Energy-saving device for producing stronger ammonia water through ammonium phosphate ammonia washing pregnant solution desorption

Abstract

The utility model relates to the technical field of ammonium phosphate ammonia washing production of stronger ammonia water, in particular to an energy-saving device for producing stronger ammonia water through ammonium phosphate ammonia washing pregnant solution desorption. Comprising a desorption tower, an ammonia condenser, a reboiler, a 1 # lean-rich liquid heat exchanger, an ammonia absorber, a concentrated ammonia water tank, an ammonia water cooler, an ammonia water deep freezer, a 1 # pipeline mixer, a 2 # pipeline mixer, a 2 # lean-rich liquid heat exchanger, a rich liquid heater and a flash evaporator. According to the utility model, the energy consumption in the desorption process of the ammonium phosphate pregnant solution is greatly reduced by increasing the recovery concentration of the ammonia steam at the top of the desorption tower and reducing the heat brought out by water vapor in the ammonia steam discharged from the desorption tower. Water balance of the ammonium phosphate solution circulating system is effectively controlled through quantitative water replenishing, and adjustment is flexible and convenient. The device can be used for directly preparing high-degree ammonia steam, the ammonia water concentration range is accurately adjusted by quantitatively supplementing water in the ammonia absorption process, the adjustment is flexible and convenient, and the quality of the obtained ammonia water product is stable.

Description

Technical Field

[0001] The utility model relates to the technical field of producing concentrated ammonia water by washing ammonia with ammonium phosphate, in particular to a device for producing concentrated ammonia water by desorption and energy saving of rich liquid of washing ammonia with ammonium phosphate. Background Art

[0002] The removal and recovery processes of ammonia impurities in coke oven gas mainly include sulfuric acid absorption ammonia production ammonium sulfate process, water washing ammonia production concentrated ammonia water or ammonia decomposition process, phosphate ammonium washing ammonia production concentrated ammonia water or anhydrous ammonia process, etc. Among them, the phosphate ammonium washing ammonia production concentrated ammonia water or anhydrous ammonia process uses phosphate ammonium solution to absorb ammonia in coal gas, while absorbing only trace amounts of acidic components (H2S, HCN, CO2) in coal gas, with good absorption selectivity. Compared with other coal gas deammoniation processes, it has better economic benefits and better market advantages.

[0003] At present, the production of concentrated ammonia water by washing ammonia with phosphate ammonium is that the coal gas enters the ammonia absorption tower, and is countercurrently contacted with the phosphate ammonium lean liquid sprayed on the top of the tower for chemical absorption. The phosphate ammonium rich liquid after absorbing ammonia is first subjected to tar removal and then heat exchange with the hot phosphate ammonium lean liquid discharged from the desorption tower to a certain temperature before entering the degasser. The phosphate ammonium rich liquid is flashed in the degasser to remove the acidic components. The deacidified phosphate ammonium rich liquid is then heat exchanged with the ammonia vapor at the top of the desorption tower by the decompressor and the desorption tower. The temperature is increased and then it enters the desorption tower. The desorption tower is operated at 0.5-1.6MPa, and 1.6MPa direct steam is introduced into the bottom of the tower as stripping steam to strip out the ammonia in the rich liquid. The concentrated acid vapor partially condensed and concentrated by the decompressor at the top of the desorption tower is then condensed into concentrated ammonia water.

[0004] There are two main problems with the current technology: First, the desorption process of phosphate ammonium rich liquid consumes a high amount of energy, which accounts for a large proportion of the overall process; when the desorption tower is operated at a medium pressure of 1.3-1.6MPa, 10-12 tons of medium-pressure steam are required to produce 1 ton of anhydrous ammonia, and 7.5-9.5 tons of medium-pressure steam are required to produce 1 ton of 20% concentrated ammonia water; if the desorption tower is operated under low pressure, the steam consumption will be higher. Second, there are many factors in the overall process to control the water balance, which is difficult to operate and difficult to achieve; there are three key factors in the existing technology to control the water balance of the overall process system: water carried out by ammonia vapor in the desorption tower, water carried out by coal gas after deammoniation, and water brought into the desorption tower by direct steam. The water balance of the overall process system can be controlled by adjusting these three key factors. However, these three factors are interrelated. For example, adjusting the direct steam volume of the desorption tower can easily lead to fluctuations in the ammonia vapor concentration at the top of the desorption tower, affecting subsequent product processes. It can also easily cause fluctuations in the phosphoric acid concentration in the phosphate ammonium lean solution, affecting the previous ammonia absorption process. The overall process operation is not flexible and convenient, and requires excellent production experience to master this process, which limits the application of this process.

[0005] A Chinese patent with patent authorization announcement number CN101531379B discloses a "method for producing anhydrous ammonia by phosphate ammonium absorption method", in which the desorption tower bottom heater is indirectly heated by heat transfer oil, which reduces the amount of sewage discharged compared with directly passing steam into the bottom of the desorption tower for desorption of phosphate ammonium rich solution; but the operating pressure of the desorption tower is a low pressure of 0.3 to 0.55 MPa. The low operating pressure of the desorption tower leads to a low temperature of the phosphate ammonium solution in the desorption tower and a low desorption efficiency. Compared with the phosphate ammonium washing ammonia production anhydrous ammonia process using medium pressure 1.4 to 1.6 MPa rich solution desorption, the energy consumption of the desorption process of this utility model method is actually increased, and there is no advantage in process energy saving, and there is no improvement in the convenience of controlling water balance operation.

[0006] The Chinese patent with the patent authorization announcement number CN104355321B discloses "a process and device for producing concentrated ammonia water by washing ammonia with phosphate ammonium with controllable product ammonia water concentration". A second-stage reducer is added to the reducer for heat exchange between the desorbed phosphate ammonium rich liquid and the ammonia vapor at the top of the desorption tower in the original technology. The second-stage reducer is cooled by circulating water. By adding additional cooling capacity, the adjustment range of the ammonia water reflux at the top of the tower is increased, and the ammonia vapor concentration at the top of the tower is conveniently controllable. However, due to the addition of additional cooling capacity, this utility model method slightly increases the heat required for the desorption process, and there is no obvious improvement in process energy saving.

[0007] The Chinese patent document with patent application publication number CN105293524A discloses a "waste heat recovery system and process for producing anhydrous ammonia from phosphate ammonium washing ammonia", which uses the waste heat of ammonia vapor after the first desorption tower cooler at the top of the desorption tower and the waste heat of phosphate ammonium lean liquid as the heat source for distillation of other process media for coal gas purification, thereby improving the energy utilization rate among various processes in the factory. However, this process does not reduce the steam energy consumption in the desorption process of phosphate ammonium rich liquid, and the steam consumption is still large, and there is no improvement in the convenience of controlling the water balance operation. Utility Model Content

[0008] In order to overcome the shortcomings of the prior art, the utility model provides a device for desorbing rich ammonia solution for washing with ammonium phosphate in an energy-saving manner to produce concentrated ammonia water, which can greatly reduce the energy consumption of the desorption process of rich ammonia solution for washing with ammonium phosphate, and can conveniently control the concentration of concentrated ammonia water product and the concentration of phosphoric acid in the lean ammonium phosphate solution.

[0009] In order to achieve the above purpose, the utility model adopts the following technical solutions:

[0010] A device for desorbing and energy-saving concentrated ammonia water by ammonium phosphate washing ammonia rich liquid, comprising a desorption tower, an ammonia condenser, a reboiler, a 1# lean-rich liquid heat exchanger, an ammonia absorber, a concentrated ammonia water tank, an ammonia water cooler, an ammonia water deep freezer, a 1# pipeline mixer, a 2# pipeline mixer, a 2# lean-rich liquid heat exchanger, a rich liquid heater and a flash evaporator; the desorption tower, the 1# lean-rich liquid heat exchanger, the 2# pipeline mixer and the 2# lean-rich liquid heat exchanger are sequentially connected by pipelines; the ammonium phosphate lean liquid water supply pipeline is connected to the 2# pipeline mixer, the ammonium phosphate rich liquid pipeline is connected to the 2# lean-rich liquid heat exchanger pipeline, the flash evaporator is connected to the coal before the ammonium phosphate washing ammonia The gas system pipeline is connected; 2# lean-rich liquid heat exchanger, rich liquid heater, flash evaporator, 1# lean-rich liquid heat exchanger, and desorption tower are connected in sequence by pipelines; the top of the desorption tower, ammonia condenser, ammonia absorber, concentrated ammonia water tank, ammonia water cooler, ammonia water deep freezer, and 1# pipeline mixer are connected in sequence by pipelines; the ammonia water make-up pipeline is connected to the 1# pipeline mixer, the 1# pipeline mixer is connected to the top pipeline of the ammonia absorber, and the top of the ammonia absorber is connected to the gas system pipeline before phosphate ammonium washing ammonia; a reboiler is arranged at the bottom of the desorption tower, the medium-pressure steam pipeline is connected to the reboiler, and the reboiler is connected to the rich liquid heater pipeline.

[0011] Furthermore, a rich liquid pump is provided on the pipeline connecting the flash evaporator and the 1# lean-rich liquid heat exchanger.

[0012] Furthermore, a concentrated ammonia water pump is provided on the pipeline connecting the concentrated ammonia water tank and the ammonia water cooler.

[0013] Furthermore, the ammonia absorber is of a packing type.

[0014] Compared with the prior art, the beneficial effects of the utility model are:

[0015] 1. In the process of desorption of ammonium phosphate rich liquid and ammonia concentration, the heat required for the desorption of ammonium phosphate rich liquid is provided by an external heat source, and heat is exchanged with the ammonium phosphate lean liquid at the bottom of the desorption tower in the reboiler at the bottom of the desorption tower to provide heat for the desorption operation. The desorbed ammonia vapor at the top of the desorption tower enters the ammonia condenser for partial condensation. The liquid phase after partial condensation is ammonia water, which flows to the top of the desorption tower as reflux liquid, and the vapor phase after partial condensation is concentrated ammonia vapor, which enters the bottom of the ammonia absorber. The utility model significantly reduces the energy consumption of the desorption process of ammonium phosphate rich liquid by increasing the concentration of ammonia vapor produced at the top of the desorption tower and reducing the heat brought out by water vapor in the ammonia vapor discharged from the desorption tower.

[0016] 2. The utility model replenishes water to the ammonium phosphate solution system, and sets a 2# pipeline mixer on the ammonium phosphate lean solution pipeline after the lean-rich solution heat exchanger to replenish final cooling water or soft water and mix with the ammonium phosphate lean solution to adjust the phosphoric acid concentration in the ammonium phosphate lean solution. The utility model is different from the prior art in terms of the operation and control of the acid concentration in the ammonium phosphate lean solution. The utility model effectively controls the water balance of the ammonium phosphate solution circulation system through quantitative water replenishment, and the adjustment is flexible and convenient.

[0017] 3. The utility model replenishes water during the ammonia absorption process, and sets a 1# pipeline mixer on the circulating concentrated ammonia pipeline after the ammonia cryocooler to replenish soft water and mix with concentrated ammonia to adjust the concentration of the concentrated ammonia product. In terms of the concentration control of the concentrated ammonia product, different from the prior art, the utility model can directly produce high-grade ammonia vapor, and accurately adjust the range of ammonia concentration by quantitatively replenishing water during the ammonia absorption process. The adjustment is flexible and convenient, and the quality of the ammonia product is stable. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] Figure 1 It is a schematic diagram of the structure and process principle of the utility model.

[0019] In the figure: 1-desorption tower, 2-ammonia condenser, 3-reboiler, 4-1# lean and rich liquid heat exchanger, 5-ammonia absorber, 6-concentrated ammonia water tank, 7-concentrated ammonia water pump, 8-ammonia water cooler, 9-ammonia water deep freezer, 10-1# pipeline mixer, 11-2# pipeline mixer, 12-2# lean and rich liquid heat exchanger, 13-rich liquid heater, 14-flash evaporator, 15-rich liquid pump. DETAILED DESCRIPTION

[0020] The embodiments of the present invention are described in detail below. In order to make the purpose, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described in combination with the drawings in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. The following description of at least one exemplary embodiment is actually only illustrative and is by no means intended to limit the present invention and its application or use. Based on the embodiments in the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0021] In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "up", "down", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", "axial", "radial", "circumferential" and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the referred device or element must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be understood as a limitation on the present invention.

[0022] In the description of the present invention, it should be noted that, unless otherwise clearly specified and limited, the terms "installed", "connected", and "connected" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a direct connection, or an indirect connection through an intermediate medium, or it can be the internal communication of two components. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0023] In the description of the utility model, it should be noted that the terms used herein are only for describing specific embodiments, and are not intended to limit the exemplary embodiments according to the utility model. As used herein, unless the context clearly indicates otherwise, the singular form is also intended to include the plural form. In addition, it should be understood that when the terms "comprise" and / or "include" are used in this specification, it indicates the presence of features, steps, operations, devices, components and / or combinations thereof.

[0024] Unless otherwise specifically stated, the relative arrangement of the parts and steps described in these embodiments, the numerical expressions and numerical values ​​do not limit the scope of the utility model. At the same time, it should be clear that, for ease of description, the sizes of the various parts shown in the drawings are not drawn according to the actual proportional relationship. The technology, methods and equipment known to ordinary technicians in the relevant field may not be discussed in detail, but in appropriate cases, the technology, methods and equipment should be regarded as part of the authorization specification. In all examples shown and discussed here, any specific value should be interpreted as merely exemplary, rather than as a limitation. Therefore, other examples of exemplary embodiments may have different values. It should be noted that similar numbers and letters represent similar items in the following drawings, so once an item is defined in one drawing, it does not need to be further discussed in subsequent drawings.

[0025] In addition, it should be noted that the use of terms such as "first" and "second" to limit components is only for the convenience of distinguishing the corresponding components. If not otherwise stated, the above terms have no special meaning and therefore cannot be understood as limiting the scope of protection of the utility model.

[0026] like Figure 1 As shown, a device for desorbing and energy-saving concentrated ammonia water by ammonium phosphate washing ammonia rich liquid includes a desorption tower 1, an ammonia condenser 2, a reboiler 3, a 1# lean and rich liquid heat exchanger 4, an ammonia absorber 5, a concentrated ammonia water tank 6, a concentrated ammonia water pump 7, an ammonia water cooler 8, an ammonia water deep freezer 9, a 1# pipeline mixer 10, a 2# pipeline mixer 11, a 2# lean and rich liquid heat exchanger 12, a rich liquid heater 13, a flash evaporator 14, a rich liquid pump 15 and connecting pipelines.

[0027] The bottom outlet of the desorption tower 1 is connected to the lean liquid inlet pipeline of the 1# lean-rich liquid heat exchanger 4. The lean liquid outlet of the 1# lean-rich liquid heat exchanger 4 is connected to the lean liquid inlet pipeline of the 2# pipeline mixer 11; the lean liquid outlet of the 2# pipeline mixer 11 is connected to the lean liquid inlet pipeline of the 2# lean-rich liquid heat exchanger 12; the lean liquid outlet of the 2# lean-rich liquid heat exchanger 12 is connected to the pipeline of the subsequent phosphate ammonium washing ammonia absorption section.

[0028] The phosphate ammonium lean solution water replenishment pipeline is connected to the 2# pipeline mixer 11 water replenishment inlet pipeline.

[0029] The phosphate ammonium rich liquid pipeline sent from the phosphate ammonium ammonia washing absorption section is connected to the rich liquid inlet pipeline of 2# lean and rich liquid heat exchanger 12; the rich liquid outlet of 2# lean and rich liquid heat exchanger 12 is connected to the rich liquid inlet pipeline of rich liquid heater 13; the rich liquid outlet of rich liquid heater 13 is connected to the rich liquid inlet pipeline of flash evaporator 14; the ammonia-containing gas outlet at the top of flash steam 14 is connected to the pipeline of the gas system before phosphate ammonium ammonia washing; the rich liquid outlet of flash evaporator 14 is connected to the rich liquid inlet pipeline of rich liquid pump 15; the rich liquid outlet of rich liquid pump 15 is connected to the rich liquid inlet pipeline of 1# lean and rich liquid heat exchanger 4; the rich liquid outlet of 1# lean and rich liquid heat exchanger 4 is connected to the rich liquid inlet pipeline in the middle of desorption tower 1.

[0030] The desorbed ammonia vapor outlet at the top of the desorption tower 1 is connected to the vapor phase inlet pipeline at the bottom of the tube side of the ammonia condenser 2; the liquid phase outlet of the tube side of the ammonia condenser 2 is connected to the liquid phase inlet at the top of the desorption tower 1; the vapor phase outlet of the tube side of the ammonia condenser 2 is connected to the vapor phase inlet at the bottom of the ammonia absorber 5; the bottom of the ammonia absorber 5 is connected to the ammonia water inlet equipment at the top of the concentrated ammonia water tank 6; the ammonia water outlet at the bottom of the concentrated ammonia water tank 6 is connected to the inlet pipeline of the concentrated ammonia water pump 7; the outlet of the concentrated ammonia water pump 7 is connected to the ammonia water inlet pipeline of the ammonia water cooler 8; the ammonia water outlet of the ammonia water cooler 8 is connected to the ammonia water inlet pipeline of the ammonia water deep freezer 9; the ammonia water outlet of the ammonia water deep freezer 9 is connected to the ammonia water inlet pipeline of the 1# pipeline mixer 10.

[0031] The ammonia outlet of 1# pipeline mixer 10 is connected to the ammonia inlet pipeline at the top of ammonia absorber 5; the non-condensable gas outlet at the top of ammonia absorber 5 is connected to the gas system pipeline before phosphate ammonium washing ammonia; the ammonia water make-up pipeline is connected to the water make-up inlet pipeline of 1# pipeline mixer 10; a reboiler 3 is arranged at the bottom of desorption tower 1; the medium-pressure steam pipeline is connected to the steam inlet pipeline of reboiler 3; the condensate outlet of reboiler 3 is connected to the condensate inlet pipeline of rich liquid heater 13.

[0032] The process principle and working process of this utility model are as follows:

[0033] 1. Desorption of ammonium phosphate rich solution and ammonia concentration:

[0034] After the acid vapor is removed, the phosphate ammonium rich liquid enters the lean-rich liquid heat exchanger 4 to exchange heat with the phosphate ammonium lean liquid discharged from the bottom of the desorption tower 1, and then enters the middle part of the desorption tower 1 for desorption operation; the heat required for the desorption operation of the phosphate ammonium rich liquid is provided by an external heat source, and is heat exchanged with the phosphate ammonium lean liquid at the bottom of the desorption tower 1 in the reboiler 3 at the bottom of the desorption tower to provide heat for the desorption operation; the ammonia vapor desorbed at the top of the desorption tower 1 enters the ammonia condenser 2 for partial condensation, and the liquid phase part after partial condensation is ammonia water, which flows to the top of the desorption tower 1 as a reflux liquid, and the vapor phase part after partial condensation is concentrated ammonia vapor, which enters the vapor phase inlet at the bottom of the ammonia absorber 5.

[0035] The temperature of the phosphate ammonium rich liquid after heat exchange in the 1# lean-rich liquid heat exchanger 4 is 160°C~200°C, the top operating pressure of the desorption tower 1 is 800kPag~2500kPag, the mass fraction of ammonia in the ammonia vapor discharged from the ammonia condenser 2 is 30%~99.9%, and the temperature of the ammonia vapor discharged from the ammonia condenser 2 is 38°C~80°C.

[0036] 2. Ammonia water circulation absorption to produce concentrated ammonia water:

[0037] The concentrated ammonia vapor entering the bottom of the ammonia absorber 5 is in countercurrent vapor-liquid contact with the concentrated ammonia water entering the top of the ammonia absorber 5 to absorb ammonia. The concentrated ammonia water after absorbing ammonia enters the concentrated ammonia water tank 6 from the bottom of the ammonia absorber 5. The concentrated ammonia water in the concentrated ammonia water tank 6 is pumped out by the concentrated ammonia water pump 7 and sent to the ammonia water cooler 8 for cooling with circulating water, and then sent to the ammonia water deep freezer 9 for further cooling with low-temperature water; a part of the cooled concentrated ammonia water is sent to the top of the ammonia absorber 5 to countercurrently absorb the ammonia vapor entering the bottom of the ammonia absorber 5, and the other part is sent to the storage process as a concentrated ammonia water product; the non-condensable gas at the top of the ammonia absorber 5 is discharged to the gas system before the phosphate ammonium ammonia washing. The temperature of the concentrated ammonia water after being cooled by the ammonia water cooler 8 is 35°C~50°C; the temperature of the concentrated ammonia water after being cooled by the ammonia water deep freezer 9 is 20°C~30°C; the concentration of the discharged concentrated ammonia water is 10%~50%; the flow ratio of the discharged concentrated ammonia water and the concentrated ammonia water entering the top of the ammonia absorber 5 is 1:5~50; the operating pressure at the top of the ammonia absorber 5 is 800kPag~2500kPag.

[0038] 3. Water replenishment of ammonium phosphate solution system:

[0039] A 2# pipeline mixer 11 is arranged on the phosphate ammonium lean solution pipeline after the lean-rich liquid heat exchanger 4 to supplement final cooling water or soft water to mix with the phosphate ammonium lean solution and adjust the phosphoric acid concentration in the phosphate ammonium lean solution; the phosphate ammonium solution system is supplemented with coal gas final cooling water or soft water.

[0040] 4. Water replenishment during ammonia absorption: A 1# pipeline mixer 10 is set on the circulating concentrated ammonia water pipeline after the ammonia water deep cooler 9 to replenish soft water and mix with the concentrated ammonia water to adjust the concentration of the concentrated ammonia water product. The water replenishment during ammonia absorption is coal gas final cooling water or soft water.

[0041] 5. Heat exchange and deacidification of ammonium phosphate rich liquid:

[0042] The phosphate ammonium rich liquid sent from the phosphate ammonium washing process enters the 2# lean-rich liquid heat exchanger 12 to exchange heat with the phosphate ammonium lean liquid, then enters the rich liquid heater 13 to exchange heat with the hot condensate water to increase the temperature, then enters the flash evaporator 14 for pressure reduction and flash evaporation to remove acid vapor, and the removed ammonia-containing vapor is discharged to the gas system before the phosphate ammonium washing; the phosphate ammonium rich liquid after the ammonia-containing vapor is removed is sent to the 1# lean-rich liquid heat exchanger through the rich liquid pump 15 to exchange heat with the phosphate ammonium lean liquid discharged from the bottom of the desorption tower 1. The temperature of the phosphate ammonium rich liquid after heat exchange in the 2# lean-rich liquid heat exchanger 12 is 80℃~110℃.

[0043] The greatest advantage of the utility model is that it can significantly reduce the energy consumption of the desorption process of the ammonium phosphate rich solution by increasing the concentration of ammonia vapor produced at the top of the desorption tower and reducing the heat brought out by water vapor in the ammonia vapor discharged from the desorption tower. At the same time, the utility model can separate and control the originally interrelated operating factors by quantitatively replenishing water in the ammonia water product and quantitatively replenishing water in the ammonium phosphate lean solution at the bottom of the tower, so as to realize convenient control of the concentration of the concentrated ammonia water product and the concentration of phosphoric acid in the ammonium phosphate lean solution.

[0044] The above description is only a preferred specific implementation manner of the present invention, but the protection scope of the present invention is not limited thereto. Any technician familiar with the technical field can make equivalent replacements or changes within the technical scope disclosed by the present invention according to the technical scheme and the utility model concept of the present invention, which should be covered by the protection scope of the present invention.

Claims

1. A device for desorption and energy-saving production of concentrated ammonia water by ammonium phosphate washing ammonia rich liquid, characterized in that: It includes desorption tower, ammonia condenser, reboiler, 1# lean-rich liquid heat exchanger, ammonia absorber, concentrated ammonia water tank, ammonia water cooler, ammonia water deep freezer, 1# pipeline mixer, 2# pipeline mixer, 2# lean-rich liquid heat exchanger, rich liquid heater and flash evaporator; The desorption tower, 1# lean-rich liquid heat exchanger, 2# pipeline mixer, and 2# lean-rich liquid heat exchanger are sequentially connected by pipelines; The phosphate ammonium lean liquid water replenishment pipeline is connected to the 2# pipeline mixer, the phosphate ammonium rich liquid pipeline is connected to the 2# lean and rich liquid heat exchanger pipeline, and the flash evaporator is connected to the gas system pipeline before the phosphate ammonium washing ammonia; The 2# lean-rich liquid heat exchanger, the rich liquid heater, the flash evaporator, the 1# lean-rich liquid heat exchanger, and the desorption tower are connected in sequence by pipelines; The top of the desorption tower, the ammonia condenser, the ammonia absorber, the concentrated ammonia water tank, the ammonia water cooler, the ammonia water deep cooler, and the No. 1 pipeline mixer are connected in sequence by pipelines; The ammonia water replenishment pipeline is connected to the 1# pipeline mixer, the 1# pipeline mixer is connected to the top pipeline of the ammonia absorber, and the top of the ammonia absorber is connected to the gas system pipeline before the phosphate ammonium washing ammonia; A reboiler is arranged at the bottom of the desorption tower, a medium-pressure steam pipeline is connected to the reboiler, and the reboiler is connected to a rich liquid heater pipeline.

2. The device for desorption and energy-saving production of concentrated ammonia water by ammonium phosphate washing ammonia rich solution according to claim 1, characterized in that: The flash evaporator is provided with a rich liquid pump on the pipeline connected to the 1# lean-rich liquid heat exchanger.

3. The device for desorption and energy-saving production of concentrated ammonia water by ammonium phosphate washing ammonia rich solution according to claim 1, characterized in that: The concentrated ammonia water tank has a concentrated ammonia water pump on a pipeline connected to the ammonia water cooler.

4. The device for desorption and energy-saving production of concentrated ammonia water by ammonium phosphate washing ammonia rich solution according to claim 1, characterized in that: The ammonia absorber adopts a packing type.

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