Clean, environment-friendly, green, efficient and energy-saving distillation ammonia gas recovery device

Abstract

The utility model discloses a clean, environment-friendly, green, efficient and energy-saving distillation ammonia gas recovery device, and relates to the technical field of ammonia gas recovery. The first ammonia recovery mechanism is used for instantaneously converting high-temperature ammonia gas and water vapor from a gas state into hot liquid ammonia water and cooling to form normal-temperature liquid ammonia water; the second ammonia recovery mechanism is used for circularly absorbing ammonia gas; the third ammonia recovery mechanism is used for absorbing overflowing ammonia gas; the carbon dioxide dissolving, carbonizing and ammonia fixing mechanism is used for net conversion of solid ammonia into ammonium carbonate; according to the device, three-time ammonia recovery is realized, meanwhile, net conversion of solid ammonia can be carried out to form an ammonium carbonate structure, a precipitant is used for a magnesium oxide synthesis process for later use, 88-90% of ammonia can be absorbed by the first ammonia recovery mechanism, and 10-12% of ammonia is absorbed by the second ammonia recovery mechanism for ammonia gas which is not condensed and cooled to be converted into liquid ammonia water; the third ammonia recovery mechanism is used for recovering trace ammonia gas escaped from an expiration port during drainage operation of each storage tank, so that pollution is reduced, and a clean control environment is ensured.

Description

Technical Field

[0001] The utility model belongs to the technical field of ammonia recovery, and particularly relates to a clean, environment-friendly, green, efficient and energy-saving distillation ammonia recovery device. Background Art

[0002] In the production of medicinal magnesium oxide to prepare the intermediate product magnesium sulfate solution of the precursor and the distillation process of the precipitant ammonium carbonate, as well as the ammonia recovery and the production process of the precipitant ammonium carbonate, in the reaction kettle of the distillation process, the light-burned magnesium oxide and the mother liquor ammonium sulfate undergo a metathesis reaction, and the reaction solution temperature is 96 - 98 °C. The ammonia gas and water generated during the reaction cannot be quickly recovered and escape from the reaction kettle in time. When the reaction in the reaction solution proceeds to 60%, the pH value in the reaction solution increases, causing the magnesium sulfate produced in the reaction solution to hydrolyze, forming magnesium hydroxide colloid flocs. The magnesium hydroxide flocs will adhere to the surface of the particle size of the light-burned magnesium oxide, affecting the hydration of magnesium oxide, reducing the metathesis reaction rate in the reaction kettle, prolonging the reaction time, increasing the natural gas power consumption, and affecting the reaction yield; in order to change the existing working conditions, improve the ammonia recovery effect, accelerate the reaction rate in the distillation reaction kettle, and save gas power, the existing equipment is improved, optimized, configured and combined to improve. Content of the Utility Model

[0003] To solve the problems mentioned in the above background art; the purpose of the utility model is to provide a clean, environment-friendly, green, efficient and energy-saving distillation ammonia recovery device.

[0004] A clean, environment-friendly, green, efficient and energy-saving distillation ammonia recovery device of the utility model includes a first ammonia recovery mechanism, a second ammonia recovery mechanism, a third ammonia recovery mechanism, and a carbon dioxide dissolution carbonization ammonia fixation mechanism; the first ammonia recovery mechanism is connected to the second ammonia recovery mechanism, the second ammonia recovery mechanism is connected to the third ammonia recovery mechanism, and the carbon dioxide dissolution carbonization ammonia fixation mechanism is respectively connected to the first ammonia recovery mechanism, the second ammonia recovery mechanism, and the third ammonia recovery mechanism;

[0005] The first ammonia recovery mechanism is used to instantaneously convert high-temperature ammonia gas and water vapor from a gaseous state into hot liquid ammonia water, and form normal-temperature liquid ammonia water after cooling;

[0006] The second ammonia recovery mechanism is used to cyclically absorb ammonia gas;

[0007] The third ammonia recovery mechanism is used to absorb the overflowing ammonia gas;

[0008] The carbon dioxide dissolution carbonization ammonia fixation mechanism is used to convert and fix ammonia into ammonium carbonate through purification.

[0009] Preferably, the first ammonia recovery mechanism includes an ammonia distillation reactor, a condenser, a cooler, a condensed ammonia water storage tank, a magnesium sulfate solution storage tank, and a synthetic magnesium sulfate preheating tank; the lower end of the magnesium sulfate solution storage tank is connected to the right end of the condenser through a pipeline, a second delivery pump, and a first valve, the right end of the condenser is connected to the cooler, the upper left end of the condenser is connected to the synthetic magnesium sulfate preheating tank through a pipeline and a sixteenth valve, the upper end of the ammonia distillation reactor is connected to the left end of the condenser through a pipeline, and the lower end of the cooler is connected to the upper end of the condensed ammonia water storage tank through a cooling and recovered ammonia water meter.

[0010] Preferably, the two upper ends of the ammonia distillation reactor are respectively provided with a light-burned magnesium oxide slurry feeding port and a mother liquor ammonium sulfate feeding port.

[0011] Preferably, the first ammonia recovery mechanism further includes a cooling mechanism, and the cooling mechanism includes a cooling tower and a cooling pond; the lower end of the cooling tower is connected to the cooling pond through a pipeline, and the lower end of the cooling pond is connected to the lower side of the cooler through a pipeline, a seventeenth valve, and an eighth valve, and the upper side of the cooler is connected to the upper end of the cooling tower through a pipeline.

[0012] Preferably, the second ammonia recovery mechanism includes a jet absorber, a tail ammonia absorption tank, a refrigerated water storage tank, a refrigerator, a cooling water storage tank, a high-lift water pump, a delivery circulation pump, and a delivery water pump; the bottoms of the tail ammonia absorption tank and the condensed ammonia water storage tank are connected to one end of the high-lift water pump through a pipeline, a second valve, and a fifth valve, and the other end of the high-lift water pump is respectively connected to the upper ends of the jet absorber and the carbonization dissolution tank through a pipeline, a third valve, and a fourth valve, the lower end of the jet absorber is connected to the upper end of the tail ammonia absorption tank, one end of the cooler inside the tail ammonia absorption tank is connected to the upper end of the cooling water storage tank through a pipeline, the lower end of the cooling water storage tank is connected to the refrigerator through a delivery water pump, the refrigerator is connected to the upper end of the refrigerated water storage tank, and the lower side of the refrigerated water storage tank is connected to the other end of the cooler inside the tail ammonia absorption tank through a pipeline, a delivery circulation pump, and a sixth valve.

[0013] Preferably, the third ammonia recovery mechanism includes a dilute sulfuric acid absorption tank, an eleventh valve, a twelfth valve, a thirteenth valve, and a fourteenth valve; the eleventh valve, the twelfth valve, the thirteenth valve, and the fourteenth valve are respectively installed on the breathing ports at the upper right ends of the tail ammonia absorption tank, the condensed ammonia water storage tank, the carbonization dissolution tank, and the precipitant purification tank, and the eleventh valve, the twelfth valve, the thirteenth valve, and the fourteenth valve are respectively connected to the inlet pipe of the dilute sulfuric acid absorption tank through a pipeline, and the outlet pipe of the dilute sulfuric acid absorption tank is inserted 10 cm below the liquid level of the 10% dilute sulfuric acid solution.

[0014] Preferably, the carbon dioxide dissolution and carbonization ammonia fixation mechanism includes a carbonization dissolution tank, a CO2 storage tank, and a precipitant purification tank; the CO2 storage tank is connected to the carbonization dissolution tank through a pipeline and a seventh valve, and the lower side of the carbonization dissolution tank is connected to the precipitant purification tank through a first delivery pump.

[0015] Compared with the prior art, the beneficial effects of the present utility model are as follows: Three - stage ammonia recovery is achieved through the mutual cooperation of the first ammonia recovery mechanism, the second ammonia recovery mechanism, the third ammonia recovery mechanism, and the carbon dioxide dissolution and carbonization ammonia - fixation mechanism. At the same time, it can perform net conversion to fix ammonia in the form of ammonium carbonate, and the precipitant is prepared for use in the magnesia synthesis process. The specific advantages are as follows:

[0016] 1. The high - temperature ammonia gas and water vapor generated by the first ammonia recovery mechanism are instantaneously converted from the gaseous state to hot liquid ammonia water through a condenser, and then cooled to below 26 degrees Celsius to form normal - temperature liquid ammonia water through a cooler. It enters the cold ammonia - water storage tank through a meter, and the ammonia absorption can reach 88 - 90%.

[0017] 2. The second ammonia recovery mechanism pumps the ammonia gas that has not been condensed and cooled to form liquid ammonia water into a jet absorber through a high - lift pump, and absorbs it with refrigerated purified water (10°C), then enters the tail - ammonia absorption storage tank, and continuously circulates for absorption. Under the cooling cycle of the cooling coil in the tail - ammonia absorption storage tank, the purified water liquid absorbed by ammonia gas is less than 16°C, and 10% - 12% of ammonia is absorbed.

[0018] 3. Through the first - stage ammonia recovery mechanism and the second - stage ammonia recovery mechanism, the boiling point of the reaction liquid in the ammonia - distilling reaction kettle is reduced to 88 degrees Celsius. The double - decomposition reaction generates ammonia gas and water vapor, which are instantaneously escaped and promptly absorbed. It solves the problem that the reaction liquid in the reaction kettle is prone to hydrolysis, improves the ammonia - distilling reaction rate, reduces the steam consumption, and improves the ammonia recovery rate.

[0019] 4. The third ammonia recovery mechanism recovers the trace ammonia gas escaping from the exhalation port during the drainage operation of each storage tank, reduces pollution, and ensures a clean control environment.

[0020] 5. The carbon dioxide dissolution and carbonization ammonia - fixation mechanism performs net conversion to fix ammonia in the form of ammonium carbonate, and the precipitant is prepared for use in the magnesia synthesis process. BRIEF DESCRIPTION OF THE DRAWINGS

[0021] For ease of explanation, the present utility model will be described in detail by the following specific embodiments and the accompanying drawings.

[0022] Figure 1 It is a structural schematic diagram of the present utility model.

[0023] In the figure: 1 - ammonia distillation reactor; 2 - condenser; 3 - cooler; 4 - jet absorber; 5 - tail ammonia absorption tank; 6 - condensed ammonia water storage tank; 7 - refrigerated water storage tank; 8 - refrigerator; 9 - cooling water storage tank; 10 - carbonation dissolution tank; 11 - magnesium sulfate solution storage tank; 12 - CO2 storage tank; 13 - precipitant purification tank; 14 - cooling and recycling ammonia water meter; 15 - cooling tower; 16 - cooling pond; 17 - valve one; 18 - dilute sulfuric acid absorption tank; 19 - high-lift water pump; 20 - transfer pump one; 21 - transfer circulation pump; 22 - transfer water pump; 23 - valve two; 24 - valve three; 25 - valve four; 26 - valve five; 27 - valve six; 28 - valve seven; 29 - valve eight; 30 - synthetic magnesium sulfate preheating tank; 31 - valve eleven; 32 - valve twelve; 33 - valve thirteen; 34 - valve fourteen; 35 - transfer pump two; 36 - valve sixteen; 37 - valve seventeen;

[0024] 1-1 - light-burned magnesium oxide slurry feeding port; 1-2 - mother liquor ammonium sulfate feeding port. Specific implementation mode

[0025] To make the purpose, technical solutions and advantages of the present utility model clearer, the present utility model will be described below through specific embodiments shown in the drawings. However, it should be understood that these descriptions are only exemplary and do not intend to limit the scope of the present utility model. The structures, ratios, sizes, etc. shown in the drawings of this specification are only used to cooperate with the content disclosed in the specification for those familiar with this technology to understand and read, and are not used to limit the limiting conditions under which the present utility model can be implemented. Therefore, they do not have a substantial technical meaning. Any modification of the structure, change of the proportional relationship or adjustment of the size, without affecting the effects that the present utility model can produce and the purposes that can be achieved, should still fall within the scope covered by the technical content disclosed by the present utility model. In addition, in the following description, the descriptions of well-known structures and technologies are omitted to avoid unnecessarily confusing the concept of the present utility model.

[0026] Here, it should also be noted that in order to avoid obscuring the present utility model due to unnecessary details, only the structures and / or processing steps closely related to the solution of the present utility model are shown in the drawings, and other details less related to the present utility model are omitted.

[0027] Such as Figure 1As shown, this specific implementation manner adopts a three-stage ammonia recovery system to collect ammonia gas. The first ammonia recovery mechanism is used to instantaneously convert high-temperature ammonia gas and water vapor from a gaseous state into hot liquid ammonia water, and then form normal-temperature liquid ammonia water after cooling. The specific structure is as follows: The first ammonia recovery mechanism includes an ammonia distillation reaction kettle 1, a condenser 2, a cooler 3, a condensed ammonia water storage tank 6, a magnesium sulfate solution storage tank 11, and a synthetic magnesium sulfate preheating tank 30. The lower end of the magnesium sulfate solution storage tank 11 is connected to the right end of the condenser 2 through a pipeline, a second delivery pump 35, and a first valve 17. The right end of the condenser 2 is connected to the cooler 3. The upper left end of the condenser 2 is connected to the synthetic magnesium sulfate preheating tank 30 through a pipeline and a sixteenth valve 36. The upper end of the ammonia distillation reaction kettle 1 is connected to the left end of the condenser 2 through a pipeline. The lower end of the cooler 3 is connected to the upper end of the condensed ammonia water storage tank 6 through a cooling recovery ammonia water meter 14. A negative pressure is formed inside the ammonia distillation reaction kettle. The mother liquor ammonium sulfate and the light-burned magnesium oxide undergo a metathesis reaction solution, and the generated ammonia gas and water vapor can be promptly escaped and absorbed. The boiling point temperature of the metathesis reaction solution is 88 degrees, and the metathesis reaction rate is accelerated. The high-temperature ammonia gas and water vapor generated by the ammonia distillation reaction kettle 1 are instantaneously converted from a gaseous state into hot liquid ammonia water through the condenser 2, and then are cooled to below 26 degrees to form normal-temperature liquid ammonia water after passing through the cooler 3, and enter the condensed ammonia water storage tank 6 through the cooling recovery ammonia water meter 14, and the ammonia absorption can reach 80-90%. The two upper ends of the ammonia distillation reaction kettle 1 are respectively provided with a light-burned magnesium oxide slurry feeding port 1-1 and a mother liquor ammonium sulfate feeding port 1-2. The first ammonia recovery mechanism further includes a cooling mechanism, and the cooling mechanism includes a cooling tower 15 and a cooling pond 16. The lower end of the cooling tower 15 is connected to the cooling pond 16 through a pipeline. The lower end of the cooling pond 16 is connected to the lower side of the cooler 3 through a pipeline, a seventeenth valve 37, and an eighth valve 29. The upper side of the cooler 3 is connected to the upper end of the cooling tower 15 through a pipeline. The condenser uses magnesium sulfate solution as a cooling medium. Open the second delivery pump 35 and the first valve 17, and the magnesium sulfate solution (26°C) in the magnesium sulfate solution storage tank 11 enters from the first valve 17 at the end of the condenser and flows out from the sixteenth valve 36 at the starting section and enters the synthesis process, and the synthetic magnesium sulfate preheating tank 30 is waiting for synthesis and standby, with a temperature of 52±1 degree. The cooling medium of the above cooler is drinking water as the cooling medium. The cooling water less than 20 degrees is pumped into the lower end of the cooler by a delivery pump and cooled from bottom to top. The cooler cools the hot ammonia solution and the ammonia gas that has not been condensed into ammonia liquid. The coolant flows out from the upper end of the cooler, enters the cooling tower, is cooled by heat dissipation and temperature reduction, flows into the cooling pond, and an appropriate amount of lost water is replenished, and the cycle cooling is carried out in turn.

[0028] In this specific embodiment, the reaction liquid of ammonium sulfate and magnesium hydroxide in the ammonia distillation reactor reacts at a negative pressure boiling point of 88 °C, and the mixed gas of ammonia and water escapes. The mixed gas is condensed into hot concentrated ammonia water by the condenser of the first ammonia absorption and recovery system, and then passes through a cooler. The temperature of the hot concentrated ammonia water solution is cooled to below 25 °C and enters the condensed ammonia water storage tank through a flow meter. The flow meter is linked with the steam heating valve for electric control. According to the evaporation amount of ammonia and steam and the flow data of condensation in the flow meter, the size of the heating steam of the reactor is automatically adjusted, and 88-90% of the ammonia and water vapor escaping from the total reaction liquid in the reactor can be recovered stably and effectively. The above-mentioned first ammonia absorption and recovery system mainly consists of a condenser 2 and a cooler 3. The condensation and cooling medium of the condenser 2 is the intermediate product magnesium sulfate solution with a temperature ≤ 26 °C. It enters from the bottom valve at the end of the condenser and flows out from the upper part at the beginning of the condenser. The temperature of the magnesium sulfate solution rises to 41 to 52 °C and flows into the preheating tank of the synthesis process for standby synthesis. The cooling medium of the cooler 3 is cooling water. The cooling water enters from the bottom of the cooler and cools the once-condensed hot ammonia water liquid and the remaining ammonia gas. The cooling water flows out from the upper end of the condenser and enters the cooling tower 15 for heat dissipation, volatilization, and cooling, and then flows into the cooling pond 16, and an appropriate amount of fresh water is added to ensure sufficient cooling water consumption, and the cooling water is recycled and utilized in turn.

[0029] In this specific embodiment, the ammonia distillation reactor, the first ammonia absorption and recovery system, and the second ammonia absorption and recovery system form a closed cycle, making the inside of the ammonia distillation reactor under negative pressure, resulting in a decrease in the boiling point of the reaction materials, enabling the timely escape of the mixed gas of ammonia and water generated by the reaction, and accelerating the speed of the double decomposition reaction between ammonium sulfate and light-burned magnesium oxide in the reactor. The ammonia is efficiently and completely recovered, and the ammonia distillation efficiency is improved.

[0030] Such as Figure 1As shown in the figure, the second ammonia recovery mechanism in this specific embodiment is used for circulating and absorbing ammonia gas; the specific structure is as follows: the second ammonia recovery mechanism includes a jet absorber 4, a tail ammonia absorption tank 5, a chilled water storage tank 7, a chiller 8, a cooling water storage tank 9, a high-lift pump 19, a transfer circulation pump 21, and a transfer water pump 22; the bottoms of the tail ammonia absorption tank 5 and the condensed ammonia water storage tank 6 are connected to one end of the high-lift pump 19 through pipelines, valve two 23, and valve five 26. The other end of the high-lift pump 19 is respectively connected to the upper ends of the jet absorber 4 and the carbonization dissolution tank 10 through pipelines, valve three 24, and valve four 25. The lower end of the jet absorber 4 is connected to the upper end of the tail ammonia absorption tank 5. One end of the cooler inside the tail ammonia absorption tank 5 is connected to the upper end of the cooling water storage tank 9 through a pipeline. The lower end of the cooling water storage tank 9 is connected to the chiller 8 through the transfer water pump 22. The chiller 8 is connected to the upper end of the chilled water storage tank 7. The lower side of the chilled water storage tank 7 is connected to the other end of the cooler inside the tail ammonia absorption tank 5 through a pipeline, the transfer circulation pump 21, and valve six 27; Second ammonia recovery system: The ammonia gas that has not been condensed and cooled into liquid ammonia water is pumped into the jet absorber by a high-lift pump and absorbed by refrigerated purified water (10°C), then enters the tail ammonia absorption storage tank and continuously circulates for absorption. Under the cooling circulation of the cooling coil in the tail ammonia absorption storage tank, the purified water liquid absorbed by ammonia gas is less than 16°C, and 10%-12% of ammonia is absorbed.

[0031] In this specific embodiment, 12% of the remaining ammonia gas is recovered for the second time, creating a negative pressure inside the ammonia distillation reactor and normalizing the low-boiling critical point reaction. (1) An optimized vacuum jet dissolution ammonia absorption system, a cooling vacuum jet dissolution ammonia absorption liquid system, and a vacuum jet dissolution ammonia absorption system are composed of a high-lift pump and a vacuum jet dissolution absorption tank for the remaining ammonia solution. Deionized water is used as the dissolution ammonia absorption medium, with a temperature of 15±1 degree. It is pumped into the vacuum jet absorber by the high-lift pump, instantaneously absorbing the remaining ammonia and water vapor in a low-temperature environment to form a vacuum system, and circulating in sequence. (2) The cooling ammonia dissolution recovery liquid system consists of a refrigeration raw water storage tank, a transfer pump, a cooling coil device in the ammonia dissolution absorption tank, a cooling raw water storage tank, a transfer pump, and a chiller. Deionized water is used as the cooling medium. The temperature of the cooled deionized water is about 10 degrees. It is pumped into the cooler of the ammonia dissolution absorption tank by the pump. After cooling, the deionized water flows into the cooling raw water storage tank, and then is pumped into the chiller by the transfer pump. The refrigerated deionized water flows into the refrigeration raw water storage tank and is used for cooling in this cycle.

[0032] As Figure 1As shown in the figure, the third ammonia recovery mechanism in this specific embodiment is used to absorb the overflowing ammonia gas; the specific structure is as follows: the third ammonia recovery mechanism includes a dilute sulfuric acid absorption tank 18, valve eleven 31, valve twelve 32, valve thirteen 33, and valve fourteen 34; valve eleven 31, valve twelve 32, valve thirteen 33, and valve fourteen 34 are respectively installed on the breathing ports at the upper right ends of the tail ammonia absorption tank 5, condensed ammonia water storage tank 6, carbonization dissolution tank 10, and precipitant purification tank 13. Valve eleven 31, valve twelve 32, valve thirteen 33, and valve fourteen 34 are respectively connected to the inlet pipe of the dilute sulfuric acid absorption tank 18 through pipelines. The outlet pipe of the dilute sulfuric acid absorption tank 18 is inserted 10 cm below the liquid level of the 10% dilute sulfuric acid solution.

[0033] In the third ammonia absorption system of this specific embodiment: it recovers the trace ammonia gas escaping from the breathing ports during the drainage operation of each storage tank, reduces pollution, and ensures a clean control environment. Connect the breathing ports of the tail ammonia absorption tank, condensed ammonia water storage tank, carbonization dissolution tank, and precipitant purification tank to the inlet pipe of the dilute sulfuric acid (10%) absorption tank. The outlet of the connecting pipe should be inserted within 10 cm below the liquid level of the 10% dilute sulfuric acid solution for acid absorption, and when it reaches a certain concentration, it is reserved for distillation.

[0034] In this specific embodiment, the residual ammonia dissolution and absorption tank has an inhalation and exhalation port, an exhalation port, and a linkage electromagnetic suction valve; the breathing port of the condensed ammonia water storage tank and the linkage electromagnetic suction valve; the exhalation port of the carbonization dissolution tank and the linkage electromagnetic valve suction valve; the exhalation port of the precipitant purification tank and the linkage electromagnetic suction valve. The breathing ports of the above-mentioned tanks are respectively connected to the breathing port of the dilute sulfuric acid solution (10%) absorption tank. For the pipe connecting the breathing ports, the exhalation pipe port should be inserted 10 cm below the liquid level in the dilute sulfuric acid solution tank to acidify and absorb the ammonia gas escaping from the exhalation port. The inhalation solenoid valves of the above-mentioned tanks are linked with the electric drain valves at the tank ports. When the automatic drain valve is opened, the inhalation solenoid valve automatically opens for inhalation after 10 seconds. However, when the liquid in each tank is closed, the inhalation solenoid valve automatically closes simultaneously to avoid the escape of ammonia gas.

[0035] As Figure 1 As shown in the figure, the carbon dioxide dissolution and carbonization ammonia fixation mechanism in this specific embodiment is used to convert ammonia into ammonium carbonate through purification; the specific structure is as follows: the carbon dioxide dissolution and carbonization ammonia fixation mechanism includes a carbonization dissolution tank 10, a CO2 storage tank 12, and a precipitant purification tank 13; the CO2 storage tank 12 is connected to the carbonization dissolution tank 10 through a pipeline and valve seven 28, and the lower side of the carbonization dissolution tank 10 is connected to the precipitant purification tank 13 through a transfer pump one 20. Carbon dioxide dissolution and absorption ammonia fixation system: Pump the concentrated ammonia water in the condensed ammonia water storage tank and the dilute ammonia water in the tail ammonia absorption tank into the carbonization dissolution tank through a transfer ammonia water pump for carbonization dissolution and absorption, and then transport it to the precipitant purification tank for net conversion to fix ammonia in the form of ammonium carbonate for use in the preparation of magnesium oxide synthesis process with the precipitant.

[0036] In this specific embodiment, when the condenser is in use, the intermediate product magnesium sulfate solution for producing magnesium carbonate precursor is used as the cooling medium to cool and condense ammonia gas and water vapor into hot ammonia water solution, so that the cooling medium magnesium sulfate solution is heated to 52 °C, reaching the target control temperature of 51 ± 1 °C of the magnesium sulfate solution used in the synthesis process for synthesizing magnesium carbonate. In this way, the heat energy is fully utilized and steam is saved. Using magnesium sulfate solution as the medium for the cold chain in the high-temperature condenser is the optimal option, which will not cause the condensation heat exchanger wall to become caked. After long-term use, the heat conduction effect of the condenser remains unchanged and its service life is long. In the low-temperature section of the cooler, using drinking water as the cooling medium is the most reasonable choice. After long-term use, it will not cause the cooler wall to become caked, and the hot ammonia water is effectively cooled to below 26 degrees. In the second cold ammonia absorption recovery system: purified water with a cooling constant temperature of 15 ± 1 °C is used as the ammonia gas absorbent, and is pumped into the jet ammonia absorber at a speed of 15 liters per second by a 38-meter high-lift pump, so that the ammonia gas is instantaneously absorbed and dissolved, and finally enters the tail ammonia gas absorption tank for cyclic ammonia absorption. It reaches the ammonia and water vapor channels in the cooler and condenser. And in the vacuum negative pressure space in the distillation reactor, the double decomposition reaction solution drops below 88 °C and boils at a low temperature, the reaction speed is accelerated, the reaction yield is increased, and the ammonia gas is completely recovered. Each storage tank in this specific embodiment is equipped with an air intake electromagnetic automatic valve connected to the discharge electromagnetic valve and pump of this tank for automatic control. The breathing port is connected to the acid absorption storage tank, and a small amount of ammonia gas escapes from the exhalation port and is acidified and absorbed by dilute sulfuric acid and supplemented into the mother liquor for distillation use. The production site environment is clean and environmentally friendly.

[0037] For those skilled in the art, it is obvious that the present utility model is not limited to the details of the above-described exemplary embodiments, and can be implemented in other specific forms without departing from the spirit or basic characteristics of the present utility model. Therefore, from any point of view, the embodiments should be regarded as exemplary and non-restrictive. The scope of the present utility model is defined by the appended claims rather than the above description. Therefore, it is intended to include all changes falling within the meaning and scope of the equivalent elements of the claims in the present utility model.

[0038] In addition, it should be understood that although this specification is described according to the embodiments, not every embodiment only contains an independent technical solution. This narrative way of the specification is only for clarity. Those skilled in the art should regard the specification as a whole, and the technical solutions in each embodiment can also be appropriately combined to form other embodiments that can be understood by those skilled in the art.

Claims

1. A clean, environmentally friendly, green, efficient and energy-saving distillation ammonia recovery device, characterized by: It includes a first ammonia recovery mechanism, a second ammonia recovery mechanism, a third ammonia recovery mechanism, and a carbon dioxide dissolving carbonization solid ammonia mechanism; the first ammonia recovery mechanism is connected to the second ammonia recovery mechanism, the second ammonia recovery mechanism is connected to the third ammonia recovery mechanism, and the carbon dioxide dissolving carbonization solid ammonia mechanism is connected to the first ammonia recovery mechanism, the second ammonia recovery mechanism, and the third ammonia recovery mechanism; The first ammonia recovery mechanism is used to convert high-temperature ammonia gas and water vapor from gaseous state into hot liquid ammonia water instantly, and then cool it to form liquid ammonia water at room temperature; The second ammonia recovery mechanism is used for circulating and absorbing ammonia; The third ammonia recovery mechanism is used to absorb the overflowed ammonia; The carbon dioxide dissolving and carbonizing ammonia solidifying mechanism is used for net conversion of solid ammonia into ammonium carbonate.

2. A clean, environmentally friendly, green, efficient and energy-saving distillation ammonia recovery device according to claim 1, characterized in that: The first ammonia recovery mechanism comprises an ammonia evaporation reactor (1), a condenser (2), a cooler (3), a condensed ammonia water storage tank (6), a magnesium sulfate liquid storage tank (11), and a synthetic magnesium sulfate preheating tank (30); the lower end of the magnesium sulfate liquid storage tank (11) is connected to the right end of the condenser (2) through a pipeline, a second delivery pump (35), and a first valve (17); the right end of the condenser (2) is connected to the cooler (3); the upper left end of the condenser (2) is connected to the synthetic magnesium sulfate preheating tank (30) through a pipeline and a sixteenth valve (36); the upper end of the ammonia evaporation reactor (1) is connected to the left end of the condenser (2) through a pipeline; and the lower end of the cooler (3) is connected to the upper end of the condensed ammonia water storage tank (6) through a cooling and recovery ammonia water meter (14).

3. A clean, environmentally friendly, green, efficient and energy-saving distillation ammonia recovery device according to claim 2, characterized in that: The two upper ends of the ammonia distillation reactor (1) are respectively provided with a light-burned magnesium oxide slurry feeding port (1-1) and a mother liquor ammonium sulfate feeding port (1-2).

4. A clean, environmentally friendly, green, efficient and energy-saving distillation ammonia recovery device according to claim 2, characterized in that: The first ammonia recovery mechanism also includes a cooling mechanism, which includes a cooling tower (15) and a cooling pool (16); the lower end of the cooling tower (15) is connected to the cooling pool (16) through a pipeline, the lower end of the cooling pool (16) is connected to the lower side of the cooler (3) through a pipeline, valve seventeen (37), and valve eight (29), and the upper side of the cooler (3) is connected to the upper end of the cooling tower (15) through a pipeline.

5. A clean, environmentally friendly, green, efficient and energy-saving distillation ammonia recovery device according to claim 1, characterized in that: The second ammonia recovery mechanism comprises a jet absorber (4), a tail ammonia absorption tank (5), a refrigeration water storage tank (7), a refrigerator (8), a cooling water storage tank (9), a high-lift water pump (19), a delivery circulation pump (21), and a delivery water pump (22); the bottom of the tail ammonia absorption tank (5) and the condensed ammonia water storage tank (6) are connected to one end of the high-lift water pump (19) through a pipeline, a second valve (23), and a fifth valve (26); the other end of the high-lift water pump (19) is connected to the jet absorber (4) through a pipeline, a third valve (24), and a fourth valve (25). The upper end of the ammonia collector (4) and the carbonization dissolution tank (10) are connected, the lower end of the jet absorber (4) is connected to the upper end of the tail ammonia absorption tank (5), one end of the cooler inside the tail ammonia absorption tank (5) is connected to the upper end of the cooling water storage tank (9) through a pipeline, the lower end of the cooling water storage tank (9) is connected to the refrigerator (8) through a delivery water pump (22), the refrigerator (8) is connected to the upper end of the cooling water storage tank (7), and the lower side of the cooling water storage tank (7) is connected to the other end of the cooler inside the tail ammonia absorption tank (5) through a pipeline and a delivery circulation pump (21).

6. A clean, environmentally friendly, green, efficient and energy-saving distillation ammonia recovery device according to claim 1, characterized in that: The second ammonia recovery mechanism comprises a jet absorber (4), a tail ammonia absorption tank (5), a refrigeration water storage tank (7), a refrigerator (8), a cooling water storage tank (9), a high-lift water pump (19), a delivery circulation pump (21), and a delivery water pump (22); the bottom of the tail ammonia absorption tank (5) and the condensed ammonia water storage tank (6) are connected to one end of the high-lift water pump (19) through a pipeline, a second valve (23), and a fifth valve (26), and the other end of the high-lift water pump (19) is connected to the jet absorber (4) through a pipeline, a third valve (24), and a fourth valve (25). ), the upper end of the carbonization dissolution tank (10), the lower end of the jet absorber (4) is connected to the upper end of the tail ammonia absorption tank (5), one end of the cooler inside the tail ammonia absorption tank (5) is connected to the upper end of the cooling water storage tank (9) through a pipeline, the lower end of the cooling water storage tank (9) is connected to the refrigerator (8) through a delivery water pump (22), the refrigerator (8) is connected to the upper end of the cooling water storage tank (7), and the lower side of the cooling water storage tank (7) is connected to the other end of the cooler inside the tail ammonia absorption tank (5) through a pipeline, a delivery circulation pump (21), and a valve six (27).

7. A clean, environmentally friendly, green, efficient and energy-saving distillation ammonia recovery device according to claim 1, characterized in that: The third ammonia recovery mechanism comprises a dilute sulfuric acid absorption tank (18), a valve 11 (31), a valve 12 (32), a valve 13 (33), and a valve 14 (34); the valve 11 (31), the valve 12 (32), the valve 13 (33), and the valve 14 (34) are respectively installed on the breathing ports at the upper right ends of the tail ammonia absorption tank (5), the condensed ammonia water storage tank (6), the carbonization dissolution tank (10), and the precipitant purification tank (13); the valve 11 (31), the valve 12 (32), the valve 13 (33), and the valve 14 (34) are respectively connected to the inlet pipe of the dilute sulfuric acid absorption tank (18) through pipelines; and the outlet pipe of the dilute sulfuric acid absorption tank (18) is inserted 10 cm below the liquid surface of the 10% dilute sulfuric acid solution.

8. A clean, environmentally friendly, green, efficient and energy-saving distillation ammonia recovery device according to claim 1, characterized in that: The carbon dioxide dissolving and carbonizing ammonia solidifying mechanism comprises a carbonization dissolving tank (10), a CO2 storage tank (12), and a precipitant purification tank (13); the CO2 storage tank (12) is connected to the carbonization dissolving tank (10) via a pipeline and a valve seven (28), and the lower side of the carbonization dissolving tank (10) is connected to the precipitant purification tank (13) via a delivery pump one (20).

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