CN204918788U - Brine removes ammonium device - Google Patents
Brine removes ammonium device Download PDFInfo
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- CN204918788U CN204918788U CN201520410147.8U CN201520410147U CN204918788U CN 204918788 U CN204918788 U CN 204918788U CN 201520410147 U CN201520410147 U CN 201520410147U CN 204918788 U CN204918788 U CN 204918788U
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- Prior art keywords
- ammonium
- brine
- bittern
- pipeline
- heat exchanger
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Abstract
The utility model discloses a brine removes ammonium device, including the brine pipeline, the brine pipeline is linked together with brine jar A's feed inlet, the naOH pipeline is linked together with brine jar A's feed inlet, brine jar A's discharge gate is linked together with brine jar B's feed inlet, naClO pipeline and air pipeline all are linked together with brine jar B's feed inlet, brine jar B's discharge gate and heat exchanger are linked together, the export of heat exchanger is linked together with the import of ammonium blowdown tower, the fan is linked together with the import of ammonium blowdown tower, the export of ammonium blowdown tower with change the salt basin and be linked together, ammonium blowdown top of the tower portion emptys. The utility model discloses an it is very obvious to remove the ammonium effect, once makes with extra care total ammonium (amine) the mean value <= 4ppm of salt solution, and nitrogen trichloride content mean value <= 40ppm in the liquid chlorine has guaranteed to remove the ammonium effect, has eliminated the nitrogen trichloride and for the major safety risks that the serial production brought, has guaranteed the system security and stablized continuous operation.
Description
Technical field
The utility model belongs to except ammonium technical field, is specifically related to a kind of Removal of Ammonium from Brine device.
Background technology
In ion-exchange membrane electrolysis alkaline production technique, in bittern, ammonium content is higher, easily produces nitrogen trichloride when electrolysis.Nitrogen trichloride severe toxicity, has strong and stimulating, and to heat, vibrations, clash into and rub quite responsive, very easily decompose and blast, its natural temperature of explosion is 95 DEG C, there is the possibility of blast when volume fraction reaches 5%-6% in chlorine.The pernicious explosion hazard of nitrogen trichloride can cause huge personal injury and property damage, brings hidden danger to the safety in production of chlorine industry.
In order to ensure the safety in production of chlorine industry, usually need to carry out, except ammonium process, ammonium content in bittern being reduced to the index required for production of caustic soda, to reduce the growing amount of nitrogen trichloride in electrolytic process to bittern.Existing ammonium technique of removing is: subsurface brine (returning light salt brine containing the electrolyzer) concentration that salt mine gathers is at 300-310g/L, be delivered to the bittern basin (H15m) of two 5000m3, NaOH solution is added at brine pump suction line note, brine ph is regulated to be that after 9-10.5, note adds NaClO solution, after titanium plate-type heat exchanger I utilizes electrolysis to return light salt brine preheating, temperature rises to 40 DEG C, then utilizes the low-pressure saturated steam of 0.25MPa to be heated to more than 60 DEG C through titanium plate-type heat exchanger II.The object adding NaClO solution removes the ammonium in bittern, and generate labile monochloro amine and dichlormaine, reaction formula is: NH
3+ HClO=NH
2cl+H
2o, NH
3+ HClO=NHCl
2+ H
2o, then enters except ammonium tower, and use the air of gas blower input to blow down, then feedingization brine storage tank, enters salt refining flow process and prepare primary purification salt solution.
There are problems in above-mentioned technique: (1) brine ph needs to control as 7-9, and present production control is at 9-11, and pH value controls higher easy blocking pipe; (2) because bittern interchanger is that the less brine temperature of plate-type heat exchanger heat does not reach 60 DEG C; (3) bittern tank does not have series operation to make bittern extract the impurity come up directly to take in production system; (4) clorox coal addition position is on the outlet conduit of brine pump, and reaction process is shorter.
Summary of the invention
The technical problems to be solved in the utility model is that existing ammonium technique of removing exists problems: (1) brine ph needs to control as 7-9, and present production control is at 9-11, and pH value controls higher easy blocking pipe; (2) because bittern interchanger is that the less brine temperature of plate-type heat exchanger heat does not reach 60 DEG C; (3) bittern tank does not have series operation to make bittern extract the impurity come up directly to take in production system; (4) clorox coal addition position is on the outlet conduit of brine pump, and reaction process is shorter, and for solving the problem, the utility model provides a kind of Removal of Ammonium from Brine device.
The purpose of this utility model realizes in the following manner:
A kind of Removal of Ammonium from Brine device, comprise bittern water pipeline, described bittern water pipeline is connected with the opening for feed of bittern tank A, NaOH pipeline is connected with the opening for feed of bittern tank A, the discharge port of bittern tank A is connected with the opening for feed of bittern tank B, NaClO pipeline and air line are all connected with the opening for feed of bittern tank B, the discharge port of bittern tank B is connected with interchanger, the import that outlet and the ammonium of interchanger blow down tower is connected, the import that blower fan blows down tower with ammonium is connected, the outlet that ammonium blows down tower is connected with change saline slot, and ammonium blows down top of tower emptying.
Described interchanger is tubular heat exchange.
Described interchanger comprises the heat exchanger I and heat exchanger II that connect successively, and the discharge port of bittern tank B is communicated with heat exchanger I, and hot device II exports and is connected with the import that ammonium blows down tower.
Described heat exchanger I and electrolysis return light salt brine pipeline and are connected, and return light salt brine provide heat by electrolysis, return light salt brine enter and return well slot through the electrolysis of heat exchange; Described heat exchanger II is connected with vapour line, provides heat by steam, enters return well slot or boiler systems through the water of condensation of heat exchange.
Described ammonium is blown down between tower with change saline slot and is connected by the pipeline be in series with except ammonium brine pump.
Described heat exchanger I and heat exchanger II are titanium tubular heat exchange.
Relative to prior art, the utility model changes original two bittern basins in parallel into series connection and uses, bittern tank A receives Brine of Salt Mine, liquid level keeps more than 85%, to annotate NaOH solution simultaneously, adjustment brine ph is 7-9, after the impurity such as silt are effectively deposited in bittern tank A, from the overflow of tank body top to bittern tank B, liquid level keeps the filling of more than 30%, NaClO solution in bittern tank B, and the free chlorine in maintenance bittern tank B is at 10-15ppm, in bittern tank B, set up air stirring pipe simultaneously, the ammonium sufficient reacting that removes in bittern tank B is completed.Solid impurity in Brine of Salt Mine and suspended impurity, fully deposited in bittern tank A, stability contorting brine ph is 8-9, extends interchanger and the life cycle except ammonium tower, for the steady running except ammonium technique is laid a good foundation.Plate-type heat exchanger is long for duration of service one, and easy fouling and clogging, substitutes plate-type heat exchanger tubular heat exchange, can extend the use technology cycle of interchanger.Change the coal addition position of NaClO into bittern tank B by brine pump suction line, the ammonium in NaClO and bittern is fully reacted, improve except ammonium effect.
Of the present utility model except ammonium effect clearly, the total ammonium of primary purification salt solution (amine) average≤4ppm, nitrogen trichloride content average≤40ppm in liquid chlorine, ensure that except ammonium effect, eliminate nitrogen trichloride and produce the major safety risks brought to system, ensure that the safety and stability of system is run continuously.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model.
Wherein, 1 is bittern water pipeline; 2 is bittern tank A; 3 is NaOH pipelines; 4 is bittern tank B; 5 is NaClO pipelines; 6 is air lines; 7 is tubular heat exchanges I; 8 is tubular heat exchanges II; 9 is that ammonium blows down tower; 10 being saline slot; 11 is that electrolysis returns light salt brine pipeline; 12 is return well slot; 13 is vapour lines; 14 is boiler systemss; 15 is except ammonium brine pump; 16 is blower fans.
Embodiment
As shown in Figure 1, a kind of Removal of Ammonium from Brine device, comprise bittern water pipeline 1, described bittern water pipeline 1 is connected with the opening for feed of bittern tank A2, NaOH pipeline 3 is connected with the opening for feed of bittern tank A2, the discharge port of bittern tank A2 is connected with the opening for feed of bittern tank B4, NaClO pipeline 5 and air line 6 are all connected with the opening for feed of bittern tank B4, the discharge port of bittern tank B4 is connected with interchanger, the import that outlet and the ammonium of interchanger blow down tower 9 is connected, the import that blower fan 16 blows down tower 9 with ammonium is connected, the outlet that ammonium blows down tower 9 is connected with change saline slot 10, ammonium blows down tower 9 top emptying.
Described interchanger is tubular heat exchange.
Described interchanger comprises the heat exchanger I 7 and heat exchanger II 8 that connect successively, and the discharge port of bittern tank B4 is communicated with heat exchanger I 7, and hot device II 8 exports and is connected with the import that ammonium blows down tower 9.
Described heat exchanger I 7 and electrolysis return light salt brine pipeline 11 and are connected, and return light salt brine provide heat by electrolysis, return light salt brine enter and return well slot 12 through the electrolysis of heat exchange; Described heat exchanger II 8 is connected with vapour line 13, provides heat by steam, enters return well slot 12 or boiler systems 14 through the water of condensation of heat exchange.
Described ammonium is blown down between tower 9 with change saline slot 10 and is connected by the pipeline be in series with except ammonium brine pump 15.
Described heat exchanger I 7 and heat exchanger II 8 are titanium tubular heat exchange.
Working process of the present utility model is as follows: bittern enters bittern tank A2 by bittern water pipeline 1, liquid level keeps more than 85%, NaOH solution injects bittern tank A2 by NaOH pipeline 3, and adjustment brine ph is 7-9, and the solid impurity in Brine of Salt Mine and suspended impurity are (as Mg
2+deng) fully deposited in bittern tank A2.Pass through the bittern bittern tank A2 top overflow of purification to bittern tank B4, liquid level keeps more than 30%, NaClO solution to inject bittern tank B4 by NaClO pipeline 5, reacts: NH
3+ HClO=NH
2cl+H
2o, NH
3+ HClO=NHCl
2+ H
2o, generates labile monochloro amine and dichlormaine, and air enters bittern tank B4 by air line 6, plays stirring action to the solution in bittern tank B4, and the ammonium sufficient reacting that removes in bittern tank B is completed.Through carrying out heat exchange except the bittern of ammonium reaction is introduced into tubular heat exchange I 7, temperature rises to about 50 DEG C, then enters tubular heat exchange II 8 and carry out heat exchange, and temperature rises to about 60 DEG C, wherein tubular heat exchange I 7 returns light salt brine by electrolysis and provides heat, and tubular heat exchange II 8 provides heat by steam.Bittern through heating up enters ammonium and blows down tower 9, opens blower fan 10, after blowing down ammonium by pressurized air, except ammonium bittern uses except in squeezing into of ammonium brine pump 15 saline slot 10.
Relative to prior art, the utility model changes original two bittern basins in parallel into series connection and uses, bittern tank A receives Brine of Salt Mine, liquid level keeps more than 85%, to annotate NaOH solution simultaneously, adjustment brine ph is 7-9, after the impurity such as silt are effectively deposited in bittern tank A, from the overflow of tank body top to bittern tank B, liquid level keeps the filling of more than 30%, NaClO solution in bittern tank B, and the free chlorine in maintenance bittern tank B is at 10-15ppm, in bittern tank B, set up air stirring pipe simultaneously, the ammonium sufficient reacting that removes in bittern tank B is completed.Solid impurity in Brine of Salt Mine and suspended impurity are fully deposited in bittern tank A, and stability contorting brine ph is 8-9, extend interchanger and the life cycle except ammonium tower, for the steady running except ammonium technique is laid a good foundation.Plate-type heat exchanger is long for duration of service one, and easy fouling and clogging, substitutes plate-type heat exchanger tubular heat exchange, can extend the use technology cycle of interchanger.Change the coal addition position of NaClO into bittern tank B by brine pump suction line, the ammonium in NaClO and bittern is fully reacted, improve except ammonium effect.
Of the present utility model except ammonium effect clearly, the total ammonium of primary purification salt solution (amine) average≤4ppm, nitrogen trichloride content average≤40ppm in liquid chlorine, ensure that except ammonium effect, eliminate nitrogen trichloride and produce the major safety risks brought to system, ensure that the safety and stability of system is run continuously.
Above-described is only preferred implementation of the present utility model; it should be pointed out that for a person skilled in the art, do not departing under the utility model general idea prerequisite; can also make some changes and improvements, these also should be considered as protection domain of the present utility model.
Claims (6)
1. a Removal of Ammonium from Brine device, comprise bittern water pipeline (1), it is characterized in that: described bittern water pipeline (1) and bittern tank A(2) opening for feed be connected, NaOH pipeline (3) and bittern tank A(2) opening for feed be connected, bittern tank A(2) discharge port and bittern tank B(4) opening for feed be connected, NaClO pipeline (5) and air line (6) all with bittern tank B(4) opening for feed be connected, bittern tank B(4) discharge port be connected with interchanger, the import that outlet and the ammonium of interchanger blow down tower (9) is connected, the import that blower fan (16) and ammonium blow down tower (9) is connected, the outlet that ammonium blows down tower (9) is connected with change saline slot (10), ammonium blows down tower (9) top emptying.
2. Removal of Ammonium from Brine device according to claim 1, is characterized in that: described interchanger is tubular heat exchange.
3. Removal of Ammonium from Brine device according to claim 1 and 2, it is characterized in that: described interchanger comprises the heat exchanger I (7) and heat exchanger II (8) that connect successively, bittern tank B(4) discharge port be communicated with heat exchanger I (7), hot device II (8) exports and is connected with the import that ammonium blows down tower (9).
4. Removal of Ammonium from Brine device according to claim 3, it is characterized in that: described heat exchanger I (7) and electrolysis return light salt brine pipeline (11) and be connected, return light salt brine by electrolysis and heat is provided, return light salt brine through the electrolysis of heat exchange and enter and return well slot (12); Described heat exchanger II (8) is connected with vapour line (13), provides heat by steam, enters return well slot (12) or boiler systems (14) through the water of condensation of heat exchange.
5. Removal of Ammonium from Brine device according to claim 1, is characterized in that: described ammonium is blown down between tower (9) with change saline slot (10) and is connected by the pipeline be in series with except ammonium brine pump (15).
6. Removal of Ammonium from Brine device according to claim 3, is characterized in that: described heat exchanger I (7) and heat exchanger II (8) are titanium tubular heat exchange.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520410147.8U CN204918788U (en) | 2015-06-15 | 2015-06-15 | Brine removes ammonium device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520410147.8U CN204918788U (en) | 2015-06-15 | 2015-06-15 | Brine removes ammonium device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN204918788U true CN204918788U (en) | 2015-12-30 |
Family
ID=54967934
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520410147.8U Expired - Fee Related CN204918788U (en) | 2015-06-15 | 2015-06-15 | Brine removes ammonium device |
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|---|---|
| CN (1) | CN204918788U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111020631A (en) * | 2019-10-11 | 2020-04-17 | 江苏梅兰化工有限公司 | Method for removing ammonium from brine |
-
2015
- 2015-06-15 CN CN201520410147.8U patent/CN204918788U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111020631A (en) * | 2019-10-11 | 2020-04-17 | 江苏梅兰化工有限公司 | Method for removing ammonium from brine |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20151230 Termination date: 20160615 |