CN106395858A - Device and method for preparing pure liquid ammonia from ammonia-containing conversion condensate wastewater - Google Patents
Device and method for preparing pure liquid ammonia from ammonia-containing conversion condensate wastewater Download PDFInfo
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- CN106395858A CN106395858A CN201610899250.2A CN201610899250A CN106395858A CN 106395858 A CN106395858 A CN 106395858A CN 201610899250 A CN201610899250 A CN 201610899250A CN 106395858 A CN106395858 A CN 106395858A
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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 invention discloses a method for preparing pure liquid ammonia from ammonia-containing conversion condensate wastewater. On the basis of single-tower pressurized side drawing and steam stripping and cooling absorption, qualified pure liquid ammonia is prepared by additional arrangement of a rectifying tower. By the method, problems of downstream combustion of waste ammonia gas and emission of nitrogen oxides due to failure in reaching treatment standards of ammonia-containing conversion condensate in a conventional conversion condensate steam stripping process are solved. The invention further discloses a device for preparing pure liquid ammonia from ammonia-containing conversion condensate wastewater.
Description
Technical field
The present invention relates to a kind of convert lime set waste water making pure liquefied ammonia technical field containing ammonia, particularly to a kind of containing ammonia conversion
The method and device of lime set waste water making pure liquefied ammonia.
Background technology
China is a few country of the many gas of coal, and at present, most of chemical enterprises are raw material all using coal, and conversion section is
The requisite workshop section of each coal chemical engineering equipment.Due to containing a small amount of ammonia in the gas after coal gasification, in the high temperature of conversion section
Gas produces substantial amounts of ammonia-containing water after heat exchange cooling.The conversion lime set waste water producing especially in coal-water slurry gasification
In ammonia content will to exceed fine coal gasification process a lot.
Mainly there is single column steam air stripping, double to the process converting lime set waste water containing ammonia in the coal plant being currently in operation
The modes such as ammonia strips, single column pressurization lateral line withdrawal function stripping+cooling absorbs taken out by tower stripping and single column pressurization side line.
As shown in figure 1, single column steam air stripping main flow is described as follows：The condensed device of all of condensed fluid in conversion section
Conversion stripper 2 top is delivered to, the bottom of towe of conversion stripper 2 is passed through a certain amount of low-pressure steam after 1 heating.In conversion lime set
Light component is separated in the presence of steam air stripping from conversion lime set, discharges from stripper top, after condensed device 1 condensation
Send into gas-liquid separator 3 and be separated into sour gas and condensation sewage.Sour gas enters torch or sulfur recovery unit, the warp of liquid containing ammonia condensing
After condenser 4 condensation, stripper top is returned by pump 5 or does not flow back and be used as wastewater disposition.
This flow process exists not enough as follows：
(1) it is derived from the conversion lime set of conversion section and typically contain the H in coal2S、CO2, ammonia, Cl-、CN-Etc. component.
These components are not if being acted upon being fed directly to convert in stripper, it will to conversion stripper, tower internals and its auxiliary device
Produce corrosion.Numerous coal plants all problems at present.
(2) as conversion lime set is processed using above-mentioned single column steam gas stripping process, if the liquid containing ammonia condensing of dephlegmator of top of the tower
Do not flow back, then have stripping sewage to need outer row.If condensed fluid return stripper in participate in washing, carbon dioxide, hydrogen sulfide and
Ammonia then can be accumulated in reflux process, causes equipment, the corrosion of pipeline and blocking.
(3) as using above-mentioned single column steam gas stripping process process conversion lime set, stripper overhead discharge be carbon dioxide,
The gaseous mixture of hydrogen sulfide and ammonia, in follow-up condensation process, vapor delivery line is because during cooling, carbon dioxide, hydrogen sulfide and ammonia is easily
Generate NH4HS and NH4HCO3Ammonium salt crystallization, causes stripper overhead column plate, the corrosion of overhead condenser and line clogging.
(4) as processed conversion lime set using above-mentioned single column steam gas stripping process, ammonia carries out burning disposal as harmful substance,
Not only waste of resource, also result in environmental pollution.
As shown in Fig. 2 double tower stripping main flow is described as follows：Urea carbon dioxide stripper is entered after conversion lime set is heated
10 tops, urea carbon dioxide stripper 10 bottom of towe is passed through the secondary low-voltage steam of aminoacid stripping tower 20 top output.Carbon dioxide and sulfur
Change hydrogen to discharge from urea carbon dioxide stripper 10 top, send into gas-liquid separator 40 after condensed device 30 condensation and be separated into acidity
Gas and condensation sewage, the sour gas that gas-liquid separator 40 top is not coagulated enters torch or sulfur recovery workshop section, urea carbon dioxide stripper
10 bottom lime set waste water enter aminoacid stripping tower 20 top, and aminoacid stripping tower 20 is passed through a certain amount of low-pressure steam, and ammonia steam is from ammonia vapour
Stripper 20 tower top is discharged, and after condenser 50 once condenses, sends in gas-liquid separator 60 and carries out gas-liquid separation, obtain rich ammonia
Gas and condensation sewage, condensation sewage returns in aminoacid stripping tower 20 as one-level condensed fluid, and rich ammonia is cold through condenser 70 2 times
Send into gas-liquid separator 80 after solidifying and carry out gas-liquid separation, gas-liquid separator 80 detached condensation sewage is as B-grade condensation liquid conduct
Wastewater disposition, rich ammonia enters torch or sulfur recovery workshop section.
This flow process overcomes the segmental defect in single column steam air stripping, but still assigns ammonia as detoxication, does not have
There is recovery, in flow process, have sewage to need outer row.
As shown in figure 3, single column pressurization lateral line withdrawal function stripping main flow is described as follows：
, after condenser 10a and heater 20a condenses respectively and heats, point hot and cold two stocks are not from vapour for conversion lime set
The top of stripper 30a and middle and upper part enter stripper 30a, the CO being stripped off2、H2The sour gas such as S and Ammonia, vapor by
Stripper 30a sends at top, is sent directly into torch or sulfur recovery unit.Ammonia in conversion lime set is rich at the middle part of stripper 30a
Collection, carries out three-level condensation through condenser 40a, 40b, 40c, 40d and gas-liquid separator 50a, 50b, 50c after being produced by side and divides
After liquid, obtain the thick ammonia of higher concentration, deliver to ammonia refining and partly process further.Raw material is returned after three-level fractional condensation liquid mixing
Tank.
This flow scheme improvements double tower stripping process, but there is also following deficiency：
(1) ammonia steam condenses through three-level, can obtain the rich ammonia that concentration is 99% about, wherein CO2Content is about
20ppm, H2S content is about 1000ppm, but still can not be used directly to prepare H2The content of S is less than 100ppm, and concentration is
20% qualified weak ammonia.
(2) second level condensation temperature generally in three-level condenser system controls at 70-90 DEG C, thus condensing certain further
The water of amount and hydrogen sulfide simultaneously improve the concentration of ammonia in gas phase.But, hydrogen sulfide strengthens with the rising of temperature to the corrosion of steel,
80 DEG C of corrosion rates reach highest, and after temperature raises again, corrosion rate starts to reduce, and when 110-120 DEG C, corrosion rate reaches
Minimum.
(3) three-level condensation flow process includes three heat exchangers and three points of flow containers, takes up an area big.
As shown in figure 4, single column pressurization lateral line withdrawal function strips+cools down absorption process main flow and is described as follows：
It is divided into two parts from converting means lime set containing ammonia conversion, a part heats up through thermal converter E1, E2 heat exchange
Enter the middle and upper part of stripper T1 afterwards.Another part is sent directly into the top of stripper T1；Stripper T1 tower bottom reboiler E3 leads to
Enter a certain amount of low pressure steam, the conversion lime set entering tower is stripped.Stripper T1 bottom of towe is qualified purification and condensation liquid
Deliver to downstream unit after pump P1, thermal converter E2, E4 cooling.Most of H2S、CO2Evaporate from stripper T1 tower top etc. component
Go out, part H2S、NH3、H2The components such as O, from stripper T1 lateral line withdrawal function, then enter back into heat exchanger E1 and are cooled to 115 DEG C about and
Enter the I section bottom to ammonia absorption tower T2.Liquid phase from ammonia absorption tower T2 ii section bottom is entered by action of gravity
To ammonia absorption tower T2 I section top.Cooling absorbs and is derived from ammonia absorption tower T2 I section bottom rising part H2S.Through supercooling
The gas phase absorbing enters into ammonia absorption tower T2 ii section bottom by chimney plate, delivers to ammonia from Partial cleansing condensed fluid and inhales
Receive the cooling of tower T2 ii section top and absorb ammonia absorption tower T2 ii section bottom rising part H2S.The gas phase absorbing through supercooling
Ammonia absorption tower T2 ii I section bottom is entered into by chimney plate.Then again ammonia absorption is delivered to using Partial cleansing condensed fluid
The cooling of tower T2 ii I section top absorbs part NH that ammonia absorption tower ii section bottom rises3.Finally produce qualified dilute ammonia
Water.Due to absorbing heat release, now it is derived from ammonia absorption tower ii I section bottom weak ammonia temperature higher, finally by aqua ammonia pump P3
Deliver to ammonia cooler E5 cooling and send battery limit (BL).Weak ammonia after another part cooling is as refrigerant circulation to ammonia absorption tower
T2 ii I section top, the cleaning mixture from ammonia absorption tower T2 I section bottom sends into the middle and upper part of stripper T1 by pump P2.
This flow process improves to some extent, but there is also following deficiency：
(1), after absorbing through air stripping and cooling, only produce the qualified weak ammonia that concentration is 20%, and the product of this kind of specification
Market purposes is few, market potential low it is impossible to effectively utilizes.
(2) as stripper operation fluctuation, it is susceptible to the exceeded problem of hydrogen sulfide in weak ammonia.
Content of the invention
One of the technical problem to be solved is to strip+cool down absorption process for single column pressurization lateral line withdrawal function
The problems of and provide a kind of containing ammonia convert lime set waste water making pure liquefied ammonia method, the method single column pressurization side line take out
On the basis of going out stripping+cooling absorption, to produce qualified pure liquefied ammonia by the way of setting up rectifying column.Often this method solve
In rule conversion lime set air stripping flow process, the conversion lime set process containing ammonia is not up to standard, and useless ammonia can only go fired downstream to discharge nitrogen oxides
A difficult problem.
The two of the technical problem to be solved are to provide the device realizing said method.
The technical problem to be solved can be achieved through the following technical solutions：
A kind of method converting lime set waste water making pure liquefied ammonia containing ammonia, is divided into two from converting means lime set containing ammonia conversion
Part, a part enters the middle and upper part of stripper after First Heat Exchanger, the second heat exchanger heat exchange heat up, and another part is direct
Send into the top of stripper, stripper tower bottom reboiler is passed through a certain amount of low pressure steam, the conversion entering stripper is coagulated
Liquid is stripped；A small amount of alkali liquor can be sent in the middle part of stripper, and most of alkali liquor is first fed into absorption tower ii section top, then returns
Neutralize with the conversion lime set containing ammonia in the middle part of back-steam stripper；
Stripper bottom of towe sends qualified purification and condensation liquid, sequentially passes through the second heat exchanger, big after the 3rd heat exchanger cooling
Part delivers to downstream unit, and fraction purification and condensation liquid is admitted to top or/and the ammonia absorption tower of ammonia absorption tower ii section
The middle part of ii I section；
Most of H2S and CO2Distillate formation sour gas from stripper overhead to send, fraction H2S and NH3、H2O is from stripper
Lateral line withdrawal function, then enters back into First Heat Exchanger and is cooled to 110～120 DEG C and enter into ammonia absorption tower I section bottom；
Liquid phase from ammonia absorption tower ii section bottom enters into ammonia absorption tower I section top by action of gravity,
Cooling absorbs and is derived from ammonia absorption tower I section bottom rising part H2S, is entered by the first chimney plate through the gas phase that supercooling absorbs
Enter to ammonia absorption tower ii section bottom；
It is admitted to the fraction purification and condensation liquid at ammonia absorption tower ii section top or be admitted to ammonia absorption tower ii section
The fraction purification and condensation liquid at top cools down absorption ammonia absorption together with being admitted to the alkali liquor at ammonia absorption tower ii section top
Tower ii section bottom rising part H2S, enters into ammonia absorption tower ii I through the gas phase that supercooling absorbs by the second chimney plate
Section bottom；
A small amount of alkali liquor can be sent in the middle part of stripper, and most of alkali liquor is first fed into absorption tower ii section top, is then back to
Neutralize with the conversion lime set containing ammonia in the middle part of stripper；
It is sent to the desalted water at ammonia absorption tower ii I section top or be sent to the de- of ammonia absorption tower ii I section top
Saline absorbs ammonia absorption tower ii section bottom with the fraction purification and condensation liquid cooling being admitted in the middle part of ammonia absorption tower ii I section
Portion rising part NH3；
The middle and upper part of stripper sent into by cleaning mixture from ammonia absorption tower I section bottom；
Weak ammonia conduct suction after the 4th heat exchanger and the 5th heat exchanger heat exchange cooling from ammonia tower bottom of rectifying tower
Receive agent and return to the top with ii section in the middle part of ammonia absorption tower ii I section, thus producing not hydrogen sulfide containing ammonia；Or come
It is qualified directly to send with the stripper bottom of towe after the second heat exchanger heat exchange cooling from the weak ammonia of ammonia tower bottom of rectifying tower
After the mixing of purification and condensation liquid, then deliver to downstream unit after the 3rd heat exchanger cooling；
Qualified ammonia, after pressure-raising preheating, sends into the middle part of ammonia rectifying column, as charging；Ammonia rectifying column tower top is steamed
Ammonia lime set is obtained, part ammonia lime set returns to ammonia rectifying column top as backflow through reflux pump, separately after the cooled water condensation of vapour
Outer a part of ammonia lime set is delivered to out-of-bounds as product liquefied ammonia；
Ammonia tower bottom of rectifying tower reboiler passes through low-pressure steam or process-stream cooling provides heat.
The weak ammonia that ammonia absorption tower ii I section bottom is sent is sent in ammonia rectifying column after the 4th heat exchanger heats
The weak ammonia part that portion or ammonia absorption tower ii I section bottom are sent is sent directly into the middle and lower part of ammonia rectifying column, another
Part is divided into two after condenser condensation, and one is sent directly in the middle part of ammonia rectifying column, and another Zhi Zuowei absorbent is sent into
Absorb with the fraction purification and condensation liquid cooling being admitted in the middle part of ammonia absorption tower ii I section in the middle part of ammonia absorption tower ii I section
Ammonia absorption tower ii section bottom rising part NH3.
A kind of device converting lime set waste water making pure liquefied ammonia containing ammonia, including stripper, ammonia absorption tower and ammonia rectification
Tower；
The bottom of described stripper is provided with stripper tower bottom reboiler and first outlet, middle part be provided with first entrance and
Second outlet, top is provided with second and third entrance, and top is provided with the 4th entrance and the 3rd outlet；
Described ammonia absorption tower I section bottom is provided with the 5th entrance and the 4th outlet, the top of ammonia absorption tower ii section
Portion is provided with the 6th entrance, is provided with the 7th entrance, described ammonia absorption tower ii I in the middle part of described ammonia absorption tower ii I section
Section top is provided with the 8th entrance and the 5th outlet；Or described ammonia absorption tower I section bottom is provided with the 5th entrance and
Four outlets, the top of ammonia absorption tower ii section is provided with the 6th entrance, and the middle part of described ammonia absorption tower ii section is provided with
9th entrance, is provided with the 7th entrance in the middle part of described ammonia absorption tower ii I section, described ammonia absorption tower ii I section top sets
It is equipped with the 8th entrance and the 5th outlet；Described ammonia absorption tower ii I section bottom is provided with the 6th outlet；
The bottom of towe of described ammonia rectifying column is provided with tower reactor reboiler and the 7th outlet, and the middle part of ammonia rectifying column is provided with
Tenth entrance or the tenth entrance and the 11st entrance, the top of described ammonia rectifying column is provided with the 8th outlet and the 12nd and enters
Mouthful；
Convert lime set delivery pipe one side from converting means containing ammonia and pass through the first pipeline and described stripper top
4th entrance connects, and is on the other hand connected with the first medium entrance of first heat exchanger by the second pipeline, the first heat exchange
The first medium outlet of device is connected with the first medium entrance of second heat exchanger by the 3rd pipeline, and the of second heat exchanger
One media outlet is connected with the second entrance on described stripper top by the 4th pipeline；
The outlet of lye tank (vat) is connected with the entrance of the first pump by the 5th pipeline, the outlet of the first pump pass through the 6th pipeline with
First entrance in the middle part of described stripper connects；
The first outlet of stripper bottom is connected with the entrance of the second pump by the 7th pipeline, described second pump outlet
It is connected with the second medium entrance of described second heat exchanger by the 8th pipeline, the second medium of described second heat exchanger goes out
Mouth is connected with the entrance of the 3rd heat exchanger by the 9th pipeline, and the outlet of the 3rd heat exchanger connects waste water outlet tube；
3rd outlet of stripper top connects a sour gas outlet tube, and the 3rd entrance on stripper top passes through the tenth and manages
Line and the 3rd pump are connected with the 4th outlet of described ammonia absorption tower I section bottom, and the second outlet in the middle part of described stripper is led to
Cross the 11st pipeline to be connected with the second medium entrance of described first heat exchanger, the second medium of described first heat exchanger goes out
Mouth is connected with the 5th entrance of described ammonia absorption tower I section bottom by the 12nd pipeline；
5th outlet at described ammonia absorption tower ii I section top connects a fixed gas outlet tube；Described ammonia absorption tower
8th entrance at ii I section top connects a desalination water inlet pipe；
The 7th entrance in the middle part of described ammonia absorption tower ii I section passes through that the 13rd pipeline connects the 5th heat exchanger
One medium inlet, the first medium outlet of described 5th heat exchanger connects described 4th heat exchanger by the 14th pipeline
First medium entrance, the first medium outlet of described 4th heat exchanger connects described ammonia rectifying tower by the 15th pipeline
7th outlet at bottom connects；6th entrance at described ammonia absorption tower ii section top is connected to described by the 16th pipeline
The outlet of one pump；6th entrance at described ammonia absorption tower ii section top connects described waste water output also by the 17th pipeline
Guan Shang, the 9th entrance in the middle part of described ammonia absorption tower ii section connects on described 13rd pipeline also by the 18th pipeline；
6th outlet of described ammonia absorption tower ii I section bottom is connected to the entrance of the 4th pump by the 19th pipeline, and the described 4th
The outlet of pump connects the second medium entrance of described 4th heat exchanger by the 20th pipeline, and the of described 4th heat exchanger
The tenth entrance that second medium outlet is connected by the 21st pipeline in the middle part of described ammonia rectifying column connects；
Or, the 7th entrance one side in the middle part of described ammonia absorption tower ii I section is passed through the 22nd pipeline and is connected institute
State waste water outlet tube, on the other hand the tenth entrance in the middle part of described ammonia rectifying column is connected by the 23rd pipeline；Described
6th entrance at ammonia absorption tower ii section top passes through the 24th pipeline and connects on described 22nd pipeline；Described ammonia
6th outlet of absorption tower ii I section bottom is connected to the entrance of the 4th pump by the 19th pipeline, the outlet of described 4th pump
Connect the entrance of described 5th heat exchanger by the 25th pipeline, the outlet of described 5th heat exchanger passes through the 26th
Pipeline connects on described 23rd pipeline, and the outlet of described 5th heat exchanger connects described ammonia also by the 27th pipeline
The 11st entrance in the middle part of crystal evaporate tower；7th outlet at described ammonia rectifying tower bottom is connected described by the 28th pipeline
Waste water outlet tube；
8th outlet at described ammonia rectifying column top connects entering of described 6th heat exchanger by the 29th pipeline
Mouthful, the outlet of described 6th heat exchanger connects the entrance of a storage tank by the 30th pipeline, and the outlet of described storage tank passes through the
31 pipelines connect the entrance of the 5th pump, and on the one hand the outlet of described 5th pump connects liquefied ammonia outlet tube, on the other hand pass through
32nd pipeline connects the 12nd entrance at described ammonia rectifying column top.
Due to employing technical scheme as above, the present invention is absorbed with existing single column pressurization lateral line withdrawal function stripping+cooling
The device of making pure liquefied ammonia is compared, and has the advantage that：
1. setting ammonia absorption tower replaces traditional three-level condensation flow process, and cooling, Absorption Desulfurization and ammonia are produced and is combined into
Integrally, equipment investment and occupation of land are reduced.
2. using process, the Partial Transformation lime set after qualified delivers to above-mentioned ammonia absorption tower ii as cooling and absorbent
Section top, is not only effectively reduced the H in gas phase2S content, can also reduce the temperature of gas phase.Now temperature just avoids
The optimum temperature of corrosion.
3. using process, the Partial Transformation lime set after qualified delivers to above-mentioned ammonia absorption tower ii I as cooling and absorbent
Section top, compares the use that traditional ammonia absorption saves desalted water.
4. due to NH3After stripper is by lateral line withdrawal function, it is substantially free of ammonia in tower top sour gas, it is to avoid ammonium salt is in stripper
The crystallization of tower top and corrosion.Downstream Crouse can be fed directly to for this tower top sour gas and reclaim sulfur.
5. due to substantially also not containing H in purification and condensation liquid2S、NH3Deng material, gasification can be fed directly to or biochemical treatment subtracts
The light burden of wastewater disposition.
6. it is additionally arranged ammonia rectifying column to produce qualified liquefied ammonia product in tower top.
7. ammonia rectifying column pressurized operation, it is ensured that rectifying tower top condenser temperature is higher, can adopt the cold of common specification
But water can meet cooling and require it is not necessary to consume low temperature cold.
8. pair newly go up lime set processing meanss, ammonia tower bottom of rectifying tower produces weak ammonia, return ammonia absorption tower.Although therefore
Ammonia rectifying column pressurized operation, its bottom temperature is not also too high, can meet rectification heat demand using low-pressure steam.
9., for transformation device, absorption plant is constructed finishes for side line air stripping such as above and cooling, then increase ammonia newly
Tower bottom of rectifying tower extraction meets the waste water of environmental requirement, now rectifying column reboiler need to using the higher middle pressure steam of potential temperature or
Process-stream is as thermal source.
10., in order to ensure the pre- anticorrosion of product liquid ammonia quality, alkali liquor can be added in the middle part of stripper and ammonia absorption tower.
11. for small-scale device, and the condenser of ammonia rectifying column tower top can be integrated with rectifying column, thus saving
One return tank and a reflux pump.
The weak ammonia of 12. ammonia tower bottom of rectifying towers returns in the middle part of ammonia absorption tower ii I section and the after recuperation of heat cooling
Two-stage nitration top recycles as absorbent.
The present invention is directed to one kind at present and converts lime set wastewater treatment process by reconfiguring containing ammonia, to solve to contain at present ammonia
Conversion lime set waste water cannot be processed or ammonia quality too low no market outlet problem after treatment.
Brief description
Fig. 1 is that existing single column steam air stripping contains the schematic device that ammonia converts lime set waste water making pure liquefied ammonia.
Fig. 2 is the schematic device that existing double tower stripping converts lime set waste water making pure liquefied ammonia containing ammonia.
Fig. 3 is the schematic device that existing single column pressurization lateral line withdrawal function stripping converts lime set waste water making pure liquefied ammonia containing ammonia.
Fig. 4 is that existing single column pressurization lateral line withdrawal function stripping+cooling absorbs the dress containing ammonia conversion lime set waste water making pure liquefied ammonia
Put schematic diagram.
Fig. 5 is the schematic device converting lime set waste water making pure liquefied ammonia containing ammonia of the embodiment of the present invention 1.
Fig. 6 is the schematic device converting lime set waste water making pure liquefied ammonia containing ammonia of the embodiment of the present invention 2.
Specific embodiment
Embodiment 1
Referring to Fig. 5, the device converting lime set waste water making pure liquefied ammonia containing ammonia shown in figure, it is mainly used in newly-increased lime set
Air-lift device, it includes stripper 100, ammonia absorption tower 200 and ammonia rectifying column 300.
The bottom of stripper 100 is provided with stripper tower bottom reboiler E3 and outlet 110, and middle part is provided with entrance 120 He
Outlet 130, top is provided with entrance 140,150, and top is provided with entrance 160 and outlet 170.
Ammonia absorption tower 200 I section bottom is provided with entrance 210 and outlet 220, the top of ammonia absorption tower 200 ii section
Portion is provided with entrance 230, is provided with entrance 240, ammonia absorption tower 200 ii I section top in the middle part of ammonia absorption tower 200 ii I section
Portion is provided with entrance 250 and outlet 260.The middle part of ammonia absorption tower 200 ii section is provided with entrance 270, ammonia absorption tower 200
The bottom of ii I section is provided with outlet 280.
The bottom of towe of ammonia rectifying column 300 is provided with tower reactor reboiler E7 and outlet 310, and the middle part of ammonia rectifying column 300 sets
It is equipped with entrance 320, the top of ammonia rectifying column 300 is provided with outlet 330 and entrance 340.
Convert lime set delivery pipe 401 1 aspect from converting means containing ammonia and pass through pipeline 402 and stripper 100 top
Entrance 160 connects, and is on the other hand connected with the first medium entrance of heat exchanger E1 by pipeline 403, and the of heat exchanger E1
One media outlet is connected with the first medium entrance of heat exchanger E2 by pipeline 404, the first medium outlet of heat exchanger E2
It is connected with the entrance 140 on stripper 100 top by pipeline 405.
The outlet of lye tank (vat) V1 is connected with the entrance of pump P3 by pipeline 406, and pipeline 407 and stripping are passed through in the outlet of pump P3
The entrance 120 at tower 100 middle part connects.
The outlet 110 of stripper 100 bottom is connected with the entrance of pump P1 by pipeline 408, and pipeline is passed through in the outlet of pump P1
409 are connected with the second medium entrance of heat exchanger E2, and pipeline 410 and heat exchange are passed through in the second medium outlet of heat exchanger E2
The entrance of device E4 connects, and the outlet of heat exchanger E4 connects waste water outlet tube 411.
The outlet 170 at stripper 100 top connects a sour gas outlet tube 412, and the entrance 150 on stripper 100 top leads to
The outlet 220 crossing pipeline 412a and pump P2 with ammonia absorption tower 200 I section bottom is connected, the outlet 130 at stripper 100 middle part
It is connected with the second medium entrance of heat exchanger E1 by pipeline 413, pipeline 414 is passed through in the second medium outlet of heat exchanger E1
It is connected with the entrance 210 of ammonia absorption tower 200 I section bottom.
The outlet 260 at ammonia absorption tower 200 ii I section top connects a fixed gas outlet tube 415；Ammonia absorption tower
The entrance 250 at III section 200 top connects a desalination water inlet pipe 416.
Entrance 240 in the middle part of ammonia absorption tower 200 ii I section connects the first medium of heat exchanger E8 by pipeline 417
Entrance, the first medium outlet of heat exchanger E8 connects the first medium entrance of heat exchanger E5, heat exchanger by pipeline 418
The first medium outlet of E5 is connected by the outlet 310 that pipeline 419 connects ammonia rectifying column 300 bottom of towe；Ammonia absorption tower 300
Entrance 230 1 aspect at II section top is connected to the outlet of pump P3 by pipeline 420, on the other hand passes through pipeline 421 connection useless
Water delivery pipe 411.
Entrance 270 in the middle part of ammonia absorption tower 300 ii section is also by pipeline 422 connecting pipeline 417；Ammonia absorption tower
The outlet 280 of 300 ii I section bottoms is connected to the entrance of pump P4 by pipeline 423, and the outlet of pump P4 is connected by pipeline 424
The second medium entrance of heat exchanger E5, the second medium outlet of heat exchanger E5 connects ammonia rectifying column 300 by pipeline 425
The entrance 320 at middle part connects.
The outlet 330 at ammonia rectifying column 300 top connects the entrance of heat exchanger E6, heat exchanger E6 by pipeline 426
Outlet connect the entrance of a storage tank V2 by pipeline 427, the outlet of storage tank V2 connects the entrance of pump P5, pump by pipeline 428
On the one hand the outlet of P5 connects liquefied ammonia outlet tube 429, on the other hand connects entering of ammonia rectifying column 300 top by pipeline 430
Mouth 340.
It is divided into two parts from converting means lime set containing ammonia conversion, a part heats up through over-heat-exchanger E1, E2 heat exchange
Enter stripper 100 middle and upper part afterwards.Stripper 100 tower bottom reboiler E3 is passed through a certain amount of low pressure steam, to the change entering tower
Change lime set to be stripped.Stripper 100 bottom of towe is that qualified purification and condensation liquid delivers to downstream dress after over-heat-exchanger E4 cooling
Put.Most of H2S、CO2Distillate from stripper 100 tower top etc. component, part H2S、NH3、H2The components such as O from lateral line withdrawal function, then
Enter back into heat exchanger E1 and be cooled to 110～120 DEG C and enter into ammonia absorption tower 300 I section bottom.From ammonia absorption tower
The liquid phase of 200 ii section bottoms enters into ammonia absorption tower 200 I section top by action of gravity.Cooling absorbs and is derived from ammonia
Absorption tower 200 I section bottom rising part H2S.Through the gas phase that supercooling absorbs, ammonia absorption tower 20 is entered into by chimney plate
Ii section bottom, delivers to ammonia absorption tower 200 ii section top from Partial cleansing condensed fluid and alkali liquor, and cooling absorbs ammonia and inhales
Receive tower 200 ii section bottom rising part H2S.Through the gas phase that supercooling absorbs, ammonia absorption tower 200 is entered into by chimney plate
Ii I section bottom.Then again the cooling of ammonia absorption tower 200 ii I section top is delivered to using desalted water and absorb ammonia absorption tower 300
Ii section bottom rising part NH3, it is also fed into ammonia absorption tower 200 ii I section from the weak ammonia of ammonia rectifying column 300 tower reactor
Middle part as absorbent, thus producing not hydrogen sulfide containing ammonia.
Qualified ammonia, after pressure-raising preheating, sends into ammonia rectifying column 300 as charging.Ammonia rectifying column 300 tower top ammonia
Ammonia lime set is obtained, part ammonia lime set returns to ammonia rectifying column 300 top as backflow through pump P5 after the cooled water condensation of steam,
Another part ammonia lime set is delivered to out-of-bounds as product liquefied ammonia.Ammonia rectifying column 300 tower reactor reboiler E7 pass through low-pressure steam or
Process-stream cooling provides heat, and the weak ammonia of ammonia rectifying column 300 tower reactor extraction is through heat exchanger E5 heat exchange and heat exchanger
Return in the middle part of ammonia absorption tower 200 ii I section as absorbent and second segment top after E8 cooling.
Embodiment 2
Referring to Fig. 6, the device converting lime set waste water making pure liquefied ammonia containing ammonia shown in figure, it is mainly used in the solidifying of reworked
Liquid air-lift device, it includes stripper 100, ammonia absorption tower 200 and ammonia rectifying column 300.
The bottom of stripper 100 is provided with stripper tower bottom reboiler E3 and outlet 110, and middle part is provided with entrance 120 He
Outlet 130, top is provided with entrance 140,150, and top is provided with entrance 160 and outlet 170.
Ammonia absorption tower 200 I section bottom is provided with entrance 210 and outlet 220, the top of ammonia absorption tower 200 ii section
Portion is provided with entrance 230, is provided with entrance 240, ammonia absorption tower 200 ii I section top in the middle part of ammonia absorption tower 200 ii I section
Portion is provided with entrance 250 and outlet 260.The bottom of ammonia absorption tower 200 ii I section is provided with outlet 280.
The bottom of towe of ammonia rectifying column 300 is provided with tower reactor reboiler E7 and outlet 310, and the middle part of ammonia rectifying column 300 sets
It is equipped with entrance 320,350, the top of ammonia rectifying column 300 is provided with outlet 330 and entrance 340.
Convert lime set delivery pipe 401 1 aspect from converting means containing ammonia and pass through pipeline 402 and stripper 100 top
Entrance 160 connects, and is on the other hand connected with the first medium entrance of heat exchanger E1 by pipeline 403, and the of heat exchanger E1
One media outlet is connected with the first medium entrance of heat exchanger E2 by pipeline 404, the first medium outlet of heat exchanger E2
It is connected with the entrance 140 on stripper 100 top by pipeline 405.
The outlet of lye tank (vat) V1 is connected with the entrance of pump P3 by pipeline 406, and pipeline 407 and stripping are passed through in the outlet of pump P3
The entrance 120 at tower 100 middle part connects.
The outlet 110 of stripper 100 bottom is connected by the second medium entrance of pipeline 408 heat exchanger E2, heat exchange
The second medium outlet of device E2 is connected with the entrance of pump P1 by pipeline 409, and pipeline 410 and heat exchanger are passed through in the outlet of pump P1
The second medium entrance of E4 connects, and the second medium outlet of heat exchanger E4 connects waste water outlet tube 411.
The outlet 170 at stripper 100 top connects a sour gas outlet tube 412, and the entrance 150 on stripper 100 top leads to
The outlet 220 crossing pipeline 412a and pump P2 with ammonia absorption tower 200 I section bottom is connected, the outlet 130 at stripper 100 middle part
It is connected with the second medium entrance of heat exchanger E1 by pipeline 413, pipeline 414 is passed through in the second medium outlet of heat exchanger E1
It is connected with the entrance 210 of ammonia absorption tower 200 I section bottom.
The outlet 260 at ammonia absorption tower 200 ii I section top connects a fixed gas outlet tube 415；Ammonia absorption tower
The entrance 250 at III section 200 top connects a desalination water inlet pipe 416.
Entrance 240 1 aspect in the middle part of ammonia absorption tower 200 ii I section is connected in ammonia rectifying column 300 by pipeline 431
The entrance 320 in portion, on the other hand connects waste water outlet tube 411 by pipeline 432；The going out of ammonia absorption tower 300 ii I section bottom
Mouth 280 is connected to the entrance of pump P4 by pipeline 423.
On the one hand the outlet of pump P4 connects the entrance of heat exchanger E7 by pipeline 424a, and the outlet of heat exchanger E7 is passed through
Pipeline 433 connecting pipeline 431, is on the other hand connected by the entrance 350 that pipeline 425 connects ammonia rectifying column 300 middle part.
The outlet 330 at ammonia rectifying column 300 top connects the entrance of heat exchanger E6, heat exchanger E6 by pipeline 426
Outlet connect the entrance of a storage tank V2 by pipeline 427, the outlet of storage tank V2 connects the entrance of pump P5, pump by pipeline 428
On the one hand the outlet of P5 connects liquefied ammonia outlet tube 429, on the other hand connects entering of ammonia rectifying column 300 top by pipeline 430
Mouth 340.
It is divided into two parts from converting means lime set containing ammonia conversion, a part heats up through over-heat-exchanger E1, E2 heat exchange
Enter stripper 100 middle and upper part afterwards.Stripper 100 tower bottom reboiler E3 is passed through a certain amount of low pressure steam, to the change entering tower
Change lime set to be stripped.Stripper 100 bottom of towe is that qualified purification and condensation liquid delivers to downstream dress after over-heat-exchanger E4 cooling
Put.
Most of H2S、CO2Distillate from stripper overhead etc. component, part H2S、NH3、H2The components such as O from lateral line withdrawal function, so
After enter back into heat exchanger E1 and be cooled to 110～120 DEG C and enter into ammonia absorption tower 200 I section bottom.From ammonia absorption tower
The liquid phase of 200 ii section bottoms enters into ammonia absorption tower 200 I section top by action of gravity, and cooling absorbs and is derived from ammonia
Absorption tower 200 I section bottom rising part H2S.
Through the gas phase that supercooling absorbs, ammonia absorption tower 200 ii section bottom is entered into by chimney plate, from partly net
Change condensed fluid and deliver to ammonia absorption tower 200 ii section top, cooling absorbs ammonia absorption tower 200 ii section bottom rising part
H2S.Through the gas phase that supercooling absorbs, ammonia absorption tower 200 ii I section bottom is entered into by chimney plate.Then adopt desalination again
Water and Partial cleansing condensed fluid are delivered to the cooling of ammonia absorption tower ii I section top and are absorbed on the ii section bottom of ammonia absorption tower 200
Rise part NH3.
Also return to after cooling in the middle part of ii I section from the qualified partial ammonia water of ammonia absorption tower 200 ii I section bottom
As absorbent, another part sends into ammonia rectifying column 300 as charging.The cooled water-cooled of ammonia rectifying column 300 overhead vapours
Ammonia lime set is obtained, part ammonia lime set returns to ammonia rectifying column 300 top as backflow through pump P5, and another part ammonia coagulates after solidifying
Liquid is delivered to out-of-bounds as product liquefied ammonia.Tower reactor reboiler E7 of ammonia rectifying column 300 passes through middle pressure steam or high-temperature position technique thing
Stream provides heat, the waste water and the stripper tower reactor waste water combination cooling that meet environmental requirement of the extraction of ammonia rectifying column 300 tower reactor
After send battery limit (BL).
This kind of flow setting is applied to transformation operating mode, when stripper 100 with ammonia absorption tower 200 is constructed finishes, such as
Factory for improving product Production of Value liquefied ammonia, then can individually increase ammonia rectifying column T3 for processing from ammonia absorption tower
Ammonia can meet needs.And two Tower Systems above are substantially without transformation.Its shortcoming need to be using height for ammonia rectifying column
The middle pressure steam of grade provides heat it is adaptable to transformation device, foregoing apparatus is changed less.
Claims (2)
1. a kind of containing ammonia convert lime set waste water making pure liquefied ammonia method it is characterised in that：Convert containing ammonia from converting means
Lime set is divided into two parts, and a part enters the middle and upper part of stripper after First Heat Exchanger, the second heat exchanger heat exchange heat up, separately
A part is sent directly into the top of stripper, and stripper tower bottom reboiler is passed through a certain amount of low pressure steam, strips to entering
The conversion lime set of tower is stripped；A small amount of alkali liquor can be sent in the middle part of stripper, and most of alkali liquor is first fed into absorption tower ii section
Top, is then back to neutralize with the conversion lime set containing ammonia in the middle part of stripper；Stripper bottom of towe sends qualified purification and condensation liquid, successively
After the second heat exchanger, the 3rd heat exchanger cooling, major part delivers to downstream unit, and fraction purification and condensation liquid is admitted to ammonia
The top of absorption tower ii section or/and the middle part of ammonia absorption tower ii I section；
Most of H2S and CO2Distillate formation sour gas from stripper overhead to send, fraction H2S and NH3、H2O is from stripper side line
Extract out, then enter back into First Heat Exchanger and be cooled to 110～120 DEG C and enter into ammonia absorption tower I section bottom；
Liquid phase from ammonia absorption tower ii section bottom enters into ammonia absorption tower I section top by action of gravity, cooling
Absorb and be derived from ammonia absorption tower I section bottom rising part H2S, entered into by the first chimney plate through the gas phase that supercooling absorbs
Ammonia absorption tower ii section bottom；
It is admitted to the fraction purification and condensation liquid at ammonia absorption tower ii section top or be admitted to ammonia absorption tower ii section top
Fraction purification and condensation liquid cool down absorption ammonia absorption tower the together with being admitted to the alkali liquor at ammonia absorption tower ii section top
II section bottom rising part H2S, enters into ammonia absorption tower ii I section bottom through the gas phase that supercooling absorbs by the second chimney plate
Portion；
A small amount of alkali liquor can be sent in the middle part of stripper, and most of alkali liquor is first fed into absorption tower ii section top, is then back to strip
Neutralize with the conversion lime set containing ammonia in the middle part of tower；
It is sent to the desalted water at ammonia absorption tower ii I section top or the desalted water being sent to ammonia absorption tower ii I section top
Absorb on the ii section bottom of ammonia absorption tower with the fraction purification and condensation liquid cooling being admitted in the middle part of ammonia absorption tower ii I section
Rise part NH3；
The middle and upper part of stripper sent into by cleaning mixture from ammonia absorption tower I section bottom；
From ammonia tower bottom of rectifying tower weak ammonia by the 4th heat exchanger and the 5th heat exchanger heat exchange cooling after as absorbent
Return to the top with ii section in the middle part of ammonia absorption tower ii I section, thus producing not hydrogen sulfide containing ammonia；Or it is derived from ammonia
The weak ammonia of crystal evaporate tower tower reactor directly sends qualified purification with the stripper bottom of towe after the second heat exchanger heat exchange cooling
After condensed fluid mixing, then deliver to downstream unit after the 3rd heat exchanger cooling；
Qualified ammonia, after pressure-raising preheating, sends into the middle part of ammonia rectifying column, as charging；Ammonia rectifying column tower top steam warp
Ammonia lime set is obtained, part ammonia lime set returns to ammonia rectifying column top as backflow through reflux pump after cooling water condensation, in addition one
Part ammonia lime set is delivered to out-of-bounds as product liquefied ammonia；
Ammonia tower bottom of rectifying tower reboiler passes through low-pressure steam or process-stream cooling provides heat；
The weak ammonia that ammonia absorption tower ii I section bottom is sent by sending into after the 4th heat exchanger heats in the middle part of ammonia rectifying column or
The weak ammonia part that person's ammonia absorption tower ii I section bottom is sent is sent directly into the middle and lower part of ammonia rectifying column, another part
It is divided into two after condenser condensation, one is sent directly in the middle part of ammonia rectifying column, another Zhi Zuowei absorbent sends into ammonia
Ammonia is absorbed with the fraction purification and condensation liquid cooling being admitted in the middle part of ammonia absorption tower ii I section in the middle part of the ii I section of absorption tower
Absorption tower ii section bottom rising part NH3.
2. a kind of containing ammonia convert lime set waste water making pure liquefied ammonia device it is characterised in that include stripper, ammonia absorption tower and
Ammonia rectifying column；
The bottom of described stripper is provided with stripper tower bottom reboiler and first outlet, and middle part is provided with first entrance and second
Outlet, top is provided with second and third entrance, and top is provided with the 4th entrance and the 3rd outlet；
Described ammonia absorption tower I section bottom is provided with the 5th entrance and the 4th outlet, and the top of ammonia absorption tower ii section sets
It is equipped with the 6th entrance, in the middle part of described ammonia absorption tower ii I section, be provided with the 7th entrance, described ammonia absorption tower ii I section top
Portion is provided with the 8th entrance and the 5th outlet；Or described ammonia absorption tower I section bottom is provided with the 5th entrance and the 4th and goes out
Mouthful, the top of ammonia absorption tower ii section is provided with the 6th entrance, and the middle part of described ammonia absorption tower ii section is provided with the 9th
Entrance, is provided with the 7th entrance in the middle part of described ammonia absorption tower ii I section, described ammonia absorption tower ii I section top is provided with
8th entrance and the 5th outlet；Described ammonia absorption tower ii I section bottom is provided with the 6th outlet；
The bottom of towe of described ammonia rectifying column is provided with tower reactor reboiler and the 7th outlet, and the middle part of ammonia rectifying column is provided with the tenth
Entrance or the tenth entrance and the 11st entrance, the top of described ammonia rectifying column is provided with the 8th outlet and the 12nd entrance；
Convert lime set delivery pipe one side from converting means containing ammonia by the first pipeline and the 4th of described stripper top
Entrance connects, and is on the other hand connected with the first medium entrance of first heat exchanger by the second pipeline, first heat exchanger
First medium outlet is connected with the first medium entrance of second heat exchanger by the 3rd pipeline, first Jie of second heat exchanger
Matter outlet is connected with the second entrance on described stripper top by the 4th pipeline；
The outlet of lye tank (vat) is connected with the entrance of the first pump by the 5th pipeline, the outlet of the first pump pass through the 6th pipeline with described
First entrance in the middle part of stripper connects；The first outlet of stripper bottom is connected with the entrance of the second pump by the 7th pipeline,
Described second pump outlet be connected with the second medium entrance of described second heat exchanger by the 8th pipeline, described second heat
The second medium outlet of exchanger is connected with the entrance of the 3rd heat exchanger by the 9th pipeline, and the outlet of the 3rd heat exchanger is even
Connect waste water outlet tube；
3rd outlet of stripper top connects a sour gas outlet tube, the 3rd entrance on stripper top pass through the tenth pipeline and
4th outlet of the 3rd pump and described ammonia absorption tower I section bottom is connected, and the second outlet in the middle part of described stripper is by the
11 pipelines are connected with the second medium entrance of described first heat exchanger, and the second medium outlet of described first heat exchanger is logical
The 5th entrance crossing the 12nd pipeline with described ammonia absorption tower I section bottom is connected；
5th outlet at described ammonia absorption tower ii I section top connects a fixed gas outlet tube；Described ammonia absorption tower ii I
8th entrance at section top connects a desalination water inlet pipe；
The 7th entrance in the middle part of described ammonia absorption tower ii I section passes through first Jie that the 13rd pipeline connects the 5th heat exchanger
Matter entrance, the first medium outlet of described 5th heat exchanger connects the first of described 4th heat exchanger by the 14th pipeline
Medium inlet, the first medium outlet of described 4th heat exchanger connects described ammonia rectifying tower bottom by the 15th pipeline
7th outlet connects；6th entrance at described ammonia absorption tower ii section top is connected to described first pump by the 16th pipeline
Outlet；6th entrance at described ammonia absorption tower ii section top connects described waste water outlet tube also by the 17th pipeline
On, the 9th entrance in the middle part of described ammonia absorption tower ii section connects on described 13rd pipeline also by the 18th pipeline；Institute
The 6th outlet stating ammonia absorption tower ii I section bottom is connected to the entrance of the 4th pump by the 19th pipeline, described 4th pump
Outlet by the 20th pipeline connect described 4th heat exchanger second medium entrance, the second of described 4th heat exchanger
Media outlet passes through the 21st pipeline and connects the tenth entrance connection in the middle part of described ammonia rectifying column；
Or, the 7th entrance one side in the middle part of described ammonia absorption tower ii I section is passed through the 22nd pipeline and is connected described giving up
Water delivery pipe, on the other hand connects the tenth entrance in the middle part of described ammonia rectifying column by the 23rd pipeline；Described ammonia
6th entrance at absorption tower ii section top passes through the 24th pipeline and connects on described 22nd pipeline；Described ammonia absorption
6th outlet of tower ii I section bottom is connected to the entrance of the 4th pump by the 19th pipeline, and the outlet of described 4th pump is passed through
25th pipeline connects the entrance of described 5th heat exchanger, and the 26th pipeline is passed through in the outlet of described 5th heat exchanger
Connect on described 23rd pipeline, the outlet of described 5th heat exchanger connects described ammonia essence also by the 27th pipeline
Evaporate the 11st entrance in the middle part of tower；7th outlet at described ammonia rectifying tower bottom connects described waste water by the 28th pipeline
Outlet tube；
8th outlet at described ammonia rectifying column top connects the entrance of described 6th heat exchanger, institute by the 29th pipeline
The outlet stating the 6th heat exchanger connects the entrance of a storage tank by the 30th pipeline, and the outlet of described storage tank passes through the 31st
Pipeline connects the entrance of the 5th pump, and on the one hand the outlet of described 5th pump connects liquefied ammonia outlet tube, on the other hand pass through the 30th
Two pipelines connect the 12nd entrance at described ammonia rectifying column top.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106964174A (en) * | 2017-05-17 | 2017-07-21 | 万和昌 | Rectifying/the method for purification and system of ammonia |
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|---|---|---|---|---|
| EP0005292A1 (en) * | 1978-04-29 | 1979-11-14 | Stamicarbon B.V. | Process for the separation of ammonia and carbon dioxide from mixtures containing ammonia, carbon dioxide and water |
| CN103408086A (en) * | 2013-08-02 | 2013-11-27 | 天华化工机械及自动化研究设计院有限公司 | MVR (Mechanical Vapor Recompression) vapor-stripping deamination system and application method thereof |
| CN104355353A (en) * | 2014-10-22 | 2015-02-18 | 青岛拓联信息技术有限公司 | Efficient water cleaning agent |
| CN206126864U (en) * | 2016-10-15 | 2017-04-26 | 上海国际化建工程咨询有限公司 | It prepares device of pure liquid ammonia to contain ammonia transform lime set waste water |
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2016
- 2016-10-15 CN CN201610899250.2A patent/CN106395858B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0005292A1 (en) * | 1978-04-29 | 1979-11-14 | Stamicarbon B.V. | Process for the separation of ammonia and carbon dioxide from mixtures containing ammonia, carbon dioxide and water |
| CN103408086A (en) * | 2013-08-02 | 2013-11-27 | 天华化工机械及自动化研究设计院有限公司 | MVR (Mechanical Vapor Recompression) vapor-stripping deamination system and application method thereof |
| CN104355353A (en) * | 2014-10-22 | 2015-02-18 | 青岛拓联信息技术有限公司 | Efficient water cleaning agent |
| CN206126864U (en) * | 2016-10-15 | 2017-04-26 | 上海国际化建工程咨询有限公司 | It prepares device of pure liquid ammonia to contain ammonia transform lime set waste water |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106964174A (en) * | 2017-05-17 | 2017-07-21 | 万和昌 | Rectifying/the method for purification and system of ammonia |
| CN106964174B (en) * | 2017-05-17 | 2024-02-13 | 万和昌 | Method and system for rectifying/purifying ammonia |
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