CN207891095U - A kind of alkali device gives up the device that light liquid is recycled with ammonia-containing gas - Google Patents
A kind of alkali device gives up the device that light liquid is recycled with ammonia-containing gas Download PDFInfo
- Publication number
- CN207891095U CN207891095U CN201721786670.6U CN201721786670U CN207891095U CN 207891095 U CN207891095 U CN 207891095U CN 201721786670 U CN201721786670 U CN 201721786670U CN 207891095 U CN207891095 U CN 207891095U
- Authority
- CN
- China
- Prior art keywords
- ammonia
- containing gas
- liquid
- ammonium hydroxide
- membrane assembly
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 248
- 239000007788 liquid Substances 0.000 title claims abstract description 125
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 120
- 239000003513 alkali Substances 0.000 title claims abstract description 51
- 239000012528 membrane Substances 0.000 claims abstract description 85
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 59
- 239000000908 ammonium hydroxide Substances 0.000 claims abstract description 59
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 56
- 238000005201 scrubbing Methods 0.000 claims abstract description 52
- 239000012466 permeate Substances 0.000 claims abstract description 36
- 239000012530 fluid Substances 0.000 claims abstract description 24
- 239000000047 product Substances 0.000 claims abstract description 23
- 239000012141 concentrate Substances 0.000 claims abstract description 3
- 238000000108 ultra-filtration Methods 0.000 claims description 29
- 238000000034 method Methods 0.000 claims description 25
- 239000004952 Polyamide Substances 0.000 claims description 4
- 239000000835 fiber Substances 0.000 claims description 4
- 239000012510 hollow fiber Substances 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 4
- 229920002647 polyamide Polymers 0.000 claims description 4
- 238000010926 purge Methods 0.000 claims description 3
- 238000009738 saturating Methods 0.000 claims description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 23
- 238000000746 purification Methods 0.000 abstract description 20
- 229910000069 nitrogen hydride Inorganic materials 0.000 abstract description 12
- 238000005406 washing Methods 0.000 abstract description 11
- 238000004140 cleaning Methods 0.000 abstract description 6
- 238000002156 mixing Methods 0.000 abstract description 6
- 238000001816 cooling Methods 0.000 abstract description 4
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 239000002699 waste material Substances 0.000 abstract description 4
- 239000002994 raw material Substances 0.000 abstract description 2
- 238000004064 recycling Methods 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 82
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 26
- 239000000243 solution Substances 0.000 description 18
- 238000012360 testing method Methods 0.000 description 16
- 239000002351 wastewater Substances 0.000 description 16
- 208000028659 discharge Diseases 0.000 description 12
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 8
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 8
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 8
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 8
- 230000015572 biosynthetic process Effects 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 5
- 238000001704 evaporation Methods 0.000 description 5
- 230000008020 evaporation Effects 0.000 description 5
- UIIMBOGNXHQVGW-DEQYMQKBSA-M Sodium bicarbonate-14C Chemical compound [Na+].O[14C]([O-])=O UIIMBOGNXHQVGW-DEQYMQKBSA-M 0.000 description 4
- 235000019270 ammonium chloride Nutrition 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 239000012452 mother liquor Substances 0.000 description 4
- 239000011780 sodium chloride Substances 0.000 description 4
- 235000002639 sodium chloride Nutrition 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- 229910021536 Zeolite Inorganic materials 0.000 description 3
- 238000007872 degassing Methods 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 229910000029 sodium carbonate Inorganic materials 0.000 description 3
- 235000017550 sodium carbonate Nutrition 0.000 description 3
- 239000010457 zeolite Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 2
- FKNQFGJONOIPTF-UHFFFAOYSA-N Sodium cation Chemical compound [Na+] FKNQFGJONOIPTF-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 238000005342 ion exchange Methods 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 229910001415 sodium ion Inorganic materials 0.000 description 2
- 239000011550 stock solution Substances 0.000 description 2
- 230000009897 systematic effect Effects 0.000 description 2
- WJEIYVAPNMUNIU-UHFFFAOYSA-N [Na].OC(O)=O Chemical compound [Na].OC(O)=O WJEIYVAPNMUNIU-UHFFFAOYSA-N 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 238000005915 ammonolysis reaction Methods 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 230000008602 contraction Effects 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000009615 deamination Effects 0.000 description 1
- 238000006481 deamination reaction Methods 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 1
- -1 iron ion Chemical class 0.000 description 1
- 238000005304 joining Methods 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 238000007781 pre-processing Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 159000000000 sodium salts Chemical class 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 235000019640 taste Nutrition 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The utility model is related to a kind of device of alkali device waste liquid exhaust gas combined governance recycling, connection alkali device gives up light liquid by being sent to hyperfiltration membrane assembly and reverse osmosis membrane assembly after useless light liquid pump boosting, forms reverse osmosis concentrated liquid and purification permeate；Connection alkali device reuse is returned after the concentrate mixing that hyperfiltration membrane assembly and reverse osmosis membrane assembly are formed；The non-tissue discharge ammonia-containing gas of connection alkali device are delivered to ammonia-containing gas scrubbing tower air inlet by wind turbine, are inversely contacted with cleaning solution in tower, tower overhead gas NH3Content is less than 1mg/m3Direct emission；Scrubbing tower tower reactor solution NH3Mass content control is two bursts of outputs at 0.1%~5% point, and circulation fluid enters scrubbing tower circulation fluid feed inlet after one cooling；Another stock by kettle liquid rear pump is delivered to ammonium hydroxide and prepares reactor to be reacted with liquefied ammonia, is finally delivered to ammonium hydroxide products pot.Using saving demineralized water dosage after reverse osmosis purification, while ammonia-containing gas washings prepare raw material as ammonium hydroxide, reduce ammonium hydroxide manufacturing cost.
Description
Technical field
The utility model is related to a kind of device of alkali device waste liquid exhaust gas combined governance recycling, the utility model especially relates to
And a kind of alkali device gives up the device that light liquid and ammonia-containing gas recycle.
Background technology
The net ammonia wash water of furnace gas condensate, recovery tower and other miscellaneous water containing ammonia in combined soda method production process are referred to as light
Liquid.Light liquid cannot be fully mixed in the systematic stock solution and recycle, and otherwise can not only water down mother liquor, and mother liquor can be caused to expand.So
Light liquid is distilled in production, ammonia therein and a small amount of carbon dioxide are recycled, to reduce the norm quota of consumption.After light liquid distillation
Tower bottoms be known as give up light liquid, when the systematic stock solution balance, this give up light liquid cannot return connection alkali system application, in addition, due to give up
Containing 200~1000mg/L ammonia nitrogens and a small amount of other sodium salts in light liquid, therefore it is unable to direct emission, is handled.
The conventional treatment method of useless light liquid mainly has direct evaporation, air stripping method, degassing embrane method, zeolite and ion to hand over
It changes, ammonia still process method etc..Directly evaporation generally directly carries out concentration and evaporation using multiple-effect evaporation or MVR evaporators to ammonia nitrogen waste water, makes
Ammonia nitrogen in waste water is crystallized out in the form of ammonia salt, generally needs the waste water of biochemical treatment that must adopt in high COD, high ammonia nitrogen
It is handled with evaporator.Steam, electrisity consumption needed for evaporation are big, and investment is big, and water outlet ammonia nitrogen also needs further still in 200-1500mg/L
It is allowed for access after deamination subsequent biochemical system.Air stripping is to carry out stripping, gas using the ammonia nitrogen waste water after air pair plus alkali：Water
3000：Under conditions of 1, NH_3-N treating effect in 70-75%, ammonia nitrogen waste water can not disposable qualified discharge, multistage stripping needs
Heating while power is big, takes up a large area, the ammonia nitrogen that blow out is since gas-water ratio is big, can not recycle, and ammonia nitrogen, which discharges, to be reached
《Emission standard for odor pollutants》The ammonia secondary discharge standard of GB14554-93.The embrane method that deaerates utilizes degassing film principle, after adding alkali
Ammonia nitrogen waste water into film side, sulfuric acid solution is in the other side, and the free ammonia of ammonia nitrogen waste water side is constantly by film by sulfuric acid side
Sulfuric acid absorption become ammonium sulfate.Ammonia nitrogen waste water reaches discharge standard after constantly absorbing.Degassing film is to ammonia nitrogen waste water
Pre-processing requirements and waste water in organic matter require high, because using sulfuric acid absorption, influent ammonium concentration is unsuitable excessively high, usually
No more than 500mg/L, therefore, the technology is due to the uncertainty of the various limitations and film service life technology of flow condition, state
Interior seldom use.Zeolite and ion-exchange carry out ion exchange using the ammonia in zeolite or ion pair waste water, to make waste water
In ammonia nitrogen qualified discharge, the technology general with biochemical BAF technical finesses ammonia nitrogen concentration 50mg/L ammonia nitrogen waste waters below, from
Son is exchanged due to regeneration issues, in Ammonia-nitrogen wastewater treatment technology using less.Ammonia still process method heats waste water using steam, makes
Ammonia in waste water carries out separation cooling and forms ammonium hydroxide at high temperature, and steam ammonium fado makes steaming using bubble-cap, float valve as tower internals
Vapour and high ammonia-nitrogen wastewater contact, but ammonia distillation process steam consumption is big, and ammonia nitrogen is discharged generally in 300mg/L or so.It is described above
Conventional connection alkali give up light liquid processing method there are complex process, the problems such as investment is big, high energy consumption, and solution discharge is also made after handling
At water resource waste.
The wet ammonia belt feeder of combined soda method device is for conveying wet ammonolysis product, since product can volatilize free ammonia, operation
There are ammonia tastes for environment.To improve operating environment, and reach《Emission standard for odor pollutants》The ammonia two level of GB14554-93 is discharged
Standard need to be recycled ammonia-containing gas, and conventional method is that ammonia-containing gas are vacuumized collection, is washed using demineralized water
It washs, in the case where joining alkali liquor contraction, washings can return to connection alkali system application.But in the condition that mother liquor is balanced or expanded
Under, washings need further concentration.
Invention content
The drawbacks of giving up light liquid with ammonia-containing gas treatment process the purpose of the utility model is to overcome original alkali device, carries
It gives up the device that light liquid and ammonia-containing gas recycle for a kind of alkali device, is realizing connection alkali device waste liquid exhaust gas comprehensive treatment
Meanwhile effective Resource recovery and producing the ammonium hydroxide product for meeting professional standard.
The technical solution of the utility model is as follows：
A kind of alkali device gives up the device that light liquid is recycled with ammonia-containing gas；2 inlet of hyperfiltration membrane assembly passes through useless light
Liquid feed-line is connected with useless light liquid pump 1；3 inlet of reverse osmosis membrane assembly passes through purge lines and 2 ultrafiltration of hyperfiltration membrane assembly
Permeate discharge port is connected, and liquid discharge port and reverse osmosis membrane assembly reverse osmosis concentrated liquid discharge port is concentrated by ultrafiltration in hyperfiltration membrane assembly
It is connected with connection alkali process units by discharge pipe line；4 top inlet 12 of ammonia-containing gas scrubbing tower and middle part inlet 13 are logical
Purification permeate feed-line is crossed with the purification permeate discharge port of reverse osmosis membrane assembly 3 to be connected；Ammonia-containing gas scrubbing tower lower part
Air inlet 14 is connected by admission line with ammonia-containing gas wind turbine 5, and 4 top inlet 12 of the ammonia-containing gas scrubbing tower is in
Circulation fluid feed inlet 17 is provided between portion's inlet 13；The first liquid outlet of ammonia-containing gas scrubbing tower tower reactor 16 passes through pipeloop
It is connected successively with kettle liquid circulating pump 8, circulation fluid heat exchanger 6 and ammonia-containing gas scrubbing tower circulation fluid feed inlet 17；Ammonium hydroxide is anti-
9 kettle liquid feed inlet of device is answered to pass through reactor line and ammonia-containing gas scrubbing tower the second liquid outlet of tower reactor equipped with kettle liquid rear pump 7
15 are connected, and ammonium hydroxide reactor liquefied ammonia feed inlet is connected with liquefied ammonia feed-line, and ammonium hydroxide reactor liquid outlet is by being connected with
The pipeline of ammonium hydroxide heat exchanger 10 is connected with ammonium hydroxide products pot 11.
The ammonium hydroxide reactor is microreactor.
The hyperfiltration membrane assembly is hollow-fibre membrane, 0.05 μm~1nm of membrane aperture.
The reverse osmosis membrane assembly is two-stage, and component membrane material is polyamide, and membrane module is hollow fiber form.
A kind of alkali device is carried out using the device of the utility model to give up the method that light liquid recycles with ammonia-containing gas, packet
Include following steps：
(1) the connection alkali device that temperature is 30~45 DEG C is given up after light liquid boosts to 1.5~2.5MpaG by the light liquid pump that gives up and is sent to
Hyperfiltration membrane assembly, forms ultrafiltration concentration liquid and ultrafiltration permeate, the ultrafiltration permeate of formation enter back into reverse osmosis membrane assembly, is formed
Reverse osmosis concentrated liquid and purification permeate；
(2) it is returned after the reverse osmosis concentrated liquid mixing that the ultrafiltration concentration liquid and reverse osmosis membrane assembly that hyperfiltration membrane assembly is formed are formed
Connection alkali process units reuse is returned, the purification permeate that reverse osmosis membrane assembly is formed is divided into two stocks and is not delivered to ammonia-containing gas washing
As wash water, control ammonia-containing gas scrubbing tower operating pressure is normal pressure for tower top and middle part inlet, and bottom temperature is 40~45
℃；
(3) the non-tissue of connection alkali device discharges ammonia-containing gas and boosts to be delivered to after 10~50kpaG by ammonia-containing gas wind turbine and contains
Ammonia gas scrubbing tower lower part air inlet, inversely contacts, tower overhead gas NH with cleaning solution in tower3Content is less than 1mg/m3Direct emission；
(4) scrubbing tower tower reactor solution NH3Mass content is controlled 0.1%~5%, is divided into two bursts of outputs, one is by kettle liquid
Circulating pump is delivered to circulation fluid heat exchanger, and ammonia-containing gas scrubbing tower is entered after circulation fluid heat exchanger is cooled to 35~40 DEG C and is recycled
Liquid feed inlet；Another stock is delivered to ammonium hydroxide reactor by kettle liquid rear pump and is reacted with liquefied ammonia, and ammonium hydroxide product conveys after reaction
35~40 DEG C are cooled to ammonium hydroxide heat exchanger, is finally delivered to ammonium hydroxide products pot.
The connection alkali device gives up light liquid from the connection light liquid destilling tower tower reactor of alkali device, and water quality characteristic is：Turbidity 1~
10NTU, PH 8~10, TDS 200~1500mg/L, 200~1000mg/L of ammonia nitrogen.
The ammonia-containing gas are characterized as from the connection wet ammonia belt feeder of alkali device, ammonia-containing gas：NH3Content 150~
500mg/m3。
The ammonia-containing gas scrubbing tower circulation fluid feed inlet be located at ammonia-containing gas scrubbing tower top and middle part inlet it
Between.
It is described as follows：
Hyperfiltration membrane assembly 2, the hyperfiltration membrane assembly is for removing insoluble solid impurities in useless light liquid, hyperfiltration membrane assembly
It is preferred that hollow-fibre membrane, membrane aperture preferably 0.05 μm~1nm.The hyperfiltration membrane assembly inlet by give up light liquid feed-line with
The light liquid pump 1 that gives up is connected；
Reverse osmosis membrane assembly 3, the reverse osmosis membrane assembly are used to remove most of soluble-salt in solution, such as carbonic acid
Sodium, sodium bicarbonate, sodium chloride, ammonium chloride etc..The preferred two-stage of the reverse osmosis membrane assembly, component membrane material preferred polyamide,
The preferred hollow fiber form of membrane module form.The reverse osmosis membrane assembly inlet is saturating by purge lines and hyperfiltration membrane assembly ultrafiltration
It crosses liquid discharge port to be connected, liquid discharge port and the discharging of reverse osmosis membrane assembly reverse osmosis concentrated liquid is concentrated by ultrafiltration in the hyperfiltration membrane assembly
Mouth is connected by discharge pipe line with connection alkali process units.
Ammonia-containing gas scrubbing tower 4, the ammonia-containing gas scrubbing tower make ammonia in gas content drop for handling ammonia-containing gas
As low as being discharged after national standard.The ammonia-containing gas scrubbing tower top inlet 12 and middle part inlet 13 is penetrated by purifying
Liquid feed-line purifies permeate discharge port with reverse osmosis membrane assembly 3 and is connected；Ammonia-containing gas scrubbing tower lower part air inlet
14 are connected by admission line with ammonia-containing gas wind turbine 5,4 top inlet 12 of the ammonia-containing gas scrubbing tower and middle part feed liquor
Be provided with circulation fluid feed inlet 17 between mouthfuls 13, the first liquid outlet of ammonia-containing gas scrubbing tower tower reactor 16 by pipeloop successively with
Kettle liquid circulating pump 8, circulation fluid heat exchanger 6 and ammonia-containing gas scrubbing tower circulation fluid feed inlet 17 are connected；
Ammonium hydroxide reactor 9, the preferred microreactor of ammonium hydroxide reactor.Ammonium hydroxide reactor kettle liquid feed inlet is by being equipped with
The reactor line of kettle liquid rear pump 7 is connected with the second liquid outlet of ammonia-containing gas scrubbing tower tower reactor 15, ammonium hydroxide reactor liquefied ammonia
Feed inlet is connected with liquefied ammonia feed-line, the ammonium hydroxide reactor liquid outlet by be connected with the pipeline of ammonium hydroxide heat exchanger 10 with
Ammonium hydroxide products pot 11 is connected.
It is had the advantage that when using the utility model method：
(1) since the connection alkali light liquid that gives up finally is prepared into ammonium hydroxide product, without discharge, therefore can specific aim reduce in solution
Carbonate, sodium ion, iron ion, fixed ammonia equal size can be real using reverse osmosis membrane assembly without largely removing free ammonia
This existing target, reduces processing cost, and after testing, the purification permeate that the reverse osmosis membrane assembly that this method uses is formed is reachable
To following standard：PH 8~11, TDS are less than 300mg/L.
(2) reverse osmosis membrane assembly concentrate returns to connection alkali device, and purification permeate is prepared for washing tail gas and ammonium hydroxide,
Under conditions of ensureing connection alkali device mother liquor balance, the resources such as carbonate, sodium ion, the ammonia in giving up light liquid have effectively been recycled.
(3) desalination water consumption can be saved using light liquid washing ammonia-containing gas of giving up after reverse osmosis purification, reduces cost, contains simultaneously
Ammonia gas washings prepare raw material as ammonium hydroxide, reduce ammonium hydroxide manufacturing cost.
Description of the drawings
Fig. 1 is that a kind of alkali device of the utility model gives up the schematic device that light liquid and ammonia-containing gas recycle.
Specific implementation mode
The utility model is described in detail with reference to specific embodiment.
A kind of alkali device of the utility model as shown in drawings gives up the device that light liquid is recycled with ammonia-containing gas, surpasses
2 inlet of filter membrane component is connected by the light liquid feed-line that gives up with useless light liquid pump 1；3 inlet of reverse osmosis membrane assembly passes through net
Change pipeline with 2 ultrafiltration permeate discharge port of hyperfiltration membrane assembly to be connected, hyperfiltration membrane assembly ultrafiltration concentration liquid discharge port and reverse osmosis
Membrane module reverse osmosis concentrated liquid discharge port is connected by discharge pipe line with connection alkali process units；4 top of ammonia-containing gas scrubbing tower
Inlet 12 and middle part inlet 13 purify permeate discharge port phase by purifying permeate feed-line with reverse osmosis membrane assembly 3
Connection；Ammonia-containing gas scrubbing tower lower part air inlet 14 is connected by admission line with ammonia-containing gas wind turbine 5, the ammonia-containing gas
It is provided with circulation fluid feed inlet 17 between 4 top inlet 12 of scrubbing tower and middle part inlet 13；Ammonia-containing gas scrubbing tower tower reactor
First liquid outlet 16 is recycled with kettle liquid circulating pump 8, circulation fluid heat exchanger 6 and ammonia-containing gas scrubbing tower successively by pipeloop
Liquid feed inlet 17 is connected；9 kettle liquid feed inlet of ammonium hydroxide reactor by reactor line equipped with kettle liquid rear pump 7 with contain ammonia
The second liquid outlet of body scrubbing tower tower reactor 15 is connected, and ammonium hydroxide reactor liquefied ammonia feed inlet is connected with liquefied ammonia feed-line, ammonium hydroxide
Reactor liquid outlet is connected by being connected with the pipeline of ammonium hydroxide heat exchanger 10 with ammonium hydroxide products pot 11.
A kind of alkali device of the utility model gives up the method that light liquid and ammonia-containing gas recycle, it includes following step
Suddenly：
(1) the connection alkali device that temperature is 30~45 DEG C is given up after light liquid boosts to 1.5~2.5MpaG by the light liquid pump that gives up and is sent to
Hyperfiltration membrane assembly, forms ultrafiltration concentration liquid and ultrafiltration permeate, the ultrafiltration permeate of formation enter back into reverse osmosis membrane assembly, is formed
Reverse osmosis concentrated liquid and purification permeate；
The connection alkali device gives up light liquid from the connection light liquid destilling tower tower reactor of alkali device, and water quality characteristic is：Turbidity 1~
10NTU, PH 8~10, TDS 200~1500mg/L, 200~1000mg/L of ammonia nitrogen.
The hyperfiltration membrane assembly preferably uses hollow-fibre membrane, and membrane aperture preferably 0.05 μm~1nm, described is reverse osmosis
The preferred two-stage of membrane module, reverse osmosis membrane assembly membrane material preferably use polyamide, the preferred hollow fiber form of membrane module form.
(2) it is returned after the reverse osmosis concentrated liquid mixing that the ultrafiltration concentration liquid and reverse osmosis membrane assembly that hyperfiltration membrane assembly is formed are formed
Connection alkali process units reuse is returned, the purification permeate that reverse osmosis membrane assembly is formed is divided into two stocks and is not delivered to ammonia-containing gas washing
As wash water, control ammonia-containing gas scrubbing tower operating pressure is normal pressure for tower top and middle part inlet, and bottom temperature is 40~45
℃；
(3) the non-tissue of connection alkali device discharges ammonia-containing gas and boosts to be delivered to after 10~50kpaG by ammonia-containing gas wind turbine and contains
Ammonia gas scrubbing tower lower part air inlet, inversely contacts, tower overhead gas NH with cleaning solution in tower3Content is less than 1mg/m3Direct emission；
The ammonia-containing gas are characterized as from the connection wet ammonia belt feeder of alkali device, ammonia-containing gas：NH3Content 150~
500mg/m3。
(4) scrubbing tower tower reactor solution NH3Mass content is controlled 0.1%~5%, is divided into two bursts of outputs, one is by kettle liquid
Circulating pump is delivered to circulation fluid heat exchanger, and ammonia-containing gas scrubbing tower cycle is returned to after circulation heat exchanger is cooled to 35~40 DEG C
Liquid feed inlet；Another stock is delivered to ammonium hydroxide reactor by kettle liquid rear pump and is reacted with liquefied ammonia, and ammonium hydroxide product conveys after reaction
35~40 DEG C are cooled to ammonium hydroxide heat exchanger, is finally delivered to ammonium hydroxide products pot.
The preferred microreactor of ammonium hydroxide reactor, the ammonia-containing gas scrubbing tower circulation fluid feed inlet, which is located at, contains ammonia
Between gas scrubbing tower top and middle part inlet, the ammonium hydroxide product meets chemical industry ministerial standard HG1-88-81 industrial ammonias
Technical indicator, i.e. concentration are more than 20%, and coloration is less than No. 80, and residue content is less than 0.3g/L.
Embodiment 1
(1) 30 DEG C of connection alkali device light liquid that gives up is boosted to by the light liquid pump that gives up and is sent to hyperfiltration membrane assembly after 1.5MpaG and is filtered,
Insoluble solid impurities in the useless light liquid of removal, obtain that liquid and ultrafiltration permeate is concentrated by ultrafiltration；The ultrafiltration permeate of formation enters back into
Reverse osmosis membrane assembly removes most of soluble-salt (sodium carbonate, sodium bicarbonate, sodium chloride, ammonium chloride etc.) in solution, obtains
Reverse osmosis concentrated liquid and purification permeate.After testing, useless light liquid water quality characteristic is：Turbidity 1.3NTU, PH 8.2, TDS 263mg/
L, ammonia nitrogen 205mg/L.After testing, purification permeate water quality characteristic is：Turbidity ＜ 0.1NTU, PH 9.6, TDS 63mg/L, ammonia nitrogen
(predominantly free ammonia) 50.8mg/L.
(2) it is returned after the reverse osmosis concentrated liquid mixing that the ultrafiltration concentration liquid and reverse osmosis membrane assembly that hyperfiltration membrane assembly is formed are formed
Connection alkali process units reuse is returned, the purification permeate that reverse osmosis membrane assembly is formed is divided into two stocks and is not delivered to ammonia-containing gas washing
As wash water, control ammonia-containing gas scrubbing tower operating pressure is normal pressure for tower top and middle part inlet, and bottom temperature is 40 DEG C；
(3) after testing, the non-tissue discharge ammonia-containing gas NH of connection alkali device3Content 156mg/m3, boosted by ammonia-containing gas wind turbine
It is delivered to ammonia-containing gas scrubbing tower lower part air inlet after to 10kpaG, is inversely contacted with cleaning solution in tower, after testing tower overhead gas NH3
Content is 0.1mg/m3, can direct emission；
(4) scrubbing tower tower reactor solution NH3Mass content is 0.1%, is divided into two bursts of outputs, one is conveyed by kettle liquid circulating pump
To circulation fluid heat exchanger, ammonia-containing gas scrubbing tower circulation fluid feed inlet is returned to after circulation heat exchanger is cooled to 35 DEG C；It is another
Stock is delivered to ammonium hydroxide reactor by kettle liquid rear pump and is reacted with liquefied ammonia, and ammonium hydroxide product is delivered to ammonium hydroxide heat exchanger drop after reaction
Temperature is finally delivered to ammonium hydroxide products pot to 35 DEG C.After testing, the ammonium hydroxide product design of preparation is 20.8%, and coloration is less than No. 80,
Residue content 72mg/L.
Embodiment 2
(1) 40 DEG C of connection alkali device light liquid that gives up is boosted to by the light liquid pump that gives up and is sent to hyperfiltration membrane assembly after 2.0MpaG and is filtered,
Insoluble solid impurities in the useless light liquid of removal, obtain that liquid and ultrafiltration permeate is concentrated by ultrafiltration；The ultrafiltration permeate of formation enters back into
Reverse osmosis membrane assembly removes most of soluble-salt (sodium carbonate, sodium bicarbonate, sodium chloride, ammonium chloride etc.) in solution, obtains
Reverse osmosis concentrated liquid and purification permeate.After testing, useless light liquid water quality characteristic is：Turbidity 5NTU, PH 9, TDS 820mg/L, ammonia
Nitrogen 660mg/L.After testing, purification permeate water quality characteristic is：Turbidity ＜ 0.1NTU, PH 10.2, TDS 127mg/L, ammonia nitrogen
(predominantly free ammonia) 115mg/L.
(2) it is returned after the reverse osmosis concentrated liquid mixing that the ultrafiltration concentration liquid and reverse osmosis membrane assembly that hyperfiltration membrane assembly is formed are formed
Connection alkali process units reuse is returned, the purification permeate that reverse osmosis membrane assembly is formed is divided into two stocks and is not delivered to ammonia-containing gas washing
As wash water, control ammonia-containing gas scrubbing tower operating pressure is normal pressure for tower top and middle part inlet, and bottom temperature is 42 DEG C；
(3) after testing, the non-tissue discharge ammonia-containing gas NH of connection alkali device3Content 386mg/m3, boosted by ammonia-containing gas wind turbine
It is delivered to ammonia-containing gas scrubbing tower lower part air inlet after to 30kpaG, is inversely contacted with cleaning solution in tower, after testing tower overhead gas NH3
Content is 0.3mg/m3, can direct emission；
(4) scrubbing tower tower reactor solution NH3Mass content is 2%, is divided into two bursts of outputs, one is delivered to by kettle liquid circulating pump
Circulation fluid heat exchanger returns to ammonia-containing gas scrubbing tower circulation fluid feed inlet after circulation heat exchanger is cooled to 37 DEG C；Another stock
Ammonium hydroxide reactor is delivered to by kettle liquid rear pump to be reacted with liquefied ammonia, ammonium hydroxide product is delivered to the cooling of ammonium hydroxide heat exchanger after reaction
To 38 DEG C, it is finally delivered to ammonium hydroxide products pot.After testing, the ammonium hydroxide product design of preparation is 21.6%, and coloration is residual less than No. 80
Slag content 121mg/L.
Embodiment 3
(1) 45 DEG C of connection alkali device light liquid that gives up is boosted to by the light liquid pump that gives up and is sent to hyperfiltration membrane assembly after 2.5MpaG and is filtered,
Insoluble solid impurities in the useless light liquid of removal, obtain that liquid and ultrafiltration permeate is concentrated by ultrafiltration；The ultrafiltration permeate of formation enters back into
Reverse osmosis membrane assembly removes most of soluble-salt (sodium carbonate, sodium bicarbonate, sodium chloride, ammonium chloride etc.) in solution, obtains
Reverse osmosis concentrated liquid and purification permeate.After testing, useless light liquid water quality characteristic is：Turbidity 10NTU, PH 9.9, TDS 1496mg/
L, ammonia nitrogen 968mg/L.After testing, purification permeate water quality characteristic is：Turbidity ＜ 0.1NTU, PH 10.8, TDS 256mg/L, ammonia
Nitrogen (predominantly free ammonia) 235mg/L.
(2) it is returned after the reverse osmosis concentrated liquid mixing that the ultrafiltration concentration liquid and reverse osmosis membrane assembly that hyperfiltration membrane assembly is formed are formed
Connection alkali process units reuse is returned, the purification permeate that reverse osmosis membrane assembly is formed is divided into two stocks and is not delivered to ammonia-containing gas washing
As wash water, control ammonia-containing gas scrubbing tower operating pressure is normal pressure for tower top and middle part inlet, and bottom temperature is 45 DEG C；
(3) after testing, the non-tissue discharge ammonia-containing gas NH of connection alkali device3Content 487mg/m3, boosted by ammonia-containing gas wind turbine
It is delivered to ammonia-containing gas scrubbing tower lower part air inlet after to 50kpaG, is inversely contacted with cleaning solution in tower, after testing tower overhead gas NH3
Content is 0.7mg/m3, can direct emission；
(4) scrubbing tower tower reactor solution NH3Mass content is 5%, is divided into two bursts of outputs, one is delivered to by kettle liquid circulating pump
Circulation fluid heat exchanger returns to ammonia-containing gas scrubbing tower circulation fluid feed inlet after circulation heat exchanger is cooled to 40 DEG C；Another stock
Ammonium hydroxide reactor is delivered to by kettle liquid rear pump to be reacted with liquefied ammonia, ammonium hydroxide product is delivered to the cooling of ammonium hydroxide heat exchanger after reaction
To 40 DEG C, it is finally delivered to ammonium hydroxide products pot.After testing, the ammonium hydroxide product design of preparation is 21.8%, and coloration is residual less than No. 80
Slag content 216mg/L.
Claims (4)
- The device that light liquid is recycled with ammonia-containing gas 1. a kind of alkali device gives up；It is characterized in that hyperfiltration membrane assembly (2) inlet By giving up, light liquid feed-line is connected with useless light liquid pump (1)；Reverse osmosis membrane assembly (3) inlet passes through purge lines and ultrafiltration Membrane module (2) ultrafiltration permeate discharge port is connected, and liquid discharge port and reverse osmosis membrane assembly reverse osmosis is concentrated by ultrafiltration in hyperfiltration membrane assembly Saturating concentrate discharge port is connected by discharge pipe line with connection alkali process units；Ammonia-containing gas scrubbing tower (4) top inlet (12) and middle part inlet (13) purifies permeate discharge port phase by purifying permeate feed-line with reverse osmosis membrane assembly (3) Connection；Ammonia-containing gas scrubbing tower lower part air inlet (14) is connected by admission line with ammonia-containing gas wind turbine (5), described to contain ammonia Circulation fluid feed inlet (17) is provided between gas scrubbing tower top inlet (12) and middle part inlet (13)；Ammonia-containing gas are washed The first liquid outlet of tower tower reactor (16) is washed by pipeloop successively with kettle liquid circulating pump (8), circulation fluid heat exchanger (6) and containing ammonia Gas scrubbing tower circulation fluid feed inlet (17) is connected；Ammonium hydroxide reactor (9) kettle liquid feed inlet is by being equipped with kettle liquid rear pump (7) Reactor line be connected with ammonia-containing gas scrubbing tower the second liquid outlet of tower reactor (15), ammonium hydroxide reactor liquefied ammonia feed inlet and liquid Ammonia feed-line is connected, and ammonium hydroxide reactor liquid outlet is by being connected with the pipeline of ammonium hydroxide heat exchanger (10) and ammonium hydroxide products pot (11) it is connected.
- 2. device as described in claim 1, it is characterized in that the ammonium hydroxide reactor is microreactor.
- 3. device as described in claim 1, it is characterised in that：The hyperfiltration membrane assembly is hollow-fibre membrane, membrane aperture 0.05 μm~1nm.
- 4. device as described in claim 1, it is characterised in that：The reverse osmosis membrane assembly is two-stage, and component membrane material is Polyamide, membrane module are hollow fiber form.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721786670.6U CN207891095U (en) | 2017-12-19 | 2017-12-19 | A kind of alkali device gives up the device that light liquid is recycled with ammonia-containing gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721786670.6U CN207891095U (en) | 2017-12-19 | 2017-12-19 | A kind of alkali device gives up the device that light liquid is recycled with ammonia-containing gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN207891095U true CN207891095U (en) | 2018-09-21 |
Family
ID=63549129
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201721786670.6U Active CN207891095U (en) | 2017-12-19 | 2017-12-19 | A kind of alkali device gives up the device that light liquid is recycled with ammonia-containing gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN207891095U (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109293525A (en) * | 2018-09-26 | 2019-02-01 | 山东新和成精化科技有限公司 | A kind of micro passage reaction and the method for preparing N- alkyloxy oxalyl alanine ester using the micro passage reaction |
| CN110318066A (en) * | 2019-06-20 | 2019-10-11 | 青岛鼎海电化学科技有限公司 | A kind of preparation method of tetra-alkyl ammonium hydroxide |
| CN111099698A (en) * | 2020-01-10 | 2020-05-05 | 中工沃特尔水技术股份有限公司 | Forward osmosis and combined soda production process co-production combined system and method |
| CN115979729A (en) * | 2023-02-22 | 2023-04-18 | 重庆湘渝盐化有限责任公司 | A sampling device for analysis and detection of free ammonia in waste light liquid |
-
2017
- 2017-12-19 CN CN201721786670.6U patent/CN207891095U/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109293525A (en) * | 2018-09-26 | 2019-02-01 | 山东新和成精化科技有限公司 | A kind of micro passage reaction and the method for preparing N- alkyloxy oxalyl alanine ester using the micro passage reaction |
| CN109293525B (en) * | 2018-09-26 | 2021-04-20 | 山东新和成精化科技有限公司 | Micro-channel reactor and method for preparing N-alkoxy oxalyl alanine ester by using same |
| CN110318066A (en) * | 2019-06-20 | 2019-10-11 | 青岛鼎海电化学科技有限公司 | A kind of preparation method of tetra-alkyl ammonium hydroxide |
| CN111099698A (en) * | 2020-01-10 | 2020-05-05 | 中工沃特尔水技术股份有限公司 | Forward osmosis and combined soda production process co-production combined system and method |
| CN115979729A (en) * | 2023-02-22 | 2023-04-18 | 重庆湘渝盐化有限责任公司 | A sampling device for analysis and detection of free ammonia in waste light liquid |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN206799345U (en) | A kind of system of high-salt wastewater purified salt | |
| CN107399876B (en) | A kind of processing method of high ammonia-nitrogen wastewater | |
| CN207891095U (en) | A kind of alkali device gives up the device that light liquid is recycled with ammonia-containing gas | |
| CN102503016B (en) | Device and method for treating ammonia nitrogen wastewater, recycling ammonia and preparing ammonium sulfate | |
| CN101786754A (en) | Zero-emission treatment process for salt-containing wastewater | |
| CN108658345B (en) | A method and system for refining salt from high-salt wastewater | |
| CN107720782A (en) | A kind of technique and system for use in carrying for dividing salt preparing potassium sulfate from high-salt wastewater | |
| CN206467086U (en) | A kind of high saliferous industrial waste water disposal device | |
| CN106186550A (en) | Sewage recycling Zero emission device and method | |
| CN106746110A (en) | A kind of device and processing method for processing high ammonia nitrogen and high salt waste water | |
| CN112047553A (en) | PTA high-salinity wastewater treatment, reuse and zero-discharge system and method | |
| CN107986397A (en) | A kind of alkali device gives up the method and device that light liquid and ammonia-containing gas recycle | |
| CN111362283A (en) | Viscose waste water recycling treatment method | |
| CN105366754A (en) | Ammonia-nitrogen wastewater treatment device and method | |
| CN110104865A (en) | Spent acid, salkali waste, the wastewater zero discharge system of crystal salt recycling and method can be achieved | |
| CN114797476A (en) | Novel bipolar membrane electrodialysis device for carbon capture and high-salinity wastewater synergistic system and process | |
| CN110937728A (en) | Desulfurization wastewater treatment method and system | |
| CN108328839B (en) | Sodium-alkali flue gas desulfurization wastewater treatment system and use method | |
| CN213977333U (en) | A zero-discharge treatment system for boiler desulfurization wastewater | |
| CN116573813A (en) | System and method for treating regenerated wastewater by coupling degassing membrane with bipolar membrane | |
| CN210528683U (en) | Wastewater zero discharge system capable of recycling waste acid, waste alkali and crystal salt | |
| CN105481160B (en) | Method and device for preparing industrial salt by strong brine with zero discharge | |
| CN104860465A (en) | Double-tower catalysis thermal-coupling reflux deamination method and deamination device thereof | |
| CN112777815A (en) | Treatment method and treatment system for salt-containing water | |
| CN210736415U (en) | Be used for high salt ammonia nitrogen waste water zero release processing system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |