CN216303318U - Ammonia distillation system - Google Patents
Ammonia distillation system Download PDFInfo
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- CN216303318U CN216303318U CN202122951986.9U CN202122951986U CN216303318U CN 216303318 U CN216303318 U CN 216303318U CN 202122951986 U CN202122951986 U CN 202122951986U CN 216303318 U CN216303318 U CN 216303318U
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Abstract
The present application provides an ammonia distillation system, comprising: the system comprises a stripping tower, a preheater, a condenser, a gas-liquid separator and a deamination wastewater pump; the stripping tower is respectively connected with the preheater and the condenser through a conveying pipeline; the gas-liquid separator is connected with the preheater through a conveying pipeline, and the deamination wastewater pump is connected with the bottom of the stripping tower through a deamination wastewater pipeline; the stripping tower is used for stripping ammonia-containing wastewater to remove NH3(ii) a The preheater is used for preheating and heating the second ammonia-containing wastewater; the condenser is used for outputting the top of the stripping towerCondensing a part of the mixed gas; the gas-liquid separator is used for carrying out gas-liquid separation on a gas-liquid mixture obtained after the heat exchange of the other part of mixed gas output from the top of the stripping tower through the preheater. The application realizes the purpose of ammonia removal by wastewater ammonia distillation, improves the desorption rate of ammonia gas, is convenient to operate, and reduces the production cost.
Description
Technical Field
The application relates to the technical field of ammonia water treatment, in particular to an ammonia distillation system.
Background
The process condensate generated in the methanol production process, namely the wastewater contains a certain amount of ammonia, the ammonia-containing wastewater is industrial wastewater with complex components, high toxicity, difficult degradation and poor biodegradability, wherein high-concentration ammonia nitrogen is directly discharged into a biochemical treatment system, and the high-ammonia nitrogen wastewater causes the collapse of the biochemical system for wastewater treatment, can cause the running obstacle of the whole wastewater treatment system and seriously affects the wastewater treatment effect. If the waste gas is directly discharged, the environment is seriously polluted. Therefore, the ammonia nitrogen with high concentration in the ammonia-containing wastewater must be removed.
A common removal treatment is desorption of ammonia by direct steam stripping. When the ammonia is evaporated, the steam is fully contacted with the wastewater, heat and substance exchange is carried out between the steam and the wastewater according to the steam stripping principle, and the ammonia is separated from the wastewater and enters the steam, so that the ammonia in the wastewater is separated and is carried out by the steam, and the aim of reducing the concentration of the ammonia in the wastewater is fulfilled. However, the ammonia distillation efficiency in the prior art is poor, ammonia nitrogen in ammonia-containing wastewater cannot be effectively discharged, so that the ammonia nitrogen is slowly enriched in the system, finally system operation obstacle is caused, and the wastewater treatment effect is influenced.
SUMMERY OF THE UTILITY MODEL
The application provides an ammonia distillation system for solve the poor problem of ammonia distillation efficiency, realized the waste water and evaporated ammonia and removed the purpose of ammonia, improved the desorption rate of ammonia, and technology convenient operation has reduced the running cost.
The present application provides an ammonia distillation system, comprising: stripping tower, preheater, condenser, vapour and liquid separator and deamination waste water pump.
The stripping tower is respectively connected with the preheater and the condenser through a conveying pipeline.
The gas-liquid separator is connected with the preheater through a conveying pipeline, and the deamination waste water pump is connected with the bottom of the stripping tower through a deamination waste water pipeline.
StrippingThe tower is used for stripping ammonia-containing wastewater to remove NH3Mixed gas of ammonia gas and water vapor is obtained at the tower top, and deamination wastewater is obtained at the tower bottom.
The preheater is used for preheating and heating the second ammonia-containing wastewater, and the heat source of the preheater is the mixed gas at the top of the stripping tower.
The condenser is used for condensing a part of mixed gas output from the top of the stripping tower.
The gas-liquid separator is used for carrying out gas-liquid separation on a gas-liquid mixture obtained after the other part of mixed gas output from the top of the stripping tower is subjected to heat exchange by the preheater to obtain an ammonia water mixture and ammonia gas.
The deamination wastewater pump is used for conveying the deamination wastewater at the bottom of the stripping tower to a wastewater biochemical treatment system for treatment and recycling.
Optionally, a packing box is arranged at the upper part of the stripping tower, and the packing for the packing box is stainless steel structured packing.
Optionally, the upper middle part of the stripping tower is provided with a first ammonia-containing wastewater inlet for inputting first ammonia-containing wastewater.
Optionally, a branch feed inlet is arranged at the top of the stripping tower, and 50-60% of the volume of the first ammonia-containing wastewater is conveyed to the stripping tower from the branch feed inlet through a branch feed pipeline.
Optionally, the stripper upper portion is provided with the second and contains the ammonia waste water import, and the preheater is connected through the second and contains ammonia waste water pipeline with the second and contain ammonia waste water import.
Optionally, a mixed gas outlet is arranged at the top of the stripping tower, and a preheater heat source inlet is connected with the mixed gas outlet through a gas phase conveying pipeline.
Optionally, a branch pipeline is led out from a gas phase conveying pipeline connected with a heat source inlet of the preheater and a mixed gas outlet to convey 85-90% of the volume of the mixed gas output from the top of the stripping tower to a condenser, and the mixed gas is condensed to obtain an ammonia water mixture.
Optionally, a gas-phase outlet of the gas-liquid separator is connected with the boiler flue and used for conveying the separated ammonia gas to the boiler flue, and a liquid-phase outlet of the gas-liquid separator is respectively connected with the flue gas desulfurization system and the sulfur recovery system and used for conveying the separated ammonia water mixture to the flue gas desulfurization system and the sulfur recovery system.
Optionally, a steam inlet is arranged at the middle lower part of the stripping tower and used for inputting steam; the steam inlet pressure is 0.5-0.55MPa, the flow rate is 1.5-2t/h, and the temperature is 145-.
The application provides an ammonia distillation system through letting in vapor to the strip tower, makes first containing ammonia waste water and second contain ammonia waste water and vapor fully contact in the strip tower, utilizes the principle that the increase temperature reduces the ammonia nitrogen and ammonia nitrogen solubility in containing ammonia waste water, has reached the purpose that the ammonia distillation removed ammonia. Meanwhile, a part of mixed gas of ammonia gas and water vapor obtained from the tower top is used as a heat source to preheat the second ammonia-containing wastewater, so that the heat is effectively utilized, and the use amount of the water vapor is saved; and the other part of mixed gas of ammonia gas and water vapor is input into the condenser, so that the gas phase flux at the top of the tower is increased, and the gas phase partial pressure of ammonia is increased. A part of the first ammonia-containing wastewater is conveyed to the stripping tower through a branch feeding pipeline, so that the contact area of the first ammonia-containing wastewater and steam is increased, and the ammonia distillation efficiency is improved; meanwhile, the ammonia water mixture obtained by steam stripping is conveyed to a sulfur recovery system, so that the system is prevented from being blocked by the enrichment of solid sulfur, the service life of equipment is prolonged, the ammonia distillation efficiency is improved, and the pressure of a subsequent wastewater biochemical treatment system is reduced. The ammonia distillation system provided by the application can also be applied to desorption of other gases capable of being dissolved in water.
Drawings
In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, the drawings needed to be used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present application, and other drawings can be obtained by those skilled in the art without creative efforts.
FIG. 1 is a schematic diagram of an ammonia distillation system according to an embodiment of the present disclosure;
FIG. 2 is a schematic diagram of an ammonia distillation system according to another embodiment of the present disclosure;
FIG. 3 is a schematic diagram of a ammonia distillation system provided in a comparative scale.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present application clearer, the technical solutions in the embodiments of the present application are clearly and completely described below, and it is obvious that the described embodiments are a part of the embodiments of the present application, but not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present application.
Fig. 1 is a schematic structural diagram of an ammonia distillation system according to an embodiment of the present application, and as shown in fig. 1, the ammonia distillation system according to the embodiment includes: a stripping tower 110, a preheater 120, a condenser 130, a gas-liquid separator 140 and a deamination waste water pump 150.
The stripping column 110 is connected to a preheater 120 and a condenser 130 through transfer lines, respectively.
The gas-liquid separator 140 is connected with the preheater 120 through a conveying pipeline, and the deamination wastewater pump 150 is connected with the bottom of the stripping tower 110 through a deamination wastewater pipeline.
The stripping tower 110 is used for stripping ammonia-containing wastewater to remove NH3Mixed gas of ammonia gas and water vapor is obtained at the tower top, and deamination wastewater is obtained at the tower bottom.
The preheater 120 is used for preheating and heating the second ammonia-containing wastewater, and the heat source of the preheater 120 is the mixed gas at the top of the stripping tower 110.
The condenser 130 is used for condensing a part of the mixed gas output from the top of the stripping tower 110.
The gas-liquid separator 140 is configured to perform gas-liquid separation on a gas-liquid mixture obtained by heat exchange of another part of the mixed gas output from the top of the stripping tower 110 by the preheater 120, so as to obtain an ammonia water mixture and ammonia gas.
The deamination wastewater pump 150 is used for conveying the deamination wastewater at the bottom of the stripping tower 110 to a wastewater biochemical treatment system for treatment and recycling.
Specifically, the first ammonia-containing wastewater and the second ammonia-containing wastewater are conveyed to the stripping tower 110, and simultaneously, steam is introduced into the stripping tower 110, so that the ammonia-containing wastewater and the steam are in vapor-liquid two-phase countercurrent contact in the stripping tower 110, and for ammonia dissolved in water, the property that the concentration of the ammonia dissolved in water is higher in the vapor phase than in the liquid phase under the vapor-liquid equilibrium condition is utilized to perform mass exchange heat, so that the ammonia in the ammonia-containing wastewater is gradually evaporated. The mixed gas of ammonia and steam is obtained at the top of the stripping tower 110, and a part of the mixed gas is conveyed to the condenser 130 through the conveying pipeline for condensation and then is conveyed to the flue gas desulfurization system, so that the gas phase flux at the top of the stripping tower is increased, the gas phase partial pressure of ammonia is increased, and the ammonia is favorably evaporated. The other part of the mixed gas output from the top of the stripping tower 110 is conveyed to the preheater 120 to be used as a heat source, and the second ammonia-containing wastewater is preheated in the preheater 120 and then is conveyed to the stripping tower 110, so that the heat of the mixed gas is reasonably utilized, and the ammonia distillation efficiency is improved; the mixed gas after heat exchange in the preheater 120 is sent to a gas-liquid separator 140 for gas-liquid separation, so as to obtain an ammonia water mixture and ammonia gas. Liquid-phase deamination wastewater obtained by the ammonia-containing wastewater after steam stripping is gathered at the bottom of the stripping tower 110, and is conveyed to a wastewater biochemical treatment system by a deamination wastewater pump 150 for recycling after being treated.
Above-mentioned system is passed through to this embodiment, through with the ammonia wastewater and vapor countercurrent contact in the stripper, evaporates the ammonia in the ammonia wastewater gradually, has realized the purpose to ammonia wastewater ammonia still. A part of mixed gas output from the top of the stripping tower is conveyed to a condenser through a conveying pipeline for condensation, so that the gas phase flux at the top of the stripping tower is increased, the gas phase partial pressure of ammonia is increased, and the ammonia gas is favorably evaporated. The other part of mixed gas output from the top of the stripping tower is conveyed to the preheater and used as a heat source, and the second ammonia-containing wastewater is preheated in the preheater to raise the temperature, so that the heat of the mixed gas is reasonably utilized, the heat exchange time of the second ammonia-containing wastewater in the stripping tower is shortened, and the ammonia distillation efficiency is also improved.
Fig. 2 is a schematic structural diagram of an ammonia distillation system according to another embodiment of the present disclosure, and as shown in fig. 2, optionally, a stuffing box 1101 is disposed at an upper portion of the stripping column 110, and the stuffing box 1101 is a stainless steel structured packing.
Specifically, the stuffing box 1101 is positioned at the upper part of the stripping tower 110, the used stuffing is stainless steel structured stuffing, and the stainless steel structured stuffing has the advantages of thin wall, cold and heat resistance, large void ratio, large flux, pressure reduction, small resistance, uniform fluid distribution, high mass and heat transfer efficiency, long service life and the like, is favorable for increasing the gas-liquid contact area, ensures that the mass exchange and heat exchange of ammonia-containing wastewater and water vapor are more sufficient, and improves the ammonia distillation efficiency.
Optionally, a first ammonia-containing wastewater inlet 1102 is arranged at the middle upper part of the stripping tower 110, and is used for inputting the first ammonia-containing wastewater.
Specifically, the ammonia-containing wastewater is divided into two parts (a first ammonia-containing wastewater and a second ammonia-containing wastewater) according to the previous process, and the two parts enter the stripping tower 110, wherein the first ammonia-containing wastewater is input into the stripping tower 110 through a first ammonia-containing wastewater inlet 1102 at the middle upper part of the stripping tower 110, and the flow rate is 1-1.5m3/h。
Optionally, a branch feeding port 1103 is disposed at the top of the stripping tower 110, and 50-60% of the volume of the first ammonia-containing wastewater is conveyed to the stripping tower 110 from the branch feeding port 1103 through a branch feeding line.
Specifically, 50-60% of the first ammonia-containing wastewater is conveyed to the stripping tower 110 from the branch feed inlet 1103, so that the first ammonia-containing wastewater is fully contacted with water vapor through the stuffing box 1101, the mass and heat transfer is increased, and the ammonia distillation efficiency is improved.
Optionally, a second ammonia-containing wastewater inlet 1104 is arranged at the upper part of the stripping tower 110, and the preheater 120 is connected with the second ammonia-containing wastewater inlet 1104 through a second ammonia-containing wastewater pipeline; the top of the stripping tower 110 is provided with a mixed gas outlet 1105, and the heat source inlet of the preheater 120 is connected with the mixed gas outlet 1105 through a gas phase conveying pipeline.
Specifically, the second ammonia-containing wastewater is first supplied to the preheater 120, preheated in the preheater 120, and then supplied to the stripper 110 through the second ammonia-containing wastewater inlet 1104 provided at an upper portion of the stripper 110 at 25 to 28m3The flow rate of the second ammonia-containing wastewater is input into the stripping tower 110, so that the heat exchange time of the second ammonia-containing wastewater in the stripping tower 110 is reduced, the heat consumption of steam is reduced, and the heat energy is saved. The mixed gas at the top of the stripping tower 110 is input into the preheater 120 through the mixed gas outlet 1105 and is used as a preheating heat source of the second ammonia-containing wastewater, so that the heat of the mixed gas is reasonably utilized, and meanwhile, the mixed gas is also providedThe ammonia distillation efficiency is high.
Optionally, a branch pipeline is led out from the gas phase conveying pipeline connecting the heat source inlet of the preheater 120 and the mixed gas outlet 1105, and 85-90% of the volume of the mixed gas output from the top of the stripping tower 110 is conveyed to the condenser 130, and the mixed gas is condensed to obtain an ammonia water mixture.
Specifically, a branch pipeline is led out from a gas phase conveying pipeline connected between the preheater 120 and the top of the stripping tower 110, 85-90% of mixed gas is conveyed to the condenser 130 for condensation, when the equipment normally operates, the pressure at the top of the tower is 0.1-0.3MPa, if the mixed gas is completely introduced into the preheater 120, the pressure at the top of the tower reaches 0.38MPa when the introduction amount of water vapor reaches 1 ton (T), at the moment, the load at the top of the tower is too heavy, and the ammonia distillation efficiency is reduced, so that the branch pipeline is led out, the load at the top of the tower is reduced, the gas phase flux at the top of the tower is increased, the gas phase partial pressure of ammonia is increased, the mass and heat transfer between phase states are better performed, the solubility of ammonia in water is reduced, and the ammonia distillation efficiency is improved. And the ammonia water mixture obtained by condensation is recycled as ammonia water for reuse or is conveyed to a flue gas desulfurization system, so that resources are saved, and the production cost is reduced. The condensate used in the condenser 130 is selected to be circulating cooling water at a temperature of 25-40 ℃.
Optionally, a gas-phase outlet of the gas-liquid separator 140 is connected to the boiler flue and is configured to deliver the separated ammonia gas to the boiler flue, and a liquid-phase outlet of the gas-liquid separator 140 is respectively connected to the flue gas desulfurization system and the sulfur recovery system and is configured to deliver the separated ammonia water mixture to the flue gas desulfurization system and the sulfur recovery system.
Specifically, the ammonia water mixture and the ammonia gas obtained by the gas-liquid separator are recycled, so that the investment of the desulfurization solution in the flue gas desulfurization system is saved; simultaneously, in the sulfur recovery system, H is introduced2After S is catalytically oxidized into sulfur, solid sulfur is enriched in the equipment, the equipment is blocked along with the long-time operation of the equipment, and the equipment needs to be stopped at regular time for cleaning, so that the ammonia water mixture is conveyed to a sulfur recovery system, the solid sulfur is dissolved into sulfate to be output, the sulfate can completely replace caustic soda flakes, 150kg of caustic soda flakes can be saved every month, and the operation period of the equipment is prolonged.
Optionally, a steam inlet 1106 is arranged at the middle lower part of the stripping tower 110 and used for inputting steam; the steam inlet pressure is 0.5-0.55MPa, the flow rate is 1.5-2t/h, and the temperature is 145-.
Specifically, a steam inlet 1106 is arranged at the middle lower part of the stripping tower 110, when steam is introduced into the stripping tower 110, the steam flows towards the top of the tower along the stripping tower 110, and ammonia-containing wastewater flows towards the bottom of the tower from the top of the tower, so that the arrangement is favorable for increasing the gas-liquid contact area. Meanwhile, the pressure, the flow and the temperature of the steam are controlled within a proper range, so that the ammonia-containing wastewater is favorable for quality change and heat exchange in the stripping tower, and the ammonia distillation efficiency is further improved.
The technical solution of the present application is illustrated in detail by the following specific examples.
Example 1
The operation flow of the ammonia distillation system in the embodiment in specific work is as follows:
(1) introducing ammonia-containing wastewater: the first ammonia-containing wastewater is added with the volume of 1.0m3The flow rate of the ammonia-containing wastewater is input into the stripping tower through the first ammonia-containing wastewater inlet, and the second ammonia-containing wastewater is simultaneously fed into the stripping tower at the flow rate of 25m3The flow rate of the/h is input into the stripping tower through a second ammonia-containing wastewater inlet. Wherein, 50% of the first ammonia-containing wastewater volume is conveyed into the stripping tower from the branch feed inlet, and the ammonia distillation efficiency is increased.
(2) Introducing water vapor: and (3) conveying the steam to the stripping tower through a steam inlet, controlling the steam pressure to be 0.5MPa, the flow to be 1.5t/h and the temperature to be 145 ℃.
(3) Ammonia distillation: the water vapor and the ammonia-containing wastewater are in countercurrent contact in the stripping tower and exchange heat, so that the equilibrium partial pressure of ammonia in the ammonia-containing wastewater is greater than the partial pressure of ammonia in a gas phase, and the ammonia in the ammonia-containing wastewater is evaporated.
(4) A condensation step: and (3) obtaining mixed gas of ammonia gas and steam at the tower top after steam stripping, conveying 85% of the volume of the mixed gas to a condenser for condensation, recovering an ammonia water mixture obtained by condensation as ammonia water for reuse or conveying the ammonia water mixture to a flue gas desulfurization system, and selecting circulating cooling water with the temperature of 25 ℃ as condensate liquid used by the condenser. And (3) conveying the rest part of mixed gas to a preheater to preheat the second ammonia-containing wastewater, conveying the second ammonia-containing wastewater to a gas-liquid separator, conveying the separated ammonia gas to a boiler flue, and conveying the separated ammonia water mixture to a flue gas desulfurization system and a sulfur recovery system. And (3) pumping the deamination wastewater obtained at the tower bottom to a wastewater biochemical treatment system through a deamination wastewater pump for recycling.
Example 2
The operation flow of the ammonia distillation system in the embodiment in specific work is as follows:
(1) introducing ammonia-containing wastewater: the first ammonia-containing wastewater is treated by the treatment of 1.2m3The flow rate of the ammonia-containing wastewater is input into the stripping tower through the first ammonia-containing wastewater inlet, and the second ammonia-containing wastewater is simultaneously fed into the stripping tower at the flow rate of 27m3The flow rate of the/h is input into the stripping tower through a second ammonia-containing wastewater inlet. Wherein, 50% of the first ammonia-containing wastewater volume is conveyed into the stripping tower from the branch feed inlet, and the ammonia distillation efficiency is increased.
(2) Introducing water vapor: and (3) conveying the steam to the stripping tower through a steam inlet, controlling the steam pressure to be 0.55MPa, the flow to be 17t/h and the temperature to be 150 ℃.
(3) Ammonia distillation: the water vapor and the ammonia-containing wastewater are in countercurrent contact in the stripping tower and exchange heat, so that the equilibrium partial pressure of ammonia in the ammonia-containing wastewater is greater than the partial pressure of ammonia in a gas phase, and the ammonia in the ammonia-containing wastewater is evaporated.
(4) A condensation step: and obtaining mixed gas of ammonia gas and steam at the tower top after steam stripping, conveying 87% of the volume of the mixed gas to a condenser for condensation, recovering an ammonia water mixture obtained by condensation as ammonia water for reuse or conveying the ammonia water mixture to a flue gas desulfurization system, and selecting circulating cooling water with the temperature of 32 ℃ as condensate liquid used by the condenser. And (3) conveying the rest part of mixed gas to a preheater to preheat the second ammonia-containing wastewater, conveying the second ammonia-containing wastewater to a gas-liquid separator, conveying the separated ammonia gas to a boiler flue, and conveying the separated ammonia water mixture to a flue gas desulfurization system and a sulfur recovery system. And (3) pumping the deamination wastewater obtained at the tower bottom to a wastewater biochemical treatment system through a deamination wastewater pump for recycling.
Example 3
The operation flow of the ammonia distillation system in the embodiment in specific work is as follows:
(1) introducing ammonia-containing wastewater: the first ammonia-containing wastewater is treated by the treatment of 1.5m3The flow rate of the second ammonia-containing wastewater is input into the stripping tower through the first ammonia-containing wastewater inlet, and the second ammonia-containing wastewater is simultaneously fed into the stripping tower at the flow rate of 28m3The flow rate of the/h is input into the stripping tower through a second ammonia-containing wastewater inlet. Wherein, 50% of the first ammonia-containing wastewater volume is conveyed into the stripping tower from the branch feed inlet, and the ammonia distillation efficiency is increased.
(2) Introducing water vapor: and (3) conveying the steam to the stripping tower through a steam inlet, controlling the steam pressure to be 0.55MPa, the flow to be 2t/h and the temperature to be 155 ℃.
(3) Ammonia distillation: the water vapor and the ammonia-containing wastewater are in countercurrent contact in the stripping tower and exchange heat, so that the equilibrium partial pressure of ammonia in the ammonia-containing wastewater is greater than the partial pressure of ammonia in a gas phase, and the ammonia in the ammonia-containing wastewater is evaporated.
(4) A condensation step: and (3) obtaining mixed gas of ammonia gas and steam at the tower top after steam stripping, conveying 90% of the volume of the mixed gas to a condenser for condensation, recovering an ammonia water mixture obtained by condensation as ammonia water for reuse or conveying the ammonia water mixture to a flue gas desulfurization system, and selecting circulating cooling water with the temperature of 40 ℃ as condensate liquid used by the condenser. And (3) conveying the rest part of mixed gas to a preheater to preheat the second ammonia-containing wastewater, conveying the second ammonia-containing wastewater to a gas-liquid separator, conveying the separated ammonia gas to a boiler flue, and conveying the separated ammonia water mixture to a flue gas desulfurization system and a sulfur recovery system. And (3) pumping the deamination wastewater obtained at the tower bottom to a wastewater biochemical treatment system through a deamination wastewater pump for recycling.
Comparative example 1
FIG. 3 is a schematic diagram of an ammonia distillation system provided in a comparative example, as shown in FIG. 3, which differs from example 1 in that:
(1) introducing ammonia-containing wastewater: the first ammonia-containing wastewater is added with 1m3The flow rate of the ammonia-containing wastewater is input into the stripping tower through the first ammonia-containing wastewater inlet, and the second ammonia-containing wastewater is simultaneously fed into the stripping tower at the flow rate of 25m3The flow rate of the/h is input into the stripping tower through a second ammonia-containing wastewater inlet.
(4) A condensation step: and after stripping, mixed gas of ammonia gas and steam is obtained at the tower top, and the mixed gas is completely conveyed to a preheater to preheat second ammonia-containing wastewater and then conveyed to a gas-liquid separator. And after separation by a gas-liquid separator, conveying the obtained ammonia gas to a boiler flue, and conveying the ammonia water mixture obtained by separation to a flue gas desulfurization system. And (3) pumping the deamination wastewater obtained at the tower bottom to a wastewater biochemical treatment system through a deamination wastewater pump for recycling.
Experimental example 1
When the steam introduction amount reaches 1 ton during ammonia distillation by using the ammonia distillation systems of examples 1 to 3 and comparative example 1, the pressure of the top of the stripping tower and the ammonia nitrogen content in the ammonia-removed wastewater after ammonia distillation were measured, 3 parallel experiments were performed for each example, and the average value was obtained to obtain the results shown in table one.
Watch 1
| Ammonia nitrogen content mg/L | pressure/MPa at the top of the column | |
| Example 1 | 68 | 0.1 |
| Example 2 | 80 | 0.24 |
| Example 3 | 100 | 0.3 |
| Comparative example 1 | 896 | 0.38 |
| Before treatment | 2800 | - |
As can be seen from the table I, compared with the ammonia distillation system of the embodiment 1 to the embodiment 3 used for ammonia distillation treatment of the ammonia-containing wastewater before the comparison example 1 and treatment, the ammonia nitrogen content in the obtained ammonia-removed wastewater is remarkably reduced, and the pressure at the top of the tower is kept between 0.1 and 0.3 MPa. Through letting in vapor to the strip tower, make first containing ammonia waste water and second containing ammonia waste water and vapor fully contact in the strip tower, utilize the principle that the improvement temperature reduces the ammonia nitrogen and contain ammonia solubility in the waste water that contains ammonia, reached the purpose that the ammonia distillation removed ammonia. Meanwhile, a part of mixed gas of ammonia gas and water vapor obtained from the top of the tower is used as a heat source to preheat the second ammonia-containing wastewater, so that the heat is effectively utilized, and the use amount of the water vapor is saved. And the other part of mixed gas of ammonia gas and water vapor is input into the condenser, so that the load on the top of the tower is reduced, the gas phase flux on the top of the tower is increased, the gas phase partial pressure of ammonia is increased, and the efficiency of removing ammonia nitrogen is obviously improved. Still carry out a part of first ammonia wastewater to the stripper through branch feeder line, increase and steam area of contact, improve ammonia distillation efficiency. Meanwhile, a part of ammonia water mixture obtained by steam stripping is conveyed to a sulfur recovery system, so that the system is prevented from being blocked by solid sulfur enrichment, the use of caustic soda flakes is saved, the service life of equipment is prolonged, the running cost is reduced, the ammonia distillation efficiency is improved, and the pressure of a subsequent wastewater biochemical treatment system is greatly relieved.
Finally, it should be noted that the above embodiments are only used for illustrating the technical solutions of the present application, and not for limiting the same; although the present application has been described in detail with reference to the foregoing embodiments, it will be understood by those skilled in the art; the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present application.
Claims (8)
1. An ammonia distillation system is characterized by comprising a stripping tower (110), a preheater (120), a condenser (130), a gas-liquid separator (140) and a deamination waste water pump (150);
the stripping tower (110) is respectively connected with the preheater (120) and the condenser (130) through conveying pipelines;
the gas-liquid separator (140) is connected with the preheater (120) through a conveying pipeline, and the deamination wastewater pump (150) is connected with the bottom of the stripping tower (110) through a deamination wastewater pipeline;
the stripping tower (110) is used for stripping ammonia-containing wastewater to remove NH3Mixed gas of ammonia gas and water vapor is obtained at the tower top, and deamination wastewater is obtained at the tower bottom;
the preheater (120) is used for preheating and heating the second ammonia-containing wastewater, and the heat source of the preheater (120) is the mixed gas at the top of the stripping tower (110);
the condenser (130) is used for condensing a part of the mixed gas output from the top of the stripping tower (110);
the gas-liquid separator (140) is used for performing gas-liquid separation on a gas-liquid mixture obtained after another part of the mixed gas output from the top of the stripping tower (110) is subjected to heat exchange by the preheater (120) to obtain an ammonia water mixture and ammonia gas;
the deamination wastewater pump (150) is used for conveying the deamination wastewater at the bottom of the stripping tower (110) to a wastewater biochemical treatment system for treatment and recycling.
2. An ammonia distillation system according to claim 1, characterized in that the stripping tower (110) is provided with a stuffing box (1101) at the upper part, and the stuffing box (1101) is filled with stainless steel structured packing.
3. The ammonia distillation system according to claim 1, wherein a first ammonia-containing wastewater inlet (1102) is arranged at the middle upper part of the stripping tower (110) and used for inputting the first ammonia-containing wastewater.
4. An ammonia distillation system according to claim 3, characterized in that the stripping column (110) is provided with a branch feed inlet (1103) at the top, and 50-60% of the volume of the first ammonia-containing wastewater is fed from the branch feed inlet (1103) to the stripping column (110) through a branch feed line.
5. The ammonia distillation system according to claim 1, wherein the stripping tower (110) is provided with a second ammonia-containing wastewater inlet (1104) at the upper part, and the preheater (120) is connected with the second ammonia-containing wastewater inlet (1104) through a second ammonia-containing wastewater pipeline;
the top of the stripping tower (110) is provided with a mixed gas outlet (1105), and a heat source inlet of the preheater (120) is connected with the mixed gas outlet (1105) through a gas phase conveying pipeline.
6. The ammonia distillation system of claim 5, wherein a bypass line is led out from a gas phase conveying line connected with the heat source inlet of the preheater (120) and the mixed gas outlet (1105) to convey 85-90% of the volume of the mixed gas output from the top of the stripping tower (110) to the condenser (130) to condense the mixed gas to obtain an ammonia water mixture.
7. The ammonia distillation system according to claim 1, wherein the gas phase outlet of the gas-liquid separator (140) is connected with a boiler flue for conveying separated ammonia gas to the boiler flue; and a liquid phase outlet of the gas-liquid separator (140) is respectively connected with the flue gas desulfurization system and the sulfur recovery system and used for conveying the ammonia water mixture obtained by separation to the flue gas desulfurization system and the sulfur recovery system.
8. The ammonia distillation system according to any one of claims 1-7, wherein a steam inlet (1106) is arranged at the middle lower part of the stripping tower (110) for inputting steam; the steam inlet pressure is 0.5-0.55MPa, the flow rate is 1.5-2t/h, and the temperature is 145-155 ℃.
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| CN202122951986.9U CN216303318U (en) | 2021-11-29 | 2021-11-29 | Ammonia distillation system |
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| CN202122951986.9U CN216303318U (en) | 2021-11-29 | 2021-11-29 | Ammonia distillation system |
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| CN115738587A (en) * | 2022-12-02 | 2023-03-07 | 珠海格力电器股份有限公司 | Waste material removes ammonia system |
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