tower, 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 is arranged between the sixth enhanced mass transfer reactor and the seventh enhanced mass transfer reactor in the horizontal direction.

7. The system according to claim 6, characterized in that An auxiliary dust collector is also provided in the dust removal tower, and the auxiliary dust collector is located between the sprayer and the sixth enhanced mass transfer reactor in the vertical direction; the auxiliary dust collector is in the shape of a cone which gradually decreases from top to bottom in the vertical direction, and the bottom opening of the auxiliary dust collector is located between the sixth enhanced mass transfer reactor and the seventh enhanced mass transfer reactor in the horizontal direction.

8. The system according to claim 1, characterized in that An eighth enhanced mass transfer reactor and a ninth enhanced mass transfer reactor are arranged in the oxidation reaction tower. The eighth enhanced mass transfer reactor and the ninth enhanced mass transfer reactor are both located below the liquid level in the oxidation reaction tower in the vertical direction; the eighth enhanced mass transfer reactor is located above the ninth enhanced mass transfer reactor in the vertical direction, and the outlets of the eighth enhanced mass transfer reactor and the ninth enhanced mass transfer reactor are opposite to each other; the eighth enhanced mass transfer reactor and the ninth enhanced mass transfer reactor are both connected with an oxidation gas pipeline.

9. The system according to any one of claims 1 to 8, characterized in that: The heat exchanger includes 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 to the oxidation reaction tower via the inner tube, and the exhaust gas pipeline is connected to 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 two adjacent baffles are staggered.

10. The system according to claim 9, characterized in that A thermal insulation plate is arranged in the heat exchange chamber, and the thermal insulation plate divides the heat exchange chamber into a first heat exchange chamber and a second heat exchange chamber along the material flow direction; the exhaust gas pipeline is connected to the dust removal tower via the first heat exchange chamber; the first conveying pipeline is connected to the preliminary carbonization reaction tower via the second heat exchange chamber.

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