Seawater concentration bromine extraction system based on deep waste heat recovery and new energy driving

Abstract

The utility model discloses a seawater concentration bromine extraction system based on deep waste heat recovery and new energy driving, and belongs to the technical field of salt chemical industry and new energy. On the basis of an existing seawater concentration bromine extraction system, a new energy mode is adopted for process heating, and heat exchange jackets are arranged on the outer walls of a sulfur combustion furnace 1 and a high-temperature SO2 flue 3; low-temperature air is sequentially fed into a heat exchange sleeve 26 and a heat exchange sleeve 20 through an air feeder 21 and exchanges heat with high-temperature and high-corrosion flue gas in a flue and higher-temperature flue gas in a sulfur combustion furnace, then the low-temperature air is fed into a miniature high-temperature waste heat hot water boiler 10, water is fed into a heating furnace, and cooled flue gas is subjected to circulating heat exchange through the air feeder 21. High-temperature water of the miniature high-temperature waste heat hot water boiler 10 is fed into the flash tank 23 and generates flash steam, and after the temperature of outlet water is reduced, the outlet water returns to the flash tank 23 for circulating heat exchange. Flash steam of the flash tank 23 is mixed with steam produced by the high-temperature heat pump steam producing device 37 and the new energy electric heating steam furnace 38, and then the mixture is sent to the liquid chlorine water bath 51 and the like for process heating.

Description

TECHNICAL FIELD

[0001] The utility model relates to a kind of seawater concentration bromine extraction systems based on depth waste heat recovery and new energy drive, belong to salt chemical industry and new energy technical field. BACKGROUND

[0002] The basic principle, process flow and energy production, distribution, use and discharge of seawater concentration bromine extraction are as follows.

[0003] Salt chemical plants based on seawater desalination can extract bromine, lithium and other substances from seawater or concentrated bitter brine after desalination. The basic principle of the commonly used "chlorine gas oxidation air blowing method for bromine production" is as follows.

[0004] Under acidic conditions, bromide ions (Br-) are oxidized to bromine molecules (Br2) using chlorine gas as an oxidizing agent. The ionic reaction is as follows.

[0005] 2Br- + Cl2 = Br2 + 2Cl-.

[0006] The free bromine is blown out with air, hence the name air blowing method.

[0007] Acidic bromine production uses sulfur dioxide as an absorbent and freshwater spray to assist in absorbing the mixture of air and bromine. The resulting liquid is called primary acid, and the chemical reaction is as follows.

[0008] Br2 + SO2 + 2H2O = 2HBr + H2SO4.

[0009] The primary acid is passed through chlorine gas oxidation, which re-releases bromine and generates hydrochloric acid. The chemical reaction is as follows.

[0010] 2HBr + Cl2 = 2HCl + Br2.

[0011] Finally, water vapor is used to distill bromine, which is separated by condensation to obtain finished bromine.

[0012] The process flow is described as follows.

[0013] The seawater (brine) is pumped into the blowing tower, dilute acid and chlorine are added into the outlet pipe of the pump, the mixed acidified chlorinated brine is sprayed from the upper part of the blowing tower and falls down, the air is blown from the bottom of the tower by the air blower, when the brine contacts with the air, the free bromine in the brine is stripped and blown out. The blown waste liquid is discharged from the bottom of the blowing tower and is used for salt making. The mixed gas discharged from the top of the blowing tower is sent into the absorption tower and is mixed and absorbed by sulfur dioxide and water mist, the formed finished liquid is called primary acid, the air after purification by the air trap is blown by the air blower and enters the bottom of the blowing tower and is used in the system. The primary acid is added from the top of the distillation tower, water vapor and chlorine are introduced from the bottom, when the primary acid flows along the filler from top to bottom, it contacts with chlorine and water vapor from bottom to top, is continuously oxidized and distilled, the bromine mixed gas with water vapor is discharged from the top of the tower, is condensed and separated, and the liquid bromine is prepared, the crude bromine water is returned to the absorption tower for continuous circulation.

[0014] The chlorine is usually prepared by gasification of liquid chlorine through a water bath tank, and the process is as follows: the liquid chlorine is sent into the water bath bottle, the bottle nozzle is connected with the chlorine clamp tightly, the water bath tank is filled with water and the water in the tank is heated by steam, the temperature is controlled at 75-83℃ by the electromagnetic valve, the temperature range can realize the gasification of liquid chlorine and avoid the generation of explosive nitrogen trichloride, and the gasified chlorine is supplied.

[0015] The preparation process of SO2 gas is as follows: the sulfur is introduced into the sulfur combustion furnace through the distributor, burns with oxygen in the air at high temperature to generate sulfur dioxide gas, is cooled by air and washed by circulating water, the temperature is controlled below 70℃, and then is introduced into the blowing and absorption tower for reduction and absorption to prepare the finished liquid for bromine production.

[0016] The distillation process for bromine extraction is as follows: the finished liquid is preheated by the recovered liquid, is introduced into the distillation tower and is oxidized by chlorine, at the same time, water vapor distillation is carried out, bromine is distilled out, the temperature at the top of the tower is controlled at 80-90℃, and the crude bromine is prepared after condensation, the bromine extraction recovered liquid is cooled by brine heat exchange and then is introduced into the collection pool and is used for brine acidification.

[0017] 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℃) generated when the sulfur combustion furnace prepares SO2 gas is usually not recovered due to its strong corrosiveness and small flue gas volume, but is directly introduced into the water washing tower for spraying and cooling to 50-60℃; and the waste sulfuric acid liquid SH1 is usually not recovered due to its strong corrosiveness, small flow and low temperature grade, and is finally wasted; the steam bromine recovery liquid discharged from the bromine extraction distillation tower is usually recovered by a special heat exchanger, but the original special heat exchanger has poor heat transfer performance and high cost, and the amount of recovered waste heat is relatively small, so that the discharge temperature of the steam bromine recovery liquid is usually still as high as 50-60℃ or above, the waste heat in the low-temperature section is still wasted, and the amount of added water vapor is relatively large, the energy consumption and operating cost are large. In summary, due to the strong corrosiveness and small flow of the flue gas and process water, a large proportion of waste heat resources is wasted, and it is necessary to recover and utilize the waste heat to realize energy saving and consumption reduction. Content of the utility model

[0018] The purpose and task of the utility model is to fundamentally abandon the fossil energy driven power system and transform into a new energy power system by using a new energy production, transportation and utilization method in view of the inherent technical limitations in the above-mentioned seawater bromine extraction process.

[0019] The utility model discloses a specific description is: a kind of seawater concentration and bromine extraction system based on depth waste heat recovery and new energy drive, by original seawater concentration and air blow method bromine extraction subsystem, original sulfur combustion furnace preparation SO2 flue gas subsystem, original liquid chlorine gasification subsystem, original bromine extraction distillation preparation liquid bromine subsystem and combustion furnace high-temperature waste heat flash steam boiler subsystem, bromine extraction distillation process waste heat depth recovery subsystem and its connecting pipeline and component composition, wherein original seawater concentration and air blow method bromine extraction subsystem includes salt field 40, bitter brine pump 41, air blow tower 42 and its connecting pipeline and component, original liquid chlorine gasification subsystem includes liquid chlorine gasification tank 50, water bath 51 and its connecting pipeline and component, original sulfur combustion furnace preparation SO2 flue gas subsystem includes sulfur combustion furnace 1, fly ash settling tank 2, high-temperature SO2 flue 3, water scrubbing tower 4, clean SO2 flue gas pipe 5, Roots blower 6, water scrubbing pump 7, absorption tower 9 and its connecting pipeline and component, original bromine extraction distillation preparation liquid bromine subsystem includes 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 and its connecting pipeline and component, characterized by, the combustion furnace high-temperature waste heat flash steam boiler subsystem of the described includes heat exchange sleeve 20, heat exchange sleeve 26, miniature high-temperature waste heat water boiler 10, feed water pump 16, flash tank 23, air blower 21, compressed working medium gas storage tank 22, mixed air door 19 and its connecting pipeline and component, the bromine extraction distillation process waste heat depth recovery subsystem of the described includes high-efficiency anticorrosion depth heat recovery device 36, high-temperature heat pump steam device 37, new energy electric heating steam furnace 38 and its connecting pipeline and component;Wherein the feed inlet of the air blow tower 42 upper portion is communicated with the water inlet pipe of sulfuric acid SH, the gas inlet pipe of chlorine gas C3 and the outlet of bitter brine pump 41 respectively, the inlet of bitter brine pump 41 is connected with the bitter brine outlet of salt field 40, and the salt field 40 is provided with the inlet of seawater Ws, the outlet of coarse salt K, the lower portion of air blow tower 42 is provided with the inlet of ambient air A, the bottom is provided with the drain outlet of acidic wastewater P, the top is the exhaust outlet of bromine and air mixture gas B4, and is connected with the gas inlet of bromine and air mixture gas B4 in the lower portion of absorption tower 9;The gas inlet of chlorine gas C3 of air blow tower 42 is connected with the chlorine gas outlet of liquid chlorine gasification tank 50, and the lower portion of liquid chlorine gasification tank 50 is arranged to the liquid inlet of liquid chlorine C4, and the liquid chlorine gasification tank 50 is arranged in the tank of water bath 51, and water bath 51 is provided with the inlet of heat source steam / water H1 and the outlet of heat source return water H2;The upper portion of the absorption tower 9 is provided with the inlet of absorption spray water R, the bottom is provided with the liquid discharge outlet of finished liquid B5, and the top is provided with the gas inlet of clean SO2 flue gas S2.The air inlet of the sulfur combustion furnace 1 is provided with a sulfur S4 inlet 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 of high-temperature SO2 flue gas S1, and is connected with the inlet of the fly ash settling tank 2; the outlet of the fly ash settling tank 2 is connected with the inlet of the high-temperature SO2 flue 3; the connection between the high-temperature SO2 flue 3 and the water washing tower 4 is the cooling SO2 flue gas S3; the top exhaust port of the water washing tower 4 is connected with the top air inlet of the absorption tower 9 through a clean SO2 flue gas pipe 5; the bottom liquid outlet of the water washing tower 4 is connected with the inlet of the water washing pump 7; the outlet of the water washing pump 7 is connected with the circulating water inlet of the water washing tower 4, the water inlet pipe of the water supplement B and the waste sulfuric acid liquid SH1 drainage pipe respectively; the outer side of the high-temperature SO2 flue 3 is provided with a heat exchange sleeve 26, and the closed annular space between the two is a region for flow heat exchange of the heat exchange medium; the air inlet of the heat exchange sleeve 26 is arranged at one end of the cooling SO2 flue gas S3, and the air outlet of the heat exchange sleeve 26 is arranged at one end of the high-temperature SO2 flue gas S1 air inlet; the outer side of the sulfur combustion furnace 1 is provided with a heat exchange sleeve 20, and the closed annular space between the two is a region for flow heat exchange of the heat exchange medium; the air inlet of the heat exchange sleeve 20 is arranged at one end of the sulfur combustion furnace 1 exhaust port, and the air outlet of the heat exchange sleeve 20 is arranged at one end of the sulfur combustion furnace 1 air inlet; the air outlet of the heat exchange sleeve 20 is connected with the high-pressure inlet of the mixed air door 19 and the inlet of the inlet rectifying section 11 of the micro high-temperature waste heat boiler 10; the micro high-temperature waste heat boiler 10 further comprises an outer shell 12, an ultra-large temperature difference heat exchanger 13 and an outlet tapered section; the medium-temperature heat exchange medium outlet of the outlet tapered section is connected with the low-pressure outlet of the mixed air door 19, the inlet of the air blower 21 and the air outlet of the compressed medium storage tank 22; the air outlet of the air blower 21 is connected with the air inlet of the heat exchange sleeve 26; the air outlet of the heat exchange sleeve 26 is connected with the air inlet of the heat exchange sleeve 20; the water inlet of the ultra-large temperature difference heat exchanger 13 is connected with the outlet of the water supply pump 16; the water outlet of the ultra-large temperature difference heat exchanger 13 is connected with the high-temperature water inlet of the flash tank 23; the medium-temperature water outlet of the flash tank 23 is communicated with the inlet of the water supply pump 16 and the water supply pipe of the desalted water supplement Bc; the outlet of the secondary steam Q2 at the top of the flash tank 23 is connected with the inlet of the heat source steam / water H1 of the water bath tank 51, the inlet of the heating steam Q of the bromine distillation tower 31, the outlet of the primary steam Q1 of the new energy electric heating steam furnace 38 and the outlet of the third steam Q3 of the high-temperature heat pump steam device 37 respectively; the new energy electric heating steam furnace 38 is further provided with the inlet of the electric boiler water supplement W2; the new energy electric heating steam furnace 38 is internally provided with an electric heater 39; the two ends of the electric heater 39 are connected with the power supply line of the new energy power supply E respectively.The low-temperature side inlet of the high-efficiency anti-corrosion deep heat recovery device 36 is connected with the liquid outlet at the bottom of the absorption tower 9 through a liquid supply pipe of the liquid B5, the low-temperature side outlet of the high-efficiency anti-corrosion deep heat recovery device 36 is connected with 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 with the liquid inlet at the upper part of the bromine distillation tower 31, the inlet of the chlorine gas C3 at the lower part of the bromine distillation tower 31 is connected with the chlorine gas outlet of the liquid chlorine gasification tank 50, the liquid outlet at the bottom of the bromine distillation tower 31 is connected with the inlet of the waste liquid pump 34, the outlet of the waste liquid pump 34 is connected with 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 with 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 communicated with the water return pipe of the bromine distillation waste liquid SH2; the top of the bromine distillation tower 31 is a gathering area of the bromine and water vapor mixed gas B1, the top gas outlet is connected with the gas inlet at the upper part of the bromine vapor condenser 33 through a bromine vapor exhaust pipe 32, the liquid outlet at the lower part of the bromine vapor condenser 33 is communicated with the water outlet pipe of the liquid bromine B3, and the liquid outlet of the crude bromine water B2 at the bottom of the bromine vapor condenser 33 is connected with the liquid inlet at the upper part of the bromine distillation tower 31; the cooling water outlet of the bromine vapor condenser 33 is connected with the low-temperature heat source inlet of the high-temperature heat pump steam device 37 through a cooling water return pipe C2, the cooling water inlet of the bromine vapor condenser 33 is connected with the low-temperature heat source outlet of the high-temperature heat pump steam device 37 through a cooling water inlet pipe C1, the heating side inlet of the high-temperature heat pump steam device 37 is communicated with the water inlet pipe of the heat pump water supply W3, and the heating side outlet of the high-temperature heat pump steam device 37 is the outlet of the third steam Q3.

[0020] The water outlet pipe section of the super-large temperature difference heat exchanger 13 is provided with a safety valve group 14 and a water supply temperature sensor 15, the flue gas outlet pipe section of the sulfur combustion furnace 1 is provided with a combustion furnace flue gas temperature sensor 17, the outlet pipe section of the air blower 21 is provided with a mixed smoke temperature sensor 18, and the connection between the high-temperature SO2 flue 3 and the water washing tower 4 is provided with a medium-temperature flue gas sensor 27; wherein the operation temperature of the water supply temperature sensor 15 is controlled by the opening degree of the electric regulating valve at the outlet of the water supply pump 16, and the low-limit temperature of the mixed smoke temperature sensor 18 is controlled by the opening degree of the mixed air door 19; the low-limit temperature of the combustion furnace flue gas temperature sensor 17 and the low-limit temperature of the medium-temperature flue gas sensor 27 are both controlled by the flow rate of the air blower 21 adjusted by the frequency converter or the air inlet guide vane.

[0021] The working medium in the compressed working medium storage tank 22 is high-pressure nitrogen or compressed air.

[0022] The material of the heat exchange sleeve 20 is carbon steel or boiler steel, and an insulation layer is arranged or not arranged outside; the material of the heat exchange sleeve 26 is carbon steel or boiler steel, and an insulation layer is arranged outside.

[0023] The super large temperature difference heat exchanger 13 adopts a serpentine coil structure, a transverse or longitudinal tube bundle structure, a plate structure or a tube-plate structure; when the transverse or longitudinal tube bundle structure is adopted, the heat exchange pipe adopts a light pipe or finned pipe structure; and the heat exchange material of the super large temperature difference heat exchanger 13 adopts carbon steel, ND steel, stainless steel 304 or stainless steel 316L.

[0024] The material of the feed water pump 16 adopts a high-temperature cast iron pump or a stainless steel water pump.

[0025] The high-efficiency corrosion-resistant deep heat recovery device 36 adopts a high-efficiency graphene plastic pipe heat exchanger; and the original waste liquid heat recovery device 35 adopts a silicon carbide heat exchanger, a glass heat exchanger and / or a fluoroplastic heat exchanger.

[0026] The heat pump host of the high-temperature heat pump steam device 37 adopts a single-stage voltage compression type high-temperature heat pump type, and a series electric heater generates water vapor.

[0027] The innovation points and beneficial effects of the utility model are as follows.

[0028] (1) A new energy production, transportation and use method is adopted to realize the process energy and power driving of seawater concentration and bromine extraction, including greatly adjusting the energy production, transportation and use process flow in the process production, greatly reducing the energy consumption through energy-saving measures, and fundamentally abandoning the power system driven by fossil energy through the use of waste heat steam, heat pump steam, new energy power generation and electric heating steam.

[0029] (2) In view of the strong corrosive nature of high-temperature SO2 flue gas, the patent is based on the acid dew point control method, which ensures that the temperature of the inner wall of the sulfur combustion furnace shell and the flue gas exhaust pipe of the boiler in contact with the flue gas is always maintained above the acid dew point, so as to ensure that there is no acid dew point corrosion, and to ensure that the original equipment system in the waste heat recovery process will not have corrosion problems.

[0030] (3) The patent adopts the method of setting a sleeve outside the sulfur combustion furnace shell and the high-temperature flue gas pipe thereafter, and heat exchange through the annular area, and the heat exchange medium is nitrogen or air, which has no corrosive nature, so that common boiler steel, carbon steel, ND steel, stainless steel 304 or stainless steel 316L, etc. can be used as the heat exchange pipe material, thereby greatly reducing the processing difficulty and cost of the heat exchanger and the entire waste heat boiler, and solving the problem of sulfur combustion furnace flue gas waste heat recovery.

[0031] (4) The waste heat boiler can produce high-parameter waste heat water, and can also produce 0.1-0.6 MPa level saturated wet steam through a flash tank, which is more convenient for recycling in process production.

[0032] (5) By precise control of the most critical boiler feed water temperature to meet the parameter needs of external heat source; control sleeve inlet temperature and combustion furnace flue gas temperature to avoid serious corrosion problems, to ensure the safe and stable operation of the equipment, improve the service life, significantly reduce the whole cycle operation cost. BRIEF DESCRIPTION OF DRAWINGS

[0033] Figure 1 is the system schematic diagram of the conventional production process of seawater concentration and bromine extraction, Figure 2 is the system schematic diagram of the utility model.

[0034] Figure 1 、 2 The numbers and names of various components in the application are as follows.

[0035] Sulfur combustion furnace 1, fly 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, miniature high-temperature waste heat hot water boiler 10, import rectifier section 11, shell 12, super large temperature difference heat exchanger 13, safety valve group 14, feed water temperature sensor 15, feed water pump 16, combustion furnace flue gas temperature sensor 17, mixed smoke temperature sensor 18, combustion furnace flue gas temperature sensor 17, mixed smoke temperature sensor 18, mixed air door 19, heat exchange sleeve 20, air blower 21, compressed working medium gas storage tank 22, flash tank 23, heat exchange sleeve 26, medium-temperature flue gas sensor 27, bromine extraction distillation tower 31, bromine vapor exhaust pipe 32, bromine vapor condenser 33, waste liquid pump 34, original waste liquid heat recovery device 35, high-efficiency corrosion-resistant deep heat recovery device 36, high-temperature heat pump steam device 37, new energy electric heating steam furnace 38, electric heater 39, salt field 40, bitter brine pump 41, air blowing tower 42, liquid chlorine gasification tank 50, water bath 51, coal or gas boiler 60, air blower 61, environmental air A, water supplement B, desalted water supplement Bc, liquid bromine B3, bromine and water vapor mixed gas B1, crude bromine water B2, bromine and air mixed gas B4, finished liquid B5, cooling incoming water C1, cooling outgoing water C2, chlorine gas C3, liquid chlorine C4, new energy power supply E, heat source steam / water H1, heat source outgoing water H2, crude salt K, heating steam Q, new steam Q0, primary steam Q1, secondary steam Q2, third steam Q3, spray water R, sulfur S4, 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 water supplement W2, heat pump feed water W3, seawater Ws. DETAILED DESCRIPTION

[0036] Figure 1 is the system schematic diagram and embodiment of the conventional production process of seawater concentration and bromine extraction, Figure 2 is the system schematic diagram and embodiment of the utility model.

[0037] The system diagram and embodiment of the conventional production process of seawater concentration bromine extraction are shown in Figure 1 The system is composed of the original seawater concentration and air blowing method bromine extraction subsystem, the original sulfur combustion furnace SO2 flue gas preparation subsystem, the original liquid chlorine gasification subsystem, the original bromine extraction distillation liquid bromine preparation subsystem and the steam boiler subsystem, and the connecting pipelines and components thereof, wherein the original seawater concentration and air blowing method bromine extraction subsystem comprises a salt field 40, a bitter brine pump 41, an air blowing tower 42 and the connecting pipelines and components thereof, the original liquid chlorine gasification subsystem comprises a liquid chlorine gasification tank 50, a water bath tank 51 and the connecting pipelines and components thereof, 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 the connecting pipelines and components thereof, the original bromine extraction distillation liquid bromine preparation subsystem comprises a bromine extraction distillation tower 31, a bromine vapor exhaust pipe 32, a bromine vapor condenser 33, a waste liquid pump 34, an original waste liquid heat recovery device 35 and the connecting pipelines and components thereof; the steam boiler subsystem comprises a coal-fired or gas-fired boiler 60, a blower 61 and the connecting pipelines and components thereof, wherein the outlet of the new steam Q0 of the coal-fired or gas-fired boiler 60 is connected with the inlet of the heat source steam / water H1 of the water bath tank 51 and the inlet of the heating steam Q of the bromine extraction distillation tower 31 respectively, the coal-fired or gas-fired boiler 60 is further provided with the inlet of the boiler feed water W1, the combustion-supporting wind inlet of the coal-fired or gas-fired boiler 60 is connected with the air outlet of the blower 61, and the air inlet of the blower 61 is communicated with the ambient air (A).

[0038] The specific embodiments of the utility model are as follows, see Figure 2The utility model discloses a kind of seawater concentration and bromine extraction systems based on depth waste heat recovery and new energy drive, and the specific description of the utility model is as follows: original seawater concentration and air blowing method bromine extraction subsystem, original sulfur combustion furnace preparation SO2 flue gas subsystem, original liquid chlorine gasification subsystem, original bromine extraction distillation preparation liquid bromine subsystem and combustion furnace high-temperature waste heat flash steam boiler subsystem, bromine extraction distillation process waste heat depth recovery subsystem and its connecting pipeline and component composition, wherein original seawater concentration and air blowing method bromine extraction subsystem includes salt field 40, bitter brine pump 41, air blowing tower 42 and its connecting pipeline and component, original liquid chlorine gasification subsystem includes liquid chlorine gasification tank 50, water bath 51 and its connecting pipeline and component, original sulfur combustion furnace preparation SO2 flue gas subsystem includes sulfur combustion furnace 1, fly 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, absorption tower 9 and its connecting pipeline and component, original bromine extraction distillation preparation liquid bromine subsystem includes 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 and its connecting pipeline and component, characterized in that, the combustion furnace high-temperature waste heat flash steam boiler subsystem includes heat exchange sleeve 20, heat exchange sleeve pipe 26, miniature high-temperature waste heat water boiler 10, feed water pump 16, flash tank 23, air blower 21, compressed working medium storage tank 22, mixed air door 19 and its connecting pipeline and component, the bromine extraction distillation process waste heat depth recovery subsystem includes high-efficiency corrosion-resistant depth heat recovery device 36, high-temperature heat pump steam device 37, new energy electric heating steam furnace 38 and its connecting pipeline and component;Wherein the air blowing tower 42 upper portion feed inlet respectively with sulfuric acid SH's water inlet pipe, chlorine C3's air inlet pipe and bitter brine pump 41's outlet, bitter brine pump 41's import and salt field 40's bitter brine outlet are connected, and salt field 40 is provided with seawater Ws's import, coarse salt K's export, air blowing tower 42 lower portion is provided with environmental air A's import, bottom is provided with acidic wastewater P's drain port, top is bromine and air mixed gas B4's exhaust port, and is connected with absorption tower 9 lower portion bromine and air mixed gas B4's air inlet;The chlorine C3 air inlet of air blowing tower 42 is connected with the chlorine outlet of liquid chlorine gasification tank 50, and the lower portion of liquid chlorine gasification tank 50 is arranged in liquid chlorine C4 inlet, and liquid chlorine gasification tank 50 is arranged in water bath 51 tank, and water bath 51 is provided with heat source steam / water H1 import and heat source return water H2 export;The upper portion of the absorption tower 9 is provided with absorption spray water R import, the bottom is provided with complete liquid B5 drain port, and the top is provided with clean SO2 flue gas S2 air inlet.The air inlet of the sulfur combustion furnace 1 is provided with a sulfur S4 inlet 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 of high-temperature SO2 flue gas S1, and is connected with the inlet of the fly ash settling tank 2; the outlet of the fly ash settling tank 2 is connected with the inlet of the high-temperature SO2 flue 3; the connection between the high-temperature SO2 flue 3 and the water washing tower 4 is the cooling SO2 flue gas S3; the top exhaust port of the water washing tower 4 is connected with the top air inlet of the absorption tower 9 through a clean SO2 flue gas pipe 5; the bottom liquid outlet of the water washing tower 4 is connected with the inlet of the water washing pump 7; the outlet of the water washing pump 7 is connected with the circulating water inlet of the water washing tower 4, the water inlet pipe of the water supplement B and the waste sulfuric acid liquid SH1 drainage pipe respectively; the outer side of the high-temperature SO2 flue 3 is provided with a heat exchange sleeve 26, and the closed annular space between the two is a region for flow heat exchange of the heat exchange medium; the air inlet of the heat exchange sleeve 26 is arranged at one end of the cooling SO2 flue gas S3, and the air outlet of the heat exchange sleeve 26 is arranged at one end of the high-temperature SO2 flue gas S1 air inlet; the outer side of the sulfur combustion furnace 1 is provided with a heat exchange sleeve 20, and the closed annular space between the two is a region for flow heat exchange of the heat exchange medium; the air inlet of the heat exchange sleeve 20 is arranged at one end of the sulfur combustion furnace 1 exhaust port, and the air outlet of the heat exchange sleeve 20 is arranged at one end of the sulfur combustion furnace 1 air inlet; the air outlet of the heat exchange sleeve 20 is connected with the high-pressure inlet of the mixed air door 19 and the inlet of the inlet rectifying section 11 of the micro high-temperature waste heat boiler 10; the micro high-temperature waste heat boiler 10 further comprises an outer shell 12, an ultra-large temperature difference heat exchanger 13 and an outlet tapered section; the medium-temperature heat exchange medium outlet of the outlet tapered section is connected with the low-pressure outlet of the mixed air door 19, the inlet of the air blower 21 and the air outlet of the compressed medium storage tank 22; the air outlet of the air blower 21 is connected with the air inlet of the heat exchange sleeve 26; the air outlet of the heat exchange sleeve 26 is connected with the air inlet of the heat exchange sleeve 20; the water inlet of the ultra-large temperature difference heat exchanger 13 is connected with the outlet of the water supply pump 16; the water outlet of the ultra-large temperature difference heat exchanger 13 is connected with the high-temperature water inlet of the flash tank 23; the medium-temperature water outlet of the flash tank 23 is communicated with the inlet of the water supply pump 16 and the water supply pipe of the desalted water supplement Bc; the outlet of the secondary steam Q2 at the top of the flash tank 23 is connected with the inlet of the heat source steam / water H1 of the water bath tank 51, the inlet of the heating steam Q of the bromine distillation tower 31, the outlet of the primary steam Q1 of the new energy electric heating steam furnace 38 and the outlet of the third steam Q3 of the high-temperature heat pump steam device 37 respectively; the new energy electric heating steam furnace 38 is further provided with the inlet of the electric boiler water supplement W2; the new energy electric heating steam furnace 38 is internally provided with an electric heater 39; the two ends of the electric heater 39 are connected with the power supply line of the new energy power supply E respectively.The low-temperature side inlet of the high-efficiency anti-corrosion deep heat recovery device 36 is connected with the liquid outlet at the bottom of the absorption tower 9 through a liquid supply pipe of the liquid B5, the low-temperature side outlet of the high-efficiency anti-corrosion deep heat recovery device 36 is connected with 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 with the liquid inlet at the upper part of the bromine distillation tower 31, the inlet of the chlorine gas C3 at the lower part of the bromine distillation tower 31 is connected with the chlorine gas outlet of the liquid chlorine gasification tank 50, the liquid outlet at the bottom of the bromine distillation tower 31 is connected with the inlet of the waste liquid pump 34, the outlet of the waste liquid pump 34 is connected with 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 with 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 communicated with the water return pipe of the bromine distillation waste liquid SH2; the top of the bromine distillation tower 31 is a gathering area of the bromine and water vapor mixed gas B1, the top gas outlet is connected with the gas inlet at the upper part of the bromine vapor condenser 33 through a bromine vapor exhaust pipe 32, the liquid outlet at the lower part of the bromine vapor condenser 33 is communicated with the water outlet pipe of the liquid bromine B3, and the liquid outlet of the crude bromine water B2 at the bottom of the bromine vapor condenser 33 is connected with the liquid inlet at the upper part of the bromine distillation tower 31; the cooling water outlet of the bromine vapor condenser 33 is connected with the low-temperature heat source inlet of the high-temperature heat pump steam device 37 through a cooling water return pipe C2, the cooling water inlet of the bromine vapor condenser 33 is connected with the low-temperature heat source outlet of the high-temperature heat pump steam device 37 through a cooling water inlet pipe C1, the heating side inlet of the high-temperature heat pump steam device 37 is communicated with the water inlet pipe of the heat pump water supply W3, and the heating side outlet of the high-temperature heat pump steam device 37 is the outlet of the third steam Q3.

[0039] The water outlet pipe section of the super-large temperature difference heat exchanger 13 is provided with a safety valve group 14 and a water supply temperature sensor 15, the flue gas outlet pipe section of the sulfur combustion furnace 1 is provided with a combustion furnace flue gas temperature sensor 17, the outlet pipe section of the air blower 21 is provided with a mixed smoke temperature sensor 18, and the connection between the high-temperature SO2 flue 3 and the water washing tower 4 is provided with a medium-temperature flue gas sensor 27; wherein the operation temperature of the water supply temperature sensor 15 is controlled by the opening degree of the electric regulating valve at the outlet of the water supply pump 16, and the low-limit temperature of the mixed smoke temperature sensor 18 is controlled by the opening degree of the mixed air door 19; the low-limit temperature of the combustion furnace flue gas temperature sensor 17 and the low-limit temperature of the medium-temperature flue gas sensor 27 are both controlled by the flow rate of the air blower 21 adjusted by the frequency converter or the air inlet guide vane.

[0040] The working medium in the compressed working medium storage tank 22 is high-pressure nitrogen or compressed air.

[0041] The material of the heat exchange sleeve 20 is carbon steel or boiler steel, and an insulation layer is arranged or not arranged outside; the material of the heat exchange sleeve 26 is carbon steel or boiler steel, and an insulation layer is arranged outside.

[0042] The super large temperature difference heat exchanger 13 adopts a serpentine coil structure, a transverse or longitudinal tube bundle structure, a plate structure or a tube-plate structure; when the transverse or longitudinal tube bundle structure is adopted, the heat exchange pipe adopts a light pipe or a finned pipe structure; and the heat exchange material of the super large temperature difference heat exchanger 13 adopts carbon steel, ND steel, stainless steel 304 or stainless steel 316L.

[0043] The material of the feed water pump 16 adopts a high-temperature cast iron pump or a stainless steel water pump.

[0044] The high-efficiency corrosion-resistant deep heat recovery device 36 adopts a high-efficiency graphene plastic pipe heat exchanger; and the original waste liquid heat recovery device 35 adopts a silicon carbide heat exchanger, a glass heat exchanger and / or a fluoroplastic heat exchanger.

[0045] The heat pump main machine of the high-temperature heat pump steam device 37 adopts a single-stage voltage compression type high-temperature heat pump type, and a series electric heater generates water vapor.

[0046] It should be noted that the utility model constructs a brand new energy power system of seawater concentration and bromine extraction, and different specific implementation measures and specific implementation devices of different structures can be adopted according to the solution, the above specific implementation mode is only one implementation type, and any other similar simple transformation mode, for example, simple increase, reduction, transformation and change of relative positions of internal components and interfaces, simple combination and adjustment of external pipelines and components, etc., all fall within the protection scope of the utility model.

Claims

1. A seawater concentration and bromine extraction system based on deep waste heat recovery and new energy drive, 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 pipes and components, wherein 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 pipes 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 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 pipes and components, the original bromine extraction 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, characterized in that, The combustion furnace high-temperature waste heat flash steam 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 feed pump (16), a flash tank (23), a blower (21), a compressed working medium gas storage tank (22), a mixing damper (19) and its connecting pipes and components. The bromine extraction distillation process waste heat deep recovery subsystem includes 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 its connecting pipes and components; wherein the feed port on the upper part of the air blowing tower (42) is respectively connected to the water inlet pipe of sulfuric acid (SH), the air inlet pipe of chlorine (C3) and the outlet of the bittern pump (41), and the bittern pump (41) The inlet of the air blowing tower (42) is connected to the bittern outlet of the salt pan (40), and the salt pan (40) is provided with an inlet of seawater (Ws) and an outlet of crude salt (K). The lower part of the air blowing tower (42) is provided with an inlet of ambient air (A), a drain outlet of acidic wastewater (P) is provided at the bottom, and an exhaust outlet of bromine and air mixture (B4) is provided at the top, and is connected to the air inlet of bromine and air mixture (B4) at the lower part of the absorption tower (9); the air inlet of chlorine (C3) 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 provided at the liquid inlet of liquid chlorine (C4), the liquid chlorine gasification tank (50) is provided in the tank of the water bath (51), and the water bath (51) is provided with an inlet of heat source steam / water (H1) and The 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 discharge port of the finished liquid (B5), 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 of sulfur (S4) 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 of 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 SO2 flue gas (S3 ), 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 supply (B) and the drain pipe of the waste sulfuric acid liquid (SH1); a heat exchange sleeve (26) is provided on the outside of the pipe 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 provided at the end where the cooling SO2 flue gas (S3) is located, and the air outlet of the heat exchange sleeve (26) is provided at the end of the air inlet where the high-temperature SO2 flue gas (S1) is located;A heat exchange sleeve (20) is provided on the outer side of 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 provided at one end of the smoke outlet of the sulfur combustion furnace (1), and the air outlet of the heat exchange sleeve (20) is provided 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 includes a shell (12), an ultra-large temperature difference heat exchanger (13) and an outlet tapered section, and the outlet of the medium-temperature heat exchange medium of the outlet tapered section is connected to the mixing damper (19). 9), the low-pressure outlet of the blower (21), the inlet of the blower (21) and the outlet of the compressed working medium storage tank (22) are connected, the outlet of the blower (21) is connected to the inlet of the heat exchange sleeve (26), and the outlet of the heat exchange sleeve (26) is connected to the 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 connected to the heat source steam / water (H1) of the water bath (51) respectively. ) inlet, the heating steam (Q) inlet of the bromine extraction distillation tower (31), the primary steam (Q1) outlet of the new energy electric steam furnace (38) and the third steam (Q3) outlet of the high-temperature heat pump steam device (37) are connected; wherein the new energy electric steam furnace (38) is also provided with an electric boiler water supply (W2) inlet, 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 (B5), 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 (B5). The 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 (C3) 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 (B1). The top gas outlet is connected to the gas 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 outlet pipe of the liquid bromine (B3). The liquid outlet of the crude bromine water (B2) at the bottom of the bromine steam condenser (33) is connected to the liquid inlet of the upper part of the bromine extraction distillation tower (31). The cooling water outlet of the bromine steam condenser (33) is connected to the cooling water outlet of the bromine steam condenser (33). The return pipe of the supercooling return water (C2) is connected to the low-temperature heat source inlet of the high-temperature heat pump steam 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 device (37) through the inlet pipe of the cooling inlet water (C1). The heating side inlet of the high-temperature heat pump steam device (37) is connected to the inlet pipe of the heat pump feed water (W3). The heating side outlet of the high-temperature heat pump steam device (37) is the outlet of the third steam (Q3).

2. The seawater concentration and bromine extraction system based on deep waste heat recovery and new energy drive according to claim 1 is characterized in that The outlet pipe section of the ultra-large temperature difference heat exchanger (13) is provided with a safety valve group (14) and a water supply temperature sensor (15); the flue gas outlet pipe section of the sulfur combustion furnace (1) is provided with a combustion furnace exhaust temperature sensor (17); the outlet pipe section of the blower (21) is provided with a mixed smoke temperature sensor (18); and the connection between the high-temperature SO2 flue (3) and the water washing tower (4) is provided with a medium-temperature flue gas sensor (27); 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. The seawater concentration and bromine extraction system based on deep waste heat recovery and new energy drive according to claim 1 is characterized in that The working medium in the compressed working medium gas storage tank (22) is high-pressure nitrogen or compressed air.

4. The seawater concentration and bromine extraction system based on deep waste heat recovery and new energy drive according to claim 1 is characterized in that The heat exchange sleeve (20) is made of carbon steel or boiler steel, and may or may not be provided with an insulation layer on the outside; the heat exchange sleeve (26) is made of carbon steel or boiler steel, and may or may not be provided with an insulation layer on the outside.

5. The seawater concentration and bromine extraction system based on deep waste heat recovery and new energy drive according to claim 1 is 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-plate 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. The seawater concentration and bromine extraction system based on deep waste heat recovery and new energy drive according to claim 1 is 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 seawater concentration and bromine extraction system based on deep waste heat recovery and new energy drive according to claim 1 is characterized in that The high-efficiency corrosion-resistant 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 seawater concentration and bromine extraction system based on deep waste heat recovery and new energy drive 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.

Images