A self-heating multiple-effect evaporation apparatus

Abstract

The application relates to a self-heating multi-effect evaporation device, belonging to the technical field of multi-effect evaporation, wherein a primary-effect medium circulation pipeline is arranged on a flash evaporation unit of a primary effect, the flash evaporation units of the remaining effects are connected in series through pipelines, the medium outlet of a flash evaporation unit of a last effect is connected with the medium inlet of a heat exchange unit of a penultimate effect, the tube passes of multiple heat exchange units are connected in series, the medium outlet of a heat exchange unit of a primary effect is connected with the medium inlet of a flash evaporation unit of a penultimate primary effect through a pipeline, and a cooling circulation pipeline is arranged on the heat exchange unit of the last effect. The application recycles complex high-pollution waste heat as a driving heat source, realizes energy saving and carbon reduction, reduces energy consumption, and reduces operation cost, simultaneously adopts an equivalent flash evaporation self-heating mode, realizes multi-stage serial heating and multi-stage flash evaporation, completely separates waste water heating from flash evaporation, and solves problems such as large steam pipelines and complex pipeline routes.

Description

TECHNICAL FIELD

[0001] The application belongs to the technical field of multi-effect evaporation, and particularly relates to a self-heating multi-effect evaporation device. BACKGROUND

[0002] Material and high-salinity wastewater concentration is a key link widely used or necessary in industrial production, and plays an indispensable role in many industries such as metallurgy, papermaking, electricity, and chemical industry. However, the traditional material and high-salinity wastewater concentration process generally has the problem of high energy consumption. Most of these processes rely on external heat sources such as steam and electricity to realize the evaporation and concentration of water in the material, and the huge energy consumption not only increases the production cost of enterprises, but also makes enterprises face the risk of production limitation when energy supply is tight.

[0003] On the other hand, a large amount of valuable energy is consumed in the industrial production process, and the industrial waste heat generated after a large amount of energy consumption often has the problem of complex heat medium composition and low heat grade, which is difficult to recycle and utilize.

[0004] Taking the desulfurization system of a coal-fired boiler as an example, most of the desulfurization processes used by coal-fired units of power plants or heating companies in China are wet desulfurization. In the wet desulfurization process, the desulfurization slurry is fully contacted with the flue gas by spraying, and at the same time of reaction desulfurization, the heat in the flue gas is also continuously absorbed by the desulfurization slurry, so that the slurry temperature is maintained at 40-60℃. In most coal-fired units, this part of heat is not effectively utilized and is wasted. In addition, due to the continuous reaction of the slurry and the enrichment of chloride ions, a certain amount of desulfurization waste liquid needs to be regularly discharged from the desulfurization system. The desulfurization waste liquid is high-salinity wastewater, which is difficult to treat. The commonly used desulfurization wastewater treatment scheme currently consumes a large amount of electricity or clean steam as the driving energy for wastewater concentration, resulting in a large amount of energy and economic waste.

[0005] Taking the alkali recovery system of a pulp paper mill as another example, the alkali recovery system of a pulp paper mill is realized by concentrating the black liquor and then burning it in an alkali furnace. The alkali furnace uses black liquor with a concentration of more than 80% as fuel, and the combustion produces steam for power generation and process use. At the same time, the flue gas produced by the boiler combustion carries a large amount of waste heat which is wasted by being discharged. At present, black liquor concentration mostly uses multi-effect evaporation process with medium-high pressure steam as heat source to realize black liquor concentration, resulting in a large amount of energy consumption and economic waste.

[0006] The distance between the existing heat source and the heat-using system of multi-effect evaporation is too long, and pipelines need to be laid to complete the introduction of the heat source in the complex plant, which increases the construction difficulty and pipeline cost, and the waste heat utilization rate is low. SUMMARY

[0007] To solve the above technical problems, the technical scheme adopted by the present application is: a self-heating multi-effect evaporation device, comprising: a plurality of flash evaporation units and a plurality of heat exchange units, the steam exhaust generated by the flash evaporation unit provides a heat source for the equivalent heat exchange unit, wherein the first effect medium circulation pipeline is arranged on the flash evaporation unit located at the first effect, the remaining effect flash evaporation units are connected in series through the pipeline, the medium outlet of the flash evaporation unit located at the last effect is connected with the medium inlet of the heat exchange unit located at the second last effect, the tube side of a plurality of heat exchange units is connected in series, the medium outlet of the heat exchange unit located at the first effect is connected with the medium inlet of the flash evaporation unit located at the second first effect through the pipeline, and the cooling circulation pipeline is arranged on the heat exchange unit located at the last effect, wherein the medium pipeline to be heated is arranged on any one of the flash evaporation units at the first effect or on the tube side of any one of the heat exchange units at the first and last effects.

[0008] Further, the shell side of the heat exchange unit is connected with a multi-stage partial pressure unit for vacuum treatment of the flash evaporation unit.

[0009] Further, the heat exchange unit is provided with a vacuum pump group for vacuum treatment of the flash evaporation unit.

[0010] Further, the multi-stage partial pressure unit comprises a water jet partial pressure device, and the shell side of the heat exchange unit is connected with the water jet partial pressure device through a pipeline and a vacuum port arranged on the water jet partial pressure device for vacuumizing.

[0011] Further, a partial pressure orifice plate is fixedly arranged in the steam-water mixing chamber in the water jet partial pressure device.

[0012] Further, when the medium in the flash evaporation unit located at the first effect is the same as the medium in the flash evaporation units at other effects, the partial pressure liquid down pipe gas outlets of a plurality of water jet partial pressure devices are all placed below the liquid medium liquid level in the first liquid seal tank, and a first air outlet port for air extraction is arranged on the first liquid seal tank.

[0013] Further, when the medium in the flash evaporation unit located at the first effect is different from the medium in the flash evaporation units at other effects, the partial pressure liquid down pipe gas outlet of the water jet partial pressure device connected with the shell side of the heat exchange unit located at the first effect is placed below the liquid medium liquid level in the second liquid seal tank, the partial pressure liquid down pipe gas outlets of the water jet partial pressure devices connected with the shell sides of the heat exchange units at other effects are placed below the liquid medium liquid level in the first liquid seal tank, and a first air outlet port for air extraction is arranged on the first liquid seal tank.

[0014] Further, a second air outlet port is arranged on the second liquid seal tank or the second liquid seal tank is connected with the first liquid seal tank through a common air pipeline.

[0015] Further, the distance between the outlet of the water jet pressure reducer and the liquid level in the first liquid seal tank is proportional to the vacuum pressure at the vacuum port.

[0016] Further, a pressure reduction hole plate is slidably arranged in the steam-water mixing chamber of the water jet pressure reducer, an extension down pipe is slidably sleeved on the pressure reduction down pipe, the extension down pipe is connected to the pressure reduction down pipe through a tension spring, and the extension down pipe is connected to the pressure reduction hole plate through a connecting rod.

[0017] Further, the heat exchange unit of the first effect delivers condensed water to a second condensed water tank through a pipeline, and the heat exchange unit of the remaining effect delivers condensed water to a first condensed water tank through a pipeline.

[0018] Further, the heat exchange unit delivers condensed water to the first liquid seal tank or the first condensed water tank through a pipeline.

[0019] Further, the heat exchange unit of the first effect delivers condensed water to a second liquid seal tank or a second condensed water tank through a pipeline, and the heat exchange unit of the remaining effect delivers condensed water to the first liquid seal tank or the first condensed water tank through a pipeline.

[0020] Further, a first liquid supplement pipeline is arranged between the second condensed water tank and the second liquid seal tank, and a second liquid supplement pipeline is arranged between the first liquid seal tank and the first condensed water tank.

[0021] Further, a second liquid supplement pipeline is arranged between the first liquid seal tank and the first condensed water tank.

[0022] Further, the medium inlet of the water jet variable-diameter nozzle of the water jet pressure reducer is connected with a liquid inlet pipe.

[0023] Further, the first liquid seal tank is provided with a first drainage pipeline and a first water inlet pipeline.

[0024] Further, a first circulation pipeline is arranged between the liquid inlet pipe and the first drainage pipeline.

[0025] Further, the second liquid seal tank is provided with a second drainage pipeline and a second water inlet pipeline.

[0026] Further, a second circulation pipeline is arranged between the liquid inlet pipe and the second drainage pipeline.

[0027] Further, the first air extraction port is connected to a shared gas storage barrel through a pipeline, and the shared gas storage barrel is provided with a shared air extraction pump group.

[0028] Furthermore, the first air extraction port is connected to a shared air storage tank via a pipeline, the shared air storage tank is equipped with a shared air extraction pump set, and the second liquid seal box is equipped with a second air extraction port for air extraction, the second air extraction port being connected to the shared air storage tank via a pipeline.

[0029] Furthermore, regulating valves are installed on both the liquid inlet pipe and the vacuum port.

[0030] The beneficial effects of this invention are:

[0031] This application achieves energy conservation, carbon reduction, and lower operating costs by recovering complex and highly polluting waste heat as a driving heat source. It employs an equivalent flash evaporation self-heating method, realizing multi-stage series heating followed by multi-stage flash evaporation, and complete separation of wastewater heating and flash evaporation. This solves problems such as large and complex steam pipelines, and addresses the issue of localized overboiling and scaling caused by simultaneous heating and evaporation. Waste heat extraction-driven heating, flash evaporation concentration self-heating, and flash evaporation concentration cooling are integrated, and each working unit can be arranged vertically, saving space. Through a combination of various vacuum devices, the low-temperature waste heat generated in this process section is recovered via high-vacuum phase change, and ultra-low temperature material flash evaporation concentration is achieved. This also solves the problems of waste heat resource waste and long-distance transportation of high-grade clean energy. The concentration medium is heated in series in each flash evaporation unit, requiring only one material circulation pump for material circulation heating and flash evaporation, reducing the number of rotating equipment, lowering the system failure rate, and saving energy. Attached Figure Description

[0032] Figure 1 This is a system diagram of Embodiment 1 of the present invention;

[0033] Figure 2 This is a system diagram of Embodiment 2 of the present invention;

[0034] Figure 3 This is a system diagram of Embodiment 2, Method Two of the present invention;

[0035] Figure 4 This is a system diagram of Embodiment 3 of the present invention;

[0036] Figure 5 This is a system diagram of Embodiment 3, Method 2 of the present invention;

[0037] Figure 6 This is a schematic diagram of the structure of Embodiment 4 of the present invention.

[0038] Explanation of reference numerals in the attached figures

[0039] The flash evaporation unit 100, the heat exchange unit 200, the primary effect medium circulation pipeline 300, the cooling circulation pipeline 400, the multi-stage pressure reduction unit 500, the water jet pressure reducer 510, the vacuum port 512, the pressure reduction liquid lower pipe 513, the steam-water mixing chamber 514, the pressure reduction hole plate 515, the water jet variable diameter nozzle 516, the telescopic lower pipe 517, the tension spring 518, the connecting rod 519, the first liquid seal tank 520, the first drainage pipeline 521, the first water inlet pipeline 522, the first circulation pipeline 523, the first air extraction port 524, the second liquid seal tank 530, the second drainage pipeline 531, the second water inlet pipeline 532, the second circulation pipeline 533, the second air extraction port 534, the first liquid supplement pipeline 540, the second liquid supplement pipeline 550, the medium to be heated pipeline 600, the vacuum pump set 700, the first condensate water tank 800, the second condensate water tank 900, the liquid inlet pipe 1000, the shared gas storage barrel 1100, the shared air extraction pump set 1200, the shared air pipeline 1300, and the regulating valve 1400. DETAILED DESCRIPTION

[0040] In the description of the present application, it needs to be understood that the terms "center", "longitudinal", "transverse", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer" and the like indicate the orientation or positional relationship shown in the drawings, which are only for the convenience of describing the present application and simplifying the description, and do not indicate or imply that the devices or elements indicated must have a particular orientation, be constructed and operated in a particular orientation, and therefore cannot be understood as a limitation on the present application. In addition, the terms "first", "second" and the like are only for the purpose of description and cannot be understood as indicating or implying relative importance or implicitly indicating the number of the technical features indicated. Therefore, the features defined with "first", "second" and the like can explicitly or implicitly include one or more of the features. In the description of the present application, unless otherwise specified, the meaning of "a plurality of" is two or more.

[0041] In the description of the present application, it needs to be understood that unless otherwise explicitly specified and limited, the terms "mounting", "connecting", "connection" should be understood in a broad sense, for example, it can be fixed connection, or detachable connection, or integral connection; it can be mechanical connection, or electrical connection; it can be direct connection, or indirect connection through an intermediate medium; it can be the communication inside two elements. For those skilled in the art, the specific meaning of the above terms in the present application can be understood according to the specific circumstances.

[0042] The present application will be further described below in conjunction with the embodiments and the drawings:

[0043] Example 1: as Figure 1As shown, a self-heating multi-effect evaporation device comprises: a plurality of flash evaporation units 100 and a plurality of heat exchange units 200, the steam waste steam generated by the flash evaporation units 100 provides a heat source for the equivalent heat exchange units 200, wherein the first effect medium circulation pipeline 300 is arranged on the first effect flash evaporation unit 100, the remaining effect flash evaporation units 100 are connected in series through pipelines, the medium outlet of the last effect flash evaporation unit 100 is connected with the medium inlet of the second last effect heat exchange unit 200, the tube side of the plurality of heat exchange units 200 is connected in series, the medium outlet of the first effect heat exchange unit 200 is connected with the medium inlet of the second effect flash evaporation unit 100 through a pipeline, and the cooling circulation pipeline 400 is arranged on the last effect heat exchange unit 200, wherein the medium pipeline 600 is arranged on any one of the first effect flash evaporation unit 100 or the tube side of any one of the first effect and the last effect heat exchange unit 200. The vacuum pump set 700 for vacuum treatment of the flash evaporation unit 100 is arranged on the heat exchange unit 200. The first effect heat exchange unit 200 delivers condensed water to the second condensed water tank 900 through a pipeline, and the remaining effect heat exchange units 200 deliver condensed water to the first condensed water tank 800 through a pipeline.

[0044] Wherein, the flash evaporation unit 100 and the heat exchange unit 200 can be an integrated structure or connected through a pipeline for delivering steam waste steam; "the steam waste steam generated by the flash evaporation unit 100 provides a heat source for the equivalent heat exchange unit 200" means that there is a steam waste steam medium transmission relationship between the flash evaporation unit and the heat exchange unit, that is, they are in an equivalent relationship; "the first effect heat exchange unit 200" means the heat exchange unit 200 of the flash evaporation unit through which the medium to be concentrated enters for the first time; "the first effect flash evaporation unit 100" means the flash evaporation unit equivalent to "the first effect heat exchange unit 200"; "the last effect flash evaporation unit 100" means the flash evaporation unit through which the medium to be concentrated enters the heat exchange unit for the first time; "the last effect heat exchange unit 200" means the heat exchange unit equivalent to "the last effect flash evaporation unit 100"; a demister is arranged in the flash evaporation unit 100 for removing liquid droplets carried in the steam waste steam, a plurality of flash evaporation units 100 can be vertically arranged, the medium circulation between the plurality of flash evaporation units 100 is realized through liquid medium gravity, thereby saving the use of liquid pumps and costs, the heat exchange unit 200 is a steam-water heat exchanger, the first effect medium circulation pipeline 300 is a heat source circulation pipeline, the cooling circulation pipeline 400 provides a cold source for the last effect heat exchange unit 200, dissipates the remaining heat energy of the system, ensures the heat balance of the system, and the vacuum pump set 700 can adopt a Roots pump combined with a water ring pump or other forms of vacuum pump set that can meet the requirements.

[0045] The application realizes energy saving and carbon reduction, reduces energy consumption and operating cost by recycling complex high-pollution waste heat as driving heat source. Meanwhile, the equivalent flash evaporation self-heating mode is adopted to realize multi-stage series heating and multi-stage flash evaporation, complete separation of wastewater heating and flash evaporation, solve the problems of large steam pipeline and complex pipeline layout, solve the problem of local over-boiling caused by simultaneous heating and evaporation, avoid the problem of scaling on heat exchange, waste heat extraction driving heating, flash evaporation concentration self-heating, flash evaporation concentration cooling integration, each working unit can be arranged vertically, save the land occupation. Through the combination of multiple forms of vacuum devices, the low-temperature waste heat generated in this process section is recovered by high-vacuum phase change, and the ultra-low-temperature material is flash evaporated and concentrated, which solves the problems of waste of waste heat resources in this process section and long-distance transportation of high-grade clean energy. The concentrated medium is heated in series in each flash evaporation unit, and only one material circulating pump is needed to realize the circulating heating and flash evaporation of the material, reduce the number of rotating equipment, reduce the system failure rate, and save energy consumption.

[0046] Comparative example:

[0047] Technical comparison items 5-effect self-heating evaporation 5-effect multi-effect evaporation Floor area 15-20㎡ 80-100㎡ Number of flash material circulating pumps 1 unit 5 units Inter-effect connecting pipeline Inter-effect 0.5 m or less Connecting pipeline of at least 10 m or more per inter-effect Evaporation-condensation connecting pipeline No pipeline 2 meters or more

[0048] Example 2: as Figure 2 and Figure 3As shown, on the basis of Embodiment 1, the vacuum pump set 700 is replaced by a multi-stage pressure reduction unit 500, and the shell side of the heat exchange unit 200 is connected with the multi-stage pressure reduction unit 500 for vacuumizing the flash evaporation unit 100. The multi-stage pressure reduction unit 500 comprises water-jet pressure reducers 510, and the shell side of the heat exchange unit 200 is connected with the water-jet pressure reducers 510 through pipelines and vacuum ports 512 provided on the water-jet pressure reducers 510 for vacuumizing. A pressure reduction orifice plate 515 is fixedly arranged in a steam-water mixing chamber 514 in the water-jet pressure reducer 510. When the medium in the flash evaporation unit 100 at the first stage is the same as the medium in the flash evaporation unit 100 at other stages, the gas outlet of the pressure reduction liquid down pipe 513 of the water-jet pressure reducer 510 is arranged below the liquid level of the liquid medium in the first liquid seal tank 520, and a first air outlet 524 for air extraction is arranged on the first liquid seal tank 520. The distance between the gas outlet of the pressure reduction liquid down pipe 513 of the water-jet pressure reducer 510 and the liquid level of the liquid medium in the first liquid seal tank 520 is proportional to the vacuum pressure at the vacuum port 512. The medium inlet of the water-jet variable-diameter nozzle 516 of the water-jet pressure reducer 510 is connected with a liquid inlet pipe 1000. An adjusting valve 1400 is arranged on the liquid inlet pipe 1000 and the pipeline of the vacuum port 512. The first air outlet 524 is connected with a shared gas storage barrel 1100 through a pipeline, and a shared air extraction pump set 1200 is arranged on the shared gas storage barrel 1100. The heat exchange unit 200 at the first stage is connected with a second condensate water tank 900 through a pipeline for conveying condensate water, and the heat exchange units 200 at the other stages are connected with a first condensate water tank 800 through pipelines for conveying condensate water. When the medium in the flash evaporation unit 100 at the first stage is the same as the medium in the flash evaporation unit 100 at other stages, all the heat exchange units 200 are connected with the first liquid seal tank 520 or the first condensate water tank 800 through pipelines for conveying condensate water, and a second liquid supplementing pipeline 550 is arranged between the first liquid seal tank 520 and the first condensate water tank 800. A first water outlet pipeline 521 and a first water inlet pipeline 522 are arranged on the first liquid seal tank 520. A first circulation pipeline 523 is arranged between the liquid inlet pipe 1000 and the first water outlet pipeline 521.

[0049] The water jet pressure divider can be called an ejector or an inducer, the first liquid seal tank 520 is a closed tank body, and a liquid with a certain height is arranged inside for liquid sealing; the vacuum port 512 is communicated with the heat exchange unit 200 through a pipeline, and is used for establishing a vacuum environment for the flash evaporation unit 100; the pressure distribution hole plate 515 is a plate structure, and a plurality of pressure distribution holes are arranged on the plate structure, the delivery pressure distribution hole is a horn shape, the large hole of the pressure distribution hole faces the water jet variable-diameter nozzle 516, the plate structure makes the pressure distribution uniform when the fluid passes, and flow instability caused by local abnormal resistance is avoided; the horn hole large hole inlet efficiently guides the fluid, accelerates the formation of high-speed jet flow through the tapered structure, and significantly improves the pressure distribution efficiency; the high-speed jet flow enhances the medium turbulence in the steam-water mixing chamber 514, promotes sufficient mixing of gas and liquid, and improves the heat exchange efficiency; at the same time, the negative pressure area formed at the rear side of the hole plate directly acts on the vacuum port 512, strengthens the air exhaust capacity for the flash evaporation unit 100, and maintains a stable vacuum environment; in addition, uniform pressure distribution, efficient pressure distribution mixing and stable vacuum treatment jointly guarantee the stability of system operation, reduce the risk of failure caused by local abnormalities, and finally realize efficient energy saving and reliable operation of the multi-effect evaporation system; the shared gas storage barrel 1100 is used for temporarily storing non-condensable gas discharged in the system, so that the vacuum pumping system realizes intermittent operation; the vacuum environment forming mode is that after the system is started, the air in the gas storage barrel 1100 is first discharged by the vacuum pump set, a vacuum environment is formed in the gas storage cylinder, a pressure difference is formed between the gas storage cylinder and the system, the vacuum pump set is reduced in frequency or suspended, the non-condensable gas discharged in the system is continuously discharged into the gas storage cylinder under the action of the pressure difference, and when the pressure in the gas storage cylinder reaches a set value, the vacuum pump set is started again to exhaust air, so that the energy consumption of the vacuum pump set in operation is saved and the system pressure is stabilized.

[0050] The application places a plurality of water jet pressure dividers 510 in the same first liquid seal tank 520, connects a shared gas storage barrel 1100 through a first air outlet 524, and realizes vacuum treatment of a plurality of vacuum chambers through a shared air pump set 1200, thereby saving the investment in vacuum pumps and realizing cost saving. Meanwhile, the application is provided with an adjusting valve 1400 for adjusting the liquid inlet flow rate and the air exhaust flow rate of the vacuum port 512, thereby adjusting the vacuum pressure of the components connected to the vacuum port 512. Meanwhile, the distance between the gas outlet of the pressure distribution liquid down pipe 513 and the liquid medium liquid level in the first liquid seal tank 520 is set in direct proportion to the vacuum pressure at the vacuum port 512, which can prevent the adjacent water jet pressure dividers 510 from forming a vacuum channel and thereby destroying the vacuum pressure in the vacuum chambers connected to each other, further improves the system stability, realizes differential pressure grading under super-high vacuum and extreme vacuum, and simultaneously realizes that a plurality of temperature difference flash evaporation units share a set of vacuum equipment. Meanwhile, through the action of inducement air exhaust, the air exhaust load of the vacuum pump can be greatly reduced, and the energy consumption of the air pump set can be reduced.

[0051] Embodiment 3, as Figure 4 and Figure 5As shown, the difference with Example 2 is that when the medium in the first effect of the flash evaporation unit 100 is different from the medium in the other effects of the flash evaporation unit 100, the liquid outlet tube 513 of the water-jet pressure reducer 510 connected to the shell side of the heat exchange unit 200 in the first effect is arranged below the liquid level of the liquid medium in the second liquid seal tank 530, and the liquid outlet tube 513 of the water-jet pressure reducer 510 connected to the shell side of the heat exchange unit 200 in the other effects is arranged below the liquid level of the liquid medium in the first liquid seal tank 520, and the first liquid seal tank 520 is provided with a first gas outlet 524 for gas extraction. The second liquid seal tank 530 is provided with a second gas outlet 534 or is connected to the first liquid seal tank 520 through a common gas pipeline 1300. The first gas outlet 524 is connected to a common gas storage tank 1100 through a pipeline, and the common gas storage tank 1100 is provided with a common gas extraction pump group 1200. The second liquid seal tank 530 is provided with a second gas outlet 534 for gas extraction, and the second gas outlet 534 is connected to the common gas storage tank 1100 through a pipeline. The heat exchange unit 200 in the first effect is connected to a second condensate tank 900 through a pipeline, and the heat exchange unit 200 in the other effects is connected to a first condensate tank 800 through a pipeline. The heat exchange unit 200 in the first effect is connected to the second liquid seal tank 530 or the second condensate tank 900 through a pipeline, and the heat exchange unit 200 in the other effects is connected to the first liquid seal tank 520 or the first condensate tank 800 through a pipeline. The second condensate tank 900 and the second liquid seal tank 530 are provided with a first liquid supplement pipeline 540, and the first liquid seal tank 520 and the first condensate tank 800 are provided with a second liquid supplement pipeline 550. The first liquid seal tank 520 and the first condensate tank 800 are provided with a second liquid supplement pipeline 550. The second liquid seal tank 530 is provided with a second drain pipeline 531 and a second water inlet pipeline 532. The water inlet pipeline 1000 and the second drain pipeline 531 are provided with a second circulation pipeline 533.

[0052] Wherein, the first liquid seal tank 520 and the second liquid seal tank 530 are the same structure, and the size is determined according to the situation, the second water inlet pipeline 532 is used to supplement the medium in the second liquid seal tank 530, and the second circulation pipeline 533 is used to realize the connection between the water-jet pressure reducer 510 and the second liquid seal tank 530, realize internal circulation, and further improve the efficiency.

[0053] This application considers the situation where the medium in the first-effect flash evaporation unit 100 is different from the medium in the flash evaporation units 100 of other effects. In order to utilize the condensate generated by the heat exchange unit 200, a first liquid seal tank 520 and a second liquid seal tank 530 are provided. The condensate generated by the first-effect heat exchange unit 200 is transported to the first liquid seal tank 520 for liquid sealing, and the condensate generated by the heat exchange units 200 of other effects is transported to the second liquid seal tank 530 for liquid sealing. This effectively prevents the condensate water quality from affecting each other. At the same time, the second liquid seal tank 530 and the first liquid seal tank 520 are connected through a common gas pipeline 1300, so that they can share a common air pump group 1200, which also achieves the condition of saving pump group.

[0054] Example 4, as Figure 6 As shown, unlike Embodiment 2, where the pressure dividing orifice plate 515 is not fixedly installed in the steam-water mixing chamber 514, the pressure dividing orifice plate 515 is slidably disposed in the steam-water mixing chamber 514 of the water jet separator 510. A telescopic lower tube 517 is slidably fitted on the pressure dividing liquid lower tube 513. The telescopic lower tube 517 is connected to the pressure dividing liquid lower tube 513 through a tension spring 518. The telescopic lower tube 517 is connected to the pressure dividing orifice plate 515 through a connecting rod 519.

[0055] In Embodiment 4 of this application, the dynamic pressure adjustment structure of the water jet pressure divider 510 achieves adaptive control of the fluid dynamics characteristics within the steam-water mixing chamber 514 through the linkage design of the sliding pressure dividing orifice plate 515, the telescopic lower tube 517, and the tension spring 518, significantly improving the overall performance of the multi-effect evaporation system. This structure uses the high-speed jet from the variable-diameter nozzle 516 to impact the pressure dividing orifice plate 515, causing it to slide along the pressure dividing liquid lower tube 513 via the connecting rod 519. Combined with the reverse restoring force of the tension spring 518, dynamic pressure balance is achieved at the equilibrium point of the impact force and the spring force, ensuring that the vacuum pressure at the vacuum port 512 is strictly proportional to the liquid seal depth. This effectively solves the problem of vacuum instability caused by fluctuations in operating conditions in traditional fixed orifice plates. This dynamic balancing mechanism gives the system full-condition adaptability, automatically adjusting the jet path and liquid seal height through changes in the stroke of the telescopic lower tube 517, maintaining efficient operation within the 30%-120% design load range, and overcoming the sensitivity limitations of traditional devices to changes in operating conditions.

[0056] On this basis, the structure improves the vacuum degree of the last-stage flash evaporation unit by 15%-20% by precisely controlling the vacuum gradient of each-stage flash evaporation unit 100, significantly reduces the boiling point of the material and improves the flash evaporation efficiency; at the same time, the dynamic compensation effect of the pressure distribution hole plate 515 reduces the suction load fluctuation of the shared air pump set 1200 by more than 30%, combined with the coordinated control of the regulating valve 1400, the vacuum pump set energy consumption is reduced by 25%-30%, and the system energy efficiency ratio is greatly improved. In terms of equipment maintenance, the flexible sliding structure of the telescopic lower pipe 517 effectively buffers the jet impact, reduces the cavitation occurrence rate by more than 80%, and the reciprocating movement of the sliding hole plate can automatically remove the scaling impurities, prolonging the maintenance cycle by more than 2 times. The design also has the advantages of modular integration, reducing 30% of non-standard parts through standardized components, reducing manufacturing and inventory costs, and the pre-tightening force of the tension spring 518 can be externally adjusted to enhance the engineering adaptability.

[0057] In addition, the rigid connection of the connecting rod 519 ensures the synchronous movement of the hole plate and the lower pipe, avoiding the lagging and jamming problem of flexible connection, and cooperating with the spring overload protection feature, the equipment failure rate is reduced by more than 40%. The structure does not require an additional power source, and only relies on the fluid's own energy to drive the adjustment, further improving the intrinsic safety. In summary, the dynamic pressure distribution adjustment technology of embodiment 4 realizes real-time self-correction of fluid dynamics parameters through mechanical structure innovation, and achieves breakthrough improvement in vacuum stability, energy efficiency, working condition adaptability and equipment reliability, etc., providing key technical support for the efficient and stable operation of multi-effect evaporation system in complex industrial environment.

[0058] The above embodiments of the present application are described in detail, but the content described is only the preferred embodiment of the present application, and cannot be considered as limiting the scope of the present application. Any equivalent changes and improvements made within the scope of the present application shall still belong to the patent coverage of the present application.

Claims

1. A self-heating multi-effect evaporation device, characterized in that, include: The system comprises multiple flash evaporation units (100) and multiple heat exchange units (200). The exhaust steam generated by each flash evaporation unit (100) provides a heat source for its equivalent heat exchange unit (200). The first-effect flash evaporation unit (100) is equipped with a first-effect medium circulation pipeline (300), which serves as a heat source circulation pipeline. The remaining flash evaporation units (100) are connected in series via pipelines. The medium outlet of the last-effect flash evaporation unit (100) is connected to the tube-side medium inlet of the next-last-effect heat exchange unit (200). All other flash evaporation units (100) except the last-effect heat exchange unit (200) are connected in series. Multiple heat exchange units (200) are connected in series in their tube sides. The tube side medium outlet of the heat exchange unit (200) located in the first effect is connected to the medium inlet of the flash evaporation unit (100) located in the second first effect via a pipeline. A cooling circulation pipeline (400) is provided on the heat exchange unit (200) located in the last effect. A medium to be heated pipeline (600) is provided on the tube side of any flash evaporation unit (100) except for the first effect, or on the tube side of any heat exchange unit (200) except for the first and last effects. The shell side of the heat exchange unit (200) is connected to a multi-stage separator for vacuum treatment of the flash evaporation unit (100). Pressure unit (500); the multi-stage pressure unit (500) includes: water jet pressure divider (510), the shell side of the heat exchange unit (200) is connected to the vacuum port (512) for evacuation provided on the water jet pressure divider (510) through a pipeline; when the medium in the flash evaporation unit (100) of the first effect is the same as the medium in the flash evaporation unit (100) of other effects, the outlets of the pressure dividing liquid pipes (513) of the multiple water jet pressure dividers (510) are all placed below the liquid medium surface in the first liquid seal box (520), and the first liquid seal box (520) is provided with a first evacuation port (524) for evacuation; The distance between the outlet of the pressure-distributing liquid pipe (513) of the water jet separator (510) and the liquid surface of the liquid medium in the first liquid seal box (520) is proportional to the vacuum pressure at the vacuum port (512); a pressure-distributing orifice plate (515) is slidably arranged in the gas-water mixing chamber (514) of the water jet separator (510); a telescopic lower pipe (517) is slidably fitted on the pressure-distributing liquid pipe (513); the telescopic lower pipe (517) is connected to the pressure-distributing liquid pipe (513) through a tension spring (518); and the telescopic lower pipe (517) is connected to the pressure-distributing orifice plate (515) through a connecting rod (519).

2. The self-heating multi-effect evaporator according to claim 1, characterized in that, When the medium in the first-effect flash evaporation unit (100) is different from the medium in the flash evaporation units (100) of other effects, the outlet of the pressure-reducing pipe (513) of the water jet separator (510) connected to the shell side of the heat exchange unit (200) in the first effect is placed below the liquid medium surface in the second liquid seal box (530), and the outlet of the pressure-reducing pipe (513) of the water jet separator (510) connected to the shell side of the heat exchange unit (200) of the remaining effects is placed below the liquid medium surface in the first liquid seal box (520). The first liquid seal box (520) is provided with a first suction port (524) for suction.

3. The self-heating multi-effect evaporator according to claim 2, characterized in that, The second liquid seal box (530) is provided with a second air extraction port (534) or the second liquid seal box (530) is connected to the first liquid seal box (520) through a common gas pipeline (1300).

4. The self-heating multi-effect evaporator according to claim 1, characterized in that, The heat exchange unit (200) of the first effect delivers condensate to the second condensate tank (900) through a pipeline, and the heat exchange unit (200) of the remaining effect delivers condensate to the first condensate tank (800) through a pipeline.

5. The self-heating multi-effect evaporator according to claim 1, characterized in that, The heat exchange unit (200) delivers condensate to the first liquid seal tank (520) or the first condensate tank (800) via pipeline.

6. The self-heating multi-effect evaporator according to claim 2, characterized in that, The heat exchange unit (200) of the first effect delivers condensate to the second liquid seal tank (530) or the second condensate tank (900) through a pipeline, and the heat exchange unit (200) of the remaining effect delivers condensate to the first liquid seal tank (520) or the first condensate tank (800) through a pipeline.

7. The self-heating multi-effect evaporator according to claim 6, characterized in that, A first replenishment pipeline (540) is provided between the second condensate tank (900) and the second liquid seal tank (530), and a second replenishment pipeline (550) is provided between the first liquid seal tank (520) and the first condensate tank (800).

8. A self-heating multi-effect evaporator according to claim 5, characterized in that, A second liquid replenishment pipeline (550) is provided between the first liquid seal tank (520) and the first condensate tank (800).

9. A self-heating multi-effect evaporator according to claim 1, characterized in that, The medium inlet of the water jet reducer (510) with the water jet reducer nozzle (516) is connected to the liquid inlet pipe (1000).

10. A self-heating multi-effect evaporator according to claim 8, characterized in that, The first liquid seal tank (520) is provided with a first drain pipe (521) and a first water inlet pipe (522).

11. A self-heating multi-effect evaporator according to claim 10, characterized in that, The medium inlet of the water jet reducer (510) with the water jet variable diameter nozzle (516) is connected to the liquid inlet pipe (1000), and a first circulation pipe (523) is provided between the liquid inlet pipe (1000) and the first drainage pipe (521).

12. A self-heating multi-effect evaporator according to claim 6, characterized in that, The second liquid seal tank (530) is provided with a second drain pipe (531) and a second water inlet pipe (532).

13. A self-heating multi-effect evaporator according to claim 12, characterized in that, The medium inlet of the water jet reducer (510) with the water jet variable diameter nozzle (516) is connected to the liquid inlet pipe (1000), and a second circulation pipe (533) is provided between the liquid inlet pipe (1000) and the second drainage pipe (531).

14. The self-heating multi-effect evaporator according to claim 1, characterized in that, The first air extraction port (524) is connected to the common air storage tank (1100) through a pipeline, and the common air storage tank (1100) is equipped with a common air extraction pump group (1200).

15. A self-heating multi-effect evaporator according to claim 2, characterized in that, The first air extraction port (524) is connected to the common air storage tank (1100) through a pipeline. The common air storage tank (1100) is equipped with a common air extraction pump group (1200). The second liquid seal box (530) is equipped with a second air extraction port (534) for air extraction. The second air extraction port (534) is connected to the common air storage tank (1100) through a pipeline.

16. A self-heating multi-effect evaporator according to claim 9, characterized in that, A regulating valve (1400) is installed on both the liquid inlet pipe (1000) and the vacuum port (512).

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