CN105110350A - Ammonia recovery system and ammonia recovery method - Google Patents
Ammonia recovery system and ammonia recovery method Download PDFInfo
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- CN105110350A CN105110350A CN201510498078.5A CN201510498078A CN105110350A CN 105110350 A CN105110350 A CN 105110350A CN 201510498078 A CN201510498078 A CN 201510498078A CN 105110350 A CN105110350 A CN 105110350A
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Abstract
The present invention provides an ammonia recovery system and an ammonia recovery method. The ammonia recovery system comprises: a desulfurization part comprising an ammonia-rich gas input end and an ammonia-rich gas output end, wherein the ammonia-rich gas input end is used to introduce ammonia-rich gases; an ammonia absorption mixing part comprising a gas ammonia-ammonia water blender, wherein the gas ammonia-ammonia water blender comprises a first inlet and a first outlet, and the first inlet is connected with the ammonia-rich gas output end; an ammonia separation part comprising an ammonia distillation column, wherein the ammonia distillation column comprises a distillation column inlet and a distillation column outlet, and the distillation column inlet is connected with the distillation column outlet; The ammonia recovery system further comprises an ammonia storage part, wherein a first interface of the ammonia storage part is connected with the distillation column outlet, and a second interface of the ammonia storage part communicates with the desulfurization part to supplement liquid ammonia to the ammonia-rich gas. The ammonia recovery system provided by the present invention can solve the problems exist in the prior art that the cost consumed by the ammonia recovery process is high and ammonia can not be thoroughly recycled for application.
Description
Technical field
The present invention relates to chemical industry recovery ammonia field, in particular to a kind of ammonia recovery system and ammonia recovery method.
Background technology
Rich ammonia gas is one of gaseous effluent common in chemical industry and Coal Chemical Industry production process, if do not reclaim the ammonia in rich ammonia gas, it can cause environmental pollution, thus cannot directly discharge rich ammonia gas.At present, the industrial mode adopting recovery part ammonia then discharging waste gas, even if after the ammonia content≤100mg/L in rich ammonia gas, then carries out biochemical treatment to rich ammonia gas, makes the waste gas discharged reach emission standard, then by exhaust gas emission more.
At present, industrial usual employing rectification method or vaporizing extract process reclaim the ammonia in rich ammonia gas.
Rectification method has direct rectification method and indirect rectification method two kinds.
Direct rectification method is directly passed in rectifying tower by steam to evaporate to reclaim ammonia.Be discharged away with the mixing of tower reactor discharge water after vapor condensation, the burden of subsequent biochemical treatment process can be caused so significantly to increase.
Although indirect rectification method does not increase the water yield of biochemical treatment, usually adopt primary energy source in rectifying, the energy consumption of its technological process is comparatively large, adds production cost.
The range of application that aforesaid method reclaims ammonia goods is narrow, although the environmental issue of solving, the available value of ammonia is not high, needs to increase extra cost simultaneously and carries out recovery ammonia, still cannot, by thorough for ammonia recycle, enterprise competitiveness be declined.
Summary of the invention
Main purpose of the present invention is to provide a kind of ammonia recovery system and ammonia recovery method, high and still cannot by the problem of thorough for ammonia recycle to solve cost that ammonia reclaiming process in prior art consumes.
To achieve these goals, according to an aspect of the present invention, provide a kind of ammonia recovery system, comprising: desulfurization portion, desulfurization portion has rich ammonia gas input terminus and rich ammonia gas output terminal, and rich ammonia gas input terminus is for introducing rich ammonia gas; Ammonia absorbs mixing unit, and ammonia absorbs mixing unit and comprises gas ammonia-ammoniacal liquor mixing tank, and gas ammonia-ammoniacal liquor mixing tank has the first import and outlet, and the first import is connected with rich ammonia gas output terminal; Ammonia separation portion, ammonia separation portion comprises ammonia distillation tower, and ammonia distillation tower has distillation tower entrance and distillation tower exports, and distillation tower entrance is communicated to outlet; Ammonia recovery system also comprises: ammonia reservoir, and the first interface of ammonia reservoir is communicated to distillation tower outlet; Wherein, the second interface of ammonia reservoir is communicated with to supplement liquefied ammonia to rich ammonia gas with desulfurization portion.
Further, ammonia absorbs mixing unit and also comprises: ammonia absorber, and ammonia absorber has the first absorption mouth and the first delivery port, and first absorbs mouth is communicated to outlet, and the first delivery port is communicated to distillation tower entrance.
Further, ammonia recovery system also comprises: ammoniacal liquor water cooler, and ammoniacal liquor water cooler has cooling import and coolant outlet, and cooling import is connected with outlet, and coolant outlet and first absorbs mouth and is connected.
Further, ammonia separation portion also comprises: bottom reboiler, and the entrance of bottom reboiler is connected with the sidewall interface bottom it of ammonia distillation tower, and the outlet of bottom reboiler is connected with the bottom interface of ammonia distillation tower.
Further, ammonia separation portion also comprises: interchanger, interchanger has the first heat exchange entrance of being interconnected and the first heat exchange outlet and the second heat exchange entrance be interconnected and the second heat exchange and exports, wherein, gas ammonia-ammoniacal liquor mixing tank also has the second import, and the first heat exchange entrance is connected with the bottom interface of ammonia distillation tower, the first heat exchange outlet to the second import, second heat exchange entrance is connected with the first delivery port, and the second heat exchange outlet is connected with distillation tower entrance.
Further, ammonia recovery system also comprises: cooler package, and the entrance of cooler package exports with the first heat exchange and is connected, and the outlet of cooler package is connected with the second import, and cooler package is used for the liquefied ammonia after being again cooled through interchanger heat exchange.
Further, cooler package comprises: air cooler, and the entrance of air cooler exports with the first heat exchange and is connected; First water cooler, the entrance of the first water cooler is connected with the outlet of air cooler, and the outlet of the first water cooler is connected with the second import.
Further, ammonia separation portion also comprises: refrigeration cycle water lines, and refrigeration cycle water lines to be arranged in ammonia distillation tower and to be positioned at the top of ammonia distillation tower, and the gaseous ammonia in ammonia distillation tower is exported by distillation tower and exports after the cooling of refrigeration cycle water lines.
Further, ammonia separation portion also comprises: the second water cooler, and the entrance of the second water cooler exports with distillation tower and is connected, and the outlet of the second water cooler is connected with the first interface of ammonia reservoir.
Further, ammonia reservoir comprises the first liquid ammonia storage tank and the second liquid ammonia storage tank that are arranged in series, and the first interface of the first liquid ammonia storage tank is connected with the outlet of the second water cooler, and the second interface of the second liquid ammonia storage tank is connected with desulfurization portion.
Further, ammonia recovery system also comprises oil trap, and oil trap is connected to collect the oil in the second liquid ammonia storage tank with the second liquid ammonia storage tank.
Further, desulfurization portion comprises: ammonia refining tank, and the entrance of ammonia refining tank is rich ammonia gas input terminus; Ammonia crystallization assembly, the entrance of ammonia crystallization assembly is connected with the outlet of ammonia refining tank; Ammonia refining assembly, the entrance of ammonia refining assembly is connected with the outlet of ammonia crystallization assembly, and the outlet of ammonia refining assembly is rich ammonia gas output terminal.
Further, ammonia crystallization assembly comprises the first ammonia crystallizer and the second ammonia crystallizer that are arranged in parallel, first ammonia crystallizer is all connected with the outlet of ammonia refining tank with the entrance of the second ammonia crystallizer, and the first ammonia crystallizer is all connected with the entrance of ammonia refining assembly with the outlet of the second ammonia crystallizer.
Further, ammonia refining assembly comprises the first ammonia refining device and the second ammonia refining device that are arranged in series, and the first ammonia refining device is connected with the outlet of ammonia crystallization assembly, and the second ammonia refining device is connected with the first import of gas ammonia-ammoniacal liquor mixing tank.
According to a further aspect in the invention, provide a kind of ammonia recovery method, ammonia recovery method comprises the following steps: desulfurized step: the rich ammonia gas of input is carried out desulfurization process, and exports the rich ammonia gas after sulfur-containing impurities and desulfurization process respectively; Mixing step: the rich ammonia gas of carrying out after desulfurized step and ammoniacal liquor are carried out mixing to obtain gaseous ammonia-ammonia water mixture; Separation of ammonia step: gaseous ammonia-ammonia water mixture that desulfurized step exports is carried out ammonia separation operation, to isolate liquefied ammonia product; Storage ammonia step: isolated liquefied ammonia product is stored, exports simultaneously and apply liquefied ammonia product and carry out.
Further, in desulfurized step, control the temperature of rich ammonia gas in the temperature range of setting.
Further, in separation of ammonia step process, ammonia recovery method also comprises: heating steps: the rich ammonia gas after desulfurization is heated to the ammonia vaporization making to be dissolved in rich ammonia gas; Cooling ammonolysis product step: the ammonia after vaporization is cooled, turns to liquefied ammonia product to make the ammoniacal liquor after vaporization.
Further, in storage ammonia step process, ammonia recovery method also comprises: oil-collecting step: collect the oil in liquefied ammonia product, to reduce the oleaginousness of liquefied ammonia product.
Apply technical scheme of the present invention, this ammonia recovery system comprises desulfurization portion, ammonia absorbs mixing unit, ammonia separation portion and ammonia reservoir, wherein, ammonia absorbs mixing unit and comprises gas ammonia-ammoniacal liquor mixing tank, ammonia separation portion comprises ammonia distillation tower, sulfur-containing impurities in rich ammonia gas removes by application desulfurization portion, then gas ammonia-ammoniacal liquor mixing tank is utilized rich ammonia gas fully to be mixed with ammoniacal liquor, then ammonia distillation tower is utilized all to be separated by the ammonia in ammonia, thus production fluid ammonolysis product, and, the heat that applying external steam in ammonia distillation tower provides carries out ammonia distillation to rich ammonia gas and the mixed strong aqua of ammoniacal liquor, thus save the energy consumption of separation of ammonia, to reduce the cost of recovery ammonia.
Accompanying drawing explanation
The Figure of description forming a application's part is used to provide a further understanding of the present invention, and schematic description and description of the present invention, for explaining the present invention, does not form inappropriate limitation of the present invention.In the accompanying drawings:
Fig. 1 shows the structural representation of the embodiment according to ammonia recovery system of the present invention.
Wherein, above-mentioned accompanying drawing comprises the following drawings mark:
10, desulfurization portion; 11, ammonia refining tank;
12, ammonia crystallization assembly; 13, ammonia refining assembly;
121, the first ammonia crystallizer; 122, the second ammonia crystallizer;
131, the first ammonia refining device; 132, the second ammonia refining device;
20, ammonia separation portion; 21, gas ammonia-ammoniacal liquor mixing tank;
22, ammonia absorber; 23, ammonia distillation tower;
24, ammoniacal liquor water cooler; 25, bottom reboiler;
26, interchanger; 27, cooler package;
271, air cooler; 272, the first water cooler;
28, refrigeration cycle water lines; 29, the second water cooler;
30, ammonia reservoir; 31, the first liquid ammonia storage tank;
32, the second liquid ammonia storage tank; 60, oil trap.
Embodiment
It should be noted that, when not conflicting, the embodiment in the application and the feature in embodiment can combine mutually.Below with reference to the accompanying drawings and describe the present invention in detail in conjunction with the embodiments.
As shown in Figure 1, according to an aspect of the present invention, a kind of ammonia recovery system is present embodiments provided.This ammonia recovery system comprises desulfurization portion 10, ammonia absorbs mixing unit, ammonia separation portion 20 and ammonia reservoir 30, and desulfurization portion 10 has rich ammonia gas input terminus and rich ammonia gas output terminal, and rich ammonia gas input terminus is for introducing rich ammonia gas.Wherein, ammonia absorbs mixing unit and comprises gas ammonia-ammoniacal liquor mixing tank 21, ammonia absorber 22, ammonia separation portion 20 comprises ammonia distillation tower 23, gas ammonia-ammoniacal liquor mixing tank 21 has the first import and outlet, first import is connected with rich ammonia gas output terminal, and ammonia absorber 22 has the first absorption mouth and the first delivery port, and first absorbs mouth is communicated to outlet, ammonia distillation tower 23 has distillation tower entrance and distillation tower exports, and distillation tower entrance is communicated to the first delivery port.The first interface of ammonia reservoir 30 is communicated to distillation tower outlet; Wherein, the second interface of ammonia reservoir 30 is communicated with to supplement liquefied ammonia to rich ammonia gas with desulfurization portion 10.
This ammonia recovery system application desulfurization portion is by sulfur-containing impurities (the mainly H in rich ammonia gas
2s) remove, when rich ammonia gas be transfused in desulfurization portion with supplement liquefied ammonia mix after, liquefied ammonia is due to volatilization heat absorption, temperature decrease in desulfurization portion, thus the sulfur-containing impurities in rich ammonia gas is separated out and precipitates, again sulfur-containing impurities and the rich ammonia gas after desulfurization process are exported respectively, then gas ammonia-ammoniacal liquor mixing tank is utilized rich ammonia gas fully to be mixed with ammoniacal liquor, then ammonia absorber is utilized rich ammonia gas to be mixed further with ammoniacal liquor, then utilize ammonia distillation tower to carry out distillation to mixed strong aqua and obtain gaseous ammonia, the ammonia of gas phase and ammoniacal liquor can mix by wherein gas ammonia-ammoniacal liquor mixing tank effectively, make ammonia can enter ammonia absorber and ammonia distillation tower substantially in liquid form to carry out fractionation by distillation to ammonia, thus production fluid ammonolysis product, and, the heat that applying external steam in ammonia distillation tower provides carries out ammonia distillation to strong aqua, thus save the energy consumption of separation of ammonia, to reduce the cost of recovery ammonia.
Particularly, desulfurization portion 10 comprises ammonia refining tank 11, ammonia crystallization assembly 12 and ammonia refining assembly 13, the entrance of the ammonia refining tank 11 of the present embodiment is rich ammonia gas input terminus, the entrance of ammonia crystallization assembly 12 is connected with the outlet of ammonia refining tank 11, the entrance of ammonia refining assembly 13 is connected with the outlet of ammonia crystallization assembly 12, the outlet of ammonia refining assembly 13 is gaseous ammonia output terminal, and this gaseous ammonia output terminal is communicated with gas ammonia-ammoniacal liquor mixing tank 21.Rich ammonia gas enters in ammonia refining tank 11 and removes H for the first time
2the operation of S, and after separate sulphur impurity, sulfur-containing impurities can be separated out and is deposited in the bottom of ammonia refining tank 11, and the sulfur-containing impurities pumping bottom ammonia refining tank 11 is gone out by pump by staff.
Rich ammonia gas is after ammonia refining tank 11, and then the operation that ammonia crystallization assembly 12 further removes sulfur-containing impurities is entered, in the present embodiment, ammonia crystallization assembly 12 comprises the first ammonia crystallizer 121 and the second ammonia crystallizer 122 be arranged in parallel, first ammonia crystallizer 121 is all connected with the outlet of ammonia refining tank 11 with the entrance of the second ammonia crystallizer 122, and the first ammonia crystallizer 121 is all connected with the entrance of ammonia refining assembly 13 with the outlet of the second ammonia crystallizer 122.The the first ammonia crystallizer 121 be arranged in parallel and the second ammonia crystallizer 122 can improve the processing power of ammonia crystallization assembly 12 pairs of sulfur-containing impurities, sulfur-containing impurities major part in this desulfurized step is removed, then sulfur-containing impurities is deposited in the bottom of the first ammonia crystallizer 121 and the second ammonia crystallizer 122, transfer line is utilized to carry the delivery conduit of sulfur-containing impurities to be communicated with the bottom of ammonia refining tank 11 first ammonia crystallizer 121 and the bottom of the second ammonia crystallizer 122 again, thus realize ammonia refining tank 11, sulfur-containing impurities in first ammonia crystallizer 121 and the second ammonia crystallizer 122 is discharged by same pipeline.
As shown in Figure 1, ammonia refining assembly 13 comprises the first ammonia refining device 131 and the second ammonia refining device 132 be arranged in series, first ammonia refining device 131 is connected with the outlet of ammonia crystallization assembly 12, and the second ammonia refining device 132 is connected with the first import of gas ammonia-ammoniacal liquor mixing tank 21.After ammonia refining assembly 13 receives the rich ammonia gas exported from ammonia crystallization assembly 12, carry out the manufacturing operation of gas ammonia, first ammonia refining device 131 is for manufacturing thick ammonia, second ammonia refining device 132 is for manufacturing smart ammonia, in the first ammonia refining device 131 and the second ammonia refining device 132, solid-state sulfur-containing impurities sorbent material is installed, when rich ammonia gas flows through ammonia refining assembly 13, sulfur-containing impurities is adsorbed to fall.Also H will be remained simultaneously
2s separates from rich ammonia gas, then the gas ammonia of formation and rich ammonia gas are carried to gas ammonia-ammoniacal liquor mixing tank 21, after rich ammonia gas and the above-mentioned remaining sulfur-containing impurities separated enter ammonia absorber 22, this part sulfur-containing impurities is exported from the top of ammonia absorber 22 by the equipment of transfer line process sulfur-containing impurities externally.
In the present embodiment, ammonia separation portion 20 also comprises ammoniacal liquor water cooler 24.When sulfur-containing impurities removes through desulfurization portion 10 by rich ammonia gas, and after gaseous ammonia and ammoniacal liquor effectively mixes in gas ammonia-ammoniacal liquor mixing tank 21, the ammonia in rich ammonia gas again can be absorbed entering ammoniacal liquor in ammonia absorber 22 in order to make rich ammonia gas, therefore, ammoniacal liquor water cooler 24 has cooling import and coolant outlet, cooling import is connected with outlet, and coolant outlet and first absorbs mouth and is connected, and utilizes ammoniacal liquor water cooler 24 to carry out cooling to rich ammonia gas and ammoniacal liquor and processes.
As shown in Figure 1, ammonia separation portion 20 also comprises bottom reboiler 25.In the lower position of ammonia distillation tower 23, bottom reboiler 25 is set, the entrance of this bottom reboiler 25 is connected with the sidewall interface bottom it of ammonia distillation tower 23, the outlet of bottom reboiler 25 is connected with the bottom interface of ammonia distillation tower 23, and, the steam that this bottom reboiler 25 utilizes plant pipe network to provide distills for the strong aqua in ammonia distillation tower 23 as thermal source, makes the ammonia in strong aqua overflow with the form of gas phase and rise to the top of ammonia distillation tower 23.In order to Heating temperature and its flow of bottom reboiler 25 can be known clearly, thus thermometer and under meter be installed on bottom reboiler 25 to detect temperature and the flow of steam, and detect Heating temperature.The effect of carrying out ammonia distillation is entered in ammonia distillation tower 23 in order to improve strong aqua further, therefore, ammonia separation portion 20 also comprises interchanger 26, interchanger 26 is utilized to carry out pre-heating temperature elevation process to the strong aqua entered in ammonia distillation tower 23, interchanger 26 has the first heat exchange entrance of being interconnected and the first heat exchange outlet and the second heat exchange entrance be interconnected and the second heat exchange and exports, wherein, gas ammonia-ammoniacal liquor mixing tank 21 also has the second import, first heat exchange entrance is connected with the bottom interface of ammonia distillation tower 23, after such strong aqua is distilled out vapor phase ammonia in ammonia distillation tower 23, light ammoniacal liquor is positioned at the bottom of ammonia distillation tower 23 tower, bottom reboiler 25 is by after the light ammoniacal liquor heating bottom ammonia distillation tower 23, part circulation is flowed back in ammonia distillation tower 23, a part flows to interchanger 26, first heat exchange outlet to the second import, second heat exchange entrance is connected with the first delivery port, second heat exchange outlet is connected with distillation tower entrance, like this, the light ammoniacal liquor flowing to interchanger 26 and the strong aqua exported from ammonia absorber 22 carry out heat exchange, and this part flows to gas ammonia-ammoniacal liquor mixing tank 21 from the light ammoniacal liquor that bottom reboiler 25 is diverted in interchanger 26 and effectively mixes with rich ammonia gas, thus realize mixing of ammoniacal liquor and rich ammonia gas, namely ammoniacal liquor first time in gas ammonia-ammoniacal liquor mixing tank 21 absorbs rich ammonia gas.
Preferably, in order to not affect the mixed effect of gas ammonia-ammoniacal liquor mixing tank 21, the light ammoniacal liquor of this part to bottom reboiler 25 is shunted out is needed to lower the temperature, therefore, ammonia separation portion 20 also comprises cooler package 27, the entrance of cooler package 27 exports with the first heat exchange and is connected, and the outlet of cooler package 27 is connected with the second import, and cooler package 27 is for being again cooled through the light ammoniacal liquor after interchanger 26 heat exchange.
Particularly, cooler package 27 comprises air cooler 271 and the first water cooler 272, the entrance of air cooler 271 exports with the first heat exchange and is connected, and the entrance of the first water cooler 272 is connected with the outlet of air cooler 271, and the outlet of the first water cooler 272 is connected with the second import.In the present embodiment, by air cooler 271, the light ammoniacal liquor of this part is lowered the temperature for the first time, then after the cooling circulating water by constantly circulating in the first water cooler 272 is fully lowered the temperature to light ammoniacal liquor again, lighter ammoniacal liquor is supplemented in gas ammonia-ammoniacal liquor mixing tank 21.
As shown in Figure 1, after bottom reboiler 25 heats the ammoniacal liquor in ammonia distillation tower 23, ammonia is distilled out and rises to the tip position of ammonia distillation tower 23, the temperature of vapor phase ammonia is now higher, therefore, need to lower the temperature to this partial gas phase ammonia, middle follow-up this partial gas phase ammonia be converted into liquefied ammonia carry out storing or exporting, thus ammonia separation portion 20 also comprises refrigeration cycle water lines 28, refrigeration cycle water lines 28 to be arranged in ammonia distillation tower 23 and to be positioned at the top of ammonia distillation tower 23, gas ammonia in ammonia distillation tower 23 is exported by distillation tower and exports after refrigeration cycle water lines 28 is lowered the temperature.Circulation conveying water coolant in refrigeration cycle water lines 28, makes water coolant ammonia distillation tower 23 in and vapor phase ammonia carries out heat exchange to export backward after the temperature reducing this partial gas phase ammonia.
In the present embodiment, store to ammonia reservoir 30 conveying after obtaining liquefied ammonia to be cooled further by the vapor phase ammonia exported after distillation, therefore, this ammonia separation portion 20 also comprises the second water cooler 29, the entrance of the second water cooler 29 exports with distillation tower and is connected, and the outlet of the second water cooler 29 is connected with the first interface of ammonia reservoir 30.By the conveying water coolant that constantly circulates in the second water cooler 29 again to reduce the temperature of the vapor phase ammonia exported from ammonia distillation tower 23, thus obtain liquefied ammonia.
As shown in Figure 1, the first interface that ammonia reservoir 30 comprises the first liquid ammonia storage tank 31 and the second liquid ammonia storage tank 32, first liquid ammonia storage tank 31 be arranged in series is connected with the outlet of the second water cooler 29.When liquefied ammonia is transported to the first liquid ammonia storage tank 31, the first liquid ammonia storage tank 31 pairs of liquefied ammonia are utilized to carry out buffering flowing, make the flows decrease of liquefied ammonia in the first liquid ammonia storage tank 31, thus the oil being conducive to containing in liquefied ammonia is separated out, then liquefied ammonia is being delivered in the second liquid ammonia storage tank 32 operation of carrying out collecting oil.Therefore, ammonia recovery system also comprises oil trap 60, and oil trap 60 is communicated with to collect the oil in the second liquid ammonia storage tank 32 with the second liquid ammonia storage tank 32.Further, second interface of the second liquid ammonia storage tank 32 is communicated with desulfurization portion 10, and the second interface of the second liquid ammonia storage tank 32 forms two branch roads, Article 1, branch road is communicated with the rich ammonia gas input terminus introducing rich ammonia gas in ammonia refining tank 11, at ammonia refining tank 11, in first ammonia crystallizer 121 and the second ammonia crystallizer 122, volatilization in ammoniacal liquor is absorbed heat and makes ammonia refining tank 11, temperature decrease in first ammonia crystallizer 121 and the second ammonia crystallizer 122, be approximately 0 degrees centigrade, from but sulfur-containing impurities separate out low temperature and be deposited at the bottom of tank, then export, Article 2 branch road is communicated with ammonia crystallization assembly 12.
Certainly, the liquefied ammonia that the second water cooler 29 exports also directly can be delivered to the second liquid ammonia storage tank 32 and store, and is namely directly communicated with by a pipeline between the second water cooler 29 with the second liquid ammonia storage tank 32.
According to a further aspect in the invention, a kind of ammonia recovery method is provided.This ammonia recovery method comprises the following steps:
Desulfurized step: the rich ammonia gas of input is carried out desulfurization process, and export the rich ammonia gas after sulfur-containing impurities and desulfurization process respectively;
Separation of ammonia step: gaseous ammonia-ammonia water mixture that desulfurized step exports is carried out ammonia separation operation, to isolate liquefied ammonia product;
Storage ammonia step: isolated liquefied ammonia product is stored, exports simultaneously and apply liquefied ammonia product and carry out.
Particularly, in desulfurized step, control the temperature of rich ammonia gas and (this temperature is set in 0 degrees centigrade, in order to be separated out by sulfur-containing impurities better, preferably this temperature be remained on less than 0 degree Celsius) in the temperature range of setting.
After desulfurized step before separation of ammonia step, this ammonia recovery method also comprises gaseous ammonia and ammoniacal liquor mixing step, rich ammonia gas fully to be mixed with ammoniacal liquor, then ammonolysis product is isolated to mixed strong aqua (i.e. gaseous ammonia-ammonia water mixture).
In the present embodiment, in separation of ammonia step process, ammonia recovery method also comprises: heating steps and cold deammoniation product step.Wherein, heating steps: heat the ammonia be dissolved in ammoniacal liquor is evaporated to the rich ammonia gas after desulfurization; Cooling ammonolysis product step: the ammonia after vaporization is cooled, turns to liquefied ammonia product to make the ammoniacal liquor after vaporization.
In storage ammonia step process, ammonia recovery method also comprises oil-collecting step: collect the oil in liquefied ammonia product, to reduce the oleaginousness of liquefied ammonia product.
Explain and illustrate: as shown in fig. 1, in figure, symbol T represents temperature, and namely T represents the thermometer being provided with detected temperatures herein; In figure, symbol F represents flow, and namely F represents the under meter being provided with and detecting flow herein; In figure, symbol P represents pressure, and namely P represents the tensimeter being provided with detecting pressure herein; In figure, symbol L represents liquid level, and namely L represents the liquidometer being provided with and detecting liquid level herein.By thermometer, under meter, tensimeter and liquidometer, corresponding temperature, flow, pressure and liquid level is everywhere monitored.
The foregoing is only the preferred embodiments of the present invention, be not limited to the present invention, for a person skilled in the art, the present invention can have various modifications and variations.Within the spirit and principles in the present invention all, any amendment done, equivalent replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (18)
1. an ammonia recovery system, is characterized in that, comprising:
Desulfurization portion (10), described desulfurization portion (10) has rich ammonia gas input terminus and rich ammonia gas output terminal, and described rich ammonia gas input terminus is for introducing rich ammonia gas;
Ammonia absorbs mixing unit, and described ammonia absorbs mixing unit and comprises gas ammonia-ammoniacal liquor mixing tank (21), and described gas ammonia-ammoniacal liquor mixing tank (21) has the first import and outlet, and described first import is connected with described rich ammonia gas output terminal;
Ammonia separation portion (20), described ammonia separation portion (20) comprises ammonia distillation tower (23), and described ammonia distillation tower (23) has distillation tower entrance and distillation tower exports, and described distillation tower entrance is communicated to described outlet;
Described ammonia recovery system also comprises: ammonia reservoir (30), and the first interface of described ammonia reservoir (30) is communicated to the outlet of described distillation tower; Wherein, the second interface of described ammonia reservoir (30) is communicated with to supplement liquefied ammonia to described rich ammonia gas with described desulfurization portion (10).
2. ammonia recovery system according to claim 1, it is characterized in that, described ammonia absorbs mixing unit and also comprises: ammonia absorber (22), described ammonia absorber (22) has the first absorption mouth and the first delivery port, described first absorbs mouth is communicated to described outlet, and described first delivery port is communicated to described distillation tower entrance.
3. ammonia recovery system according to claim 2, is characterized in that, described ammonia recovery system also comprises:
Ammoniacal liquor water cooler (24), described ammoniacal liquor water cooler (24) has cooling import and coolant outlet, and described cooling import is connected with described outlet, and described coolant outlet and described first absorbs mouth and is connected.
4. ammonia recovery system according to claim 2, is characterized in that, described ammonia separation portion (20) also comprises:
Bottom reboiler (25), the entrance of described bottom reboiler (25) is connected with the sidewall interface bottom it of described ammonia distillation tower (23), and the outlet of described bottom reboiler (25) is connected with the bottom interface of described ammonia distillation tower (23).
5. ammonia recovery system according to claim 4, is characterized in that, described ammonia separation portion (20) also comprises:
Interchanger (26), described interchanger (26) has the first heat exchange entrance of being interconnected and the first heat exchange outlet and the second heat exchange entrance be interconnected and the second heat exchange and exports, wherein, described gas ammonia-ammoniacal liquor mixing tank (21) also has the second import, described first heat exchange entrance is connected with the bottom interface of described ammonia distillation tower (23), described first heat exchange outlet is to described second import, described second heat exchange entrance is connected with described first delivery port, and described second heat exchange outlet is connected with described distillation tower entrance.
6. ammonia recovery system according to claim 5, is characterized in that, described ammonia recovery system also comprises:
Cooler package (27), the entrance of described cooler package (27) exports with described first heat exchange and is connected, the outlet of described cooler package (27) is connected with described second import, and described cooler package (27) is for being again cooled through the liquefied ammonia after described interchanger (26) heat exchange.
7. ammonia recovery system according to claim 6, is characterized in that, described cooler package (27) comprising:
Air cooler (271), the entrance of described air cooler (271) exports with described first heat exchange and is connected;
First water cooler (272), the entrance of described first water cooler (272) is connected with the outlet of described air cooler (271), and the outlet of described first water cooler (272) is connected with described second import.
8. ammonia recovery system according to claim 5, is characterized in that, described ammonia separation portion (20) also comprises:
Refrigeration cycle water lines (28), described refrigeration cycle water lines (28) to be arranged in described ammonia distillation tower (23) and to be positioned at the top of described ammonia distillation tower (23), and the gaseous ammonia in described ammonia distillation tower (23) is exported by described distillation tower and exports after described refrigeration cycle water lines (28) cooling.
9. ammonia recovery system according to claim 8, it is characterized in that, described ammonia separation portion (20) also comprises:
Second water cooler (29), the entrance of described second water cooler (29) exports with described distillation tower and is connected, and the outlet of described second water cooler (29) is connected with the first interface of described ammonia reservoir (30).
10. ammonia recovery system according to claim 9, it is characterized in that, described ammonia reservoir (30) comprises the first liquid ammonia storage tank (31) and the second liquid ammonia storage tank (32) that are arranged in series, the described first interface of described first liquid ammonia storage tank (31) is connected with the outlet of described second water cooler (29), and described second interface of described second liquid ammonia storage tank (32) is connected with described desulfurization portion (10).
11. ammonia recovery systems according to claim 10, it is characterized in that, described ammonia recovery system also comprises oil trap (60), and described oil trap (60) is connected to collect the oil in described second liquid ammonia storage tank (32) with described second liquid ammonia storage tank (32).
12. ammonia recovery systems according to claim 1, it is characterized in that, described desulfurization portion (10) comprising:
Ammonia refining tank (11), the entrance of described ammonia refining tank (11) is described rich ammonia gas input terminus;
Ammonia crystallization assembly (12), the entrance of described ammonia crystallization assembly (12) is connected with the outlet of described ammonia refining tank (11);
Ammonia refining assembly (13), the entrance of described ammonia refining assembly (13) is connected with the outlet of described ammonia crystallization assembly (12), and the outlet of described ammonia refining assembly (13) is described rich ammonia gas output terminal.
13. ammonia recovery systems according to claim 12, it is characterized in that, described ammonia crystallization assembly (12) comprises the first ammonia crystallizer (121) and the second ammonia crystallizer (122) that are arranged in parallel, described first ammonia crystallizer (121) is all connected with the outlet of described ammonia refining tank (11) with the entrance of described second ammonia crystallizer (122), and described first ammonia crystallizer (121) is all connected with the entrance of described ammonia refining assembly (13) with the outlet of described second ammonia crystallizer (122).
14. ammonia recovery systems according to claim 12, it is characterized in that, described ammonia refining assembly (13) comprises the first ammonia refining device (131) and the second ammonia refining device (132) that are arranged in series, described first ammonia refining device (131) is connected with the outlet of described ammonia crystallization assembly (12), and described second ammonia refining device (132) is connected with the first import of described gas ammonia-ammoniacal liquor mixing tank (21).
15. 1 kinds of ammonia recovery methods, is characterized in that, described ammonia recovery method comprises the following steps:
Desulfurized step: the rich ammonia gas of input is carried out desulfurization process, and export the rich ammonia gas after sulfur-containing impurities and desulfurization process respectively;
Mixing step: the rich ammonia gas of carrying out after described desulfurized step and ammoniacal liquor are carried out mixing to obtain gaseous ammonia-ammonia water mixture;
Separation of ammonia step: described gaseous ammonia-ammonia water mixture is carried out ammonia separation operation, to isolate liquefied ammonia product;
Storage ammonia step: isolated described liquefied ammonia product is stored, exports simultaneously and apply described liquefied ammonia product and carry out.
16. ammonia recovery methods according to claim 15, is characterized in that, in described desulfurized step, control the temperature of described rich ammonia gas in the temperature range of setting.
17. ammonia recovery methods according to claim 15, is characterized in that, in described separation of ammonia step process, described ammonia recovery method also comprises:
Heating steps: the rich ammonia gas after desulfurization is heated to the ammonia vaporization making to be dissolved in described rich ammonia gas;
Cooling ammonolysis product step: the ammonia after vaporization is cooled, turns to described liquefied ammonia product to make the ammoniacal liquor after vaporization.
18. ammonia recovery methods according to claim 15, is characterized in that, in described storage ammonia step process, described ammonia recovery method also comprises:
Oil-collecting step: collect the oil in described liquefied ammonia product, to reduce the oleaginousness of described liquefied ammonia product.
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| CN106964174A (en) * | 2017-05-17 | 2017-07-21 | 万和昌 | Rectifying/the method for purification and system of ammonia |
| CN107235593A (en) * | 2017-07-03 | 2017-10-10 | 天津晟远环境有限公司 | The system and method that a kind of coal gasification water system recovery ammonia is removed with sulphur |
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| CN1657411A (en) * | 2005-02-17 | 2005-08-24 | 昆明理工大学 | Method for recoverying and utilization of pulluted ammonia water of brown coal pressurized gasification |
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