Seawater concentration bromine extraction process system driven by carbon neutralization energy power system

Abstract

The invention discloses a seawater concentration bromine extraction process system driven by a carbon neutralization energy power system, and belongs to the technical field of salt chemical industry and new energy. By adopting various brand-new waste heat deep recovery process methods and special equipment, waste heat resources, including waste heat of high-temperature waste liquid of a bromine extraction distillation section, of all process sections of a whole plant are recovered to the maximum extent and are used for process heating, and the load demand of an external heat source is greatly reduced by 70%-90%; steam is produced by a boiler through high-temperature SO2 flue gas waste heat of a sulfur incinerator, steam is produced by bromine steam discharged by a bromine extraction distillation tower through a high-temperature condensation waste heat heat pump, and heating steam supply and liquid chlorine gasification heat source requirements of the bromine extraction distillation tower are met in modes of electric heating, boiler steam production and the like based on photovoltaic, wind power and other new energy power generation; and the original boiler steam production and fossil fuel consumption are completely replaced, so that the original boiler is converted into an emergency standby heat source, a seawater concentration bromine extraction process driven by a carbon neutralization energy power system is realized, and the energy operation cost is remarkably reduced.

Description

Technical Field

[0001] The present invention relates to a seawater concentration and bromine extraction process system driven by a carbon-neutral energy power system, and belongs to the field of salt chemical industry and new energy technology. Background Art

[0002] Under the background of the dual carbon policy, various economic and industrial sectors have developed and adopted suitable energy-saving and emission reduction technologies to ultimately achieve the goal of carbon neutrality. In particular, many industrial enterprises that require more thermal energy to drive need to fundamentally seek technical approaches and methods to achieve carbon neutrality. The "new energy revolution" has become an inevitable choice for the development of the times. Against the background of this major trend in the development of the industry, the salt chemical industry has also begun to explore possible carbon neutrality implementation paths. This patent aims to shut down the steam boiler in the seawater concentration and bromine extraction production workshop, and achieve a new energy supply and drive system by significantly adjusting the energy production and use methods, building a new thermal process, and using new energy electric drive, and enter the carbon neutral era.

[0003] The basic principles, process flow, energy production, distribution, use and discharge of bromine extraction from seawater concentration are briefly introduced as follows.

[0004] Salt chemical plants based on seawater salt production can extract bromine, lithium and other substances from seawater or concentrated bittern after salt production. The basic principle of the commonly used "chlorine oxidation air blowing method to produce bromine" is as follows.

[0005] Under acidic conditions, using chlorine as an oxidant, bromide ions (Br-) are oxidized into bromine molecules (Br2), and the ion reaction equation is as follows.

[0006] 2Br-+Cl2= Br2+2 Cl-.

[0007] The free bromine is blown out with air, so it is called the air blowing method.

[0008] Acidic bromine production uses sulfur dioxide as the absorbent and fresh water spray to assist in absorbing the mixture of air and bromine. The absorbed liquid is called primary acid. The chemical reaction formula is as follows.

[0009] Br2+SO2+2H2O=2HBr+H2SO4.

[0010] Chlorine gas is passed into the primary acid for oxidation, bromine is liberated again, and hydrochloric acid is generated. The chemical reaction formula is as follows.

[0011] 2HBr+Cl2=2HCl+Br2.

[0012] Finally, the bromine is distilled out with water vapor and separated by condensation to obtain the finished bromine.

[0013] The process flow is described as follows.

[0014] Seawater (brine) is pumped to the blow-out tower, and dilute acid and chlorine are added to the outlet pipe of the pump. The mixed acidified chlorinated brine is sprayed down from the top of the blow-out tower, and the blower blows air from the bottom of the tower. When the brine contacts the air, the free bromine in the brine is resolved and blown out. The blown waste liquid is discharged from the bottom of the blow-out tower and enters the salt field for drying. The mixed gas discharged from the top of the blow-out tower is sent to the absorption tower, where it is mixed and absorbed by sulfur dioxide and water mist. The finished liquid formed is called primary acid, which is collected in the acid storage tank. The air purified by the foam collector is blown by the blower and enters the bottom of the blow-out tower for recycling in the system. The primary acid is added from the top of the distillation tower, and water vapor and chlorine are introduced from the bottom of the tower. When the primary acid flows from top to bottom along the filler, it contacts the chlorine and water vapor from bottom to top, and is continuously oxidized and distilled. The mixed gas of bromine and water vapor is discharged from the top of the tower, separated by condensation, and liquid bromine is obtained. The crude bromine water returns to the absorption tower for continuous circulation.

[0015] Among them, chlorine is usually produced by gasifying liquid chlorine in a water bath. The process method is as follows: liquid chlorine is sent into a water bath bottle, the bottle mouth of which is tightly connected to the chlorine clamp, the chlorine water bath is filled with water and steam is used to heat the water in the tank, and the temperature is controlled at 75°C-83°C by a solenoid valve. This temperature range can realize the gasification of liquid chlorine and avoid the formation of nitrogen trichloride explosives, and the gasified chlorine is supplied.

[0016] The preparation process of SO2 gas is as follows: sulfur enters the sulfur combustion furnace through a distributor, and burns with oxygen in the blown air at high temperature to generate sulfur dioxide gas. After air cooling and circulating water washing cooling, the temperature is controlled below 70°C, and then enters the blowing and absorption tower for reduction absorption to produce bromine production complete liquid.

[0017] The bromine extraction distillation process is as follows: after the completed liquid is preheated by the recovered liquid, it enters the distillation tower to be oxidized by chlorine gas, and water vapor distillation is carried out at the same time, the bromine is evaporated, and the top temperature of the tower is controlled at 80-90°C. After condensation, crude bromine is obtained. The bromine recovery liquid is cooled by brine heat exchange and enters the collection tank, and then used for brine acidification.

[0018] There is obvious energy waste in the above-mentioned traditional seawater bromine extraction process. For example, the high-temperature flue gas (up to 600-700°C) produced when preparing SO2 gas in a sulfur combustion furnace is usually not recycled due to its strong corrosiveness and small flue gas volume, but directly enters the water washing tower for spraying and cooling to 50-60°C; and the discharged waste sulfuric acid liquid SH1 is usually not recycled due to its extremely strong corrosiveness, small flow rate and low temperature grade, and is ultimately wasted; although the bromine recovery liquid discharged from the bromine extraction distillation tower is usually equipped with a special heat exchanger to recover part of the waste heat, the original special heat exchanger has poor heat transfer performance and high cost, and the waste heat recovery amount is relatively small, so that the discharge temperature of the bromine recovery liquid is usually still as high as 50-60°C or above, and the waste heat in the low-temperature section is still wasted, which leads to relatively more water vapor added, and higher energy consumption and operating costs. In short, since the flue gas and discharged process water are highly corrosive and have a small flow rate, a large proportion of various waste heat resources are wasted. Under the current dual-carbon policy background, it is even more necessary to recycle and reuse them to achieve energy saving and consumption reduction. Summary of the invention

[0019] The purpose and task of the present invention is to adopt a new method of energy production, distribution and use in response to the inherent technical limitations in the above-mentioned seawater bromine extraction process, fundamentally abandon the power system driven by fossil energy, and transform it into a new energy power system that meets the requirements of the carbon neutral era.

[0020] The specific description of the present invention is: a seawater concentration and bromine extraction process system driven by a carbon-neutral energy power system, which consists of a raw seawater concentration and air blowing method bromine extraction subsystem, a raw sulfur combustion furnace SO2 flue gas preparation subsystem, a raw liquid chlorination subsystem, a raw bromine extraction distillation preparation liquid bromine subsystem and a combustion furnace high-temperature waste heat flash steam production boiler subsystem, a bromine extraction distillation process waste heat deep recovery subsystem and its connecting pipelines and components. The raw seawater concentration and air blowing method bromine extraction subsystem includes a salt field 40, a bittern pump 41, an air blowing tower 42 and its connecting pipelines and components, and the raw liquid chlorination subsystem includes a liquid chlorine gasification tank 50, a water bath 51 and its connecting pipelines and components. The original sulfur combustion furnace SO2 flue gas preparation subsystem includes a sulfur combustion furnace 1, an ash settling tank 2, a high-temperature SO2 flue 3, a water washing tower 4, a clean SO2 flue gas pipe 5, a Roots blower 6, a water washing pump 7, an absorption tower 9 and its connecting pipelines and components. The original bromine extraction and distillation preparation liquid bromine subsystem includes a bromine extraction distillation tower 31, a bromine steam exhaust pipe 32, a bromine steam condenser 33, a waste liquid pump 34, an original waste liquid heat recovery device 35 and its connecting pipelines and components. It is characterized in that the combustion furnace high-temperature waste heat flash steam production boiler subsystem includes a heat exchange sleeve 20, a heat exchange sleeve 26, a micro high-temperature waste heat hot water boiler 10, a water supply pump 16, a flash tank 23, The blower 21, the compressed working medium gas storage tank 22, the mixing damper 19 and the connecting pipelines and components thereof, the waste heat deep recovery subsystem of the bromine extraction distillation process includes a high-efficiency anti-corrosion deep heat recovery device 36, a high-temperature heat pump steam making device 37, a new energy electric steam furnace 38 and the connecting pipelines and components thereof; wherein the feed inlet at the top of the air blowing tower 42 is respectively connected to the water inlet pipe of sulfuric acid SH, the air inlet pipe of chlorine CL and the outlet of the bitter brine pump 41, the inlet of the bitter brine pump 41 is connected to the bitter brine outlet of the salt pan 40, the salt pan 40 is provided with an inlet of seawater Ws and an outlet of crude salt Na, the lower part of the air blowing tower 42 is provided with an inlet of ambient air A, and the bottom is provided with There is a drain outlet for acidic waste water P, the top is an exhaust outlet for bromine and air mixed gas BrA, and is connected to the air inlet of bromine and air mixed gas BrA at the bottom of the absorption tower 9; the air inlet of chlorine gas CL of the air blowing tower 42 is connected to the chlorine outlet of the liquid chlorine gasification tank 50, the lower part of the liquid chlorine gasification tank 50 is arranged at the liquid chlorine CLy will be expected, the liquid chlorine gasification tank 50 is arranged in the tank of the water bath 51, the water bath 51 is provided with an inlet of heat source steam / water H1 and an outlet of heat source retreat water H2; the upper part of the absorption tower 9 is provided with an inlet of absorption spray water R, the bottom is provided with a drain outlet of the finished liquid BrH, and the top is provided with an air inlet of clean SO2 flue gas S2;The air inlet end of the sulfur combustion furnace 1 is provided with an inlet for sulfur S and an air inlet, wherein the air inlet is connected to the ambient air A through a Roots blower 6, and the smoke exhaust end of the sulfur combustion furnace 1 is provided with an outlet for high-temperature SO2 flue gas S1, and is connected to the inlet of the soot settling tank 2, and the outlet of the soot settling tank 2 is connected to the inlet of the high-temperature SO2 flue 3, and the connection between the high-temperature SO2 flue 3 and the water washing tower 4 is for cooling the SO2 flue gas S3, and the top exhaust port of the water washing tower 4 is connected to the top air inlet of the absorption tower 9 through the clean SO2 flue gas pipe 5, and the bottom liquid outlet of the water washing tower 4 is connected to the inlet of the water washing pump 7, and the outlet of the water washing pump 7 is respectively connected to the circulating water inlet of the water washing tower 4 and the inlet of the make-up water B. The water pipe is connected to the drainage pipe of the waste sulfuric acid liquid SH1; a heat exchange sleeve 26 is arranged on the outside of the pipeline of the high-temperature SO2 flue 3, and the closed annular space between the two is the area where the heat exchange medium flows and exchanges heat, wherein the air inlet of the heat exchange sleeve 26 is arranged at the end where the cooling SO2 flue gas S3 is located, and the air outlet of the heat exchange sleeve 26 is arranged at the air inlet end where the high-temperature SO2 flue gas S1 is located; a heat exchange sleeve 20 is arranged on the outside of the shell of the sulfur combustion furnace 1, and the closed annular space between the two is the area where the heat exchange medium flows and exchanges heat, wherein the air inlet of the heat exchange sleeve 20 is arranged at one end of the smoke outlet of the sulfur combustion furnace 1, and the air outlet of the heat exchange sleeve 20 is arranged at the sulfur combustion furnace 1; the air outlet of the heat exchange sleeve 20 is connected to the high-pressure inlet of the mixing damper 19 and the inlet of the inlet rectifying section 11 of the micro high-temperature waste heat hot water boiler 10, and the micro high-temperature waste heat hot water boiler 10 also includes a shell 12, a super large temperature difference heat exchanger 13 and an outlet tapered section, the outlet of the medium-temperature heat exchange medium of the outlet tapered section is connected to the low-pressure outlet of the mixing damper 19, the inlet of the blower 21 and the outlet of the compressed medium gas storage tank 22, the outlet of the blower 21 is connected to the air inlet of the heat exchange sleeve 26, and the air outlet of the heat exchange sleeve 26 is connected to the air inlet of the heat exchange sleeve 20; wherein the water inlet of the super large temperature difference heat exchanger 13 is connected to the outlet of the water feed pump 16, and the super large temperature difference heat exchanger 1 The water outlet of 3 is connected to the high-temperature water inlet of the flash tank 23, the medium-temperature water outlet of the flash tank 23 is connected to the inlet of the water pump 16 and the water supply pipe of the demineralized water makeup Bc, and the outlet of the secondary steam Q2 at the top of the flash tank 23 is respectively connected to the inlet of the heat source steam / water H1 of the water bath 51, the inlet of the heating steam Q of the bromine extraction distillation tower 31, the outlet of the primary steam Q1 of the new energy electric steam furnace 38 and the outlet of the third steam Q3 of the high-temperature heat pump steam making device 37; wherein the new energy electric steam furnace 38 is also provided with an inlet of the electric boiler makeup water W2, and the interior of the new energy electric steam furnace 38 is provided with an electric heater 39, and both ends of the electric heater 39 are respectively connected to the power line of the new energy power source E;The low temperature side inlet of the high efficiency anti-corrosion deep heat recovery device 36 is connected to the discharge port at the bottom of the absorption tower 9 through the liquid supply pipe of the finished liquid BrH, the low temperature side outlet of the high efficiency anti-corrosion deep heat recovery device 36 is connected to the low temperature side inlet of the original waste liquid heat recovery device 35, the low temperature side outlet of the original waste liquid heat recovery device 35 is connected to the feed liquid inlet of the upper part of the bromine extraction distillation tower 31, the chlorine gas CL inlet of the lower part of the bromine extraction distillation tower 31 is connected to the chlorine gas outlet of the liquid chlorine gasification tank 50, the bottom feed liquid outlet of the bromine extraction distillation tower 31 is connected to the inlet of the waste liquid pump 34, the outlet of the waste liquid pump 34 is connected to the high temperature side inlet of the original waste liquid heat recovery device 35, the high temperature side outlet of the original waste liquid heat recovery device 35 is connected to the high temperature side inlet of the high efficiency anti-corrosion deep heat recovery device 36, and the high temperature side outlet of the high efficiency anti-corrosion deep heat recovery device 36 is connected to the water withdrawal pipe of the bromine extraction waste liquid SH2; bromine extraction distillation The top of the tower 31 is the gathering area of ​​the bromine and water vapor mixed gas Br1. The top gas outlet is connected to the air inlet of the upper part of the bromine steam condenser 33 through the bromine steam exhaust pipe 32. The lower liquid outlet of the bromine steam condenser 33 is connected to the water outlet pipe of the liquid bromine Br. The liquid outlet of the crude bromine water Br2 at the bottom of the bromine steam condenser 33 is connected to the liquid inlet of the upper part of the bromine distillation tower 31. The cooling water outlet of the bromine steam condenser 33 is connected to the low-temperature heat source inlet of the high-temperature heat pump steam making device 37 through the water return pipe of the cooling return water C2. The cooling water inlet of the bromine steam condenser 33 is connected to the low-temperature heat source water outlet of the high-temperature heat pump steam making device 37 through the water inlet pipe of the cooling incoming water C1. The heating side inlet of the high-temperature heat pump steam making device 37 is connected to the water inlet pipe of the heat pump feed water W3. The heating side outlet of the high-temperature heat pump steam making device 37 is the outlet of the third steam Q3. ;

[0021] A safety valve group 14 and a water supply temperature sensor 15 are arranged on the water outlet pipe section of the super-large temperature difference heat exchanger 13, a combustion furnace exhaust temperature sensor 17 is arranged on the flue gas outlet pipe section of the sulfur combustion furnace 1, a mixed smoke temperature sensor 18 is arranged on the outlet pipe section of the blower 21, and a medium-temperature flue gas sensor 27 is arranged at the connection between the high-temperature SO2 flue 3 and the water washing tower 4; wherein the operating temperature of the water supply temperature sensor 15 is controlled by the opening of the electric regulating valve at the outlet of the water supply pump 16, and the lower limit temperature of the mixed smoke temperature sensor 18 is controlled by the opening of the mixing air door 19; the lower limit temperature of the combustion furnace exhaust temperature sensor 17 and the lower limit temperature of the medium-temperature flue gas sensor 27 are both controlled by the blower 21 through the flow rate adjusted by the frequency converter or the air inlet guide vane.

[0022] The working medium in the compressed working medium gas storage tank 22 is high-pressure nitrogen or compressed air.

[0023] The heat exchange sleeve 20 is made of carbon steel or boiler steel, with or without an external insulation layer; the heat exchange sleeve 26 is made of carbon steel or boiler steel, with an external insulation layer.

[0024] The ultra-large temperature difference heat exchanger 13 adopts a serpentine coil structure, a transverse or longitudinal tube bundle structure, a plate structure or a tube-sheet structure; when a transverse or longitudinal tube bundle structure is adopted, the heat exchange tube adopts a plain tube or a fin tube structure; the heat exchange material of the ultra-large temperature difference heat exchanger 13 adopts carbon steel, ND steel, stainless steel 304 or stainless steel 316L.

[0025] The material of the water supply pump 16 is a high-temperature cast iron pump or a stainless steel water pump.

[0026] The high-efficiency anti-corrosion deep heat recovery device 36 adopts a high-efficiency graphene plastic tube heat exchanger; the original waste liquid heat recovery device 35 adopts a silicon carbide heat exchanger, a glass heat exchanger and / or a fluoroplastic heat exchanger.

[0027] The heat pump main unit of the high-temperature heat pump steam making device 37 adopts a single-stage electric compression high-temperature heat pump type, and is connected in series with an electric heater to generate water vapor.

[0028] The innovative features and beneficial effects of the present invention are as follows.

[0029] (1) Adopting a completely new energy production, distribution and utilization method to realize the process energy consumption and power drive for seawater concentration and bromine extraction, including significantly adjusting the process flow of energy production, distribution and utilization in process production, significantly reducing energy consumption through energy-saving measures, and fundamentally abandoning the power system driven by fossil energy by using waste heat to generate steam, heat pump to generate steam, new energy power generation and electric heating to generate steam, so as to enable this field to enter the era of carbon-neutral energy and power.

[0030] (2) In view of the highly corrosive nature of high-temperature SO2 flue gas, this patent is based on the acid dew point control method to ensure that the temperature of the inner wall of the sulfur combustion furnace shell and the boiler exhaust pipe that are in contact with the flue gas is always maintained above the acid dew point, thereby ensuring that acid dew point corrosion will not occur and that the original equipment system will not have corrosion problems during the waste heat recovery process.

[0031] (3) This patent adopts a method in which a sleeve is arranged on the outer side of the outer shell of the sulfur combustion furnace and the high-temperature flue gas pipeline behind it, and heat exchange is carried out through an annular area. The heat exchange medium is nitrogen or air, which has no corrosion problem. Therefore, commonly used boiler steel and other carbon steel, ND steel, stainless steel 304 or stainless steel 316L, etc. can be used as the heat exchange tube material, thereby greatly reducing the processing difficulty and cost of the heat exchanger and the entire waste heat boiler, and solving the problem of waste heat recovery of flue gas from the sulfur combustion furnace.

[0032] (4) The waste heat boiler can produce high-parameter waste hot water, and can also produce 0.1-0.6MPa saturated wet steam through a flash tank, which is more convenient for reuse in process production.

[0033] (5) By precisely controlling the most critical boiler water supply temperature to meet the parameter requirements of the external heat source; controlling the sleeve air inlet temperature and the combustion furnace exhaust temperature to avoid serious corrosion problems, the safe, stable and reliable operation of the equipment is ensured, the service life is increased, and the full-cycle operation cost is significantly reduced. BRIEF DESCRIPTION OF THE DRAWINGS

[0034] Figure 1 This is a system diagram of the conventional production process of bromine extraction from seawater concentration. Figure 2 It is a system schematic diagram of the present invention.

[0035] Figure 1 , 2 The part numbers and names are as follows.

[0036] Sulfur combustion furnace 1, ash settling tank 2, high-temperature SO2 flue 3, water washing tower 4, clean SO2 flue gas pipe 5, Roots blower 6, water washing pump 7, original heat exchanger 8, absorption tower 9, micro high-temperature waste heat hot water boiler 10, imported rectifier section 11, shell 12, super large temperature difference heat exchanger 13, safety valve group 14, water supply temperature sensor 15, water supply pump 16, combustion furnace exhaust temperature sensor 17, mixed smoke temperature sensor 18, combustion furnace exhaust temperature sensor 17, mixed smoke temperature sensor 18, mixing damper 19, heat exchange sleeve 20, blower 21, compressed working fluid gas storage tank 22, flash tank 23, heat exchange sleeve 26, medium temperature flue gas sensor 27, bromine extraction distillation tower 31, bromine steam exhaust pipe 32, bromine steam condenser 33, waste liquid pump 34, original waste liquid heat recovery device 35, high-efficiency anti-corrosion deep heat recovery device 36, high-temperature heat pump steam making device 37, new energy electric heating Steam furnace 38, electric heater 39, salt pan 40, bittern pump 41, air blowing tower 42, chlorine gasification tank 50, water bath 51, coal-fired or gas-fired boiler 60, blower 61, ambient air A, make-up water B, demineralized make-up water Bc, liquid bromine Br, bromine and water vapor mixed gas Br1, crude bromine water Br2, bromine and air mixed gas BrA, finished liquid BrH, cooling water C1, cooling water C2, chlorine gas CL, liquid chlorine CLy, New energy power supply E, heat source steam / water H1, heat source retreat water H2, crude salt Na, heating steam Q, new steam Q0, primary steam Q1, secondary steam Q2, tertiary steam Q3, spray water R, sulfur S, high-temperature SO2 flue gas S1, clean SO2 flue gas S2, cooling SO2 flue gas S3, sulfuric acid SH, waste sulfuric acid liquid SH1, bromine extraction waste liquid SH2, boiler feed water W1, electric boiler make-up water W2, heat pump feed water W3, seawater Ws. DETAILED DESCRIPTION

[0037] Figure 1 It is a system diagram and example of a conventional production process for extracting bromine from seawater by concentration. Figure 2 It is a system schematic diagram and embodiment of the present invention.

[0038] See the system diagram and examples of the conventional production process for extracting bromine from seawater by concentration. Figure 1 The system is composed of a subsystem for extracting bromine by the original seawater concentration and air blowing method, a subsystem for preparing SO2 flue gas by the original sulfur combustion furnace, a subsystem for gasification of raw liquid chlorination, a subsystem for preparing liquid bromine by distillation of the original bromine extraction, and a steam boiler subsystem and their connecting pipes and components. The subsystem for extracting bromine by the original seawater concentration and air blowing method includes a salt pan 40, a bittern pump 41, an air blowing tower 42 and their connecting pipes and components. The subsystem for gasification of raw liquid chlorination includes a liquid chlorine gasification tank 50, a water bath 51 and their connecting pipes and components. The subsystem for preparing SO2 flue gas by the original sulfur combustion furnace includes a sulfur combustion furnace 1, a soot settling tank 2, a high-temperature SO2 flue 3, a water washing tower 4, a clean SO2 flue pipe 5, a Roots blower 6, a water washing pump 7, an absorption tower 9 and its connecting pipes and components. The pipes and components are connected. The original bromine extraction and distillation preparation liquid bromine subsystem includes a bromine extraction distillation tower 31, a bromine steam exhaust pipe 32, a bromine steam condenser 33, a waste liquid pump 34, an original waste liquid heat recovery device 35 and its connecting pipes and components; the steam boiler subsystem includes a coal-fired or gas-fired boiler 60, a blower 61 and its connecting pipes and components, wherein the outlet of the new steam Q0 of the coal-fired or gas-fired boiler 60 is respectively connected to the inlet of the heat source steam / water H1 of the water bath 51 and the inlet of the heating steam Q of the bromine extraction distillation tower 31, the coal-fired or gas-fired boiler 60 is also provided with an inlet of boiler feed water W1, the combustion-supporting air inlet of the coal-fired or gas-fired boiler 60 is connected to the air outlet of the blower 61, and the air inlet of the blower 61 is communicated with the ambient air (A).

[0039] The specific embodiments of the present invention are as follows, see Figure 2As shown. The specific description of the present invention is: a seawater concentration and bromine extraction process system driven by a carbon-neutral energy power system, which consists of a raw seawater concentration and air blowing method bromine extraction subsystem, a raw sulfur combustion furnace SO2 flue gas preparation subsystem, a raw liquid chlorination subsystem, a raw bromine extraction distillation preparation liquid bromine subsystem and a combustion furnace high-temperature waste heat flash steam production boiler subsystem, a bromine extraction distillation process waste heat deep recovery subsystem and its connecting pipelines and components, wherein the raw seawater concentration and air blowing method bromine extraction subsystem includes a salt field 40, a brine pump 41, an air blowing tower 42 and its connecting pipelines and components, and the raw liquid chlorination subsystem includes a liquid chlorine gasification tank 50, a water bath 51 and its connecting pipelines and components. The original sulfur combustion furnace SO2 flue gas preparation subsystem includes a sulfur combustion furnace 1, an ash settling tank 2, a high-temperature SO2 flue 3, a water washing tower 4, a clean SO2 flue gas pipe 5, a Roots blower 6, a water washing pump 7, an absorption tower 9 and its connecting pipelines and components. The original bromine extraction and distillation preparation liquid bromine subsystem includes a bromine extraction distillation tower 31, a bromine steam exhaust pipe 32, a bromine steam condenser 33, a waste liquid pump 34, an original waste liquid heat recovery device 35 and its connecting pipelines and components. It is characterized in that the combustion furnace high-temperature waste heat flash steam production boiler subsystem includes a heat exchange sleeve 20, a heat exchange sleeve 26, a micro high-temperature waste heat hot water boiler 10, a water supply pump 16, a flash tank 23, The blower 21, the compressed working medium gas storage tank 22, the mixing damper 19 and the connecting pipelines and components thereof, the waste heat deep recovery subsystem of the bromine extraction distillation process includes a high-efficiency anti-corrosion deep heat recovery device 36, a high-temperature heat pump steam making device 37, a new energy electric steam furnace 38 and the connecting pipelines and components thereof; wherein the feed inlet at the top of the air blowing tower 42 is respectively connected to the water inlet pipe of sulfuric acid SH, the air inlet pipe of chlorine CL and the outlet of the bitter brine pump 41, the inlet of the bitter brine pump 41 is connected to the bitter brine outlet of the salt pan 40, the salt pan 40 is provided with an inlet of seawater Ws and an outlet of crude salt Na, the lower part of the air blowing tower 42 is provided with an inlet of ambient air A, and the bottom is provided with There is a drain outlet for acidic waste water P, the top is an exhaust outlet for bromine and air mixed gas BrA, and is connected to the air inlet of bromine and air mixed gas BrA at the bottom of the absorption tower 9; the air inlet of chlorine gas CL of the air blowing tower 42 is connected to the chlorine outlet of the liquid chlorine gasification tank 50, the lower part of the liquid chlorine gasification tank 50 is arranged at the liquid chlorine CLy will be expected, the liquid chlorine gasification tank 50 is arranged in the tank of the water bath 51, the water bath 51 is provided with an inlet of heat source steam / water H1 and an outlet of heat source retreat water H2; the upper part of the absorption tower 9 is provided with an inlet of absorption spray water R, the bottom is provided with a drain outlet of the finished liquid BrH, and the top is provided with an air inlet of clean SO2 flue gas S2;The air inlet end of the sulfur combustion furnace 1 is provided with an inlet for sulfur S and an air inlet, wherein the air inlet is connected to the ambient air A through a Roots blower 6, and the smoke exhaust end of the sulfur combustion furnace 1 is provided with an outlet for high-temperature SO2 flue gas S1, and is connected to the inlet of the soot settling tank 2, and the outlet of the soot settling tank 2 is connected to the inlet of the high-temperature SO2 flue 3, and the connection between the high-temperature SO2 flue 3 and the water washing tower 4 is for cooling the SO2 flue gas S3, and the top exhaust port of the water washing tower 4 is connected to the top air inlet of the absorption tower 9 through the clean SO2 flue gas pipe 5, and the bottom liquid outlet of the water washing tower 4 is connected to the inlet of the water washing pump 7, and the outlet of the water washing pump 7 is respectively connected to the circulating water inlet of the water washing tower 4 and the inlet of the make-up water B. The water pipe is connected to the drainage pipe of the waste sulfuric acid liquid SH1; a heat exchange sleeve 26 is arranged on the outside of the pipeline of the high-temperature SO2 flue 3, and the closed annular space between the two is the area where the heat exchange medium flows and exchanges heat, wherein the air inlet of the heat exchange sleeve 26 is arranged at the end where the cooling SO2 flue gas S3 is located, and the air outlet of the heat exchange sleeve 26 is arranged at the air inlet end where the high-temperature SO2 flue gas S1 is located; a heat exchange sleeve 20 is arranged on the outside of the shell of the sulfur combustion furnace 1, and the closed annular space between the two is the area where the heat exchange medium flows and exchanges heat, wherein the air inlet of the heat exchange sleeve 20 is arranged at one end of the smoke outlet of the sulfur combustion furnace 1, and the air outlet of the heat exchange sleeve 20 is arranged at the sulfur combustion furnace 1; the air outlet of the heat exchange sleeve 20 is connected to the high-pressure inlet of the mixing damper 19 and the inlet of the inlet rectifying section 11 of the micro high-temperature waste heat hot water boiler 10, and the micro high-temperature waste heat hot water boiler 10 also includes a shell 12, a super large temperature difference heat exchanger 13 and an outlet tapered section, the outlet of the medium-temperature heat exchange medium of the outlet tapered section is connected to the low-pressure outlet of the mixing damper 19, the inlet of the blower 21 and the outlet of the compressed medium gas storage tank 22, the outlet of the blower 21 is connected to the air inlet of the heat exchange sleeve 26, and the air outlet of the heat exchange sleeve 26 is connected to the air inlet of the heat exchange sleeve 20; wherein the water inlet of the super large temperature difference heat exchanger 13 is connected to the outlet of the water feed pump 16, and the super large temperature difference heat exchanger 1 The water outlet of 3 is connected to the high-temperature water inlet of the flash tank 23, the medium-temperature water outlet of the flash tank 23 is connected to the inlet of the water pump 16 and the water supply pipe of the demineralized water makeup Bc, and the outlet of the secondary steam Q2 at the top of the flash tank 23 is respectively connected to the inlet of the heat source steam / water H1 of the water bath 51, the inlet of the heating steam Q of the bromine extraction distillation tower 31, the outlet of the primary steam Q1 of the new energy electric steam furnace 38 and the outlet of the third steam Q3 of the high-temperature heat pump steam making device 37; wherein the new energy electric steam furnace 38 is also provided with an inlet of the electric boiler makeup water W2, and the interior of the new energy electric steam furnace 38 is provided with an electric heater 39, and both ends of the electric heater 39 are respectively connected to the power line of the new energy power source E;The low temperature side inlet of the high efficiency anti-corrosion deep heat recovery device 36 is connected to the discharge port at the bottom of the absorption tower 9 through the liquid supply pipe of the finished liquid BrH, the low temperature side outlet of the high efficiency anti-corrosion deep heat recovery device 36 is connected to the low temperature side inlet of the original waste liquid heat recovery device 35, the low temperature side outlet of the original waste liquid heat recovery device 35 is connected to the feed liquid inlet of the upper part of the bromine extraction distillation tower 31, the chlorine gas CL inlet of the lower part of the bromine extraction distillation tower 31 is connected to the chlorine gas outlet of the liquid chlorine gasification tank 50, the bottom feed liquid outlet of the bromine extraction distillation tower 31 is connected to the inlet of the waste liquid pump 34, the outlet of the waste liquid pump 34 is connected to the high temperature side inlet of the original waste liquid heat recovery device 35, the high temperature side outlet of the original waste liquid heat recovery device 35 is connected to the high temperature side inlet of the high efficiency anti-corrosion deep heat recovery device 36, and the high temperature side outlet of the high efficiency anti-corrosion deep heat recovery device 36 is connected to the water withdrawal pipe of the bromine extraction waste liquid SH2; bromine extraction distillation The top of the tower 31 is the gathering area of ​​the bromine and water vapor mixed gas Br1. The top gas outlet is connected to the air inlet of the upper part of the bromine steam condenser 33 through the bromine steam exhaust pipe 32. The lower liquid outlet of the bromine steam condenser 33 is connected to the water outlet pipe of the liquid bromine Br. The liquid outlet of the crude bromine water Br2 at the bottom of the bromine steam condenser 33 is connected to the liquid inlet of the upper part of the bromine distillation tower 31. The cooling water outlet of the bromine steam condenser 33 is connected to the low-temperature heat source inlet of the high-temperature heat pump steam making device 37 through the water return pipe of the cooling return water C2. The cooling water inlet of the bromine steam condenser 33 is connected to the low-temperature heat source water outlet of the high-temperature heat pump steam making device 37 through the water inlet pipe of the cooling incoming water C1. The heating side inlet of the high-temperature heat pump steam making device 37 is connected to the water inlet pipe of the heat pump feed water W3. The heating side outlet of the high-temperature heat pump steam making device 37 is the outlet of the third steam Q3. ;

[0040] A safety valve group 14 and a water supply temperature sensor 15 are arranged on the water outlet pipe section of the super-large temperature difference heat exchanger 13, a combustion furnace exhaust temperature sensor 17 is arranged on the flue gas outlet pipe section of the sulfur combustion furnace 1, a mixed smoke temperature sensor 18 is arranged on the outlet pipe section of the blower 21, and a medium-temperature flue gas sensor 27 is arranged at the connection between the high-temperature SO2 flue 3 and the water washing tower 4; wherein the operating temperature of the water supply temperature sensor 15 is controlled by the opening of the electric regulating valve at the outlet of the water supply pump 16, and the lower limit temperature of the mixed smoke temperature sensor 18 is controlled by the opening of the mixing air door 19; the lower limit temperature of the combustion furnace exhaust temperature sensor 17 and the lower limit temperature of the medium-temperature flue gas sensor 27 are both controlled by the blower 21 through the flow rate adjusted by the frequency converter or the air inlet guide vane.

[0041] The working medium in the compressed working medium gas storage tank 22 is high-pressure nitrogen or compressed air.

[0042] The heat exchange sleeve 20 is made of carbon steel or boiler steel, with or without an external insulation layer; the heat exchange sleeve 26 is made of carbon steel or boiler steel, with an external insulation layer.

[0043] The ultra-large temperature difference heat exchanger 13 adopts a serpentine coil structure, a transverse or longitudinal tube bundle structure, a plate structure or a tube-sheet structure; when a transverse or longitudinal tube bundle structure is adopted, the heat exchange tube adopts a plain tube or a fin tube structure; the heat exchange material of the ultra-large temperature difference heat exchanger 13 adopts carbon steel, ND steel, stainless steel 304 or stainless steel 316L.

[0044] The material of the water supply pump 16 is a high-temperature cast iron pump or a stainless steel water pump.

[0045] The high-efficiency anti-corrosion deep heat recovery device 36 adopts a high-efficiency graphene plastic tube heat exchanger; the original waste liquid heat recovery device 35 adopts a silicon carbide heat exchanger, a glass heat exchanger and / or a fluoroplastic heat exchanger.

[0046] The heat pump main unit of the high-temperature heat pump steam making device 37 adopts a single-stage electric compression high-temperature heat pump type, and is connected in series with an electric heater to generate water vapor.

[0047] It should be noted that the present invention constructs a new energy and power system for seawater concentration and bromine extraction, and according to this solution, there can be different specific implementation measures and specific implementation devices with different structures. The above-mentioned specific implementation method is only one of the implementation types. Any other similar simple deformation implementation methods, such as simple increase, decrease, deformation, change of relative position of internal components and interfaces, simple combination and adjustment of external pipelines and components, etc., all fall within the protection scope of the present invention.

Claims

1. A seawater concentration and bromine extraction process system driven by a carbon-neutral energy power system, comprising a raw seawater concentration and air blowing method bromine extraction subsystem, a raw sulfur combustion furnace SO2 flue gas preparation subsystem, a raw liquid chlorination subsystem, a raw bromine extraction distillation preparation liquid bromine subsystem and a combustion furnace high-temperature waste heat flash steam production boiler subsystem, a bromine extraction distillation process waste heat deep recovery subsystem and its connecting pipelines and components, wherein the raw seawater concentration and air blowing method bromine extraction subsystem includes a salt pan (40), a bittern pump (41), an air blowing tower (42) and its connecting pipelines and components, and the raw liquid chlorination subsystem includes a liquid chlorine gasification tank ( 50), a water bath (51) and its connecting pipes and components, the original sulfur combustion furnace SO2 flue gas preparation subsystem comprises a sulfur combustion furnace (1), an ash settling tank (2), a high-temperature SO2 flue (3), a water washing tower (4), a clean SO2 flue gas pipe (5), a Roots blower (6), a water washing pump (7), an absorption tower (9) and its connecting pipes and components, the original bromine extraction distillation preparation liquid bromine subsystem comprises a bromine extraction distillation tower (31), a bromine steam exhaust pipe (32), a bromine steam condenser (33), a waste liquid pump (34), an original waste liquid heat recovery device (35) and its connecting pipes and components, characterized in that, The combustion furnace high-temperature waste heat flash steam boiler subsystem comprises a heat exchange sleeve (20), a heat exchange sleeve (26), a micro high-temperature waste heat hot water boiler (10), a water feed pump (16), a flash tank (23), a blower (21), a compressed working fluid gas storage tank (22), a mixing damper (19) and connecting pipes and components thereof; the bromine extraction distillation process waste heat deep recovery subsystem comprises a high-efficiency corrosion-resistant deep heat recovery device (36), a high-temperature heat pump steam making device (37), a new energy electric steam furnace (38) and connecting pipes and components thereof; wherein the feed inlet at the top of the air blowing tower (42) is respectively connected to the water inlet pipe of sulfuric acid (SH), the air inlet pipe of chlorine (CL) and the outlet of the brine pump (41); the brine pump (41) is connected to the outlet of the brine pump (41). The inlet is connected to the bittern outlet of the salt pan (40), the salt pan (40) is provided with an inlet for seawater (Ws) and an outlet for crude salt (Na), the lower part of the air blowing tower (42) is provided with an inlet for ambient air (A), the bottom is provided with a drain outlet for acidic wastewater (P), the top is provided with an exhaust outlet for a bromine and air mixture (BrA), and is connected to the air inlet of the bromine and air mixture (BrA) at the lower part of the absorption tower (9); the air inlet of the chlorine gas (CL) of the air blowing tower (42) is connected to the chlorine gas outlet of the liquid chlorine gasification tank (50), the lower part of the liquid chlorine gasification tank (50) is provided at the liquid chlorine (CLy) will be expected, the liquid chlorine gasification tank (50) is provided in the tank of the water bath (51), the water bath (51) is provided with an inlet of a heat source steam / water (H1) The upper part of the absorption tower (9) is provided with an inlet for absorption spray water (R), the bottom is provided with a discharge port for the finished liquid (BrH), and the top is provided with an air inlet for clean SO2 flue gas (S2); the air inlet end of the sulfur combustion furnace (1) is provided with an inlet for sulfur (S) and an air inlet, wherein the air inlet is communicated with the ambient air (A) through a Roots blower (6); the exhaust end of the sulfur combustion furnace (1) is provided with an outlet for high-temperature SO2 flue gas (S1), and is connected to the inlet of the soot settling tank (2); the outlet of the soot settling tank (2) is connected to the inlet of the high-temperature SO2 flue (3), and the connection between the high-temperature SO2 flue (3) and the water washing tower (4) is for cooling the SO2 flue gas (S2). 3), the top exhaust port of the water washing tower (4) is connected to the top air inlet of the absorption tower (9) through the clean SO2 flue gas pipe (5), the bottom liquid outlet of the water washing tower (4) is connected to the inlet of the water washing pump (7), and the outlet of the water washing pump (7) is respectively connected to the circulating water inlet of the water washing tower (4), the water pipe of the water replenishment (B) and the drainage pipe of the waste sulfuric acid liquid (SH1); a heat exchange sleeve (26) is arranged on the outside of the pipeline of the high-temperature SO2 flue (3), and the closed annular space between the two is the area where the heat exchange medium flows and exchanges heat, wherein the air inlet of the heat exchange sleeve (26) is arranged at the end where the cooling SO2 flue gas (S3) is located, and the air outlet of the heat exchange sleeve (26) is arranged at the end of the air inlet where the high-temperature SO2 flue gas (S1) is located;A heat exchange sleeve (20) is arranged outside the shell of the sulfur combustion furnace (1), and the closed annular space between the two is a region where the heat exchange medium flows and exchanges heat, wherein the air inlet of the heat exchange sleeve (20) is arranged at one end of the smoke outlet of the sulfur combustion furnace (1), and the air outlet of the heat exchange sleeve (20) is arranged at one end of the air inlet of the sulfur combustion furnace (1); the air outlet of the heat exchange sleeve (20) is connected to the high-pressure inlet of the mixing damper (19) and the inlet of the inlet rectifying section (11) of the micro high-temperature waste heat hot water boiler (10), and the micro high-temperature waste heat hot water boiler (10) further comprises a shell (12), an ultra-large temperature difference heat exchanger (13) and an outlet tapered section, and the medium-temperature heat exchange medium outlet of the outlet tapered section is connected to the mixing damper (19) ), the inlet of the blower (21) and the air outlet of the compressed working medium storage tank (22), the air outlet of the blower (21) is connected to the air inlet of the heat exchange sleeve (26), and the air outlet of the heat exchange sleeve (26) is connected to the air inlet of the heat exchange sleeve (20); wherein the water inlet of the ultra-large temperature difference heat exchanger (13) is connected to the outlet of the water feed pump (16), the water outlet of the ultra-large temperature difference heat exchanger (13) is connected to the high-temperature water inlet of the flash tank (23), the medium-temperature water outlet of the flash tank (23) is connected to the inlet of the water feed pump (16) and the water supply pipe of the desalted water replenishment (Bc), and the outlet of the secondary steam (Q2) at the top of the flash tank (23) is respectively connected to the heat source steam / water (H1) of the water bath (51) The inlet of the high-efficiency anti-corrosion deep heat recovery device (36) is connected to the inlet of the heating steam (Q) of the bromine extraction distillation tower (31), the outlet of the primary steam (Q1) of the new energy electric steam furnace (38) and the outlet of the third steam (Q3) of the high-temperature heat pump steam making device (37); wherein the new energy electric steam furnace (38) is also provided with an inlet of electric boiler make-up water (W2), the interior of the new energy electric steam furnace (38) is provided with an electric heater (39), and the two ends of the electric heater (39) are respectively connected to the power line of the new energy power supply (E); the low-temperature side inlet of the high-efficiency anti-corrosion deep heat recovery device (36) is connected to the drain port at the bottom of the absorption tower (9) through the liquid supply pipe of the finished liquid (BrH), and the low-temperature side outlet of the high-efficiency anti-corrosion deep heat recovery device (36) is connected to the drain port at the bottom of the absorption tower (9) through the liquid supply pipe of the finished liquid (BrH), and the low-temperature side outlet of the high-efficiency anti-corrosion deep heat recovery device (36) is connected to the drain port at the bottom of the absorption tower (9). The inlet of the original waste liquid heat recovery device (35) is connected to the low temperature side inlet of the original waste liquid heat recovery device (35), the low temperature side outlet of the original waste liquid heat recovery device (35) is connected to the feed liquid inlet of the upper part of the bromine extraction distillation tower (31), the chlorine gas (CL) inlet of the lower part of the bromine extraction distillation tower (31) is connected to the chlorine gas outlet of the liquid chlorine gasification tank (50), the bottom feed liquid outlet of the bromine extraction distillation tower (31) is connected to the inlet of the waste liquid pump (34), the outlet of the waste liquid pump (34) is connected to the high temperature side inlet of the original waste liquid heat recovery device (35), the high temperature side outlet of the original waste liquid heat recovery device (35) is connected to the high temperature side inlet of the high efficiency anti-corrosion deep heat recovery device (36), and the high temperature side outlet of the high efficiency anti-corrosion deep heat recovery device (36) is connected to the water return pipe of the bromine extraction waste liquid (SH2);The top of the bromine extraction distillation tower (31) is a gathering area for the bromine and water vapor mixed gas (Br1), the top gas outlet is connected to the gas inlet at the top of the bromine steam condenser (33) through a bromine steam exhaust pipe (32), the lower liquid outlet of the bromine steam condenser (33) is connected to the water outlet pipe of the liquid bromine (Br), the liquid outlet of the crude bromine water (Br2) at the bottom of the bromine steam condenser (33) is connected to the feed liquid inlet at the top of the bromine extraction distillation tower (31); the cooling water outlet of the bromine steam condenser (33) The return pipe of the cooling return water (C2) is connected to the low-temperature heat source inlet of the high-temperature heat pump steam making device (37); the cooling water inlet of the bromine steam condenser (33) is connected to the low-temperature heat source outlet of the high-temperature heat pump steam making device (37) through the inlet pipe of the cooling inlet water (C1); the heating side inlet of the high-temperature heat pump steam making device (37) is connected to the inlet pipe of the heat pump feed water (W3); and the heating side outlet of the high-temperature heat pump steam making device (37) is the outlet of the third steam (Q3). ; 2. A seawater concentration and bromine extraction process system driven by a carbon-neutral energy power system as claimed in claim 1, characterized in that A safety valve group (14) and a water supply temperature sensor (15) are arranged on the water outlet pipe section of the ultra-large temperature difference heat exchanger (13); a combustion furnace exhaust temperature sensor (17) is arranged on the flue gas outlet pipe section of the sulfur combustion furnace (1); a mixed smoke temperature sensor (18) is arranged on the outlet pipe section of the blower (21); and a medium-temperature flue gas sensor (27) is arranged at the connection between the high-temperature SO2 flue (3) and the water washing tower (4); wherein the operating temperature of the water supply temperature sensor (15) is controlled by the opening of the electric regulating valve at the outlet of the water supply pump (16), and the lower limit temperature of the mixed smoke temperature sensor (18) is controlled by the opening of the mixing air door (19); the lower limit temperature of the combustion furnace exhaust temperature sensor (17) and the lower limit temperature of the medium-temperature flue gas sensor (27) are both controlled by the flow rate adjusted by the blower (21) through the frequency converter or the air inlet guide vane.

3. A seawater concentration and bromine extraction process system driven by a carbon-neutral energy power system as claimed in claim 1, characterized in that The working fluid in the compressed working fluid gas storage tank (22) is high-pressure nitrogen or compressed air.

4. A seawater concentration and bromine extraction process system driven by a carbon-neutral energy power system as claimed in claim 1, characterized in that The heat exchange sleeve (20) is made of carbon steel or boiler steel, and may or may not have an external insulation layer; the heat exchange sleeve (26) is made of carbon steel or boiler steel, and may have an external insulation layer.

5. A seawater concentration and bromine extraction process system driven by a carbon-neutral energy power system as claimed in claim 1, characterized in that The ultra-large temperature difference heat exchanger (13) adopts a serpentine coil structure, a transverse or longitudinal tube bundle structure, a plate structure or a tube-sheet structure; when the transverse or longitudinal tube bundle structure is adopted, the heat exchange tube adopts a plain tube or fin tube structure; the heat exchange material of the ultra-large temperature difference heat exchanger (13) adopts carbon steel, ND steel, stainless steel 304 or stainless steel 316L.

6. A seawater concentration and bromine extraction process system driven by a carbon-neutral energy power system as claimed in claim 1, characterized in that The water supply pump (16) is made of a high-temperature cast iron pump or a stainless steel water pump.

7. The waste heat deep recovery type bromine extraction distillation tower system according to claim 1, characterized in that The high-efficiency anti-corrosion deep heat recovery device (36) adopts a high-efficiency graphene plastic tube heat exchanger; the original waste liquid heat recovery device (35) adopts a silicon carbide heat exchanger, a glass heat exchanger and / or a fluoroplastic heat exchanger.

8. The waste heat deep recovery type bromine extraction distillation tower system according to claim 1, characterized in that The heat pump main unit of the high-temperature heat pump steam making device (37) adopts a single-stage electric compression high-temperature heat pump type, and is connected in series with an electric heater to generate water vapor.

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