CN106395858B - A kind of method and device converting lime set waste water making pure liquefied ammonia containing ammonia - Google Patents
A kind of method and device converting lime set waste water making pure liquefied ammonia containing ammonia Download PDFInfo
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- CN106395858B CN106395858B CN201610899250.2A CN201610899250A CN106395858B CN 106395858 B CN106395858 B CN 106395858B CN 201610899250 A CN201610899250 A CN 201610899250A CN 106395858 B CN106395858 B CN 106395858B
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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
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Abstract
A kind of method converting lime set waste water making pure liquefied ammonia containing ammonia disclosed by the invention produces qualified pure liquefied ammonia on the basis of single column pressurization lateral line withdrawal function stripping+cooling absorbs by the way of adding rectifying column.This method solve containing in routine variations lime set air lift flow, ammonia transformation lime set processing is not up to standard, and useless ammonia can only go the problem of fired downstream discharge nitrogen oxides.The invention also discloses a kind of devices converting lime set waste water making pure liquefied ammonia containing ammonia.
Description
Technical field
The present invention relates to one kind converting lime set waste water making pure liquefied ammonia technical field containing ammonia, more particularly to a kind of to be converted containing ammonia
The method and device of lime set waste water making pure liquefied ammonia.
Background technology
China is the few country of the more gas of coal, currently, it is raw material that most of chemical enterprises, which are all made of coal, and conversion section is
Each essential workshop section of 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 a large amount of ammonia-containing water after heat exchange is cooling.The transformation lime set waste water especially generated in coal-water slurry gasification
In ammonia content to be higher by fine coal gasification process very much.
Mainly there is single column steam air lift, double to the processing for converting lime set waste water containing ammonia in the coal plant being currently in operation
The modes such as tower strips and single column pressurization side line takes out ammonia stripping, single column pressurization lateral line withdrawal function stripping+cooling absorbs.
As shown in Figure 1, single column steam air lift main flow is described as follows：The condensed device of all condensate liquids in conversion section
It is sent after 1 heating to 2 top of transformation stripper, the bottom of tower of transformation stripper 2 is passed through a certain amount of low-pressure steam.It converts in lime set
Light component is separated under the action of steam air lift from transformation lime set, is discharged from stripper top, after condensed device 1 condenses
It is sent into gas-liquid separator 3 and is separated into sour gas and condensation sewage.Sour gas is discharged into torch or sulfur recovery unit, the warp of liquid containing ammonia condensing
After condenser 4 condenses, returns to stripper top by pump 5 or do not flow back and be used as wastewater disposition.
This flow exists following insufficient：
(1) H in coal is typically contained in the transformation lime set from conversion section2S、CO2, ammonia, Cl-、CN-Etc. components.
These components are fed directly to if not being pocessed in transformation stripper, it will to transformation stripper, tower internals and its auxiliary device
Generate corrosion.All have there are problems in current numerous coal plants.
(2) as converted lime set using the processing of above-mentioned single column steam gas stripping process, if the liquid containing ammonia condensing of dephlegmator of top of the tower
It does not flow back, then there is stripping sewage to need outer row.If condensate liquid return stripper in participate in washing, carbon dioxide, hydrogen sulfide and
Ammonia can then be accumulated in reflux process, cause the corrosion and blocking of equipment, pipeline.
(3) as using above-mentioned single column steam gas stripping process processing transformation lime set, stripper overhead discharge be carbon dioxide,
The gaseous mixture of hydrogen sulfide and ammonia, in subsequent condensation process, vapor delivery line because cooling when carbon dioxide, hydrogen sulfide and ammonia easily
Generate NH4HS and NH4HCO3Ammonium salt crystallization causes the corrosion and line clogging of stripper overhead column plate, overhead condenser.
(4) as using above-mentioned single column steam gas stripping process processing transformation lime set, ammonia carries out burning disposal as harmful substance,
Not only waste of resource also results in environmental pollution.
As shown in Fig. 2, double tower stripping main flow is described as follows：It is heated rear into urea carbon dioxide stripper to convert lime set
10 tops, 10 bottom of tower of urea carbon dioxide stripper are passed through the secondary low-voltage steam of 20 top output of aminoacid stripping tower.Carbon dioxide and sulphur
Change hydrogen from 10 top discharge of urea carbon dioxide stripper, condensed device 30 is sent into gas-liquid separator 40 after condensing and is separated into acidity
Gas and condensation sewage, solidifying sour gas is not discharged into torch or sulfur recovery workshop section, urea carbon dioxide stripper at gas-liquid separator 40 top
10 bottom lime set waste water enter 20 top of aminoacid stripping tower, and aminoacid stripping tower 20 is passed through a certain amount of low-pressure steam, and ammonia steam is from ammonia vapour
20 tower top of stripper is discharged, and after condenser 50 once condensation, is sent into gas-liquid separator 60 and carries out gas-liquid separation, obtain rich ammonia
Gas and condensation sewage, condensation sewage are returned as level-one condensate liquid in aminoacid stripping tower 20, and it is cold that rich ammonia passes through condenser 70 2 times
It is sent into gas-liquid separator 80 after solidifying and carries out gas-liquid separation, the condensation sewage that gas-liquid separator 80 detaches is as B-grade condensation liquid conduct
Wastewater disposition, rich ammonia are discharged into torch or sulfur recovery workshop section.
This flow overcomes the segmental defect in single column steam air lift, but still assigns ammonia as detoxication, does not have
There is recycling, there is sewage to need outer row in flow.
As shown in figure 3, single column pressurization lateral line withdrawal function stripping main flow is described as follows：
Lime set is converted after condenser 10a and heater 20a is condensed and heated respectively, is divided to hot and cold two stock not from vapour
The top and middle and upper part of stripper 30a enters stripper 30a, the CO being stripped off2、H2The sour gas such as S and Ammonia, vapor by
It is sent out at the top of stripper 30a, is sent directly into torch or sulfur recovery unit.The ammonia converted in 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 come by side extraction and divides
After liquid, the thick ammonia of higher concentration is obtained, send to ammonia refining part and is further processed.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 is condensed by three-level, can obtain a concentration of 99% or so rich ammonia, wherein CO2Content is about
20ppm, H2S contents are about 1000ppm, but still cannot be used directly to prepare H2The content of S is less than 100ppm, a concentration of
20% qualified weak aqua ammonia.
(2) second level condensation temperature usually in three-level condenser system is controlled at 70-90 DEG C, to which further condensation is certain
The water and hydrogen sulfide of amount and the concentration for improving ammonia in gas phase.But hydrogen sulfide enhances the corrosion of steel with the raising of temperature,
80 DEG C of corrosion rates reach highest, and after temperature increases again, corrosion rate starts to reduce, and at 110-120 DEG C, corrosion rate reaches
It is minimum.
(3) three-level condensation flow includes three heat exchangers and three liquid separation tanks, is taken 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：
The lime set containing ammonia transformation from converting means is divided into two parts, and a part is by thermal converter E1, E2 heat exchange heating
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 reboilers E3 is logical
Enter a certain amount of low pressure steam, the transformation lime set to entering tower strips.The bottoms of tower stripper T1 are the purification and condensation liquid of qualification
It is sent to downstream unit after pump P1, thermal converter E2, E4 cooling.Most of H2S、CO2Etc. components evaporated from stripper T1 tower tops
Go out, part H2S、NH3、H2The components such as O from stripper T1 lateral line withdrawal functions, then enter back into heat exchanger E1 be cooled to 115 DEG C or so into
Enter the I section bottom to ammonium hydroxide absorption tower T2.Liquid phase from ammonium hydroxide absorption tower T2 Section II sections bottom is entered by gravity
At the top of to ammonium hydroxide absorption tower T2 Is section.Cooling absorb comes from ammonium hydroxide absorption tower T2 I sections bottom rising part H2S.Through supercooling
The gas phase of absorption enters ammonium hydroxide absorption tower T2 Section II sections bottom by chimney plate, send to ammonium hydroxide and inhales from Partial cleansing condensate liquid
Receive cooling absorption ammonium hydroxide absorption tower T2 Section II sections bottom rising part H at the top of tower T2 Section II section2S.The gas phase absorbed through supercooling
Ammonium hydroxide absorption tower T2 Section III sections bottom is entered by chimney plate.Then it is sent to ammonium hydroxide and is absorbed using Partial cleansing condensate liquid again
The cooling part NH for absorbing ammonium hydroxide absorption tower Section II section bottom and rising at the top of tower T2 Section III section3.It is final to produce qualified dilute ammonia
Water.It is higher from ammonium hydroxide absorption tower Section III section bottom weak aqua ammonia temperature at this time due to absorbing heat release, finally by aqua ammonia pump P3
It send to the E5 coolings of ammonium hydroxide cooler and sends out battery limit (BL).Another part weak aqua ammonia after cooling is as refrigerant circulation to ammonium hydroxide absorption tower
At the top of T2 Section III section, the cleaning solution from ammonium hydroxide absorption tower T2 I sections bottom is sent into the middle and upper part of stripper T1 by pumping P2.
This flow improves to some extent, but there is also following deficiencies：
(1) through air lift and it is cooling absorb after, only produce a concentration of 20% qualified weak aqua ammonia, and the product of such specification
Market purposes is few, and market potential is low, can not efficiently use.
(2) such as stripper operation fluctuation, it is easy to happen the exceeded problem of hydrogen sulfide in weak aqua ammonia.
Invention content
The first technical problem to be solved by the present invention be for single column pressurization lateral line withdrawal function strip+cool down absorption process
The problems of and provide it is a kind of containing ammonia convert lime set waste water making pure liquefied ammonia method, this method single column pressurization side line take out
Go out on the basis of stripping+cooling absorption, qualified pure liquefied ammonia is produced by the way of adding rectifying column.This method solve normal
The transformation lime set processing containing ammonia is not up to standard in rule transformation lime set air lift flow, and useless ammonia can only remove fired downstream discharge nitrogen oxides
Problem.
The second technical problem to be solved by the present invention is to provide the device for realizing the above method.
The technical problems to be solved by the invention can be achieved through the following technical solutions：
A method of lime set waste water making pure liquefied ammonia being converted containing ammonia, the lime set containing ammonia transformation from converting means is divided into two
Part, a part enter the middle and upper part of stripper after First Heat Exchanger, the heat exchange heating of the second heat exchanger, and another part is direct
It is sent into the top of stripper, stripper tower bottom reboiler is passed through a certain amount of low pressure steam, solidifying to the transformation for entering stripper
Liquid is stripped；A small amount of lye is sent into the middle part of stripper, and most of lye is first fed at the top of the Section II section of absorption tower, is then back to
It is neutralized with the transformation lime set containing ammonia in the middle part of stripper；
Qualified purification and condensation liquid is sent out in stripper bottom of tower, big after the second heat exchanger, the cooling of third heat exchanger successively
Part is sent to downstream unit, and fraction purification and condensation liquid is admitted to top or/and the ammonium hydroxide absorption tower of ammonium hydroxide absorption tower Section II section
The middle part of Section III section；
Most of H2S and CO2It distillates to form sour gas submitting, fraction H from stripper overhead2S 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 the ammonium hydroxide absorption tower bottoms IDuan；
Liquid phase from ammonium hydroxide absorption tower Section II section bottom is entered by gravity at the top of the I section of ammonium hydroxide absorption tower,
Cooling absorb comes from the ammonium hydroxide absorption tower bottoms IDuan rising part H2S, through supercooling absorb gas phase by the first chimney plate into
Enter to ammonium hydroxide absorption tower Section II section bottom；
The fraction purification and condensation liquid that is admitted at the top of the Section II section of ammonium hydroxide absorption tower is admitted to ammonium hydroxide absorption tower Section II section
The fraction purification and condensation liquid at top cooling ammonium hydroxide that absorbs together with the lye being admitted at the top of the Section II section of ammonium hydroxide absorption tower absorbs
Tower Section II section bottom rising part H2S, the gas phase absorbed through supercooling enter ammonium hydroxide absorption tower Section III by the second chimney plate
Section bottom；
The desalted water that is sent at the top of the Section III section of ammonium hydroxide absorption tower is sent to de- at the top of the Section III section of ammonium hydroxide absorption tower
Brine but absorbs ammonium hydroxide absorption tower Section II section bottom with the fraction purification and condensation liquid cooling being admitted in the middle part of the Section III section of ammonium hydroxide absorption tower
Portion rising part NH3；
Cleaning solution from the ammonium hydroxide absorption tower bottoms IDuan is sent into the middle and upper part of stripper；
Weak aqua ammonia from ammonium hydroxide tower bottom of rectifying tower after the 4th heat exchanger and the heat exchange cooling of the 5th heat exchanger by being used as suction
It receives agent and returns to the top in the middle part of the Section III section of ammonium hydroxide absorption tower with Section II section, to produce not hydrogen sulfide containing ammonium hydroxide；Or come
From the weak aqua ammonia of ammonium hydroxide tower bottom of rectifying tower directly with by the second heat exchanger exchange heat stripper bottom of tower after cooling send out it is qualified
After the mixing of purification and condensation liquid, then sent to downstream unit after the cooling of third heat exchanger；
Qualified ammonium hydroxide is sent into the middle part of ammonium hydroxide rectifying column, as charging after pressure-raising preheats；Ammonium hydroxide rectifying column tower top is steamed
Vapour obtains ammonia lime set after cooling water condensation, and part ammonia lime set is used as back to ammonium hydroxide rectifying column top through reflux pump and flows back, separately
Outer a part of ammonia lime set is sent as product liquefied ammonia to out-of-bounds；
Ammonium hydroxide tower bottom of rectifying tower reboiler provides heat by low-pressure steam or process-stream cooling.
The weak aqua ammonia that ammonium hydroxide absorption tower Section III section bottom is sent out is sent into after being heated by the 4th heat exchanger in ammonium hydroxide rectifying column
The weak aqua ammonia part that portion or ammonium hydroxide absorption tower Section III section bottom are sent out is sent directly into the middle and lower part of ammonium hydroxide rectifying column, another
Part is divided into two after condenser condenses, and one is sent directly into the middle part of ammonium hydroxide rectifying column, and another Zhi Zuowei absorbents are sent into
It is but absorbed with the fraction purification and condensation liquid cooling being admitted in the middle part of the Section III section of ammonium hydroxide absorption tower in the middle part of the Section III section of ammonium hydroxide absorption tower
Ammonium hydroxide absorption tower Section II section bottom rising part NH3。
A kind of device converting lime set waste water making pure liquefied ammonia containing ammonia, including stripper, ammonium hydroxide absorption tower and ammonium hydroxide rectifying
Tower；
The bottom of the stripper is provided with stripper tower bottom reboiler and first outlet, middle part be provided with first entrance and
Second outlet, top are provided with second and third entrance, and top is provided with the 4th entrance and third outlet；
The ammonium hydroxide absorption tower bottoms IDuan are provided with the 5th entrance and the 4th outlet, the top of ammonium hydroxide absorption tower Section II section
Portion is provided with the 6th entrance, and the 7th entrance, ammonium hydroxide absorption tower Section III are provided in the middle part of the ammonium hydroxide absorption tower Section III section
Section top is provided with the 8th entrance and the 5th outlet；Or the ammonium hydroxide absorption tower bottoms IDuan are provided with the 5th entrance and
Four export, and are provided with the 6th entrance at the top of the Section II section of ammonium hydroxide absorption tower, are provided in the middle part of the ammonium hydroxide absorption tower Section II section
9th entrance, the ammonium hydroxide absorption tower Section III section middle part are provided with the 7th entrance, are set at the top of the ammonium hydroxide absorption tower Section III section
It is equipped with the 8th entrance and the 5th outlet；Ammonium hydroxide absorption tower Section III section bottom is provided with the 6th outlet；
The bottom of tower of the ammonium hydroxide rectifying column is provided with tower reactor reboiler and the 7th outlet, is provided in the middle part of ammonium hydroxide rectifying column
Tenth entrance or the tenth entrance and the 11st entrance are provided with the 8th outlet and the 12nd at the top of the ammonium hydroxide rectifying column and enter
Mouthful；
On the one hand the transformation lime set delivery pipe containing ammonia from converting means passes through the first pipeline and the stripper top
4th entrance connects, and is on the other hand connected by the second pipeline and the first medium entrance of first heat exchanger, the first heat exchange
The first medium outlet of device is connected by the first medium entrance of third pipeline and second heat exchanger, and the of second heat exchanger
One media outlet is connect by the 4th pipeline with the second entrance on the stripper top；
The outlet of lye tank (vat) connect by the 5th pipeline with the entrance of the first pump, the first outlet pumped by the 6th pipeline and
First entrance connection in the middle part of the stripper；
The first outlet of stripper bottom is connect by the 7th pipeline with the entrance of the second pump, and the outlet of second pump is logical
It crosses the 8th pipeline to connect with the second medium entrance of the second heat exchanger, the second medium outlet of the second heat exchanger
It is connect with the entrance of third heat exchanger by the 9th pipeline, the outlet of third heat exchanger connects waste water efferent duct；
The one sour gas efferent duct of third outlet connection of stripper top, the third entrance on stripper top pass through the tenth pipe
Line and third pump and the 4th outlet of the ammonium hydroxide absorption tower bottoms IDuan connect, and the second outlet in the middle part of the stripper is logical
It crosses the 11st pipeline to connect with the second medium entrance of the first heat exchanger, the second medium of the first heat exchanger goes out
Mouth is connect by the 12nd pipeline with the 5th entrance of the ammonium hydroxide absorption tower bottoms IDuan；
The 5th one fixed gas efferent duct of outlet connection at the top of the ammonium hydroxide absorption tower Section III section；The ammonium hydroxide absorption tower
The 8th entrance at the top of Section III section connects a desalination water inlet pipe；
The 7th entrance in the middle part of the ammonium hydroxide absorption tower Section III section connects the of the 5th heat exchanger by the 13rd pipeline
The first medium outlet of one medium inlet, the 5th heat exchanger connects the first of the 4th heat exchanger by the 14th pipeline
Medium inlet, the first medium of the 4th heat exchanger is exported connects ammonium hydroxide rectifying tower bottom by the 15th pipeline
7th outlet connection；The 6th entrance at the top of the ammonium hydroxide absorption tower Section II section is connected to first pump by the 16th pipeline
Outlet；The 6th entrance at the top of the ammonium hydroxide absorption tower Section II section also connects the waste water efferent duct by the 17th pipeline
On, the 9th entrance in the middle part of the ammonium hydroxide absorption tower Section II section is also connected by the 18th pipeline on the 13rd pipeline；Institute
The 6th outlet for stating ammonium hydroxide absorption tower Section III section bottom is connected to the entrance of the 4th pump, the 4th pump by the 19th pipeline
Outlet connect the second medium entrance of the 4th heat exchanger by the 20th pipeline, the second of the 4th heat exchanger
Media outlet connects the connection of the tenth entrance in the middle part of the ammonium hydroxide rectifying column by the 21st pipeline；
Alternatively, on the one hand the 7th entrance in the middle part of the ammonium hydroxide absorption tower Section III section connects institute by the 22nd pipeline
Waste water efferent duct is stated, the tenth entrance being on the other hand connected to by the 23rd pipeline in the middle part of the ammonium hydroxide rectifying column；It is described
The 6th entrance at the top of the Section II section of ammonium hydroxide absorption tower is connected by the 24th pipeline on the 22nd pipeline；The ammonium hydroxide
6th outlet of absorption tower Section III section bottom is connected to the entrance of the 4th pump, the outlet of the 4th pump by the 19th pipeline
The entrance of the 5th heat exchanger is connected by the 25th pipeline, the outlet of the 5th heat exchanger passes through the 26th
Pipeline connects on the 23rd pipeline, and the outlet of the 5th heat exchanger also connects the ammonia by the 27th pipeline
The 11st entrance in the middle part of crystal evaporate tower；7th outlet at ammonium hydroxide rectifying tower bottom passes through described in the connection of the 28th pipeline
Waste water efferent duct；
The 8th outlet at the top of the ammonium hydroxide rectifying column connects entering for the 6th heat exchanger by the 29th pipeline
Mouthful, the outlet of the 6th heat exchanger connects the entrance of a storage tank by the 30th pipeline, and the outlet of the storage tank passes through the
On the one hand the outlet of the entrance of the 5th pump of 31 pipelines connection, the 5th pump connects liquefied ammonia efferent duct, on the other hand pass through
32nd pipeline connects the 12nd entrance at the top of the ammonium hydroxide rectifying column.
As a result of technical solution 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 is had the following advantages that：
Replace traditional three-level to condense flow 1. ammonium hydroxide absorption tower is arranged, cooling, Absorption Desulfurization and ammonium hydroxide are produced and are combined into
One reduces equipment investment and occupation of land.
2. being sent to above-mentioned ammonium hydroxide absorption tower Section II as cooling and absorbent using Partial Transformation lime set of the processing after qualified
Section top, the H being not only effectively reduced in gas phase2S contents can also reduce the temperature of gas phase.Temperature just avoids at this time
The optimum temperature of corrosion.
3. being sent to above-mentioned ammonium hydroxide absorption tower Section III as cooling and absorbent using Partial Transformation lime set of the processing after qualified
Section top, the use for saving desalted water is absorbed compared to traditional ammonium hydroxide.
4. due to NH3After stripper is by lateral line withdrawal function, it is substantially free of ammonia in tower top sour gas, avoids ammonium salt in stripper
The crystallization and corrosion of tower top.Tower top sour gas can be fed directly to downstream Crouse and recycle sulphur thus.
5. since H is also free of in purification and condensation liquid substantially2S、NH3Equal substances, can be fed directly to gasification or biochemical treatment subtracts
The light burden of wastewater disposition.
6. being additionally arranged ammonium hydroxide rectifying column with the liquefied ammonia product qualified in tower top production.
7. ammonium hydroxide rectifying column pressurized operation ensures that rectifying tower top condenser temperature is higher, the cold of common specification may be used
But water can meet cooling requirement, need not consume low temperature cold.
8. pair newly upper lime set processing unit, ammonium hydroxide tower bottom of rectifying tower produce weak aqua ammonia, return to ammonium hydroxide absorption tower.Although therefore
Ammonium hydroxide rectifying column pressurized operation, bottom temperature is not also excessively high, can meet rectifying heat demand using low-pressure steam.
9. for device is transformed, as front side line air lift and it is cooling absorption plant is constructed finishes, then increase ammonium hydroxide newly
Tower bottom of rectifying tower, which produces, meets the waste water of environmental requirement, at this time rectifying tower reboiler need to use the higher middle pressure steam of potential temperature or
Process-stream is as heat source.
10. in order to ensure the pre- anticorrosion of product liquid ammonia quality, lye can be added in the middle part of stripper and ammonium hydroxide absorption tower.
11. for small-scale device, the condenser of ammonium hydroxide rectifying column tower top can be integrated with rectifying column, to save
One return tank and a reflux pump.
12. the weak aqua ammonia of ammonium hydroxide tower bottom of rectifying tower returns in the middle part of ammonium hydroxide absorption tower Section III section and the after recuperation of heat cools down
Two sections of tops are recycled as absorbent.
The present invention contains ammonia transformation lime set wastewater treatment process for a kind of at present by reconfiguring, to solve to contain ammonia at present
Transformation lime set waste water can not handle or the too low no market outlet problem of ammonium hydroxide quality after treatment.
Description of the drawings
Fig. 1 is the schematic device that existing single column steam air lift converts lime set waste water making pure liquefied ammonia containing ammonia.
Fig. 2 is that existing double tower strips the schematic device that lime set waste water making pure liquefied ammonia is converted 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 that lime set waste water making pure liquefied ammonia is converted containing ammonia
Set schematic diagram.
Fig. 5 is the schematic device that lime set waste water making pure liquefied ammonia is converted containing ammonia of the embodiment of the present invention 1.
Fig. 6 is the schematic device that lime set waste water making pure liquefied ammonia is converted containing ammonia of the embodiment of the present invention 2.
Specific implementation mode
Embodiment 1
Referring to Fig. 5, the device shown in figure that lime set waste water making pure liquefied ammonia is converted containing ammonia is mainly used for newly-increased lime set
Air-lift device comprising stripper 100, ammonium hydroxide absorption tower 200 and ammonium hydroxide 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 120 He of entrance
Outlet 130, top are provided with entrance 140,150, and top is provided with entrance 160 and outlet 170.
200 I section bottom of ammonium hydroxide absorption tower is provided with entrance 210 and outlet 220, the top of 200 Section II section of ammonium hydroxide absorption tower
Portion is provided with entrance 230, and entrance 240,200 Section III section top of ammonium hydroxide absorption tower are provided in the middle part of 200 Section III section of ammonium hydroxide absorption tower
Portion is provided with entrance 250 and outlet 260.It is provided with entrance 270, ammonium hydroxide absorption tower 200 in the middle part of 200 Section II section of ammonium hydroxide absorption tower
The bottom of Section III section is provided with outlet 280.
The bottom of tower of ammonium hydroxide rectifying column 300 is provided with tower reactor reboiler E7 and outlet 310, and the middle part of ammonium hydroxide rectifying column 300 is set
It is equipped with entrance 320, the top of ammonium hydroxide rectifying column 300 is provided with outlet 330 and entrance 340.
Pass through 100 top of pipeline 402 and stripper containing 401 one side of ammonia transformation lime set delivery pipe from converting means
Entrance 160 connects, and is on the other hand connect with the first medium entrance of heat exchanger E1 by pipeline 403, and the of heat exchanger E1
One media outlet is connect by pipeline 404 with the first medium entrance of heat exchanger E2, the first medium outlet of heat exchanger E2
It is connect with the entrance 140 on 100 top of stripper by pipeline 405.
The outlet of lye tank (vat) V1 is connect by pipeline 406 with the entrance for pumping P3, and the outlet for pumping P3 passes through pipeline 407 and stripping
The entrance 120 at 100 middle part of tower connects.
The outlet 110 of 100 bottom of stripper is connect by pipeline 408 with the entrance of pump P1, and the outlet for pumping P1 passes through pipeline
409 connect with the second medium entrance of heat exchanger E2, and the second medium outlet of heat exchanger E2 passes through pipeline 410 and heat exchange
The entrance of device E4 connects, the outlet connection waste water efferent duct 411 of heat exchanger E4.
The outlet 170 at 100 top of stripper connects a sour gas efferent duct 412, and the entrance 150 on 100 top of stripper is logical
It crosses pipeline 412a and pump P2 is connect with the outlet 220 of 200 I section bottom of ammonium hydroxide absorption tower, the outlet 130 at 100 middle part of stripper
It is connect with the second medium entrance of heat exchanger E1 by pipeline 413, the second medium outlet of heat exchanger E1 passes through pipeline 414
It is connect with the entrance 210 of 200 I section bottom of ammonium hydroxide absorption tower.
Outlet 260 at the top of 200 Section III section of ammonium hydroxide absorption tower connects a fixed gas efferent duct 415；Ammonium hydroxide absorption tower
The entrance 250 at 200 top of III sections connects a desalination water inlet pipe 416.
Entrance 240 in the middle part of 200 Section III section of ammonium hydroxide absorption tower connects the first medium of heat exchanger E8 by pipeline 417
Entrance, the first medium outlet of heat exchanger E8 connect the first medium entrance of heat exchanger E5, heat exchanger by pipeline 418
The outlet 310 that the first medium outlet of E5 connects 300 bottom of tower of ammonium hydroxide rectifying column by pipeline 419 connects；Ammonium hydroxide absorption tower 300
230 one side of entrance at II sections of tops is connected to the outlet of pump P3 by pipeline 420, is on the other hand connected by pipeline 421 useless
Water delivery pipe 411.
Entrance 270 in the middle part of 300 Section II section of ammonium hydroxide absorption tower is also by 422 connecting pipeline 417 of pipeline；Ammonium hydroxide absorption tower
The outlet 280 of 300 Section III section bottoms is connected to the entrance of pump P4 by pipeline 423, and the outlet for pumping P4 is connected by pipeline 424
The second medium outlet of the second medium entrance of heat exchanger E5, heat exchanger E5 connects ammonium hydroxide rectifying column 300 by pipeline 425
The entrance 320 at middle part connects.
The outlet 330 at 300 top of ammonium hydroxide rectifying column connects the entrance of heat exchanger E6, heat exchanger E6 by pipeline 426
Outlet by pipeline 427 connect a storage tank V2 entrance, storage tank V2 outlet by pipeline 428 connection pump P5 entrance, pump
On the one hand the outlet of P5 connects liquefied ammonia efferent duct 429, on the other hand pass through pipeline 430 and connect entering for 300 top of ammonium hydroxide rectifying column
Mouth 340.
The lime set containing ammonia transformation from converting means is divided into two parts, and a part is through over-heat-exchanger E1, E2 heat exchange heating
Enter 100 middle and upper part of stripper afterwards.100 tower bottom reboiler E3 of stripper is passed through a certain amount of low pressure steam, to entering the change of tower
Lime set is changed to be stripped.100 bottom of tower of stripper is that qualified purification and condensation liquid is sent after over-heat-exchanger E4 coolings to downstream dress
It sets.Most of H2S、CO2Etc. components distillated from 100 tower top of stripper, part H2S、NH3、H2The components such as O are from lateral line withdrawal function, then
It enters back into heat exchanger E1 and is cooled to 110~120 DEG C and enter 300 I section bottom of ammonium hydroxide absorption tower.From ammonium hydroxide absorption tower
The liquid phase of 200 Section II section bottoms is entered by gravity at the top of 200 I section of ammonium hydroxide absorption tower.Cooling absorb comes from ammonium hydroxide
200 I section bottom rising part H of absorption tower2S.The gas phase absorbed through supercooling enters ammonium hydroxide absorption tower 20 by chimney plate
Section II section bottom is sent from Partial cleansing condensate liquid and lye to 200 Section II section of ammonium hydroxide absorption tower, and the cooling ammonium hydroxide that absorbs is inhaled
Receive 200 Section II section bottom rising part H of tower2S.The gas phase absorbed through supercooling enters ammonium hydroxide absorption tower 200 by chimney plate
Section III section bottom.Then it is sent again to cooling absorption ammonium hydroxide absorption tower 300 at the top of 200 Section III section of ammonium hydroxide absorption tower using desalted water
Section II section bottom rising part NH3, the weak aqua ammonia from 300 tower reactor of ammonium hydroxide rectifying column is also fed into 200 Section III section of ammonium hydroxide absorption tower
Middle part is as absorbent, to produce not hydrogen sulfide containing ammonium hydroxide.
Qualified ammonium hydroxide is sent into ammonium hydroxide rectifying column 300 as charging after pressure-raising preheats.300 tower top ammonia of ammonium hydroxide rectifying column
Steam obtains ammonia lime set after cooling water condensation, and part ammonia lime set is used as reflux through pumping P5 back to 300 top of ammonium hydroxide rectifying column,
Another part ammonia lime set is sent as product liquefied ammonia to out-of-bounds.300 tower reactor reboiler E7 of ammonium hydroxide rectifying column by low-pressure steam or
Process-stream cooling provides heat, and the weak aqua ammonia of 300 tower reactor of ammonium hydroxide rectifying column extraction is through heat exchanger E5 heat exchange and heat exchanger
After E8 coolings 200 Section III section middle part of ammonium hydroxide absorption tower and second segment top are returned to as absorbent.
Embodiment 2
Referring to Fig. 6, the device shown in figure that lime set waste water making pure liquefied ammonia is converted containing ammonia is mainly used for the solidifying of reworked
Liquid air-lift device comprising stripper 100, ammonium hydroxide absorption tower 200 and ammonium hydroxide 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 120 He of entrance
Outlet 130, top are provided with entrance 140,150, and top is provided with entrance 160 and outlet 170.
200 I section bottom of ammonium hydroxide absorption tower is provided with entrance 210 and outlet 220, the top of 200 Section II section of ammonium hydroxide absorption tower
Portion is provided with entrance 230, and entrance 240,200 Section III section top of ammonium hydroxide absorption tower are provided in the middle part of 200 Section III section of ammonium hydroxide absorption tower
Portion is provided with entrance 250 and outlet 260.The bottom of 200 Section III section of ammonium hydroxide absorption tower is provided with outlet 280.
The bottom of tower of ammonium hydroxide rectifying column 300 is provided with tower reactor reboiler E7 and outlet 310, and the middle part of ammonium hydroxide rectifying column 300 is set
It is equipped with entrance 320,350, the top of ammonium hydroxide rectifying column 300 is provided with outlet 330 and entrance 340.
Pass through 100 top of pipeline 402 and stripper containing 401 one side of ammonia transformation lime set delivery pipe from converting means
Entrance 160 connects, and is on the other hand connect with the first medium entrance of heat exchanger E1 by pipeline 403, and the of heat exchanger E1
One media outlet is connect by pipeline 404 with the first medium entrance of heat exchanger E2, the first medium outlet of heat exchanger E2
It is connect with the entrance 140 on 100 top of stripper by pipeline 405.
The outlet of lye tank (vat) V1 is connect by pipeline 406 with the entrance for pumping P3, and the outlet for pumping P3 passes through pipeline 407 and stripping
The entrance 120 at 100 middle part of tower connects.
The outlet 110 of 100 bottom of stripper is connected by the second medium entrance of 408 heat exchanger E2 of pipeline, heat exchange
The second medium outlet of device E2 is connect by pipeline 409 with the entrance for pumping P1, and the outlet for pumping P1 passes through pipeline 410 and heat exchanger
The second medium entrance of E4 connects, the second medium outlet connection waste water efferent duct 411 of heat exchanger E4.
The outlet 170 at 100 top of stripper connects a sour gas efferent duct 412, and the entrance 150 on 100 top of stripper is logical
It crosses pipeline 412a and pump P2 is connect with the outlet 220 of 200 I section bottom of ammonium hydroxide absorption tower, the outlet 130 at 100 middle part of stripper
It is connect with the second medium entrance of heat exchanger E1 by pipeline 413, the second medium outlet of heat exchanger E1 passes through pipeline 414
It is connect with the entrance 210 of 200 I section bottom of ammonium hydroxide absorption tower.
Outlet 260 at the top of 200 Section III section of ammonium hydroxide absorption tower connects a fixed gas efferent duct 415；Ammonium hydroxide absorption tower
The entrance 250 at 200 top of III sections connects a desalination water inlet pipe 416.
240 one side of entrance in the middle part of 200 Section III section of ammonium hydroxide absorption tower is connected by pipeline 431 in ammonium hydroxide rectifying column 300
On the other hand the entrance 320 in portion connects waste water efferent duct 411 by pipeline 432；300 Section III section bottom of ammonium hydroxide absorption tower goes out
Mouth 280 is connected to the entrance of pump P4 by pipeline 423.
The outlet of P4 is pumped on the one hand by the entrance of pipeline 424a connection heat exchangers E7, the outlet of heat exchanger E7 passes through
433 connecting pipeline 431 of pipeline, the entrance 350 that 300 middle part of ammonium hydroxide rectifying column is on the other hand connected by pipeline 425 connect.
The outlet 330 at 300 top of ammonium hydroxide rectifying column connects the entrance of heat exchanger E6, heat exchanger E6 by pipeline 426
Outlet by pipeline 427 connect a storage tank V2 entrance, storage tank V2 outlet by pipeline 428 connection pump P5 entrance, pump
On the one hand the outlet of P5 connects liquefied ammonia efferent duct 429, on the other hand pass through pipeline 430 and connect entering for 300 top of ammonium hydroxide rectifying column
Mouth 340.
The lime set containing ammonia transformation from converting means is divided into two parts, and a part is through over-heat-exchanger E1, E2 heat exchange heating
Enter 100 middle and upper part of stripper afterwards.100 tower bottom reboiler E3 of stripper is passed through a certain amount of low pressure steam, to entering the change of tower
Lime set is changed to be stripped.100 bottom of tower of stripper is that qualified purification and condensation liquid is sent after over-heat-exchanger E4 coolings to downstream dress
It sets.
Most of H2S、CO2Etc. components distillated from stripper overhead, part H2S、NH3、H2The components such as O are from lateral line withdrawal function, so
After enter back into heat exchanger E1 and be cooled to 110~120 DEG C and enter 200 I section bottom of ammonium hydroxide absorption tower.From ammonium hydroxide absorption tower
The liquid phase of 200 Section II section bottoms is entered by gravity at the top of 200 I section of ammonium hydroxide absorption tower, and cooling absorb comes from ammonium hydroxide
200 I section bottom rising part H of absorption tower2S。
The gas phase absorbed through supercooling enters 200 Section II section bottom of ammonium hydroxide absorption tower by chimney plate, net from part
Change condensate liquid to send to 200 Section II section of ammonium hydroxide absorption tower, it is cooling to absorb 200 Section II section bottom rising part of ammonium hydroxide absorption tower
H2S.The gas phase absorbed through supercooling enters 200 Section III section bottom of ammonium hydroxide absorption tower by chimney plate.Then desalination is used again
Water and Partial cleansing condensate liquid are sent to cooling 200 Section II section bottom of absorption ammonium hydroxide absorption tower at the top of the Section III section of ammonium hydroxide absorption tower
Ascending part divides NH3。
It is also returned to after cooling in the middle part of Section III section from the qualified partial ammonia water of 200 Section III section bottom of ammonium hydroxide absorption tower
As absorbent, another part is sent into ammonium hydroxide rectifying column 300 as charging.300 overhead vapours of ammonium hydroxide rectifying column is through cooling water cooling
Ammonia lime set is obtained after solidifying, for part ammonia lime set through pumping P5 back to 300 top of ammonium hydroxide rectifying column as flowing back, another part ammonia is solidifying
Liquid is sent as product liquefied ammonia to out-of-bounds.The tower reactor reboiler E7 of ammonium hydroxide rectifying column 300 passes through middle pressure steam or high-temperature position technique object
Stream provides heat, the waste water for meeting environmental requirement and stripper tower reactor waste water combination cooling of the extraction of 300 tower reactor of ammonium hydroxide rectifying column
After send out battery limit (BL).
This type of flow setting is suitable for transformation operating mode, and when stripper 100 and ammonium hydroxide absorption tower 200 is constructed finishes, such as
Factory produces liquefied ammonia to promote value of the product, then can individually increase ammonium hydroxide rectifying column T3 and be used for handling from ammonium hydroxide absorption tower
Ammonium hydroxide can meet needs.And two Tower Systems of front do not have to transformation substantially.Its disadvantage, which is ammonium hydroxide rectifying column, need to use height
The middle pressure steam of grade provides heat, is suitable for transformation device, is changed to foregoing apparatus less.
Claims (2)
1. a kind of method converting lime set waste water making pure liquefied ammonia containing ammonia, it is characterised in that：Converting 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 heat exchange heating of the second heat exchanger, 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, is stripped to entering
The transformation lime set of tower is stripped；A small amount of lye is sent into the middle part of stripper, and most of lye is first fed into absorption tower Section II section top
Portion is then back in the middle part of stripper and is neutralized with the transformation lime set containing ammonia；Qualified purification and condensation liquid is sent out in stripper bottom of tower, passes through successively
It is largely sent to downstream unit after crossing the second heat exchanger, the cooling of third heat exchanger, fraction purification and condensation liquid is admitted to ammonium hydroxide suction
Receive the top of tower Section II section or/and the middle part of ammonium hydroxide absorption tower Section III section；
Most of H2S and CO2It distillates to form sour gas submitting, fraction H from stripper overhead2S and NH3、H2O is from stripper side line
Extraction, then enters back into First Heat Exchanger and is cooled to 110~120 DEG C and enter the ammonium hydroxide absorption tower bottoms IDuan；
Liquid phase from ammonium hydroxide absorption tower Section II section bottom is entered by gravity at the top of the I section of ammonium hydroxide absorption tower, cooling
It absorbs and comes from the ammonium hydroxide absorption tower bottoms IDuan rising part H2S, the gas phase absorbed through supercooling are entered by the first chimney plate
Ammonium hydroxide absorption tower Section II section bottom；
The fraction purification and condensation liquid that is admitted at the top of the Section II section of ammonium hydroxide absorption tower is admitted at the top of the Section II section of ammonium hydroxide absorption tower
Fraction purification and condensation liquid cooling together with the lye being admitted at the top of the Section II section of ammonium hydroxide absorption tower absorb ammonium hydroxide absorption tower the
II sections of bottom rising part H2S, the gas phase absorbed through supercooling enter ammonium hydroxide absorption tower Section III section bottom by the second chimney plate
Portion；
The desalted water being sent at the top of the Section III section of ammonium hydroxide absorption tower or the desalted water being sent at the top of the Section III section of ammonium hydroxide absorption tower
It is but absorbed with the fraction purification and condensation liquid cooling being admitted in the middle part of the Section III section of ammonium hydroxide absorption tower on the Section II section bottom of ammonium hydroxide absorption tower
Ascending part divides NH3；
Cleaning solution from the ammonium hydroxide absorption tower bottoms IDuan is sent into the middle and upper part of stripper；
Weak aqua ammonia from ammonium hydroxide tower bottom of rectifying tower after the 4th heat exchanger and the heat exchange cooling of the 5th heat exchanger by being used as absorbent
In the middle part of back to the ammonium hydroxide absorption tower Section III section and top of Section II section, to produce not hydrogen sulfide containing ammonium hydroxide；Or come from ammonia
Purification of the weak aqua ammonia of crystal evaporate tower tower reactor directly with the submitting qualification in stripper bottom of tower after cooling that exchanges heat by the second heat exchanger
After condensate liquid mixing, then sent to downstream unit after the cooling of third heat exchanger；
Qualified ammonium hydroxide is sent into the middle part of ammonium hydroxide rectifying column, as charging after pressure-raising preheats；Ammonium hydroxide rectifying column tower top steam passes through
Obtain ammonia lime set after cooling water condensation, part ammonia lime set through reflux pump back at the top of ammonium hydroxide rectifying column as flowing back, in addition one
Part ammonia lime set is sent as product liquefied ammonia to out-of-bounds；
Ammonium hydroxide tower bottom of rectifying tower reboiler provides heat by low-pressure steam or process-stream cooling；
The weak aqua ammonia that ammonium hydroxide absorption tower Section III section bottom is sent out be sent into after being heated by the 4th heat exchanger in the middle part of ammonium hydroxide rectifying column or
The weak aqua ammonia part that person's ammonium hydroxide absorption tower Section III section bottom is sent out is sent directly into the middle and lower part of ammonium hydroxide rectifying column, another part
It is divided into two after condenser condenses, one is sent directly into the middle part of ammonium hydroxide rectifying column, and another Zhi Zuowei absorbents are sent into ammonium hydroxide
In the middle part of the Section III section of absorption tower ammonium hydroxide is but absorbed with the fraction purification and condensation liquid cooling being admitted in the middle part of the Section III section of ammonium hydroxide absorption tower
Absorption tower Section II section bottom rising part NH3。
2. it is a kind of containing ammonia convert lime set waste water making pure liquefied ammonia device, which is characterized in that including stripper, ammonium hydroxide absorption tower and
Ammonium hydroxide rectifying column；
The bottom of the stripper is provided with stripper tower bottom reboiler and first outlet, and middle part is provided with first entrance and second
Outlet, top are provided with second and third entrance, and top is provided with the 4th entrance and third outlet；
The ammonium hydroxide absorption tower bottoms IDuan are provided with the 5th entrance and the 4th outlet, are set at the top of the Section II section of ammonium hydroxide absorption tower
It is equipped with the 6th entrance, the 7th entrance, ammonium hydroxide absorption tower Section III section top are provided in the middle part of the ammonium hydroxide absorption tower Section III section
Portion is provided with the 8th entrance and the 5th outlet；Or the ammonium hydroxide absorption tower bottoms IDuan are provided with the 5th entrance and the 4th and go out
Mouthful, it is provided with the 6th entrance at the top of the Section II section of ammonium hydroxide absorption tower, the 9th is provided in the middle part of the ammonium hydroxide absorption tower Section II section
Entrance, the ammonium hydroxide absorption tower Section III section middle part are provided with the 7th entrance, are provided at the top of the ammonium hydroxide absorption tower Section III section
8th entrance and the 5th outlet；Ammonium hydroxide absorption tower Section III section bottom is provided with the 6th outlet；
The bottom of tower of the ammonium hydroxide rectifying column is provided with tower reactor reboiler and the 7th outlet, and the tenth is provided in the middle part of ammonium hydroxide rectifying column
Entrance or the tenth entrance and the 11st entrance are provided with the 8th outlet and the 12nd entrance at the top of the ammonium hydroxide rectifying column；
On the one hand the transformation lime set delivery pipe containing ammonia from converting means passes through the first pipeline and the 4th of the stripper top the
Entrance connects, and is on the other hand connected by the second pipeline and the first medium entrance of first heat exchanger, first heat exchanger
First medium outlet is connected by third pipeline and the first medium entrance of second heat exchanger, and the first of second heat exchanger is situated between
Matter outlet is connect by the 4th pipeline with the second entrance on the stripper top；
Lye tank (vat) outlet by the 5th pipeline with first pump entrance connect, first pump outlet by the 6th pipeline with it is described
First entrance connection in the middle part of stripper；The first outlet of stripper bottom is connect by the 7th pipeline with the entrance of the second pump,
The outlet of second pump is connect by the 8th pipeline with the second medium entrance of the second heat exchanger, and second heat is handed over
The second medium outlet of parallel operation is connect by the 9th pipeline with the entrance of third heat exchanger, the outlet connection of third heat exchanger
Waste water efferent duct；
The one sour gas efferent duct of third outlet connection of stripper top, the third entrance on stripper top by the tenth pipeline and
Third is pumped to be connected with the 4th of the ammonium hydroxide absorption tower bottoms IDuan outlet, and the second outlet in the middle part of the stripper passes through the
11 pipelines are connect with the second medium entrance of the first heat exchanger, and the second medium outlet of the first heat exchanger is logical
The 12nd pipeline is crossed to connect with the 5th entrance of the ammonium hydroxide absorption tower bottoms IDuan；
The 5th one fixed gas efferent duct of outlet connection at the top of the ammonium hydroxide absorption tower Section III section；Ammonium hydroxide absorption tower Section III
8th entrance at section top connects a desalination water inlet pipe；
The 7th entrance in the middle part of the ammonium hydroxide absorption tower Section III section connects first Jie of the 5th heat exchanger by the 13rd pipeline
Matter entrance, the first medium outlet of the 5th heat exchanger connect the first medium of the 4th heat exchanger by the 14th pipeline
The first medium outlet of entrance, the 4th heat exchanger connects the 7th of ammonium hydroxide rectifying tower bottom by the 15th pipeline
Outlet connection；The 6th entrance at the top of the ammonium hydroxide absorption tower Section II section is connected to going out for first pump by the 16th pipeline
Mouthful；The 6th entrance at the top of the ammonium hydroxide absorption tower Section II section is also connected by the 17th pipeline on the waste water efferent duct, institute
The 9th entrance in the middle part of the Section II section of ammonium hydroxide absorption tower is stated also to connect on the 13rd pipeline by the 18th pipeline；The ammonium hydroxide
6th outlet of absorption tower Section III section bottom is connected to the entrance of the 4th pump, the outlet of the 4th pump by the 19th pipeline
The second medium entrance of the 4th heat exchanger is connected by the 20th pipeline, the second medium of the 4th heat exchanger goes out
Mouth connects the connection of the tenth entrance in the middle part of the ammonium hydroxide rectifying column by the 21st pipeline；
Alternatively, on the one hand the 7th entrance in the middle part of the ammonium hydroxide absorption tower Section III section connects described give up by the 22nd pipeline
Water delivery pipe, the tenth entrance being on the other hand connected to by the 23rd pipeline in the middle part of the ammonium hydroxide rectifying column；The ammonium hydroxide
The 6th entrance at the top of the Section II section of absorption tower is connected by the 24th pipeline on the 22nd pipeline；The ammonium hydroxide absorbs
6th outlet of tower Section III section bottom is connected to the entrance of the 4th pump by the 19th pipeline, and the outlet of the 4th pump passes through
25th pipeline connects the entrance of the 5th heat exchanger, and the outlet of the 5th heat exchanger passes through the 26th pipeline
It connects on the 23rd pipeline, the outlet of the 5th heat exchanger also connects the ammonium hydroxide essence by the 27th pipeline
Evaporate the 11st entrance in the middle part of tower；7th outlet at ammonium hydroxide rectifying tower bottom connects the waste water by the 28th pipeline
Efferent duct；
The 8th outlet at the top of the ammonium hydroxide rectifying column connects the entrance of the 6th heat exchanger by the 29th pipeline, and described the
The outlet of six heat exchangers connects the entrance of a storage tank by the 30th pipeline, and the outlet of the storage tank passes through the 31st pipeline
The entrance of the 5th pump is connected, on the one hand the outlet of the 5th pump connects liquefied ammonia efferent duct, on the other hand passes through the 32nd pipe
Line connects the 12nd entrance at the top of the ammonium hydroxide rectifying column.
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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 |
-
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 |
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