CN106185985B - The technique for being free of phosphate radical and sodium ion when phosphorus ammonium washes ammonia production anhydrous ammonia in ammonium hydroxide - Google Patents
The technique for being free of phosphate radical and sodium ion when phosphorus ammonium washes ammonia production anhydrous ammonia in ammonium hydroxide Download PDFInfo
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- CN106185985B CN106185985B CN201610532099.9A CN201610532099A CN106185985B CN 106185985 B CN106185985 B CN 106185985B CN 201610532099 A CN201610532099 A CN 201610532099A CN 106185985 B CN106185985 B CN 106185985B
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- ammonia
- ammonium hydroxide
- ammonium
- sodium ion
- desorber
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/10—Separation of ammonia from ammonia liquors, e.g. gas liquors
Abstract
The present invention provides the technique for being free of phosphate radical and sodium ion when a kind of phosphorus ammonium washes ammonia production anhydrous ammonia in ammonium hydroxide, 1~5 block of column plate or high 200~500mm fillers is arranged in the system without phosphate radical and sodium ion on desorber rich solution feed inlet in ammonium hydroxide when the phosphorus ammonium washes ammonia production anhydrous ammonia, first block of column plate of upper number or filler top are arranged flusher, first block of column plate or flusher import and are connected to one or more of the steam condensate (SC) outlet outside desorber heater steam condensation-water drain, rectifying column heater steam condensation-water drain and battery limit (BL) by pipeline；The system without phosphate radical and sodium ion further includes mixing channel in ammonium hydroxide when phosphorus ammonium washes ammonia production anhydrous ammonia, it is provided with alkali liquor inlet and ammonia inlet on the mixing channel, the ammonia inlet and ammonium hydroxide feeder trough outlet, mixing channel outlet is connected to rectifying column, it is described be derived from mixing channel without sodium ion ammonium hydroxide before.The system can be effectively reduced the consumption of raw material phosphoric acid, and ammonium hydroxide is directly used.
Description
Technical field
The present invention relates to be free of sodium ion technology more particularly to one in phosphate radical entrainment and ammonium hydroxide when removing anhydrous ammonia desorption
The technique for being free of phosphate radical and sodium ion when kind phosphorus ammonium washes ammonia production anhydrous ammonia in ammonium hydroxide.
Background technology
It is with the ammonia in phosphorus ammonium barren liquor washing absorption ammonia-containing gas, generation phosphorus ammonium richness that phosphorus ammonium, which washes ammonia and produces anhydrous ammonia process,
Liquid.Phosphorus ammonium pregnant liquor is by desorption, and regenerated phosphorus ammonium barren liquor returns to absorption cycle and uses, while ammonia is desorbed in the form of ammonia vapour
Come, then ammonium hydroxide is obtained through cooling, ammonium hydroxide adds rectifying after alkali, obtains anhydrous ammonia product.Ammonia carries phosphate radical secretly when due to desorption, with
And lye is directly added into ammonium hydroxide feeder trough so that ammonium hydroxide contains phosphate radical and sodium ion before rectifying.Patent of invention " inhale by phosphorus ammonium
Receipts method production anhydrous ammonia method " (patent No. ZL 2,009 1 0068522.4), which does not propose how to obtain, is free of phosphate radical and sodium
The ammonium hydroxide of ion.
Ammonia vapour carries phosphate radical secretly so that phosphoric acid consumption increases.Contain sodium ion in ammonium hydroxide, for flue gas ammonia method desulfurizing
When, cause sulphur ammonium to be difficult to crystallize；Ammonia process of desulfurization ammonium hydroxide is only prepared by anhydrous ammonia and desalted water mixing at this time, the latter makes
It obtains energy consumption of rectification increase and water consumption increases.
Invention content
It is an object of the present invention to which there are phosphate radicals and sodium in ammonium hydroxide when washing ammonia production anhydrous ammonia for above-mentioned conventional phosphorus ammonium
The problem of ion, it is proposed that the system for being free of phosphate radical and sodium ion when a kind of phosphorus ammonium washes ammonia production anhydrous ammonia in ammonium hydroxide, this is
System can be effectively reduced the consumption of raw material phosphoric acid, and ammonium hydroxide is directly used.
To achieve the above object, the technical solution adopted by the present invention is：When a kind of phosphorus ammonium washes ammonia production anhydrous ammonia in ammonium hydroxide
System without phosphate radical and sodium ion is arranged 1~5 block of column plate on desorber rich solution feed inlet or high 200~500mm is filled out
Flusher is arranged in material, first block of column plate of upper number or filler top, and first block of column plate or flusher import pass through pipeline
Go out with the steam condensate (SC) outside desorber heater steam condensation-water drain, rectifying column heater steam condensation-water drain and battery limit (BL)
The connection of one or more of mouth；
The system without phosphate radical and sodium ion further includes mixing channel in ammonium hydroxide when phosphorus ammonium washes ammonia production anhydrous ammonia, described mixed
It closes and is provided with alkali liquor inlet and ammonia inlet on slot, the ammonia inlet and ammonium hydroxide feeder trough outlet, the mixing channel go out
Mouthful be connected to rectifying column, it is described be derived from mixing channel without sodium ion ammonium hydroxide before.
Another object of the present invention additionally provide when a kind of phosphorus ammonium washes ammonia production anhydrous ammonia in ammonium hydroxide without phosphate radical and
Sodium ion technique, includes the following steps：
Steam condensate (SC) is introduced to first block of column plate of upper number or filler top flusher, the steam condensate (SC) of decline with
The ammonia vapour risen from feed inlet carries out step by step tray heat and mass, and is less than or equal to 10g/m what is carried secretly in ammonia vapour3Phosphoric acid is eradicated
Go, i.e., on upward first block of column plate of number or filler top flusher be introduced into steam condensate (SC) can effectively solve desorption ammonia vapour in phosphorus
The entrainment of acid group；
After lye and being mixed in mixing channel without sodium ion ammonium hydroxide in ammonium hydroxide feeder trough, pass through rectifying column feed pump
It is delivered in rectifying column, i.e., can obtain the ammonium hydroxide without sodium ion before mixing channel.
Further, the steam condensate (SC) comes from：Desorber heater steam condensation-water drain, rectifying column heater
Steam condensate (SC) exports one or more in being exported with the steam condensate (SC) outside battery limit (BL).The i.e. described steam condensate (SC) comes from solution
Inhale tower heater steam condensation-water drain；Or rectifying column heater steam condensation-water drain；Or the steam condensate (SC) outside battery limit (BL) goes out
Mouthful；Or desorber heater steam condensation-water drain and rectifying column heater steam condensation-water drain；Or desorber heater steams
Steam condensate (SC) outlet outside vapour condensation-water drain and battery limit (BL)；Or the steaming outside rectifying column heater steam condensation-water drain and battery limit (BL)
Vapour condensation-water drain；Or the steaming outside desorber heater steam condensation-water drain, rectifying column heater condensation-water drain and battery limit (BL)
Vapour condensation-water drain.
Further, the steam condensate (SC) introduction volume is to desorb 5~50wt% of ammonia vol, preferably 20~
40wt%.
System in ammonium hydroxide without phosphate radical and sodium ion and simple for process, conjunction when phosphorus ammonium of the present invention washes ammonia production anhydrous ammonia
Reason, craft science, effect is good, is had the following advantages compared with current art.
In conventional anhydrous ammonia process, phosphate radical is entrained out with desorption ammonia vapour, and is stayed in ammonium hydroxide；It is free of
The ammonium hydroxide of phosphate radical and sodium ion, it is necessary to which the anhydrous ammonia obtained with rectifying is prepared with desalted water；This allows for the phosphorus that phosphorus ammonium washes ammonia
Acid consumption increases, energy consumption of rectification increases, water consumption increases.
The system of phosphate radical and sodium ion is free of in desorber rich solution in ammonium hydroxide when phosphorus ammonium of the present invention washes ammonia production anhydrous ammonia
1~5 block of column plate or high 200~500mm fillers, first block of column plate of upper number or filler top setting sprinkling dress are set on feed inlet
It sets, appropriate steam condensate (SC) is added in first block of column plate or flusher import, removes desorption phosphate radical entrainment.Phosphorus of the present invention
The system without phosphate radical and sodium ion also sets up and is mixed there are one ammonium hydroxide and lye in ammonium hydroxide when ammonium washes ammonia production anhydrous ammonia
Mixing channel, without sodium ion ammonium hydroxide be derived from mixing channel system and technique.
To sum up, the system and technique of phosphate radical and sodium ion are free of when phosphorus ammonium of the present invention washes ammonia production anhydrous ammonia in ammonium hydroxide,
The ammonium hydroxide without phosphate radical and sodium ion is directly obtained, phosphoric acid consumption and energy consumption of rectification and water consumption are reduced.
Description of the drawings
Fig. 1 is to connect to show with the system of sodium ion without phosphate radical in ammonium hydroxide when 1 phosphorus ammonium of embodiment washes ammonia production anhydrous ammonia
It is intended to；
Fig. 2 is to connect to show with the system of sodium ion without phosphate radical in ammonium hydroxide when 2 phosphorus ammonium of embodiment washes ammonia production anhydrous ammonia
It is intended to；
Fig. 3 is to connect to show with the system of sodium ion without phosphate radical in ammonium hydroxide when 3 phosphorus ammonium of embodiment washes ammonia production anhydrous ammonia
It is intended to；
Fig. 4 is to connect to show with the system of sodium ion without phosphate radical in ammonium hydroxide when 4 phosphorus ammonium of embodiment washes ammonia production anhydrous ammonia
It is intended to.
Wherein reference numeral is respectively：
1- ammonia absorbers；2- desorbers；3- rectifying columns；4- ammonia absorber circulating pumps；5- poor rich liquid heat exchangers；6- depicklings
Device；7- desorber feed pumps；8- desorbers cooler (on)；9- desorbers but device (under)；10- desorber heaters；11- ammonium hydroxide
Feeder trough；12- mixing channels；13- rectifying column feed pumps；14- rectifying column condensers；15- return tanks；16- products and reflux pump；
17- rectifying column heaters；18- lean solution coolers；First block of column plate of 19-；20- fillers.
Specific implementation mode
The invention discloses a kind of phosphorus ammoniums to wash the system for being free of phosphate radical and sodium ion when ammonia produces anhydrous ammonia in ammonium hydroxide, packet
It includes and 1~5 block of column plate or high 200~500mm fillers is set on desorber rich solution feed inlet, in first block of column plate of upper number or filler
Flusher is arranged in top, and appropriate steam condensate (SC) is added in first block of column plate or flusher, removes desorption phosphate radical folder
Band.I.e. described first block of column plate 19 of upper number or 20 top flusher import of filler are condensed with desorber heater outlet steam
Waterpipe connection or described first block of column plate 19 of upper number or 20 top flusher import of filler and rectifying column heater outlet
Steam condensate (SC) pipeline connects；Or first block of column plate 19 of the upper number or 20 top flusher import of filler are steamed with outside battery limit (BL)
Vapour condensing water conduit connects；Or first block of column plate 19 of the upper number or 20 top flusher import of filler are heated with desorber
Device outlet is connected with rectifying column heater outlet steam condensate (SC) pipeline；Or on first block of column plate 19 of the upper number or filler 20
Portion's flusher import is heated steam condensate (SC) pipeline outside its outlet and battery limit (BL) with desorber heater outlet and rectifying column and is connect；
Or first block of column plate 19 of the upper number or 20 top flusher import of filler are steamed with outside desorber heater outlet and battery limit (BL)
Vapour condensing water conduit connects；Or first block of column plate 19 of the upper number or 20 top flusher import of filler are heated with rectifying column
Device outlet is connected with steam condensate (SC) pipeline outside battery limit (BL)；
The invention also includes the mixing channel that an ammonium hydroxide and lye mix, it is derived from before mixing channel without sodium ion ammonium hydroxide and is
System and technique.The mixing channel import is connected with the outlet of ammonium hydroxide feeder trough, and mixing channel outlet is connect with ammonium hydroxide feed pump, is mixed
Have on slot and adds alkali mouth, the no sodium ion ammonium hydroxide, the ammonium hydroxide being derived from before mixing channel import.
Ammonia is washed the invention also discloses a kind of phosphorus ammonium and produces anhydrous ammonia system, which washes ammonia using above-mentioned phosphorus ammonium and produce
The system and technique of phosphate radical and sodium ion are free of when anhydrous ammonia in ammonium hydroxide, which washes the connection figure that ammonia produces anhydrous ammonia system
As shown in Figure 1, including 1- ammonia absorbers；2- desorbers；3- rectifying columns；4- ammonia absorber circulating pumps；5- poor rich liquid heat exchangers；6-
Depickling device；7- desorber feed pumps；8- desorbers cooler (on)；9- desorbers but device (under)；10- desorber heaters；11-
Ammonium hydroxide feeder trough；12- mixing channels；13- rectifying column feed pumps；14- rectifying column condensers；15- return tanks；16- products and reflux
Pump；17- rectifying column heaters；18- lean solution coolers；First block of column plate of 19-；20- fillers.
Ammonia-containing gas enter 1 lower part of ammonia absorber outside battery limit (BL), rich with the cycle phosphorus ammonium of middle part sprinkling respectively in tower
Liquid and the phosphorus ammonium barren liquor of top sprinkling carry out counter current contacting.Gas leaves from 1 top of ammonia absorber outside battery limit (BL) after deamination.Ammonia is inhaled
The phosphorus ammonium pregnant liquor for receiving 1 bottom of tower is extracted out with ammonia absorber circulating pump 4, is largely sent to 1 middle part cycle sprinkling coal gas of ammonia absorber,
Small part rich solution is sent into poor rich liquid heat exchanger 5, enters depickling device 6 after exchanging heat with phosphorus ammonium barren liquor.
Phosphorus ammonium pregnant liquor flashes off sour gas in depickling device 6, and sour gas goes to 1 lower part of ammonia absorber.Phosphorus ammonium pregnant liquor is again
With desorber feed pump 7 pump to desorber cooler (on) 8, with ammonia vapour exchange heat after enter 2 rich solution feed inlet of desorber.
The ammonia vapour of the top of desorber 2 effusion respectively desorber cooler (on) 8 and desorption tower cooler device (under) in 9, heating
After phosphorus ammonium pregnant liquor and cooled water cooling, forms ammonium hydroxide and flow into ammonium hydroxide feeder trough 11.
Steam condensate (SC) is added in first block of column plate 19 of number on desorber, and steam condensate (SC) comes from 10 He of desorber heater
Rectifying column heater 17.
The phosphorus ammonium barren liquor for coming from 2 bottom of desorber is heated in desorber heater 10 using indirect steam.2 bottom of desorber
Phosphorus ammonium barren liquor, respectively in poor rich liquid heat exchanger 5 and lean solution cooler 18, after heating phosphorus ammonium pregnant liquor and cooled water cooling, into
Enter the sprinkling of 1 top of ammonia absorber.A 10 steam condensate (SC) part of desorber heater is sent into several first column plates 19 on desorber 2,
It is arranged outside remainder.
An ammonium hydroxide part in ammonium hydroxide feeder trough 11 is used as directly to be sent outside without phosphate radical and sodium ion ammonium hydroxide product, remaining
Part enters mixing channel 12, and lye is added in mixing channel 12.
Ammonium hydroxide rectifying column feed pump 13 in mixing channel 12 is pumped to rectifying column 3.Rectifying column 3 pushes up anhydrous ammonia gas in essence
Evaporating the water cooling that is cooled in tower condenser 14 becomes liquid anhydrous ammonia inflow return tank 15.In return tank 15 anhydrous ammonia product and
Reflux pump 16 is extracted out, is partly sent to rectifying column 3 and is pushed up as reflux, remainder is sent outside as product.
The waste water for coming from 3 bottom of rectifying column is heated in rectifying column heater 17 using indirect steam.3 bottom waste water of rectifying column
Outer row.A 17 steam condensate (SC) part of rectifying column heater is sent into first block of column plate 19 of number on desorber 2, is arranged outside remainder.
Above-mentioned first block of column plate 19 or 20 top flusher import of filler are condensed with 10 steam of desorber heater respectively
One or more of steam condensate (SC) outlet outside water out and the outlet of 17 steam condensate (SC) of rectifying column heater and battery limit (BL) is even
It is logical；11 ammonium hydroxide of the ammonium hydroxide feeder trough outlet is connect with 12 import of mixing channel, and mouth is added in 12 top of mixing channel, institute in the lye
It states the outlet of 12 ammonium hydroxide of mixing channel to connect with 13 import of ammonium hydroxide feed pump, the sodium ion ammonium hydroxide that is free of is in 11 ammonium hydroxide of ammonium hydroxide feeder trough
Outlet is taken out, and before 12 import of mixing channel.
The system and technique for being free of phosphate radical and sodium ion when phosphorus ammonium of the present invention washes ammonia production anhydrous ammonia in ammonium hydroxide, according to feelings
Condition is taken the cold condensed water of different steam and is applied in combination.When phosphorus ammonium of the present invention washes ammonia production anhydrous ammonia phosphate radical is free of in ammonium hydroxide
It can be widely used for the ammonia separation field of the unstripped gas containing ammonia with the system and technique of sodium ion.
The present invention is further described with reference to embodiments
Embodiment 1：
Present embodiment discloses a kind of phosphorus ammoniums to wash the system for being free of phosphate radical and sodium ion when ammonia produces anhydrous ammonia in ammonium hydroxide,
As shown in Figure 1, on desorber rich solution feed inlet be arranged 5 blocks of column plates, 19 import of above-mentioned first block of column plate by pipeline respectively with
10 steam condensate (SC) of desorber heater exports and 17 steam condensate (SC) outlet of rectifying column heater；
The system without phosphate radical and sodium ion further includes mixing channel 12 in ammonium hydroxide when phosphorus ammonium washes ammonia production anhydrous ammonia, described
Alkali liquor inlet and ammonia inlet, the ammonia inlet and 11 outlet of ammonium hydroxide feeder trough are provided on mixing channel 12, it is described mixed
Conjunction slot goes out 12 mouthfuls and is connected to rectifying column 3 by rectifying column feed pump 13.
The present embodiment combines Fig. 1 to the present embodiment phosphorus ammonium so that semi-coke coal gas washes ammonia production anhydrous ammonia using phosphorus ammonium as an example
The technique without phosphate radical and sodium ion illustrates in ammonium hydroxide when washing ammonia production anhydrous ammonia.
The ammon amount external from battery limit (BL) is less than or equal to 22g/m3Ammonia-containing gas enter 1 lower part of ammonia absorber, in tower point
Phosphorus ammonium barren liquor not with the cycle phosphorus ammonium pregnant liquor of middle part sprinkling and top sprinkling carries out counter current contacting.Gas ammonia content exists after deamination
100mg/m3Hereinafter, being left outside battery limit (BL) from 1 top of ammonia absorber.The phosphorus ammonium pregnant liquor of 1 bottom of ammonia absorber is followed with ammonia absorber
4 extraction of ring pump is largely sent to 1 middle part cycle sprinkling coal gas of ammonia absorber, and small part rich solution is sent into poor rich liquid heat exchanger 5, with
Enter depickling device 6 after phosphorus ammonium barren liquor heat exchange.
Phosphorus ammonium pregnant liquor flashes off sour gas in depickling device 6, and sour gas goes to 1 lower part of ammonia absorber.Phosphorus ammonium pregnant liquor is again
With desorber feed pump 7 pump to desorber cooler (on) 8, with ammonia vapour exchange heat after enter 2 rich solution feed inlet of desorber.
The ammonia vapour of the top of desorber 2 effusion respectively desorber cooler (on) 8 and desorption tower cooler device (under) in 9, heating
After phosphorus ammonium pregnant liquor and cooled water cooling, forms ammonium hydroxide and flow into ammonium hydroxide feeder trough 11.
The steam condensate (SC) for being equivalent to ammonia vol about 5%, the steam of decline is added on first block of column plate of number on desorber 2
Condensed water carries out step by step tray heat and mass with the ammonia vapour risen from feed inlet, is less than or equal to 8g/m what is carried secretly in ammonia vapour3Phosphoric acid
Elimination is gone.Steam condensate (SC) comes from desorber heater 10 and rectifying column heater 17.
The phosphorus ammonium barren liquor for coming from 2 bottom of desorber is heated in desorber heater 10 using indirect steam.2 bottom of desorber
Phosphorus ammonium barren liquor, respectively in poor rich liquid heat exchanger 5 and lean solution cooler 18, after heating phosphorus ammonium pregnant liquor and cooled water cooling, into
Enter the sprinkling of 1 top of ammonia absorber.A 10 steam condensate (SC) part of desorber heater is sent into first block of column plate of number on desorber 2
19。
An ammonium hydroxide part in ammonium hydroxide feeder trough 11 is used as directly to be sent outside without phosphate radical and sodium ion ammonium hydroxide product, remaining
Part enters mixing channel 12, and lye is added in mixing channel 12.
Ammonium hydroxide rectifying column feed pump 13 in mixing channel 12 is pumped to rectifying column 3.Rectifying column 3 pushes up anhydrous ammonia gas in essence
Evaporating the water cooling that is cooled in tower condenser 14 becomes liquid anhydrous ammonia inflow return tank 15.In return tank 15 anhydrous ammonia product and
Reflux pump 16 is extracted out, is partly sent to rectifying column 3 and is pushed up as reflux, remainder is sent outside as product.
The waste water for coming from 3 bottom of rectifying column is heated in rectifying column heater 17 using indirect steam.3 bottom waste water of rectifying column
Outer row.A 17 steam condensate (SC) part of rectifying column heater is sent into first block of column plate 19 of number on desorber 2, is arranged outside remainder.
Embodiment 2：
Present embodiment discloses a kind of phosphorus ammoniums to wash the system for being free of phosphate radical and sodium ion when ammonia produces anhydrous ammonia in ammonium hydroxide,
As shown in Fig. 2, on desorber rich solution feed inlet be arranged 4 blocks of column plates, first piece of 19 import of column plate of upper number by pipeline respectively with
17 steam condensate (SC) of rectifying column heater exports and the steam condensate (SC) outlet outside battery limit (BL)；
The system without phosphate radical and sodium ion further includes mixing channel 12 in ammonium hydroxide when phosphorus ammonium washes ammonia production anhydrous ammonia, described
Alkali liquor inlet and ammonia inlet, the ammonia inlet and 11 outlet of ammonium hydroxide feeder trough are provided on mixing channel 12, it is described mixed
Slot outlet is closed to be connected to rectifying column 3 by rectifying column feed pump 13.
The present embodiment is tied for containing ammonia, hydrogen sulfide, carbon dioxide submarine discharge cooperation phosphorus ammonium and washing ammonia production anhydrous ammonia
The technique without phosphate radical and sodium ion illustrates in ammonium hydroxide when conjunction Fig. 2 washes ammonia production anhydrous ammonia to the present embodiment phosphorus ammonium.
The ammon amount external from battery limit (BL) is less than or equal to 0.9kg/m3Ammonia-containing gas enter 1 lower part of ammonia absorber, divide in tower
Phosphorus ammonium barren liquor not with the cycle phosphorus ammonium pregnant liquor of middle part sprinkling and top sprinkling carries out counter current contacting.Gas content exists after deamination
10g/m3Hereinafter, being left outside battery limit (BL) from 1 top of ammonia absorber.The phosphorus ammonium pregnant liquor of 1 bottom of ammonia absorber is recycled with ammonia absorber
4 extraction of pump is largely sent to 1 middle part cycle sprinkling coal gas of ammonia absorber, and small part rich solution is sent into poor rich liquid heat exchanger 5, with phosphorus
Enter depickling device 6 after the heat exchange of ammonium lean solution.
Phosphorus ammonium pregnant liquor flashes off sour gas in depickling device 6, and sour gas goes to 1 lower part of ammonia absorber.Phosphorus ammonium pregnant liquor is again
With desorber feed pump 7 pump to desorber cooler (on) 8, with ammonia vapour exchange heat after enter 2 rich solution feed inlet of desorber.
The ammonia vapour of the top of desorber 2 effusion respectively desorber cooler (on) 8 and desorption tower cooler device (under) in 9, heating
After phosphorus ammonium pregnant liquor and cooled water cooling, forms ammonium hydroxide and flow into ammonium hydroxide feeder trough 11.
The steam condensate (SC) for being equivalent to ammonia vol about 10% is added on first block of column plate 19 of number on desorber 2, decline
Steam condensate (SC) carries out step by step tray heat and mass with the ammonia vapour risen from feed inlet, is less than or equal to 5g/m what is carried secretly in ammonia vapour3
Phosphate radical removes.Steam condensate (SC) comes from steam condensate (SC) pipeline outside rectifying column heater 17 and battery limit (BL).
The phosphorus ammonium barren liquor for coming from 2 bottom of desorber is heated in desorber heater 10 using indirect steam.2 bottom of desorber
Phosphorus ammonium barren liquor, respectively in poor rich liquid heat exchanger 5 and lean solution cooler 18, after heating phosphorus ammonium pregnant liquor and cooled water cooling, into
Enter the sprinkling of 1 top of ammonia absorber.It is arranged outside 10 steam condensate (SC) of desorber heater.
An ammonium hydroxide part in ammonium hydroxide feeder trough 11 is used as directly to be sent outside without phosphate radical and sodium ion ammonium hydroxide product, remaining
Part enters mixing channel 12, and lye is added in mixing channel 12.
Ammonium hydroxide rectifying column feed pump 13 in mixing channel 12 is pumped to rectifying column 3.Rectifying column 3 pushes up anhydrous ammonia gas in essence
Evaporating the water cooling that is cooled in tower condenser 14 becomes liquid anhydrous ammonia inflow return tank 15.In return tank 15 anhydrous ammonia product and
Reflux pump 16 is extracted out, is partly sent to rectifying column 3 and is pushed up as reflux, remainder is sent outside as product.
The waste water for coming from 3 bottom of rectifying column is heated in rectifying column heater 17 using indirect steam.3 bottom waste water of rectifying column
Outer row.A 17 steam condensate (SC) part of rectifying column heater is sent into first block of column plate 19 of number on desorber 2, is arranged outside remainder.
Embodiment 3：
Present embodiment discloses a kind of phosphorus ammoniums to wash the system for being free of phosphate radical and sodium ion when ammonia produces anhydrous ammonia in ammonium hydroxide,
As shown in figure 3, on desorber rich solution feed inlet be arranged 1 block of column plate, first piece of 19 import of column plate of upper number by pipeline respectively with
Steam condensation outside the outlet of 10 steam condensate (SC) of desorber heater and the outlet of 17 steam condensate (SC) of rectifying column heater and battery limit (BL)
Water out is connected to；
The system without phosphate radical and sodium ion further includes mixing channel 12 in ammonium hydroxide when phosphorus ammonium washes ammonia production anhydrous ammonia, described
Alkali liquor inlet and ammonia inlet, the ammonia inlet and 11 outlet of ammonium hydroxide feeder trough are provided on mixing channel 12, it is described mixed
Slot outlet is closed to be connected to rectifying column 3 by rectifying column feed pump 13.
The present embodiment combines Fig. 3 to the present embodiment phosphorus ammonium so that coke gas washes ammonia production anhydrous ammonia using phosphorus ammonium as an example
The technique without phosphate radical and sodium ion illustrates in ammonium hydroxide when washing ammonia production anhydrous ammonia.
The ammon amount external from battery limit (BL) is less than or equal to 10g/m3Ammonia-containing gas enter 1 lower part of ammonia absorber, in tower respectively
Counter current contacting is carried out with the cycle phosphorus ammonium pregnant liquor of middle part sprinkling and the phosphorus ammonium barren liquor of top sprinkling.Gas ammonia content exists after deamination
100mg/m3Hereinafter, being left outside battery limit (BL) from 1 top of ammonia absorber.The phosphorus ammonium pregnant liquor of 1 bottom of ammonia absorber is followed with ammonia absorber
4 extraction of ring pump is largely sent to 1 middle part cycle sprinkling coal gas of ammonia absorber, and small part rich solution is sent into poor rich liquid heat exchanger 5, with
Enter depickling device 6 after phosphorus ammonium barren liquor heat exchange.
Phosphorus ammonium pregnant liquor flashes off sour gas in depickling device 6, and sour gas goes to 1 lower part of ammonia absorber.Phosphorus ammonium pregnant liquor is again
With desorber feed pump 7 pump to desorber cooler (on) 8, with ammonia vapour exchange heat after enter 2 rich solution feed inlet of desorber.
The ammonia vapour of the top of desorber 2 effusion respectively desorber cooler (on) 8 and desorption tower cooler device (under) in 9, heating
After phosphorus ammonium pregnant liquor and cooled water cooling, forms ammonium hydroxide and flow into ammonium hydroxide feeder trough 11.
The steam condensate (SC) for being equivalent to ammonia vol about 20% is added on first block of column plate 19 of number on desorber 2, decline
Steam condensate (SC) carries out step by step tray heat and mass with the ammonia vapour risen from feed inlet, is less than or equal to 6g/m what is carried secretly in ammonia vapour3
Phosphate radical removes.Steam condensate (SC) comes from steam condensate (SC) pipe outside desorber heater 10 and rectifying column heater 17 and battery limit (BL)
Road.
The phosphorus ammonium barren liquor for coming from 2 bottom of desorber is heated in desorber heater 10 using indirect steam.2 bottom of desorber
Phosphorus ammonium barren liquor, respectively in poor rich liquid heat exchanger 5 and lean solution cooler 18, after heating phosphorus ammonium pregnant liquor and cooled water cooling, into
Enter the sprinkling of 1 top of ammonia absorber.A 10 steam condensate (SC) part of desorber heater is sent into first block of column plate of number on desorber 2
19, remainder is arranged outside.
An ammonium hydroxide part in ammonium hydroxide feeder trough 11 is used as directly to be sent outside without phosphate radical and sodium ion ammonium hydroxide product, remaining
Part enters mixing channel 12, and lye is added in mixing channel 12.
Ammonium hydroxide rectifying column feed pump 13 in mixing channel 12 is pumped to rectifying column 3.Rectifying column 3 pushes up anhydrous ammonia gas in essence
Evaporating the water cooling that is cooled in tower condenser 14 becomes liquid anhydrous ammonia inflow return tank 15.In return tank 15 anhydrous ammonia product and
Reflux pump 16 is extracted out, is partly sent to rectifying column 3 and is pushed up as reflux, remainder is sent outside as product.
The waste water for coming from 3 bottom of rectifying column is heated in rectifying column heater 17 using indirect steam.3 bottom waste water of rectifying column
Outer row.A 17 steam condensate (SC) part of rectifying column heater is sent into first block of column plate 19 of number on desorber 2, is arranged outside remainder.
Embodiment 4：
Present embodiment discloses a kind of phosphorus ammoniums to wash the system for being free of phosphate radical and sodium ion when ammonia produces anhydrous ammonia in ammonium hydroxide,
As shown in figure 4, high about 350mm fillers 20 are arranged on desorber rich solution feed inlet, 20 top flusher import of filler passes through
Pipeline and 10 steam condensate (SC) outlet of desorber heater；
The system without phosphate radical and sodium ion further includes mixing channel 12 in ammonium hydroxide when phosphorus ammonium washes ammonia production anhydrous ammonia, described
Alkali liquor inlet and ammonia inlet, the ammonia inlet and 11 outlet of ammonium hydroxide feeder trough are provided on mixing channel 12, it is described mixed
Slot outlet is closed to be connected to rectifying column 3 by rectifying column feed pump 13.
The present embodiment combines Fig. 4 to this so that coking propylhomoserin mixed raw material gas cooperation phosphorus ammonium washes ammonia production anhydrous ammonia as an example
The technique without phosphate radical and sodium ion illustrates in ammonium hydroxide when embodiment phosphorus ammonium washes ammonia production anhydrous ammonia.
The ammon amount external from battery limit (BL) is less than or equal to 0.7kg/m3Ammonia-containing gas enter 1 lower part of ammonia absorber, divide in tower
Phosphorus ammonium barren liquor not with the cycle phosphorus ammonium pregnant liquor of middle part sprinkling and top sprinkling carries out counter current contacting.Gas ammonia content exists after deamination
9g/m3Hereinafter, being left outside battery limit (BL) from 1 top of ammonia absorber.The phosphorus ammonium pregnant liquor ammonia absorber circulating pump of 1 bottom of ammonia absorber
4 extractions are largely sent to 1 middle part cycle sprinkling coal gas of ammonia absorber, and small part rich solution is sent into poor rich liquid heat exchanger 5, with phosphorus ammonium
Enter depickling device 6 after lean solution heat exchange.
Phosphorus ammonium pregnant liquor flashes off sour gas in depickling device 6, and sour gas goes to 1 lower part of ammonia absorber.Phosphorus ammonium pregnant liquor is again
With desorber feed pump 7 pump to desorber cooler (on) 8, with ammonia vapour exchange heat after enter 2 rich solution feed inlet of desorber.
The ammonia vapour of the top of desorber 2 effusion respectively desorber cooler (on) 8 and desorption tower cooler device (under) in 9, heating
After phosphorus ammonium pregnant liquor and cooled water cooling, forms ammonium hydroxide and flow into ammonium hydroxide feeder trough 11.
The steam condensate (SC) for being equivalent to ammonia vol about 30% is added on 2 top filler of desorber, 20 top flusher,
The steam condensate (SC) of decline carries out step by step tray heat and mass with the ammonia vapour risen from feed inlet, is less than or equal to what is carried secretly in ammonia vapour
0.5g/m3Phosphate radical removes.Condensed water comes from desorber heater 10.
The phosphorus ammonium barren liquor for coming from 2 bottom of desorber is heated in desorber heater 10 using indirect steam.2 bottom of desorber
Phosphorus ammonium barren liquor, respectively in poor rich liquid heat exchanger 5 and lean solution cooler 18, after heating phosphorus ammonium pregnant liquor and cooled water cooling, into
Enter the sprinkling of 1 top of ammonia absorber.A 10 steam condensate (SC) part of desorber heater is sent into 2 top filler of desorber, 20 top spray
Device sprinkling is spilt, is arranged outside remainder.
An ammonium hydroxide part in ammonium hydroxide feeder trough 11 is used as directly to be sent outside without phosphate radical and sodium ion ammonium hydroxide product, remaining
Part enters mixing channel 12, and lye is added in mixing channel 12.
Ammonium hydroxide rectifying column feed pump 13 in mixing channel 12 is pumped to rectifying column 3.Rectifying column 3 pushes up anhydrous ammonia gas in essence
Evaporating the water cooling that is cooled in tower condenser 14 becomes liquid anhydrous ammonia inflow return tank 15.In return tank 15 anhydrous ammonia product and
Reflux pump 16 is extracted out, is partly sent to rectifying column 3 and is pushed up as reflux, remainder is sent outside as product.
The waste water for coming from 3 bottom of rectifying column is heated in rectifying column heater 17 using indirect steam.3 bottom waste water of rectifying column
Outer row.It is arranged outside 17 steam condensate (SC) of rectifying column heater.
Finally it should be noted that：The above embodiments are only used to illustrate the technical solution of the present invention., rather than its limitations；To the greatest extent
Present invention has been described in detail with reference to the aforementioned embodiments for pipe, it will be understood by those of ordinary skill in the art that：Its according to
So can with technical scheme described in the above embodiments is modified, either to which part or all technical features into
Row equivalent replacement；And these modifications or replacements, various embodiments of the present invention technology that it does not separate the essence of the corresponding technical solution
The range of scheme.
Claims (2)
1. the technique of phosphate radical and sodium ion is free of when a kind of phosphorus ammonium washes ammonia production anhydrous ammonia in ammonium hydroxide, which is characterized in that use
The system for being free of phosphate radical and sodium ion when phosphorus ammonium washes ammonia production anhydrous ammonia in ammonium hydroxide, is arranged 1 on desorber rich solution feed inlet
Flusher, first piece of tower is arranged in~5 blocks of column plates or high 200~500mm fillers, first block of column plate of upper number or filler top
Plate or flusher import are gone out by pipeline and desorber heater steam condensation-water drain, rectifying column heater steam condensed water
Mouth is connected to one or more of the steam condensate (SC) outlet outside battery limit (BL)；
The system without phosphate radical and sodium ion further includes mixing channel in ammonium hydroxide when the phosphorus ammonium washes ammonia production anhydrous ammonia, described mixed
It closes and is provided with alkali liquor inlet and ammonia inlet on slot, the ammonia inlet and ammonium hydroxide feeder trough outlet, the mixing channel go out
Mouth is connected to rectifying column, and the ammonium hydroxide without sodium ion is derived from before mixing channel；
The technique without phosphate radical and sodium ion includes the following steps in ammonium hydroxide when phosphorus ammonium washes ammonia production anhydrous ammonia：Steam is cold
Condensate introduces upper first block of column plate of number or high 200~500mm fillers, the steam condensate (SC) of decline and the ammonia risen from feed inlet
Vapour carry out step by step tray heat and mass, and carried secretly in ammonia vapour~phosphate radical remove；Lye and in ammonium hydroxide feeder trough without sodium
It after ion ammonium hydroxide mixes in mixing channel, is delivered in rectifying column, is derived from without sodium ion ammonium hydroxide mixed by rectifying column feed pump
Before closing slot；
The steam condensate (SC) comes from：Desorber heater steam condensation-water drain, rectifying column heater steam condensed water go out
It is one or more in steam condensate (SC) outlet outside mouth and battery limit (BL)；
The steam condensate (SC) introduction volume is to desorb 5~50wt% of ammonia vol.
The technique of phosphate radical and sodium ion is free of when 2. phosphorus ammonium washes ammonia production anhydrous ammonia according to claim 1 in ammonium hydroxide,
It is characterized in that, the steam condensate (SC) introduction volume is to desorb 20~40wt% of ammonia vol.
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| CN201610532099.9A CN106185985B (en) | 2016-07-04 | 2016-07-04 | The technique for being free of phosphate radical and sodium ion when phosphorus ammonium washes ammonia production anhydrous ammonia in ammonium hydroxide |
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| CN201610532099.9A CN106185985B (en) | 2016-07-04 | 2016-07-04 | The technique for being free of phosphate radical and sodium ion when phosphorus ammonium washes ammonia production anhydrous ammonia in ammonium hydroxide |
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| CN101531379B (en) * | 2009-04-17 | 2011-01-26 | 天津天达联合工程技术有限公司 | Method for producing anhydrous ammonia by absorbing ammonium phosphate |
| CN202156935U (en) * | 2011-04-14 | 2012-03-07 | 重庆紫光化工股份有限公司 | System for recycling ammonia from gas containing hydrocyanic acid |
| CN104355321B (en) * | 2014-10-23 | 2016-06-08 | 中冶焦耐工程技术有限公司 | The controlled phosphorus ammonium of product ammonia concn is washed ammonia and is produced strong aqua ammonia technique and device |
| CN105293524A (en) * | 2015-11-20 | 2016-02-03 | 薛斌 | Recovery system and process for waste heat in production of anhydrous ammonia from ammonium phosphate through ammonia washing |
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