CN109264828A - Membrane technology separates the processing system and method for uranyl ion under cone nitric acid system - Google Patents
Membrane technology separates the processing system and method for uranyl ion under cone nitric acid system Download PDFInfo
- Publication number
- CN109264828A CN109264828A CN201811358039.5A CN201811358039A CN109264828A CN 109264828 A CN109264828 A CN 109264828A CN 201811358039 A CN201811358039 A CN 201811358039A CN 109264828 A CN109264828 A CN 109264828A
- Authority
- CN
- China
- Prior art keywords
- pressure pump
- buffer tank
- nanofiltration membrane
- tank
- water
- 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.)
- Pending
Links
- 239000012528 membrane Substances 0.000 title claims abstract description 116
- WYICGPHECJFCBA-UHFFFAOYSA-N dioxouranium(2+) Chemical compound O=[U+2]=O WYICGPHECJFCBA-UHFFFAOYSA-N 0.000 title claims abstract description 49
- 238000000034 method Methods 0.000 title claims abstract description 36
- 238000005516 engineering process Methods 0.000 title claims abstract description 26
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 title claims abstract description 24
- 229910017604 nitric acid Inorganic materials 0.000 title claims abstract description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 85
- 238000001728 nano-filtration Methods 0.000 claims abstract description 71
- 239000007788 liquid Substances 0.000 claims abstract description 45
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 45
- 239000002699 waste material Substances 0.000 claims abstract description 22
- 238000000926 separation method Methods 0.000 claims abstract description 20
- 239000012141 concentrate Substances 0.000 claims description 32
- 238000003672 processing method Methods 0.000 claims description 4
- 239000002351 wastewater Substances 0.000 claims description 4
- 229910052770 Uranium Inorganic materials 0.000 abstract description 14
- JFALSRSLKYAFGM-UHFFFAOYSA-N uranium(0) Chemical group [U] JFALSRSLKYAFGM-UHFFFAOYSA-N 0.000 abstract description 14
- 239000000463 material Substances 0.000 abstract description 10
- 230000014759 maintenance of location Effects 0.000 abstract description 8
- 238000001914 filtration Methods 0.000 description 10
- 238000004590 computer program Methods 0.000 description 7
- 238000010586 diagram Methods 0.000 description 7
- 239000002253 acid Substances 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 5
- 150000002500 ions Chemical class 0.000 description 4
- 230000006870 function Effects 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- TVEXGJYMHHTVKP-UHFFFAOYSA-N 6-oxabicyclo[3.2.1]oct-3-en-7-one Chemical compound C1C2C(=O)OC1C=CC2 TVEXGJYMHHTVKP-UHFFFAOYSA-N 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 230000003139 buffering effect Effects 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 230000003287 optical effect Effects 0.000 description 2
- 230000003204 osmotic effect Effects 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000011347 resin Substances 0.000 description 2
- 229920005989 resin Polymers 0.000 description 2
- 125000005289 uranyl group Chemical group 0.000 description 2
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 239000010808 liquid waste Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000010287 polarization Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/20—Heavy metals or heavy metal compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/10—Nature of the water, waste water, sewage or sludge to be treated from quarries or from mining activities
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Nanotechnology (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The present invention provides processing systems and method that a kind of membrane technology separates uranyl ion under cone nitric acid system, and wherein system includes: inlet tank 1；First high-pressure pump 2；One section of nanofiltration membrane group 3, one section of nanofiltration membrane group 3；First buffer tank 4；Second high-pressure pump 5；First-stage reverse osmosis film group 6；Second buffer tank 7；Third high-pressure pump 8；Two sections of nanofiltration membrane groups 9.The processing system and method for uranyl ion under the membrane technology separation cone nitric acid system provided through the invention, utilize the lower retention efficiency of nanofiltration membrane, make part uranyl ion through membrane material, increase the concentration for producing water side, the influent side for making seperation film and the concentration difference for producing water side reduce, and then the permeable pressure head of film two sides is reduced, reach the target for reducing operating pressure；Then the higher retention efficiency of reverse osmosis membrane is utilized, the removal efficiency of uranyl ion in uranium-bearing waste liquid is improved, it is made to meet processing requirement.
Description
Technical field
The present invention relates to uranyl ion process field more particularly to a kind of membrane technology separation cone nitric acid system under uranyl from
The processing system and method for son.
Background technique
During carrying out uranium ore purifying using nitric acid at present, a large amount of acid uranium-bearing waste liquid can be generated.In order to avoid containing
The waste of uranyl ion and the pollution to environment in uranium waste liquid need to separate acid uranium-bearing waste liquid and be concentrated as far as possible
The concentration of uranyl ion can be multiplexed.
In acid condition, uranyl ion is with cation (UO2 2+) form exist, molecular weight 267.Usually in uranium ore
Exploitation etc. generates the place of uranium-bearing waste liquid, uranyl ion can be removed and be isolated and purified using base exchange method.It is this
Method is advantageous in that technology relative maturity, and optional resin types are more, also achieves resin production domesticization.However this method
Have the shortcomings that larger, i.e. ion exchange resin capacity is limited, limits regeneration solution concentration (i.e. concentrate uranium-bearing strength of fluid), together
When ion-exchange be difficult by uranium-containing waste water processing to low concentration level.With the development of membrane technology, especially nanofiltration membrane
Development carries out feed separation using membrane technology and is gradually known application.In membrane separating process, salinity separation can be realized
Film type be nanofiltration membrane and reverse osmosis membrane.Wherein reverse osmosis membrane is higher to monovalence and divalent ion retention efficiency, Neng Gouyou
Most salinities in the removal waste liquid of effect；And nanofiltration membrane is relatively inefficient to the retention of ion, can make a part of ion
Through membrane material, the separation of different type ion can be realized.
However when using membrane technology processing high-salt-content liquid waste, maximum application barrier is operating pressure.When salt is dense
When spending high, salt branch produces the biggish osmotic pressure of water in influent side, and especially under the conditions of concentration polarization, film surface osmotic pressure will
High degree can be reached.And in order to maintain to produce water, this just needs to improve the operating pressure of system.At present when influent side and production water
When side concentration difference reaches 50g/L (in terms of NaCl), the operating pressure needed will be greater than 4MPa.It is passed through by membrane material resistance to pressure and water pump
Ji property limitation, can not unconfined raising operating pressure, i.e., when influent side and produce water side concentration it is higher when, system will be unable to transport
Row.It is exactly influenced by above-mentioned reason, the reverse osmosis recommendation process salt content of current high pressure is also no more than 100g/L, it is difficult to
Reach concentration material to 250g/L or more target.
Therefore a kind of new membrane technology is needed to separate the processing system and method for uranyl ion under cone nitric acid system.
Summary of the invention
The present invention is intended to provide a kind of membrane technology separation for overcoming the above problem or at least being partially solved the above problem
The processing system and method for uranyl ion under cone nitric acid system.
In order to achieve the above objectives, technical solution of the present invention is specifically achieved in that
One aspect of the present invention provides the processing system of uranyl ion under a kind of membrane technology separation cone nitric acid system,
It include: inlet tank 1, the first end of inlet tank 1 connects waste water input terminal；First high-pressure pump 2, the first end of the first high-pressure pump 3 with
The second end of inlet tank 1 is connected to；One section of nanofiltration membrane group 3, the second end of the first end of one section of nanofiltration membrane group 3 and the first high-pressure pump 2
Connection；The first end of first buffer tank 4, the first buffer tank 4 is connected to the second end of one section of nanofiltration membrane group 3；Second high pressure
Pump 5, the first end of the second high-pressure pump 5 is connected to the second end of the first buffer tank 4；First-stage reverse osmosis film group 6, first-stage reverse osmosis
The first end of film group 6 is connected to the second end of the second high-pressure pump 5, and the second end connection of first-stage reverse osmosis film group 8 produces water output end；
Second buffer tank 7, the first end of the second buffer tank 7 are connected to the third end of inlet tank 1；Third high-pressure pump 8, third high pressure
The first end of pump 8 is connected to the second end of the second buffer tank 7；Two sections of nanofiltration membrane groups 9, the first end of two sections of nanofiltration membrane groups 9 with
The second end of third high-pressure pump 8 is connected to, and the second end of two sections of nanofiltration membrane groups 9 is connected to the third end of inlet tank 1, two sections of nanofiltration membranes
4th end of group 9 is connected to concentrated water output end.
Wherein, the third end of one section of nanofiltration membrane group 3 is connected to the third end of inlet tank 1, and with the second buffer tank 7
One end connection.
Wherein, the third end of first-stage reverse osmosis film group 6 is connected to the third end of the first buffer tank 4, and with inlet tank 1
The connection of third end.
Wherein, the third end of two sections of nanofiltration membrane groups 9 is connected to the first end of the second buffer tank 7.
Wherein, the third end of inlet tank 1 is connected to the first end of the second buffer tank 7.
Wherein, setting first liquid level gauge 11 and the first conductivity meter 12 in inlet tank 1；Setting the in first buffer tank 4
Two liquidometers 41 and the second conductivity meter 42；Setting third liquid level gauge 71 and third conductivity meter 72 in second buffer tank 7.
Wherein, first sensor 23 is set between first high-pressure pump 2 and one section of nanofiltration membrane group 3；Second high-pressure pump 5 and level-one
Second sensor 56 is set between reverse osmosis membrane group 6；3rd sensor is set between third high-pressure pump 8 and two sections of nanofiltration membrane groups 9
89。
Another aspect of the present invention provides the processing method of uranyl ion under a kind of membrane technology separation cone nitric acid system, packet
It includes: processing system of the setting such as uranyl ion under above-mentioned membrane technology separation cone nitric acid system；Waste liquid to be processed is enabled to enter
Inlet tank enters one section of nanofiltration membrane group by the first high-pressure pump, and sequence batch processing obtains product water and concentrate；Product water is introduced
First buffer tank, and first-stage reverse osmosis film group is entered by the second high-pressure pump, product water is generated, and product water is discharged into production water
Output end；Concentrate is introduced into the second buffer tank, and enters inlet tank after entering two sections of nanofiltration membrane groups by third high-pressure pump,
Obtained concentrated water is exported by concentrated water output end.
Wherein, after sequence batch processing obtains product water and concentrate, method further include: concentrate is back to inlet tank.
Wherein, product water is being introduced into the first buffer tank, and after entering first-stage reverse osmosis film group by the second high-pressure pump,
Method further include: be sent into the first buffer tank.
Wherein, after third high-pressure pump enters two sections of nanofiltration membrane groups, method further include: be sent into the second buffer tank.
Wherein, method further include: the water of inlet tank is sent into the second buffer tank.
It can be seen that provide through the invention membrane technology separation cone nitric acid system under uranyl ion processing system and
Method makes part uranyl ion through membrane material, increases the concentration for producing water side using the lower retention efficiency of nanofiltration membrane, makes point
The concentration difference of influent side and production water side from film reduces, and then reduces the permeable pressure head of film two sides, and reaching reduces operating pressure
Target；Then the higher retention efficiency of reverse osmosis membrane is utilized, the removal efficiency of uranyl ion in uranium-bearing waste liquid is improved, makes its satisfaction
Processing requirement.
Detailed description of the invention
In order to illustrate the technical solution of the embodiments of the present invention more clearly, required use in being described below to embodiment
Attached drawing be briefly described, it should be apparent that, drawings in the following description are only some embodiments of the invention, for this
For the those of ordinary skill in field, without creative efforts, it can also be obtained according to these attached drawings other
Attached drawing.
Fig. 1 is that membrane technology provided in an embodiment of the present invention separates the processing system of uranyl ion under cone nitric acid system and shows
It is intended to.
Specific embodiment
Exemplary embodiments of the present disclosure are described in more detail below with reference to accompanying drawings.Although showing the disclosure in attached drawing
Exemplary embodiment, it being understood, however, that may be realized in various forms the disclosure without should be by embodiments set forth here
It is limited.On the contrary, these embodiments are provided to facilitate a more thoroughly understanding of the present invention, and can be by the scope of the present disclosure
It is fully disclosed to those skilled in the art.
Fig. 1 shows the processing system of uranyl ion under membrane technology separation cone nitric acid system provided in an embodiment of the present invention
Schematic diagram, referring to Fig. 1, the processing system of uranyl ion under membrane technology provided in an embodiment of the present invention separation cone nitric acid system
System, comprising:
The first end of inlet tank 1, inlet tank 1 connects waste water input terminal；
The first end of first high-pressure pump 2, the first high-pressure pump 3 is connected to the second end of inlet tank 1；
One section of nanofiltration membrane group 3, the first end of one section of nanofiltration membrane group 3 are connected to the second end of the first high-pressure pump 2；
The first end of first buffer tank 4, the first buffer tank 4 is connected to the second end of one section of nanofiltration membrane group 3；
Second high-pressure pump 5, the first end of the second high-pressure pump 5 are connected to the second end of the first buffer tank 4；
First-stage reverse osmosis film group 6, the first end of first-stage reverse osmosis film group 6 are connected to the second end of the second high-pressure pump 5, level-one
The second end connection of reverse osmosis membrane group 8 produces water output end；
Second buffer tank 7, the first end of the second buffer tank 7 are connected to the third end of inlet tank 1；
Third high-pressure pump 8, the first end of third high-pressure pump 8 are connected to the second end of the second buffer tank 7；
The first end of two sections of nanofiltration membrane groups 9, two sections of nanofiltration membrane groups 9 is connected to the second end of third high-pressure pump 8, two sections of nanofiltrations
The second end of film group 9 is connected to the third end of inlet tank 1, and the 4th end of two sections of nanofiltration membrane groups 9 is connected to concentrated water output end.
It can be seen from the above that the present invention makes use of the lower retention efficiency of nanofiltration membrane, make part uranyl ion through membrane material, increase
The concentration for producing water side, the influent side for making seperation film and the concentration difference for producing water side reduce, and then reduce the permeable pressure head of film two sides, reach
To the target for reducing operating pressure；Then the higher retention efficiency of reverse osmosis membrane is utilized, uranyl ion in uranium-bearing waste liquid is improved
Removal efficiency makes it meet processing requirement.
As an optional embodiment of the embodiment of the present invention, the of the third end of one section of nanofiltration membrane group 3 and inlet tank 1
The connection of three ends, and be connected to the first end of the second buffer tank 7.It is possible thereby to by the concentrate of one section of nanofiltration membrane group 3 is passed through again
It is for re-filtering after secondary entrance inlet tank 1 or the second buffer tank 7, improve filter capacity.
As an optional embodiment of the embodiment of the present invention, the third end of first-stage reverse osmosis film group 6 and the first buffering
The third end of water tank 4 is connected to, and is connected to the third end of inlet tank 1.It is possible thereby to the product that first-stage reverse osmosis film group 6 will be passed through
It is for re-filtering after water is again introduced into the first buffer tank 4 or inlet tank 1, improve the ability of filtering.
As an optional embodiment of the embodiment of the present invention, the third end of two sections of nanofiltration membrane groups 9 and the second buffered water
The first end of case 7 is connected to.It is possible thereby to after the second buffer tank 7 being again introduced by the concentrate of two sections of nanofiltration membrane groups 9, into
Row filters again, improves filter capacity.
As an optional embodiment of the embodiment of the present invention, the of the third end of inlet tank 1 and the second buffer tank 7
One end connection.It is possible thereby to the water in inlet tank 1 is sent into the second buffer tank 7, and with for re-filtering, raising filtering energy
Power.
As an optional embodiment of the embodiment of the present invention, first liquid level gauge 11 and the first electricity are set in inlet tank 1
Electrical conductivity instrument 12；Setting second liquid level gauge 41 and the second conductivity meter 42 in first buffer tank 4；Setting in second buffer tank 7
Third liquid level gauge 71 and third conductivity meter 72.It is possible thereby to be carried out in each water tank according to the liquidometer of setting and conductivity meter
The judgement of water whereabouts.
As an optional embodiment of the embodiment of the present invention, it is arranged between the first high-pressure pump 2 and one section of nanofiltration membrane group 3
First sensor 23；Second sensor 56 is set between second high-pressure pump 5 and first-stage reverse osmosis film group 6；Third high-pressure pump 8 and two
3rd sensor 89 is set between section nanofiltration membrane group 9.It can be according to sensor come to high-pressure pump and nanofiltration membrane group and/or reverse osmosis
The case where between film group, is monitored.
Hereinafter, the processing method of uranyl ion under a kind of membrane technology separation cone nitric acid system is provided, this method comprises:
The processing system of uranyl ion under above-mentioned membrane technology separation cone nitric acid system is arranged in S101；
S102 enables waste liquid to be processed enter inlet tank, enters one section of nanofiltration membrane group, sequence batch processing by the first high-pressure pump
Obtain product water and concentrate；
Product water is introduced the first buffer tank, and enters first-stage reverse osmosis film group by the second high-pressure pump by S103, is generated
Product water, and product water is discharged into and produces water output end；
Concentrate is introduced the second buffer tank, and entered after entering two sections of nanofiltration membrane groups by third high-pressure pump by S104
Inlet tank, obtained concentrated water are exported by concentrated water output end.
As an optional embodiment of the embodiment of the present invention, after sequence batch processing obtains product water and concentrate, side
Method further include: concentrate is back to inlet tank.It is possible thereby to by being again introduced by the concentrate of one section of nanofiltration membrane group into water
It is for re-filtering after case, improve filter capacity.
As an optional embodiment of the embodiment of the present invention, product water is being introduced into the first buffer tank, and is being passed through
After second high-pressure pump enters first-stage reverse osmosis film group, method further include: be sent into the first buffer tank.It is possible thereby to which level-one will be passed through
It is for re-filtering after the product water of reverse osmosis membrane group is again introduced into the first buffer tank, improve the ability of filtering.
As an optional embodiment of the embodiment of the present invention, after third high-pressure pump enters two sections of nanofiltration membrane groups, side
Method further include: be sent into the second buffer tank.It is possible thereby to by the second buffering is again introduced by the concentrate of two sections of nanofiltration membrane groups
It is for re-filtering after water tank, improve filter capacity.
As an optional embodiment of the embodiment of the present invention, membrane technology separates uranyl ion under cone nitric acid system
Processing method further include: the water of inlet tank is sent into the second buffer tank.Delay it is possible thereby to which the water in inlet tank is sent into second
Waste preventer, with for re-filtering, raising filter capacity.
One kind presented below specifically operates detailed step, but the present invention is not limited thereto:
Step 1: acid uranium-bearing waste liquid to be processed is injected into inlet tank.Sentenced by the high liquid level of first liquid level gauge in inlet tank
Disconnected inflow.Then it will be pumped into after waste liquid boost in pressure in one section of nanofiltration membrane group using the first feed pump and the first high-pressure pump, one
The product water of section nanofiltration membrane group is directly entered the first buffer tank, and the concentrate of one section of nanofiltration membrane group is back at inlet tank circulation
Reason.When first liquid level gauge low liquid level prompt liquid level reaches lower or the first conductivity meter conductivity prompt water tank in inlet tank
When interior concentration is higher, the first feed pump and the first high-pressure pump are closed.Then concentrate in inlet tank is arranged using the first feed pump
Enter the second buffer tank.
Step 2: the product water of one section of nanofiltration membrane group in the first buffer tank is mentioned by the second feed pump, the second high-pressure pump
It is pumped into first-stage reverse osmosis film group after boosting power, the product water direct emission of first-stage reverse osmosis film group enters product water tank, and level-one is anti-
The concentrate of permeable membrane group is back to circular treatment in the first buffer tank.When second liquid level gauge low liquid level in the first buffer tank
When prompt liquid level reaches that concentration is higher in lower or the second conductivity meter conductivity prompt water tank, close the second feed pump and
Second high-pressure pump.Then concentrate in inlet tank is discharged into inlet tank using the second feed pump waits next batch to handle.
Step 3: the concentrate of one section of nanofiltration membrane group in the second buffer tank is mentioned by third feed pump, third high-pressure pump
It is pumped into first-stage reverse osmosis film group after boosting power, the product water direct emission of first-stage reverse osmosis film group enters inlet tank, level-one reverse osmosis
The concentrate of permeable membrane group is back to circular treatment in the second buffer tank.When the second buffer tank third liquid level gauge low liquid level prompts
When liquid level reaches that concentration is higher in lower or third conductivity meter conductivity prompt water tank, third feed pump and third are closed
High-pressure pump.Concentrate in slow second waste preventer is system concentrate, is emitted into concentrate water tank using third feed pump.
Wherein, the product water that first-stage reverse osmosis film group generates in step 2 is that system produces water, in step 3 two sections it is reverse osmosis produced
Raw concentrate is system concentrate.
It can be seen that the present invention selects suitable membrane material, using the difference of membrane material rejection, system configuration is carried out,
Operating pressure bring work limitation is avoided, uranyl ion under nitric acid system can be made to realize separation concentration, reach 95% or more
The enrichment factor of removal rate and 5 times or more.
Two different specific implementation cases presented below, but the present invention is not limited thereto.
Case 1 is embodied:
Present case uses system processing uranyl ion concentration for 20g/L, and volume is the acid uranium-bearing waste liquid of 1m3.
Inlet tank, the first buffer tank, the second buffer tank volume be set as 1.5m3、1.5m3、0.5m3；First water supply
It pumps, the processing flow of the first high-pressure pump is 4m3/ h, lift are respectively 30m and 300m；Second feed pump, second high-pressure pump
Handling flow is 3m3/ h, lift are respectively 30m and 400m；Third feed pump, third high-pressure pump processing flow be 1m3/
H, lift are respectively 30m and 600m.When liquidometer high liquid level, the water point of inlet tank, the first buffer tank, the second buffer tank
It Wei not 1.3m3、1.0m3And 0.3m3, when liquidometer low liquid level, the water point of inlet tank, the first buffer tank, the second buffer tank
It Wei not 0.3m3、0.15m3And 0.15m3。
One section of nanofiltration membrane group, two sections of nanofiltration membrane groups, reverse osmosis membrane group be respectively 80% to the diaphragm rejection of uranyl ion,
98.5%, 65%, the rate of recovery is respectively 77%, 85%, 50%.At this point, one section of nanofiltration membrane group, two sections of nanofiltration membrane groups, reverse osmosis
The operating pressure of film group is respectively 2.5MPa, 3.5MPa, 5.5MPa.
Since steps 1 and 2,3 are circulate operations, work as and intake as 1m3When, waste liquid volumetric concentration is practical in inlet tank is
1.3m3.After one cycle, in inlet tank in addition to have newly into 20g/L concentration waste liquid other than, there are also first-stage reverse osmosis concentrations
Liquid 0.15m3, two sections of nanofiltration product water 0.15m3.Therefore actually after step 1, uranyl ion concentration is about 25g/ in inlet tank
L, product water and concentrate concentration are respectively 12g/L and 68g/L.After step 2, system product water uranyl ion concentration is 0.95g/
L, i.e. system are 95.5% or so to the removal efficiency of uranyl ion.After step 3, system concentrate uranyl ion concentration is
102g/L, i.e. system are 5 times to the cycles of concentration of uranyl ion.
Case study on implementation 2:
Present case uses system processing uranyl ion concentration for 50g/L, and volume is the acid uranium-bearing waste liquid of 1m3.
Inlet tank, the first buffer tank, the second buffer tank volume be set as 2.0m3、1.5m3、0.7m3；First water supply
It pumps, the processing flow of the first high-pressure pump is 4m3/ h, lift are respectively 30m and 600m；Second feed pump, second high-pressure pump
Handling flow is 3m3/ h, lift are respectively 30m and 400m；Third feed pump, third high-pressure pump processing flow be 1m3/
H, lift are respectively 30m and 800m.When liquidometer high liquid level, the water point of inlet tank, the first buffer tank, the second buffer tank
It Wei not 1.6m3、1.2m3And 0.4m3, when liquidometer low liquid level, the water point of inlet tank, the first buffer tank, the second buffer tank
It Wei not 0.4m3、0.35m3And 0.15m3。
One section of nanofiltration membrane group, two sections of nanofiltration membrane groups, reverse osmosis membrane group be respectively 70% to the diaphragm rejection of uranyl ion,
99%, 55%, the rate of recovery is respectively 75%, 70%, 62.5%.At this point, one section of nanofiltration membrane group, two sections of nanofiltration membrane groups, reverse osmosis
The operating pressure of film group is respectively 6MPa, 4MPa, 8MPa.
Since steps 1 and 2,3 are circulate operations, when water inlet is 1m3, waste liquid volumetric concentration is practical in inlet tank is
1.6m3.After one cycle, in inlet tank in addition to have newly into 50g/L concentration waste liquid other than, there are also first-stage reverse osmosis concentrations
Liquid 0.35m3, two sections of nanofiltration product water 0.25m3.Therefore actually after step 1, uranyl ion concentration is about in inlet tank
52g/L, product water and concentrate concentration are respectively 20g/L and 160g/L.After step 2, system product water uranyl ion concentration is
0.58g/L, i.e. system are 99% or so to the removal efficiency of uranyl ion.After step 3, system concentrate uranyl ion concentration is
251g/L, i.e. system are 5 times to the cycles of concentration of uranyl ion.
It can be seen that the present invention can be effectively reduced operating pressure in membrane method treating process, when water inlet uranyl ion concentration
When no more than 50g/L, operating pressure is not more than 8MPa；Present invention employs reverse osmosis membrane groups simultaneously, can effectively reduce useless
Uranyl ion concentration in liquid effectively removes rate greater than 95%.
In conclusion provide through the invention membrane technology separation cone nitric acid system under uranyl ion processing system and
Method selects suitable membrane material, using the difference of membrane material rejection, carries out system configuration, avoids operating pressure bring
Work limitation can make uranyl ion under nitric acid system realize separation concentration, reach the dense of 95% or more removal rate and 5 times or more
Shrinkage.
It should be understood by those skilled in the art that, embodiments herein can provide as method, system or computer program
Product.Therefore, complete hardware embodiment, complete software embodiment or reality combining software and hardware aspects can be used in the application
Apply the form of example.Moreover, it wherein includes the computer of computer usable program code that the application, which can be used in one or more,
The computer program implemented in usable storage medium (including but not limited to magnetic disk storage, CD-ROM, optical memory etc.) produces
The form of product.
The application is referring to method, the process of equipment (system) and computer program product according to the embodiment of the present application
Figure and/or block diagram describe.It should be understood that every one stream in flowchart and/or the block diagram can be realized by computer program instructions
The combination of process and/or box in journey and/or box and flowchart and/or the block diagram.It can provide these computer programs
Instruct the processor of general purpose computer, special purpose computer, Embedded Processor or other programmable data processing devices to produce
A raw machine, so that being generated by the instruction that computer or the processor of other programmable data processing devices execute for real
The device for the function of being specified in present one or more flows of the flowchart and/or one or more blocks of the block diagram.
These computer program instructions, which may also be stored in, is able to guide computer or other programmable data processing devices with spy
Determine in the computer-readable memory that mode works, so that it includes referring to that instruction stored in the computer readable memory, which generates,
Enable the manufacture of device, the command device realize in one box of one or more flows of the flowchart and/or block diagram or
The function of being specified in multiple boxes.
These computer program instructions also can be loaded onto a computer or other programmable data processing device, so that counting
Series of operation steps are executed on calculation machine or other programmable devices to generate computer implemented processing, thus in computer or
The instruction executed on other programmable devices is provided for realizing in one or more flows of the flowchart and/or block diagram one
The step of function of being specified in a box or multiple boxes.
In a typical configuration, calculating equipment includes one or more processors (CPU), input/output interface, net
Network interface and memory.
Memory may include the non-volatile memory in computer-readable medium, random access memory (RAM) and/
Or the forms such as Nonvolatile memory, such as read-only memory (ROM) or flash memory (flash RAM).Memory is computer-readable Jie
The example of matter.
Computer-readable medium includes permanent and non-permanent, removable and non-removable media can be by any method
Or technology come realize information store.Information can be computer readable instructions, data structure, the module of program or other data.
The example of the storage medium of computer includes, but are not limited to phase change memory (PRAM), static random access memory (SRAM), moves
State random access memory (DRAM), other kinds of random access memory (RAM), read-only memory (ROM), electric erasable
Programmable read only memory (EEPROM), flash memory or other memory techniques, read-only disc read only memory (CD-ROM) (CD-ROM),
Digital versatile disc (DVD) or other optical storage, magnetic cassettes, tape magnetic disk storage or other magnetic storage devices
Or any other non-transmission medium, can be used for storage can be accessed by a computing device information.As defined in this article, it calculates
Machine readable medium does not include temporary computer readable media (transitory media), such as the data-signal and carrier wave of modulation.
The above is only embodiments herein, are not intended to limit this application.To those skilled in the art,
Various changes and changes are possible in this application.It is all within the spirit and principles of the present application made by any modification, equivalent replacement,
Improve etc., it should be included within the scope of the claims of this application.
Claims (12)
1. the processing system of uranyl ion under a kind of membrane technology separation cone nitric acid system characterized by comprising
The first end of inlet tank (1), the inlet tank (1) connects waste water input terminal；
The first end of first high-pressure pump (2), first high-pressure pump (3) is connected to the second end of the inlet tank (1)；
The second end of one section of nanofiltration membrane group (3), the first end of one section of nanofiltration membrane group (3) and first high-pressure pump (2) connects
It is logical；
First buffer tank (4), the second end of the first end of first buffer tank (4) and one section of nanofiltration membrane group (3)
Connection；
Second high-pressure pump (5), the first end of second high-pressure pump (5) are connected to the second end of first buffer tank (4)；
The second of first-stage reverse osmosis film group (6), the first end of the first-stage reverse osmosis film group (6) and second high-pressure pump (5)
The second end connection of end connection, the first-stage reverse osmosis film group (8) produces water output end；
The first end of second buffer tank (7), second buffer tank (7) is connected to the third end of the inlet tank (1)；
Third high-pressure pump (8), the first end of the third high-pressure pump (8) are connected to the second end of second buffer tank (7)；
The second end of two sections of nanofiltration membrane groups (9), the first end of two sections of nanofiltration membrane groups (9) and the third high-pressure pump (8) connects
Logical, the second end of two sections of nanofiltration membrane groups (9) is connected to the third end of the inlet tank (1), two sections of nanofiltration membrane groups (9)
The 4th end be connected to concentrated water output end.
2. system according to claim 1, which is characterized in that the third end of one section of nanofiltration membrane group (3) and it is described into
The third end of water tank (1) is connected to, and is connected to the first end of second buffer tank (7).
3. system according to claim 1 or 2, which is characterized in that the third end of the first-stage reverse osmosis film group (6) and institute
The third end connection of the first buffer tank (4) is stated, and is connected to the third end of the inlet tank (1).
4. system according to any one of claims 1 to 3, which is characterized in that the third end of two sections of nanofiltration membrane groups (9)
It is connected to the first end of second buffer tank (7).
5. system according to any one of claims 1 to 4, which is characterized in that
The third end of the inlet tank (1) is connected to the first end of second buffer tank (7).
6. system according to claim 1, which is characterized in that
Setting first liquid level gauge (11) and the first conductivity meter (12) in the inlet tank (1)；
Setting second liquid level gauge (41) and the second conductivity meter (42) in first buffer tank (4)；
Setting third liquid level gauge (71) and third conductivity meter (72) in second buffer tank (7).
7. system according to claim 1, which is characterized in that
First sensor (23) are set between first high-pressure pump (2) and one section of nanofiltration membrane group (3)；
Second sensor (56) are set between second high-pressure pump (5) and the first-stage reverse osmosis film group (6)；
3rd sensor (89) are set between the third high-pressure pump (8) and two sections of nanofiltration membrane groups (9).
8. the processing method of uranyl ion under a kind of membrane technology separation cone nitric acid system characterized by comprising
The processing system of uranyl ion under membrane technology separation cone nitric acid system as described in any one of claim 1 to 7 is set；
It enables waste liquid to be processed enter inlet tank, one section of nanofiltration membrane group is entered by the first high-pressure pump, sequence batch processing obtains product
Water and concentrate；
The product water is introduced into the first buffer tank, and first-stage reverse osmosis film group is entered by the second high-pressure pump, generates product
Water, and the product water is discharged into and produces water output end；
The concentrate is introduced into the second buffer tank, and entered after two sections of nanofiltration membrane groups by third high-pressure pump enter it is described into
Water tank, obtained concentrated water are exported by concentrated water output end.
9. according to the method described in claim 8, it is characterized in that, after the sequence batch processing obtains product water and concentrate,
Further include:
The concentrate is back to the inlet tank.
10. method according to claim 8 or claim 9, which is characterized in that the product water is introduced the first buffered water described
Case, and after entering first-stage reverse osmosis film group by the second high-pressure pump, further includes: it is sent into first buffer tank.
11. according to the described in any item methods of claim 8 to 10, which is characterized in that enter two sections in the third high-pressure pump
After nanofiltration membrane group, further includes: be sent into second buffer tank.
12. method according to any one of claims 8 to 11, which is characterized in that further include: the water of the inlet tank is sent
Enter second buffer tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811358039.5A CN109264828A (en) | 2018-11-15 | 2018-11-15 | Membrane technology separates the processing system and method for uranyl ion under cone nitric acid system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811358039.5A CN109264828A (en) | 2018-11-15 | 2018-11-15 | Membrane technology separates the processing system and method for uranyl ion under cone nitric acid system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN109264828A true CN109264828A (en) | 2019-01-25 |
Family
ID=65189011
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201811358039.5A Pending CN109264828A (en) | 2018-11-15 | 2018-11-15 | Membrane technology separates the processing system and method for uranyl ion under cone nitric acid system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109264828A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112679020A (en) * | 2020-12-25 | 2021-04-20 | 成都硕特环保科技有限公司 | Low-cost shale gas fracturing flowback fluid treatment system and treatment method |
| CN114000160A (en) * | 2021-11-30 | 2022-02-01 | 中国原子能科学研究院 | Preparation device and method of tetravalent uranium |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201427903Y (en) * | 2009-04-02 | 2010-03-24 | 厦门市天泉鑫膜科技有限公司 | Nickel electroplating rinse water cleaning system |
| CN202729960U (en) * | 2012-08-14 | 2013-02-13 | 上海晶宇环境工程有限公司 | Equipment special for landfill leachate advanced treatment |
| US20130039823A1 (en) * | 2010-04-19 | 2013-02-14 | Andrew Bassil | Industrial Extraction of Uranium Using Ammonium Carbonate and Membrane Separation |
| CN105366838A (en) * | 2014-12-25 | 2016-03-02 | 南京源泉环保科技股份有限公司 | Zero-discharge treatment method for trivalent chromium passivation wastewater |
| CN107308819A (en) * | 2017-07-06 | 2017-11-03 | 中核四0四有限公司 | The pure level uranyl nitrate solution enrichment facility of one seed nucleus |
| CN209442700U (en) * | 2018-11-15 | 2019-09-27 | 北京清核朝华科技有限公司 | Membrane technology separates the processing system of uranyl ion under cone nitric acid system |
-
2018
- 2018-11-15 CN CN201811358039.5A patent/CN109264828A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201427903Y (en) * | 2009-04-02 | 2010-03-24 | 厦门市天泉鑫膜科技有限公司 | Nickel electroplating rinse water cleaning system |
| US20130039823A1 (en) * | 2010-04-19 | 2013-02-14 | Andrew Bassil | Industrial Extraction of Uranium Using Ammonium Carbonate and Membrane Separation |
| CN202729960U (en) * | 2012-08-14 | 2013-02-13 | 上海晶宇环境工程有限公司 | Equipment special for landfill leachate advanced treatment |
| CN105366838A (en) * | 2014-12-25 | 2016-03-02 | 南京源泉环保科技股份有限公司 | Zero-discharge treatment method for trivalent chromium passivation wastewater |
| CN107308819A (en) * | 2017-07-06 | 2017-11-03 | 中核四0四有限公司 | The pure level uranyl nitrate solution enrichment facility of one seed nucleus |
| CN209442700U (en) * | 2018-11-15 | 2019-09-27 | 北京清核朝华科技有限公司 | Membrane technology separates the processing system of uranyl ion under cone nitric acid system |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112679020A (en) * | 2020-12-25 | 2021-04-20 | 成都硕特环保科技有限公司 | Low-cost shale gas fracturing flowback fluid treatment system and treatment method |
| CN114000160A (en) * | 2021-11-30 | 2022-02-01 | 中国原子能科学研究院 | Preparation device and method of tetravalent uranium |
| CN114000160B (en) * | 2021-11-30 | 2023-12-12 | 中国原子能科学研究院 | Preparation device and method of tetravalent uranium |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103745759B (en) | Method and device for processing radioactive wastewater | |
| KR101954820B1 (en) | Apparatus and method for analyzing influence on fouling in sea water desalination of membrane | |
| CN109264828A (en) | Membrane technology separates the processing system and method for uranyl ion under cone nitric acid system | |
| CN209442700U (en) | Membrane technology separates the processing system of uranyl ion under cone nitric acid system | |
| CN106548816A (en) | A kind of knockdown Spent Radioactive water treatment facilities | |
| JPS59500358A (en) | Diffusion barriers by fixed immobilization of inorganic compounds and methods of using such diffusion barriers to separate small molecules in solution. | |
| CN108176233A (en) | Novel three Room electrodialysis desalination device | |
| Li et al. | Electrodialysis for the volume reduction of the simulated radionuclides containing seawater | |
| CN110349690B (en) | Method and device for treating radioactive waste liquid | |
| CN110391034A (en) | Boron-containing radioactive liquid waste treating apparatus and method | |
| Cordoba et al. | Improved batch reverse osmosis configuration for better energy effiency | |
| CN103663808A (en) | Film integrated treatment process and device for heavy metal waste water | |
| CN105668723B (en) | Capacitor deionizing instrument, system and capacitive deionization method | |
| CN206203953U (en) | A kind of Membrane seawater desalination two-pass reverse osmosis NF concentrated water reuse device | |
| CN212303101U (en) | Be used for radioactive liquid waste deep purification processing apparatus | |
| CN203754515U (en) | Double membrane system for treating circulating water for coke dry quenching power generation | |
| CN106020292B (en) | A kind of counter-infiltration system and concentrated water circulation controlling means | |
| CN210915626U (en) | Radioactive wastewater resource recovery system | |
| CN104961197B (en) | A kind of Copper foil handling process of water saving and its device | |
| CN209740898U (en) | Fastener surface treatment waste water's processing apparatus | |
| CN207361986U (en) | A kind of polyamide -6 produces sewage recovering system | |
| CN104795119A (en) | Device, system and method for disposing radioactive waste water through forward osmosis | |
| CN208279394U (en) | A kind of geothermal tail water cleaning treatment system | |
| CN113963834B (en) | Radioactive wastewater treatment system and treatment method | |
| Ammari Allahyari et al. | Modeling and experimental validation of the steady-state counteractive facilitated transport of Th (IV) and hydrogen ions through hollow-fiber renewal liquid membrane |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information | ||
| CB02 | Change of applicant information |
Address after: Room 6401, 4th Floor, Building 1, No. 17 Shangdi 6th Street, Haidian District, Beijing, 100085 Applicant after: BEIJING CLEANNUS TECHNOLOGY CO.,LTD. Address before: 100085 no.18-2-3002, 3rd floor, No.7 shangdixinxi Road, Haidian District, Beijing Applicant before: BEIJING CLEANNUS TECHNOLOGY CO.,LTD. |