A system and method for preparing heavy grade soda ash using a cogeneration coupling wind power supply

Abstract

The present application relates to the technical field of natural soda production, and in particular to a system and method for preparing heavy soda ash by using cogeneration coupled with wind power supply. The system for preparing heavy soda ash by using cogeneration coupled with wind power supply comprises a coal-fired cogeneration device, a wind power generation device and a heavy soda ash production system. The coal-fired cogeneration device is used to provide steam and electric energy. The wind power generation device is used to provide electric energy. The heavy soda ash production system uses the steam and electric energy provided by the coal-fired cogeneration device and the electric energy provided by the wind power generation device to produce heavy soda ash. The present application can solve the technical problems of large energy consumption and large carbon emissions in the existing natural soda production.

Description

Technical Field

[0001] This invention relates to the field of natural soda ash production technology, specifically to a system and method for preparing heavy soda ash using combined heat and power coupled with wind power. Background Technology

[0002] Natural soda ash is prepared using an evaporation method, with the core process being the evaporator. The evaporator utilizes the heat energy provided by steam to evaporate and concentrate the natural soda ash brine. When the brine concentration is greater than or equal to the solubility of sodium carbonate, sodium carbonate crystals precipitate out. After calcination, drying, and cooling, it becomes industrial soda ash, which is then packaged and sold. Currently, the evaporators used in Anpeng's natural soda ash processing in China are four-effect and five-effect evaporators, while those used in Tamusu's natural soda ash processing are multi-effect evaporators and MVR (Mechanical Vapor Recompression) technology. ① Multi-effect evaporators mainly utilize fresh steam provided by a boiler to heat and evaporate the brine; ② MVR mainly utilizes a high-efficiency compressor to compress steam, converting electrical energy into heat energy, improving the recycling of secondary steam heat, and eliminating the need for external fresh steam supply.

[0003] Natural alkali processing plants are high-energy-consuming enterprises, with the main energy consumption coming from the steam demand of the alkali processing technology, and a smaller portion from the electricity demand of the alkali processing equipment. Statistics show that the comprehensive energy consumption per ton of alkali is 335 kgce / ton. Currently, large-scale natural alkali processing plants both domestically and internationally all use coal-fired combined heat and power (CHP) technology to provide steam and electricity, such as the Kazan natural alkali processing project in Turkey and the Tamusu natural alkali processing project in China.

[0004] Cogeneration (CHP) is listed as an encouraged project in the "Guidance Catalogue for Industrial Structure Adjustment (2024 Edition)" and is widely used. However, its main drawback lies in carbon emissions. According to statistics, natural alkali processing projects using coal-fired CHP have approximately 0.91 tons of CO2-eq / ton of alkali produced. Based on a production capacity of one million tons of soda ash, the annual carbon emissions of a natural alkali processing plant are 910,000 tons of CO2-eq. Under the national policy of "peak carbon and carbon neutrality," this high carbon emission contradicts national policy, and using coal-fired CHP is insufficient to solve the carbon emission reduction problem. The purpose of this invention is to achieve carbon emission reduction in natural alkali processing plants by integrating a new low-carbon energy supply method with its matching natural alkali processing technology.

[0005] Patent CN110097475A discloses an economical electric thermal storage device control system and method. This patent application describes a method for absorbing wind and solar green electricity with the aim of optimal economic efficiency. However, the scale of this green electricity is insufficient to supply the entire energy demand of the heating unit. During off-peak hours at night, when electricity prices are low, the electric boiler purchases electricity from the main grid, and the electric thermal storage device stores the heat. This method does not consider 100% green electricity application scenarios, requiring supplemental grid power and failing to achieve zero carbon dioxide emissions.

[0006] Patent application CN107420969A discloses a high-efficiency off-peak electricity energy storage heating system and its control method. This patent application discloses a scheme that utilizes off-peak electricity at night to generate heat, and then stores the heat using electric thermal storage. It does not consider wind power integration, only the economics of off-peak electricity thermal storage, and its application scenario is heating; it does not consider the large-scale energy consumption scenario of natural alkali processing plants.

[0007] The invention patent with authorization announcement number CN101503204B discloses a process for producing alkali by wet decomposition and evaporation of NaHCO3 alkaline brine. This patent application discloses a technology for processing heavy soda ash using a four-effect five-body vacuum evaporation crystallization process. Because it uses a four-effect five-body vacuum evaporation crystallization process to achieve wet decomposition and evaporation concentration, which is completed in one piece of equipment, the wet decomposition process cannot be controlled, the wet decomposition rate is low, the yield of heavy soda ash is only 60%-70%, the energy supply method does not consider new energy sources, and the carbon emissions are large.

[0008] Patent application CN109809437A discloses a novel energy-saving and environmentally friendly process and system for producing heavy soda ash. This patent application discloses a two-stage wet decomposition tower and a monohydrate soda ash crystallizer for producing heavy soda ash. The steam used in the wet decomposition tower and monohydrate soda ash crystallizer is secondary steam, which is recycled by mechanically compressing the steam with a steam compressor to increase its temperature. Its main heat energy comes from the conversion of electrical energy into heat energy, and the amount of fresh steam used is relatively small. However, its energy supply method does not consider new energy sources, resulting in high carbon emissions.

[0009] Patent CN112850753B discloses a process for producing natural soda ash. This patent application describes a process for obtaining heavy soda ash through steps including leaching, pretreatment, stripping and concentration, crystallization and separation of sodium carbonate decahydrate, dissolution of sodium carbonate decahydrate, crystallization and separation of sodium carbonate monohydrate, and drying of sodium carbonate monohydrate. It employs a two-stage crystallization process (sodium carbonate decahydrate crystallization + sodium carbonate decahydrate dissolution + sodium carbonate monohydrate crystallization), resulting in high energy consumption and, since it does not consider renewable energy sources, significant carbon emissions. Summary of the Invention

[0010] In view of this, the present invention proposes a system and method for producing heavy soda ash using combined heat and power coupled with wind power, which can at least solve the technical problems of high energy consumption and high carbon emissions in the existing natural soda ash production.

[0011] The first aspect of this invention provides a system for producing heavy soda ash using a combined heat and power (CHP) system coupled with wind power, comprising: a coal-fired CHP unit, a wind power generation unit, and a heavy soda ash production system. The coal-fired CHP unit provides steam and electricity. The wind power generation unit provides electricity. The heavy soda ash production system uses the steam and electricity provided by the coal-fired CHP unit and the electricity provided by the wind power generation unit to produce heavy soda ash.

[0012] In some embodiments, the heavy soda ash production system employs an MVR evaporation and concentration process, wherein the compressor used in the MVR evaporation and concentration process is powered at least partially by electricity provided by a wind power generation unit.

[0013] In some embodiments, the compressor used in the MVR evaporation and concentration process is powered by electricity provided by a wind power generation unit and electricity provided by a coal-fired combined heat and power unit.

[0014] In some embodiments, the system for producing heavy soda ash using cogeneration coupled with wind power also includes an energy management system, which is communicatively connected to the coal-fired cogeneration unit and the wind power generation unit for allocating power between the two.

[0015] In some embodiments, the energy management system includes priority control logic configured to prioritize the use of electricity provided by wind power generation devices. When the electricity provided by wind power generation devices is insufficient to meet the demand, electricity provided by coal-fired cogeneration devices will be used instead.

[0016] In some embodiments, the energy management system includes a power generation monitoring module, a power consumption prediction module, and an energy distribution module; the power generation monitoring module is configured to monitor the power generation of the wind power generation device in real time; the power consumption prediction module is configured to predict the immediate and future energy demand of the heavy soda ash production system based on historical and real-time data; and the energy distribution module is configured to dynamically adjust the proportion of electricity obtained by the heavy soda ash production system from the coal-fired cogeneration unit according to the power generation of the wind power generation device and the predicted data of the heavy soda ash production system.

[0017] In some embodiments, the heavy soda ash production system includes a pretreatment module, a decomposition module, a crystallization module, and a posttreatment module. The pretreatment module is used to settle, filter, and adsorb impurities in the brine. The decomposition module is used to decompose sodium bicarbonate in the brine into sodium carbonate and concentrate the brine. The crystallization module is used to further evaporate and concentrate the concentrated brine to obtain brine. The posttreatment module is used to centrifuge, dry, and calcine the brine to obtain heavy soda ash products. The decomposition module, crystallization module, and post-processing module use steam provided by the coal-fired cogeneration unit, while the pre-processing module, crystallization module, and post-processing module use electricity provided by the coal-fired cogeneration unit and / or electricity provided by the wind power generation unit.

[0018] In some embodiments, the pretreatment module includes a brine settling tank, a multi-media filter, and a multi-stage activated carbon adsorption device to settle, filter, and adsorb impurities in the brine. The brine settling tank and the multi-media filter are connected by an auxiliary pump, which uses electricity provided by a coal-fired cogeneration unit and / or wind power generation unit.

[0019] In some embodiments, the decomposition module includes a primary stripping decomposition tower and a secondary stripping decomposition tower, which use steam provided by a coal-fired cogeneration unit to assist in decomposition and concentration.

[0020] In some embodiments, the crystallization module includes a multi-stage MVR, which uses steam provided by a coal-fired cogeneration unit when starting up, and the compressor of the multi-stage MVR uses electrical energy provided by the coal-fired cogeneration unit and / or electrical energy provided by a wind power generation unit.

[0021] In some embodiments, the post-processing module includes a centrifugal dryer and a fluidized bed calcination device, wherein the centrifugal dryer uses electrical energy provided by a coal-fired cogeneration unit and / or a wind power generation unit, and the fluidized bed calcination device uses steam provided by a coal-fired cogeneration unit.

[0022] In some embodiments, the system for producing heavy soda ash using combined heat and power coupled with wind power further includes an electric thermal storage device, which uses a portion of the electrical energy provided by the wind power generator to convert water into steam and supply it to the heavy soda ash production system.

[0023] A second aspect of this invention provides a method for preparing heavy soda ash using cogeneration coupled with wind power, comprising the following steps: Steam and electricity are generated through coal-fired combined heat and power (CHP) units; Electricity is generated through wind power generation devices; Steam and electricity generated by coal-fired cogeneration units, as well as electricity generated by wind power generation units, are supplied to the heavy soda ash production system to assist in the production of heavy soda ash.

[0024] In some embodiments, the heavy soda ash production system employs an MVR evaporation and concentration process, wherein the compressor used in the MVR evaporation and concentration process is powered at least partially by electricity generated by a wind power generation device.

[0025] In some embodiments, electricity generated by wind power generation is preferentially used to power the compressor used in the MVR evaporation and concentration process. When the electricity generated by wind power generation is insufficient to meet the demand, electricity generated by coal-fired cogeneration is used to power the compressor used in the MVR evaporation and concentration process.

[0026] In some embodiments, the method for producing heavy soda ash using combined heat and power coupled with wind power further includes: Real-time monitoring of wind power generation equipment output; Predict the immediate and future energy demand for heavy soda ash production based on historical and real-time data. Based on the power generation of the wind power generation unit and the predicted data of the heavy soda ash production system, the proportion of electricity obtained by the heavy soda ash production system from the coal-fired cogeneration unit is dynamically adjusted.

[0027] In some embodiments, steam generated by a coal-fired cogeneration unit is supplied to a heavy soda ash production system to assist in the production of heavy soda ash, including: Some of the steam is supplied to the decomposition module in the heavy soda ash production system to assist in the decomposition and concentration of the brine. Some of the steam is supplied to the crystallization module in the heavy soda ash production system to assist in the evaporation and crystallization of the brine. Some of the steam is supplied to the post-processing module within the heavy soda ash production system to assist in the high-temperature drying of the brine.

[0028] In some embodiments, the electricity generated by a coal-fired cogeneration unit and the electricity generated by a wind power generation unit are supplied to the heavy soda ash production system to assist in the production of heavy soda ash, including: The electricity generated by the coal-fired cogeneration unit and / or part of the electricity generated by the wind power generation unit is supplied to the pretreatment module in the heavy soda ash production system to assist in the sedimentation, filtration and impurity adsorption of the brine. The electricity generated by the coal-fired cogeneration unit and / or part of the electricity generated by the wind power generation unit is supplied to the crystallization module in the heavy soda ash production system to assist in the further evaporation and concentration of the concentrated brine. The electricity generated by the coal-fired cogeneration unit and / or part of the electricity generated by the wind power generation unit is supplied to the post-processing module in the heavy soda ash production system to assist in the centrifugation, drying and calcination of the brine.

[0029] In some embodiments, supplying electrical energy generated by a coal-fired cogeneration unit and / or a portion of the electrical energy generated by a wind power generation unit to a pretreatment module within a heavy soda ash production system includes: The electricity generated by the coal-fired cogeneration unit and / or part of the electricity generated by the wind power generation unit is supplied to the booster pump of the pretreatment module for auxiliary transportation. Supplying electricity generated by a coal-fired combined heat and power (CHP) unit and / or a portion of the electricity generated by a wind power unit to the crystallization module within the heavy soda ash production system includes: The electricity generated by the coal-fired cogeneration unit and / or part of the electricity generated by the wind power generation unit is supplied to the crystallization module of the multi-stage MVR. Supplying electrical energy generated by a coal-fired combined heat and power (CHP) unit and / or a portion of the electrical energy generated by a wind power unit to the post-processing module of the heavy soda ash production system includes: The electricity generated by the coal-fired cogeneration unit and / or part of the electricity generated by the wind power generation unit is supplied to the centrifugal dryer and fluidized bed calcination unit.

[0030] In some embodiments, a portion of the electrical energy generated by a wind power generation device is used to convert water into steam, and the steam is used to produce heavy soda ash.

[0031] The beneficial effects of this invention are as follows: The coal-fired cogeneration unit of this application can provide low-grade steam to the heavy soda ash production system, and the generated high-grade steam can be used for power generation, thereby realizing the cascade utilization of energy and significantly improving the comprehensive utilization rate of energy. Wind power, as a clean energy source, does not produce greenhouse gases or other pollutants during its power generation process, helping to reduce the carbon emissions of enterprises. At the same time, the coal-fired cogeneration unit provides backup power when wind power is insufficient, ensuring the continuity and stability of production, while also avoiding the high costs caused by energy shortages. The coal-fired cogeneration unit and wind power generation unit are coupled together; compared with traditional single power generation methods, this combined production method can more effectively utilize the heat in the fuel, reduce carbon emissions, and avoid energy waste. Attached Figure Description

[0032] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other embodiments can be obtained based on these drawings without creative effort.

[0033] Figure 1 This is a schematic diagram of a system for producing heavy soda ash using cogeneration coupled with wind power, provided in one embodiment of the present invention. Figure 2 This is a flowchart of a method for preparing heavy soda ash using combined heat and power coupled with wind power, provided as an embodiment of the present invention.

[0034] Explanation of reference numerals in the attached figures: 1. Brine settling tank; 2. Booster pump; 3. Multi-media filter; 4. Primary activated carbon adsorption tank; 5. Secondary activated carbon adsorption tank; 6. Primary stripping decomposition tower; 7. Secondary stripping decomposition tower; 8. Primary MVR; 9. Secondary MVR; 10. Centrifugal dryer; 11. Fluidized bed calcination device. Detailed Implementation

[0035] To make the objectives, technical solutions, and advantages of the present invention clearer, the embodiments of the present invention will be further described in detail below with reference to specific examples and the accompanying drawings.

[0036] It should be noted that all uses of "first" and "second" in the embodiments of the present invention are for the purpose of distinguishing two entities or parameters with the same name but different names. It is clear that "first" and "second" are only for the convenience of expression and should not be construed as limiting the embodiments of the present invention. Subsequent embodiments will not explain this in detail.

[0037] The first aspect of this invention provides a system for producing heavy soda ash using a combined heat and power (CHP) system coupled with wind power, comprising: a coal-fired CHP unit, a wind power generation unit, and a heavy soda ash production system. The coal-fired CHP unit provides steam and electricity. The wind power generation unit provides electricity. The heavy soda ash production system uses the steam and electricity provided by the coal-fired CHP unit and the electricity provided by the wind power generation unit to produce heavy soda ash.

[0038] Specifically, the coal-fired cogeneration unit of this application can supply low-grade steam to the heavy soda ash production system, while the generated high-grade steam can be used for power generation, thereby achieving cascaded energy utilization and significantly improving the overall energy utilization rate. Wind power, as a clean energy source, does not produce greenhouse gases or other pollutants during its power generation process, helping to reduce the company's carbon emissions. Simultaneously, the coal-fired cogeneration unit provides backup power when wind power is insufficient, ensuring the continuity and stability of production, while also avoiding the high costs caused by energy shortages. The coupling of the coal-fired cogeneration unit with wind power generation, compared to traditional single power generation methods, allows for more efficient utilization of the heat in the fuel, reducing carbon emissions and avoiding energy waste.

[0039] In some embodiments, the heavy soda ash production system employs an MVR (Multi-Effect Vapor Reduction) evaporation and concentration process, where the compressor is powered at least partially by electricity generated by a wind power plant. Specifically, the MVR evaporation and concentration process primarily utilizes electricity to evaporate, concentrate, and crystallize brine, while traditional multi-effect evaporation mainly uses steam. By replacing multi-effect evaporation (four-effect or five-effect evaporators) with the MVR evaporation and concentration process, steam consumption can be reduced while electricity consumption can be increased. In this application, the compressor in the MVR evaporation and concentration process uses at least partially green electricity provided by a wind farm, which reduces carbon emissions and is more energy-efficient and environmentally friendly.

[0040] In some embodiments, the compressor used in the MVR evaporation concentration process is powered by electricity generated by wind power and by a coal-fired cogeneration unit. Wind power is a renewable energy source, helping to reduce dependence on fossil fuels. The coal-fired cogeneration unit provides a stable power supply, ensuring the continuous operation of the MVR system. By combining the two, the intermittent nature of wind power generation can be compensated for by the stability of the coal-fired cogeneration, guaranteeing the stable operation of the MVR system. Compared to traditional single-power generation methods, this approach more effectively improves overall energy efficiency, reduces carbon emissions, and avoids energy waste.

[0041] In some embodiments, the system for producing heavy soda ash using combined heat and power (CHP) coupled with wind power also includes an energy management system (EMS). The EMS is communicatively connected to both the coal-fired CHP unit and the wind power generation unit, and is used to allocate the power supply from both. By setting the EMS to rationally allocate the power supply ratio between the coal-fired CHP and wind power generation, the system's regulation capability can be improved, thereby better absorbing wind power. Furthermore, the EMS can dynamically adjust the output of the coal-fired CHP unit based on the uncertainty of wind power output, reducing wind curtailment caused by wind power fluctuations.

[0042] In some embodiments, the energy management system includes priority control logic configured to prioritize the use of electricity provided by wind power generation units. Only when the electricity provided by wind power generation units is insufficient to meet demand will electricity from coal-fired combined heat and power (CHP) units be used. By prioritizing wind power generation, the utilization of renewable energy can be maximized, reducing dependence on fossil fuels. This not only helps reduce operating costs but also reduces carbon emissions, meeting environmental protection and sustainable development requirements. The EMS can monitor and analyze the usage of various energy sources in real time. Through priority control logic, energy can be allocated and utilized more effectively, avoiding energy waste and improving energy efficiency while reducing overall energy consumption.

[0043] In some embodiments, the energy management system includes a power generation monitoring module, a power consumption forecasting module, and an energy allocation module. The power generation monitoring module is configured to monitor the power generation of the wind power generation unit in real time, ensuring maximum utilization of renewable energy. The power consumption forecasting module is configured to predict the immediate and future energy needs of the heavy soda ash production system based on historical and real-time data, making energy allocation more accurate and avoiding energy waste. The energy allocation module is configured to dynamically adjust the proportion of electricity obtained by the heavy soda ash production system from the coal-fired combined heat and power unit based on the power generation of the wind power generation unit and the forecast data of the heavy soda ash production system. Intelligent scheduling reduces unnecessary energy expenditures, further lowering overall operating costs, and ensures the stable operation of the heavy soda ash production system.

[0044] In some embodiments, the heavy soda ash production system includes a pretreatment module, a decomposition module, a crystallization module, and a posttreatment module. The pretreatment module is used to settle, filter, and adsorb impurities in the brine. The decomposition module is used to decompose sodium bicarbonate in the brine into sodium carbonate and concentrate the brine. The crystallization module is used to further evaporate and concentrate the concentrated brine to obtain brine. The posttreatment module is used to centrifuge, dry, and calcine the brine to obtain heavy soda ash product.

[0045] The decomposition, crystallization, and post-processing modules utilize steam supplied by a coal-fired cogeneration unit, while the pre-processing, crystallization, and post-processing modules utilize electricity supplied by the coal-fired cogeneration unit and / or wind power generation. In the heavy soda ash production system, the decomposition and crystallization modules, powered by steam from the coal-fired cogeneration unit, effectively decompose sodium bicarbonate and concentrate the brine. The use of steam ensures the high-temperature requirements of the production process, improving the efficiency and speed of the chemical reactions. The pre-processing, crystallization, and post-processing modules, powered by electricity, allow for flexible adjustment of equipment operation to meet different production needs.

[0046] In some embodiments, such as Figure 1 As shown, the pretreatment module includes a brine settling tank 1, a multi-media filter 3, and a multi-stage activated carbon adsorption device to settle, filter, and adsorb impurities in the brine, removing suspended solids and TOC (total organic carbon) to obtain refined brine, thereby improving its purity and ensuring the quality of the final product. A booster pump 2 provides auxiliary transport between the brine settling tank 1 and the multi-media filter 3, using electricity provided by a coal-fired cogeneration unit and / or a wind power generation unit. Specifically, the multi-stage activated carbon adsorption device includes a primary activated carbon adsorption tank 4 and a secondary activated carbon adsorption tank 5 connected in series, utilizing the adsorption properties of activated carbon to remove organic matter, odors, and residual chlorine from the brine.

[0047] In some embodiments, the decomposition module includes a primary stripping decomposition tower 6 and a secondary stripping decomposition tower 7, which use steam provided by a coal-fired cogeneration unit to assist in decomposition and concentration. Specifically, the refined brine is preheated and then fed to the primary stripping decomposition tower 6, where primary wet decomposition and concentration are performed. Part of the NaHCO3 decomposes to generate Na2CO3, CO2, and H2O. When the primary wet decomposition rate reaches 50%-60%, primary wet decomposition concentrated brine is obtained. The primary wet decomposition concentrated brine is then fed to the secondary stripping decomposition tower 7, where secondary wet decomposition and concentration are performed to obtain secondary wet decomposition concentrated brine. Subsequently, NaOH solution is added to the discharged secondary wet decomposition concentrated brine. The NaOH reacts with the NaHCO3 in the secondary wet decomposition concentrated brine to generate Na2CO3, resulting in highly saturated concentrated brine whose main component is Na2CO3.

[0048] In some embodiments, the crystallization module includes a multi-stage MVR. The multi-stage MVR uses steam provided by a coal-fired cogeneration unit during startup, and its compressor uses electrical energy provided by the coal-fired cogeneration unit and / or a wind power generation unit. Specifically, the multi-stage MVR includes a first-stage MVR8 and a second-stage MVR9 connected in sequence. These utilize steam to heat a highly saturated concentrated brine whose main component is Na2CO3, further evaporating and concentrating it. Na2CO3 monohydrate (Na2CO3•H2O) crystallizes out of the highly saturated concentrated brine, yielding a concentrated crystallization solution.

[0049] In some embodiments, the post-processing module includes a centrifugal dryer 10 and a fluidized bed calcination device 11. The centrifugal dryer 10 uses electrical energy provided by a coal-fired cogeneration unit and / or a wind power generation unit, while the fluidized bed calcination device 11 uses steam provided by the coal-fired cogeneration unit. Specifically, the resulting concentrated crystallization solution containing sodium carbonate monohydrate (Na2CO3·H2O) and mother liquor is transferred together with the mother liquor to the centrifugal dryer 10. In the centrifugal dryer 10, the solid and liquid are separated by centrifugal force generated by high-speed rotation, yielding sodium carbonate monohydrate filter cake (solid) and mother liquor (liquid). The sodium carbonate monohydrate filter cake obtained by centrifugal drying is transferred to the fluidized bed calcination device 11. In the fluidized bed calcination device 11, high-temperature air or superheated steam is introduced to remove moisture from the sodium carbonate monohydrate filter cake, while a decomposition reaction occurs, converting Na2CO3·H2O into Na2CO3. After calcination and dehydration, heavy soda ash product is obtained.

[0050] In some embodiments, the system for producing heavy soda ash using combined heat and power coupled with wind power further includes an electric thermal storage device. This device uses a portion of the electricity provided by the wind power generator to convert water into steam, which is then supplied to the heavy soda ash production system. By coupling with the wind power generator, the electric thermal storage device can convert electrical energy into heat energy and store it when the wind power supply is sufficient (e.g., during off-peak hours at night), then release it during peak hours or when needed. This effectively improves energy utilization efficiency and helps balance grid load, reducing electricity waste. As a backup heat source, the electric thermal storage device can provide a stable heat supply when the coal-fired combined heat and power unit fails or is under maintenance, ensuring the continuous operation of the heavy soda ash production system and enhancing the stability and reliability of the entire production system.

[0051] A second aspect of this invention provides a method for preparing heavy soda ash using cogeneration coupled with wind power, comprising the following steps: Steam and electricity are generated through coal-fired combined heat and power (CHP) units; Electricity is generated through wind power generation devices; Steam and electricity generated by coal-fired cogeneration units, as well as electricity generated by wind power generation units, are supplied to the heavy soda ash production system to assist in the production of heavy soda ash.

[0052] This application achieves comprehensive utilization of multiple energy forms by combining a coal-fired cogeneration unit and a wind power generation unit. The coal-fired cogeneration unit generates electricity and also produces steam as a byproduct, while the wind power generation unit provides additional electricity. This multi-source power supply method allows for more efficient use of energy.

[0053] In some embodiments, the heavy soda ash production system employs an MVR evaporation and concentration process, wherein the compressor used in the MVR evaporation and concentration process is powered at least partially by electricity generated by a wind power generation device.

[0054] In some embodiments, electricity generated by wind power generation is preferentially used to power the compressors used in the MVR evaporation and concentration process. When the electricity generated by wind power generation is insufficient to meet demand, electricity generated by a coal-fired cogeneration unit is then used to power the compressors in the MVR evaporation and concentration process. By prioritizing the use of wind power, the utilization of renewable energy can be maximized, reducing dependence on fossil fuels. This not only helps reduce operating costs but also reduces carbon emissions, meeting the requirements of environmental protection and sustainable development.

[0055] In some embodiments, the method for producing heavy soda ash using combined heat and power coupled with wind power further includes: Real-time monitoring of wind power generation to ensure maximum utilization of renewable energy; Predicting the immediate and future energy needs for heavy soda ash production based on historical and real-time data enables more precise energy allocation and avoids energy waste. Based on the power generation of the wind power generation unit and the forecast data of the heavy soda ash production system, the proportion of electricity obtained by the heavy soda ash production system from the coal-fired cogeneration unit is dynamically adjusted to reduce unnecessary energy expenditures, further reduce overall operating costs, and ensure the stable operation of the heavy soda ash production system.

[0056] In some embodiments, steam generated by a coal-fired cogeneration unit is supplied to a heavy soda ash production system to assist in the production of heavy soda ash, including: Some of the steam is supplied to the decomposition module in the heavy soda ash production system to assist in the decomposition and concentration of the brine, thereby accelerating the chemical reaction and improving production efficiency. Some of the steam is supplied to the crystallization module in the heavy soda ash production system to assist in the evaporation and crystallization of the brine. Some of the steam is supplied to the post-processing module within the heavy soda ash production system to assist in the high-temperature drying of the brine.

[0057] In some embodiments, the electricity generated by a coal-fired cogeneration unit and the electricity generated by a wind power generation unit are supplied to the heavy soda ash production system to assist in the production of heavy soda ash, including: The electricity generated by the coal-fired cogeneration unit and / or part of the electricity generated by the wind power generation unit is supplied to the pretreatment module in the heavy soda ash production system to assist in the sedimentation, filtration and impurity adsorption of the brine. The electricity generated by the coal-fired cogeneration unit and / or part of the electricity generated by the wind power generation unit is supplied to the crystallization module in the heavy soda ash production system to assist in the further evaporation and concentration of the concentrated brine. The electricity generated by the coal-fired cogeneration unit and / or part of the electricity generated by the wind power generation unit is supplied to the post-processing module in the heavy soda ash production system to assist in the centrifugation, drying and calcination of the brine.

[0058] In some embodiments, supplying electrical energy generated by a coal-fired cogeneration unit and / or a portion of electrical energy generated by a wind power generation unit to a pretreatment module within a heavy soda ash production system includes: supplying a booster pump to the pretreatment module for auxiliary conveying of electrical energy generated by the coal-fired cogeneration unit and / or a portion of electrical energy generated by the wind power generation unit.

[0059] Supplying electricity generated by a coal-fired cogeneration unit and / or a portion of the electricity generated by a wind power generation unit to the crystallization module within a heavy soda ash production system includes: supplying electricity generated by a coal-fired cogeneration unit and / or a portion of the electricity generated by a wind power generation unit to the crystallization module via a multi-stage MVR.

[0060] Supplying the electrical energy generated by the coal-fired cogeneration unit and / or a portion of the electrical energy generated by the wind power generation unit to the post-processing module within the heavy soda ash production system includes: supplying the electrical energy generated by the coal-fired cogeneration unit and / or a portion of the electrical energy generated by the wind power generation unit to the centrifugal dryer and the fluidized bed calcination unit.

[0061] In some embodiments, a portion of the electrical energy generated by a wind power plant is used to convert water into steam, and the steam is then used to produce heavy soda ash. By converting wind energy into electrical energy, and then using the electrical energy to heat water to generate steam, electrical energy can be converted into heat energy and stored when the power supply of the wind power plant is sufficient (such as during off-peak hours at night), and then released during peak hours or when needed. This effectively improves energy utilization efficiency, helps balance grid load, reduces electricity waste, and enhances the stability and reliability of the entire production system.

[0062] The following description, using the aforementioned system for producing heavy soda ash via cogeneration coupled with wind power, further illustrates the process of preparing heavy soda ash in the heavy soda ash production system of this application. Figure 2 As shown, it mainly includes the following steps: S1, refined brine: The extracted brine first enters brine settling tank 1 for preliminary settling treatment to remove solid impurities and suspended matter.

[0063] After settling, the brine is pumped to a multi-media filter 3 via a booster pump 2 for further filtration to remove finer particles and impurities.

[0064] Next, the brine enters the primary activated carbon adsorption tank 4 and the secondary activated carbon adsorption tank 5 in sequence, using the adsorption properties of activated carbon to remove organic matter, odors and residual chlorine from the brine.

[0065] S2, wet decomposition and concentration: After being refined and preheated, the brine is sent to the primary stripping decomposition tower 6 for primary wet decomposition and concentration. Part of the NaHCO3 decomposes to form Na2CO3, CO2, and H2O. When the primary wet decomposition rate reaches 50%-60%, primary wet decomposition concentrated brine is obtained.

[0066] The primary wet decomposition concentrated brine is fed to the secondary stripping decomposition tower 7, where secondary wet decomposition and concentration are carried out to obtain secondary wet decomposition concentrated brine. Then, NaOH solution is added to the discharged secondary wet decomposition concentrated brine. The NaOH reacts with the NaHCO3 in the secondary wet decomposition concentrated brine to form Na2CO3, resulting in highly saturated concentrated brine whose main component is Na2CO3.

[0067] S3, further evaporation and concentration: The highly saturated concentrated brine is sequentially transported to the first-stage MVR8 and the second-stage MVR9. The highly saturated concentrated brine, whose main component is Na2CO3, is heated by steam to further evaporate and concentrate it. The Na2CO3 in the highly saturated concentrated brine crystallizes out as alkali monohydrate (Na2CO3•H2O) to obtain a concentrated crystallized solution.

[0068] S4, centrifugal drying: The resulting concentrated crystallization solution containing sodium hydroxide monohydrate (Na2CO3·H2O) and mother liquor is transferred together with the mother liquor to centrifugal dryer 10. In centrifugal dryer 10, the solid and liquid are separated by centrifugal force generated by high-speed rotation, yielding sodium hydroxide monohydrate filter cake (solid) and mother liquor (liquid).

[0069] S5, calcination and dehydration: The monohydrate soda ash filter cake obtained by centrifugal drying is transferred to a fluidized bed calcination apparatus 11. In the fluidized bed calcination apparatus 11, high-temperature air or superheated steam is introduced to remove moisture from the monohydrate soda ash filter cake, while a decomposition reaction occurs, converting Na₂CO₃·H₂O to Na₂CO₃. After calcination and dehydration, heavy soda ash product is obtained.

[0070] This invention takes a 5 million tons / year natural soda ash processing project as an example, and further describes the scheme of this application by combining a system for producing heavy soda ash using cogeneration coupled with wind power: The required fresh steam volume for the two-stage stripping decomposition tower and MVR startup is 757 t / h, which translates to a heat load of 530 MW and an electrical load of 260 MW, with an electrification rate of 32.9%.

[0071] One new coal-fired combined heat and power (CHP) unit with an installed capacity of 160MW will be constructed, providing 6 million tons of steam annually and generating 526 million kWh of electricity annually. One new wind power plant with an installed capacity of 500MW will also be constructed, generating 1.602 billion kWh of electricity annually. Each kWh of wind power can reduce carbon emissions by 0.785 kg. Calculations show that the natural alkali processing plant's annual use of 1.602 billion kWh of wind power can reduce carbon emissions by 1.25757 million tons. If the 5 million tons / year of natural alkali produced entirely by the coal-fired CHP unit were used, the processing plant would generate an average of 4.55 million tons of carbon emissions annually. Therefore, the CHP coupled with wind power used in this application for natural alkali processing can reduce carbon emissions by 27.6%.

[0072] The technical features of the above embodiments can be combined in any way. For the sake of brevity, not all possible combinations of the technical features in the above embodiments are described. However, as long as there is no contradiction in the combination of these technical features, they should be considered to be within the scope of this specification.

[0073] The embodiments described above are merely illustrative of several implementation methods of this application, and while the descriptions are relatively specific and detailed, they should not be construed as limiting the scope of the invention patent. It should be noted that those skilled in the art can make various modifications and improvements without departing from the concept of this application, and these all fall within the protection scope of this application. Therefore, the protection scope of this patent application should be determined by the appended claims.

Claims

1. A system for producing heavy soda ash using combined heat and power coupled with wind power, characterized in that, include: A coal-fired cogeneration unit, wherein the coal-fired cogeneration unit is used to provide steam and electricity; A wind power generation device, wherein the wind power generation device is used to provide electrical energy; A heavy soda ash production system that uses steam and electricity provided by the coal-fired cogeneration unit and electricity provided by the wind power generation unit to produce heavy soda ash.

2. The system for producing heavy soda ash using cogeneration coupled with wind power as described in claim 1, characterized in that, The heavy soda ash production system adopts the MVR evaporation and concentration process, and the compressor used in the MVR evaporation and concentration process is powered at least partially by the electricity provided by the wind power generation device.

3. The system for producing heavy soda ash using cogeneration coupled with wind power as described in claim 2, characterized in that, The compressor used in the MVR evaporation and concentration process is powered by electricity provided by the wind power generation unit and the coal-fired cogeneration unit.

4. The system for producing heavy soda ash using cogeneration coupled with wind power as described in claim 1, characterized in that, It also includes an energy management system, which is communicatively connected to the coal-fired cogeneration unit and the wind power generation unit, and is used to allocate the power supply of both.

5. The system for producing heavy soda ash using cogeneration coupled with wind power as described in claim 4, characterized in that, The energy management system is equipped with priority control logic, which is configured to prioritize the use of electrical energy provided by the wind power generation device. When the electrical energy provided by the wind power generation device is insufficient to meet the demand, the electrical energy provided by the coal-fired cogeneration device will be used.

6. The system for producing heavy soda ash using cogeneration coupled with wind power as described in claim 4, characterized in that, The energy management system includes a power generation monitoring module, a power consumption prediction module, and an energy distribution module. The power generation monitoring module is configured to monitor the power generation of the wind power generation device in real time. The power consumption prediction module is configured to predict the immediate and future energy demand of the heavy soda ash production system based on historical and real-time data. The energy distribution module is configured to dynamically adjust the proportion of electricity obtained by the heavy soda ash production system from the coal-fired cogeneration unit according to the power generation of the wind power generation device and the predicted data of the heavy soda ash production system.

7. The system for producing heavy soda ash using cogeneration coupled with wind power as described in claim 1, characterized in that, The heavy soda ash production system includes a pretreatment module, a decomposition module, a crystallization module, and a post-treatment module. The pretreatment module is used for sedimentation, filtration, and impurity adsorption of the brine. The decomposition module is used to decompose sodium bicarbonate in the brine into sodium carbonate and concentrate the brine. The crystallization module is used to further evaporate and concentrate the concentrated brine to obtain a brine stock. The post-treatment module is used to centrifuge, dry, and calcine the brine stock to obtain the heavy soda ash product. The decomposition module, the crystallization module, and the post-processing module use steam provided by the coal-fired cogeneration unit, while the pre-processing module, the crystallization module, and the post-processing module use electrical energy provided by the coal-fired cogeneration unit and / or electrical energy provided by the wind power generation unit.

8. The system for producing heavy soda ash using cogeneration coupled with wind power as described in claim 7, characterized in that, The pretreatment module includes a brine settling tank, a multi-media filter, and a multi-stage activated carbon adsorption device to settle, filter, and adsorb impurities in the brine. The brine settling tank and the multi-media filter are connected by an auxiliary pump, which uses electricity provided by the coal-fired cogeneration unit and / or the wind power generation unit.

9. The system for producing heavy soda ash using cogeneration coupled with wind power as described in claim 7, characterized in that, The decomposition module includes a primary stripping decomposition tower and a secondary stripping decomposition tower, which use steam provided by the coal-fired cogeneration unit to assist in decomposition and concentration.

10. The system for producing heavy soda ash using cogeneration coupled with wind power as described in claim 7, characterized in that, The crystallization module includes a multi-stage MVR. When the multi-stage MVR starts up, it uses steam provided by the coal-fired cogeneration unit. The compressor of the multi-stage MVR uses electrical energy provided by the coal-fired cogeneration unit and / or electrical energy provided by the wind power generation unit.

11. The system for producing heavy soda ash using cogeneration coupled with wind power as described in claim 7, characterized in that, The post-processing module includes a centrifugal dryer and a fluidized bed calcination device. The centrifugal dryer uses electrical energy provided by the coal-fired cogeneration unit and / or the wind power generation unit, and the fluidized bed calcination device uses steam provided by the coal-fired cogeneration unit.

12. The system for producing heavy soda ash using cogeneration coupled with wind power as described in claim 1, characterized in that, It also includes an electric thermal energy storage device, which uses a portion of the electrical energy provided by the wind power generation device to convert water into steam and supply it to the heavy soda ash production system.

13. A method for producing heavy soda ash using combined heat and power coupled with wind power, characterized in that, Includes the following steps: Steam and electricity are generated through coal-fired combined heat and power (CHP) units; Electricity is generated through wind power generation devices; The steam and electricity generated by the coal-fired cogeneration unit and the electricity generated by the wind power generation unit are supplied to the heavy soda ash production system to assist in the production of heavy soda ash.

14. The method for preparing heavy soda ash using cogeneration coupled with wind power according to claim 13, characterized in that, The heavy soda ash production system adopts the MVR evaporation and concentration process, and the compressor used in the MVR evaporation and concentration process is powered at least partially by the electricity generated by the wind power generation device.

15. The method for producing heavy soda ash using cogeneration coupled with wind power according to claim 14, characterized in that, The power generated by the wind power generation device is used first to power the compressor used in the MVR evaporation and concentration process. When the power generated by the wind power generation device is insufficient to meet the demand, the power generated by the coal-fired cogeneration device is used to power the compressor used in the MVR evaporation and concentration process.

16. The method for preparing heavy soda ash using cogeneration coupled with wind power according to claim 13, characterized in that, Also includes: Real-time monitoring of the power generation of the wind power generation device; Predict the immediate and future energy demand for heavy soda ash production based on historical and real-time data. Based on the power generation of the wind power generation device and the predicted data of the heavy soda ash production system, the proportion of electricity obtained by the heavy soda ash production system from the coal-fired cogeneration device is dynamically adjusted.

17. The method for preparing heavy soda ash using cogeneration coupled with wind power according to claim 13, characterized in that, The steam generated by the coal-fired cogeneration unit is supplied to the heavy soda ash production system to assist in the production of heavy soda ash, including: A portion of the steam is supplied to the decomposition module within the heavy soda ash production system to assist in the decomposition and concentration of the brine. Some of the steam is supplied to the crystallization module in the heavy soda ash production system to assist in the evaporation and crystallization of the brine. Some of the steam is supplied to the post-processing module within the heavy soda ash production system to assist in the high-temperature drying of the brine.

18. The method for preparing heavy soda ash using cogeneration coupled with wind power according to claim 17, characterized in that, The electricity generated by the coal-fired cogeneration unit and the electricity generated by the wind power generation unit are supplied to the heavy soda ash production system to assist in the production of heavy soda ash, including: The electrical energy generated by the coal-fired cogeneration unit and / or part of the electrical energy generated by the wind power generation unit are supplied to the pretreatment module in the heavy soda ash production system to assist in the sedimentation, filtration and impurity adsorption of the brine. The electrical energy generated by the coal-fired cogeneration unit and / or part of the electrical energy generated by the wind power generation unit is supplied to the crystallization module in the heavy soda ash production system to assist in the further evaporation and concentration of the concentrated brine. The electrical energy generated by the coal-fired cogeneration unit and / or part of the electrical energy generated by the wind power generation unit is supplied to the post-processing module in the heavy soda ash production system to assist in the centrifugation, drying and calcination of the brine.

19. The method for preparing heavy soda ash using cogeneration coupled with wind power according to claim 13, characterized in that, The process of supplying electrical energy generated by the coal-fired cogeneration unit and / or a portion of the electrical energy generated by the wind power generation unit to the pretreatment module within the heavy soda ash production system includes: The electrical energy generated by the coal-fired cogeneration unit and / or part of the electrical energy generated by the wind power generation unit are supplied to the booster pump of the pretreatment module for auxiliary transportation. Supplying the electrical energy generated by the coal-fired cogeneration unit and / or a portion of the electrical energy generated by the wind power generation unit to the crystallization module within the heavy soda ash production system includes: The electrical energy generated by the coal-fired cogeneration unit and / or part of the electrical energy generated by the wind power generation unit are supplied to the multi-stage MVR of the crystallization module; The process of supplying electrical energy generated by the coal-fired cogeneration unit and / or a portion of the electrical energy generated by the wind power generation unit to the post-processing module within the heavy soda ash production system includes: The electrical energy generated by the coal-fired cogeneration unit and / or a portion of the electrical energy generated by the wind power generation unit are supplied to the centrifugal dryer and the fluidized bed calcining unit.

20. The method for preparing heavy soda ash using cogeneration coupled with wind power according to claim 13, characterized in that, A portion of the electrical energy generated by the wind power generation device is used to convert water into steam, and the steam is used to produce heavy soda ash.

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