CN100513324C - Pre-treatment method for sea salt water - Google Patents
Pre-treatment method for sea salt water Download PDFInfo
- Publication number
- CN100513324C CN100513324C CNB2006100602406A CN200610060240A CN100513324C CN 100513324 C CN100513324 C CN 100513324C CN B2006100602406 A CNB2006100602406 A CN B2006100602406A CN 200610060240 A CN200610060240 A CN 200610060240A CN 100513324 C CN100513324 C CN 100513324C
- Authority
- CN
- China
- Prior art keywords
- water
- extra large
- salt water
- ion
- treatment process
- 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.)
- Expired - Fee Related
Links
Images
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Treatment Of Water By Ion Exchange (AREA)
Abstract
A method for pre-treating saline sea water comprises the following steps. Step 1, clarify, to produce a certain amount of slurry waste water and add a ''xianchaoling'' purifying agent in the saline sea water. The purifying agent is an ionic hydrocarbon polymer with the molecular weight of 8M-15M containing an alkali metal ferrate and an alkali metal aluminum carbonate salt and alkali metal ammonium phosphate mixed salt prepared in proportion by dissolving in an amine-contained alkali solution, which is slowly reduced to 65-90 degree and maintained for a certain period of time till strongly viscous high molecular polymer is produced. Step 2, ion exchange in ion-exchange apparatus. Step 3, put the saline sea water after step 2 in a desalting apparatus for desalting to produce the products concentrated water and plain water. Step 4, the concentrated water obtained in step 3 is partly used as industrial pure saline water and partly used as regeneration pure saline water which is returned to the ion-exchange apparatus in step 2 to regenerate the ion-exchange resin and then produce regeneration waste water.
Description
Technical field
The present invention relates to a kind of extra large desalination treatment process, relate in particular to a kind of treatment process of extra large salt water.
Background technology
In the prior art, it generally is the technical process of adopting as shown in Figure 1 that the desalination of extra large salt water is handled.
Desalination in this technical process comprises one or more combinations in the equipment such as electrodialysis, reverse osmosis, distillation.Five processes in this technical process before the desalination is referred to as the processing of extra large salt water.This technical process widespread use, fresh water yield from several kilograms, tens tons of hundreds ofs, several kilotons example is all arranged in running all over the world.
But this technical process has substantial defective:
1, can not remove fouling tendency compound in the treating water, cause the power consumption height;
The finings that it uses, it is conventional alite compound, as Tai-Ace S 150, iron(ic) chloride, aluminum chloride etc. and polymkeric substance thereof, it is the just effective finings of a kind of fresh water, and in the extra large salt water of the high electric charge of polyelectrolyte concentration, its charge neutrality clarification mechanism is very limited, and not only clarifying effect is very poor, and fouling tendency compound in can not most removal water.Though in technical process, added Scale inhibitors before the desalination, only to play the effect of fouling tendency compound complexing in water, attempt improves the solubleness of fouling tendency compound in water, but hidden danger still exists and effect is limited.Fouling in the desalting plant is stopped up still and is often taken place, and causes the regular shutdown of desalination system, unpicks and washes, back flushing.And the saturating flux reduction of film, thereby energy consumption height.
2, water utilization rate is low;
Technical process has three kinds of waste water to dump in a large number in this, comprise avoid fouling stop up and discharge concentrate extra large salt water in a large number, filter processing apparatus and consume the light waste water of backwash that a large amount of fresh water back flushinges form, the mud (water ratio is more than 95%) that the clarification processing apparatus is discharged for cleaning each.These three kinds of waste water have accounted for the 70-80% of whole desalination system flooding quantity, and 1 ton of fresh water of promptly every production has at least 3-5 ton water resources contaminated and dump.
3, waste water resource can not effectively utilize;
Above-mentioned three kinds of waste water have comprised whole resources and the pollutent except that fresh water in the extra large salt water, owing to amount mixes greatly, still can't purify recovery cheaply at present, the result had both wasted resource, polluted environment again, waste water is discharged to and causes the soil salinization to recover in the soil.
4, the system complex investment is big;
This technical process treating part just comprises 5 basic working procedure, also needs to increase utility appliance, robot control system(RCS), and system is complicated more, and reliability is poor more, error accident probability height, and investment is high.
Summary of the invention
The objective of the invention is to overcome the above-mentioned defective that exists in the extra large desalination traditional technology, improve fresh water production technology.
For achieving the above object, the invention provides a kind of extra large salt water treatment process, it may further comprise the steps:
Step 1: clarification produces some mud waste waters; At extra large salt water scavenging agent, this scavenging agent is the ionic hydrocarbon polymer with basic metal ferrate, basic metal carbonic acid aluminium salt, basic metal ammonium phosphate double salt and molecular weight 800-1500 ten thousand, ratio in 1:3.8-6.8:1-8:0.01-0.08 is composite, under the 85-150 degree celsius temperature, being dissolved in the basic solution that contains amine reacted 5 hours, slowly be cooled to 65-90 degree centigrade, be incubated 5 hours and the strong viscosity high molecular polymer that generates;
Step 2: in ion-exchange unit, carry out ion exchange treatment;
Step 3: the extra large salt water of handling through step 2 enters the desalting plant desalination, obtains finished product fresh water and dense water;
Step 4: the dense water that obtains in the step 3, a part are as industrial pure salt solution, and another part returns in the ion-exchange unit of step 2 with pure salt solution as regeneration and makes ion exchange resin regeneration, the generation regenerative wastewater.
The present invention has following beneficial effect:
1, added scavenging agent, desalting plant can structure not stop up again; Also noting be used in extra large salt water enters and adds Scale inhibitors before the desalting plant;
2, owing to there is not the sorrow of fouling obstruction, all prevent that the various autocontrol part aided processes of the stifled match of desalting plant structure from can omit, and have simplified technical process, have reduced cost of investment and desalinating cost;
3, the dense water that comes out of desalting plant can be made technical pure salt solution and the pure salt solution of regenerating, and has fully utilized resource, non-environmental-pollution, and the fresh water cost is lower.
Description of drawings
Fig. 1 is the process flow sheet that the desalination of the extra large salt water of prior art is handled.
Fig. 2 is the technological principle schema of the present invention sea salt water treatment process.
Fig. 3 is the process flow sheet of the embodiment one of the present invention sea salt water treatment process.
Embodiment
A kind of extra large salt water treatment process, it may further comprise the steps:
Step 1: clarification produces some mud waste waters;
In this step, at extra large salt water scavenging agent, chemical reaction takes place in them, generates the mud waste water that a kind of high-density, sedimentation are fast, have the Adsorption and Sterilization filtering function, makes the disposable realization of extra large salt water not have the sand clarification, and stain removal bactericidal is removed the fouling tendency compound.This step can be realized in existing various clarification equipment pond.
This scavenging agent is the ionic hydrocarbon polymer of a kind of basic metal ferrate, a kind of basic metal carbonic acid aluminium salt, basic metal ammonium phosphate double salt, molecular weight 800-1500 ten thousand, ratio according to 1:3.8-6.8:1-8:0.01-0.08 is composite, under the 85-150 degree celsius temperature, being dissolved in the basic solution that contains amine reacted 5 hours, slowly be cooled to 65-90 degree centigrade, be incubated 5 hours and the strong viscosity high molecular polymer that generates.
Step 2: in ion-exchange unit, carry out ion exchange treatment;
This is the amberlite lipoprotein mixture that a kind of zwitterion reaches 1:10, can further adsorb Ca, Mg and Fe plasma and dissolved organic matter in the extra large salt water, and extra large salt water is further purified, and becomes pure extra large salt water.Existing commercially available ion exchange tower just can adapt to this operation.
Step 3: the extra large salt water of handling through step 2 enters the desalting plant desalination, obtains finished product fresh water and dense water;
Existing various desalting plant can be applied mechanically this process as electrodialysis, reverse osmosis, distillation etc.Because various suspended substances, pollutent, bacterium in the extra large salt water, foulant is all clarified and the ion-exchange step Ex-all, and therefore problems such as fouling obstruction can not take place again, can produce finished product fresh water smoothly.
Step 4: the dense water that obtains in the step 3, a part offers industrial salt manufacturing or soda ash as industrial pure salt solution, and another part returns in the ion-exchange unit of step 2 with pure salt solution as regeneration and makes ion exchange resin regeneration, the generation regenerative wastewater;
The dense water that desalting plant is discharged in this step 3, salt concentration is higher, purer to be pure strong brine (sodium chloride concentration 5-10%), can directly be applied in industrial salt manufacturing, system soda ash or other industrial salt occasions.Some returns this dense water in the ion exchange tower, and effect is to make the saturated ion exchange resin regeneration that adsorbs Ca, Mg and Fe.
Step 5: the mud waste water of generation in the step 1 and the regenerative wastewater of step 4 generation are handled through polyreaction, generated composite water purifying agent.
The mud waste water of discharging in the clarification steps contains the ferro-aluminum composition in the scavenging agent, but has become the slurry of oxyhydroxide.Contain the positively charged ions such as magnesium calcium iron boron in the extra large salt water in the regenerative wastewater in the ion exchange treatment step, these two kinds of waste water are mixed, be adjusted to about PH3-3.5 with sulfuric acid, these compositions polyreaction mutually then, become a kind of normally used iron magnalium calcium compound type purifying agent, in wastewater treatment, it has flocculation, clarification, decolouring function.See also Fig. 2, understand complete more clear present method.
Embodiment one
System with 10 tons of extra large salt water treatment capacities is an example below, and specific embodiments of the present invention is described, the water source, coastal inland river that this scheme is specially adapted to influenced by the salty tide of seawater is handled, the salty tidewater of popular title.
According to technical process shown in Figure 3, assembling main equipment, instrument, pipe valve etc.
The specification of various device and function see also following table:
| Device name | Specification | Function |
| Tank | 100-200m 3 | Store the salty tidewater in inland river |
| The pressure type clarifying filter | 7-13m 3/ hour, pressure of supply water 3kg/cm 2 | Make salty tidewater clarification, sterilization, removal pollutent, remove part fouling tendency compound |
| Ion exchange tower | Cation type resin 600 liters | Further purifying salty tidewater is pure NaCl salt solution |
| Electrodialyzer | 2 grades or 3 grades of 7-13m 3/ hour | The pure NaCl saline water conversion that ion exchange tower is come out is a fresh water |
| Counter-osmosis device | 2 grades or 3 grades of 0.7-1.3m 3/ hour | The dense water that electrodialyzer is come out is condensed into pure salt solution of regeneration and industrial pure salt solution |
| Mud waste water and regenerative wastewater bin | 2-3m 3 | Store mud waste water and regenerative wastewater, regulating pH value becomes composite water purifying agent |
| The finished product fresh-water tank | 20-30m 3 | Store fresh water |
This tank, very important to reducing the fresh water cost in native system, because along with the ebb of rising, salty tidewater saliferous total amount changes between fresh water 300ppm at seawater value 30000ppm, in the time of most of at 3000ppm between the 1500ppm.10-20 hour consumption of tank water storage, the operation on keep away salty get light, when promptly salty tidewater saltiness is high, the water inlet of cut-out tank after the ebb, recovers water storage, the salinity of the water in the tank is controlled between the 500-1500ppm, and this moment, desalinating cost and power consumption were minimum.
For improving the reliability of operation, native system equipment designs by the highest salinity 1500ppm that contains of tank.
As can be seen from Figure 3, the present invention sea salt water treatment process may further comprise the steps:
Step 1: send extra large salt water to a tank;
As mentioned above, tank water storage operation is gone up to keep away and is saltyly got lightly, when promptly salty tidewater saltiness is high, cuts off the tank water inlet, after the ebb, recovers water storage, and the salinity of the water in the tank is controlled between the 500-1500ppm, and desalinating cost and power consumption are minimum at this moment.
Step 2: clarification produces some mud waste waters;
In this step, in extra large salt water, use scavenging agent, chemical reaction takes place in them, generates the mud waste water that a kind of high-density, sedimentation are fast, have the Adsorption and Sterilization filtering function, makes the disposable realization clarification of extra large salt water, and stain removal bactericidal is removed the fouling tendency compound.Clarification equipment in the present embodiment promptly is pressure type clarifying filter above-mentioned.
Step 3: in ion-exchange unit, carry out ion exchange treatment;
The ion exchange tower that present embodiment is used has 600 liter cation type resins, can further adsorb Ca, Mg and Fe plasma and dissolved organic matter in the extra large salt water, and extra large salt water is further purified, and becomes pure NaCl salt solution.
Step 4: the extra large salt water after ion exchange treatment enters the electrodialyzer desalination, obtains finished product fresh water and dense water;
Step 5: the dense water that comes out from electrodialyzer enters the counter-osmosis device desalination, obtains finished product fresh water and dense water;
Step 4 and step 5 all belong to the desalination step.
Step 6: the dense water that obtains in the step 5, industrial salt manufacturing or soda ash are directly used or offered to a part as industrial pure salt solution, another part returns in the ion-exchange unit of step 3 with pure salt solution as regeneration and makes ion exchange resin regeneration, the generation regenerative wastewater;
The dense water that counter-osmosis device is discharged in this step 5, salt concentration is higher, purer to be pure strong brine (sodium chloride concentration 5-10%), can directly be applied in industrial salt manufacturing, system soda ash or other industrial salt solution occasions.Some returns this dense water in the ion exchange tower, and effect is to make the saturated ion exchange resin regeneration that adsorbs Ca, Mg and Fe.
Step 7: the mud waste water of generation in the step 2 and the regenerative wastewater of step 6 generation are handled through polyreaction, generated composite water purifying agent.
The mud waste water of discharging in the clarification steps contains the ferro-aluminum composition in the scavenging agent, but has become the slurry of oxyhydroxide.Contain the positively charged ions such as magnesium calcium iron boron in the extra large salt water in the regenerative wastewater in the ion exchange treatment step, these two kinds of waste water are mixed, be adjusted to about PH3-3.5 with 98% sulfuric acid or 30% hydrochloric acid, these compositions polyreaction mutually then, become a kind of normally used iron magnalium calcium compound type purifying agent, in wastewater treatment, it has flocculation, clarification, decolouring function.
Claims (7)
1, a kind of extra large salt water treatment process is characterized in that it may further comprise the steps:
Step 1: clarification produces some mud waste waters; This step is used scavenging agent in extra large salt water, this scavenging agent is the ionic hydrocarbon polymer with basic metal ferrate, basic metal carbonic acid aluminium salt, basic metal ammonium phosphate double salt and molecular weight 800-1500 ten thousand, ratio in 1:3.8-6.8:1-8:0.01-0.08 is composite, under the 85-150 degree celsius temperature, being dissolved in the basic solution that contains amine reacted 5 hours, slowly be cooled to 65-90 degree centigrade, be incubated 5 hours and the strong viscosity high molecular polymer that generates;
Step 2: in ion-exchange unit, carry out ion exchange treatment;
Step 3: the extra large salt water of handling through step 2 enters the desalting plant desalination, obtains finished product fresh water and dense water;
Step 4: the dense water that obtains in the step 3, a part are as industrial pure salt solution, and another part returns in the ion-exchange unit of step 2 with pure salt solution as regeneration and makes ion exchange resin regeneration, the generation regenerative wastewater.
2, extra large salt water treatment process according to claim 1 is characterized in that, this sea salt water treatment process also comprises step 5: the mud waste water of generation in the step 1 and the regenerative wastewater of step 4 generation are handled through polyreaction, generated composite water purifying agent.
3, extra large salt water treatment process according to claim 2, it is characterized in that, the mud waste water that step 1 is discharged contains the ferro-aluminum composition in the scavenging agent, contain the positively charged ions such as magnesium calcium iron boron in the extra large salt water in the regenerative wastewater of step 4, these two kinds of waste water are mixed, be adjusted to PH3-3.5 with sulfuric acid or hydrochloric acid, these compositions are polyreaction mutually, becomes a kind of iron magnalium calcium compound type purifying agent.
4, extra large salt water treatment process according to claim 1 is characterized in that, this step 2 comprises a step 2a: the extra large salt water after ion exchange treatment enters the electrodialyzer desalination, obtains finished product fresh water and dense water; And step 2b: the dense water that comes out from electrodialyzer enters the counter-osmosis device desalination, obtains finished product fresh water and dense water.
5, extra large salt water treatment process according to claim 1 is characterized in that, also has a step before step 1: send extra large salt water to a tank.
6, extra large salt water treatment process according to claim 5 is characterized in that, should keep away in the tank water storage operation salty get light, be salty tidewater saltiness high the time, cut off the tank water inlet, after the ebb, recover water storage, the salinity of the water in the tank is controlled between the 500-1500ppm.
7, extra large salt water treatment process according to claim 1 is characterized in that, this ion-exchange unit contains the amberlite lipoprotein mixture that zwitterion reaches 1:10.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100602406A CN100513324C (en) | 2006-04-10 | 2006-04-10 | Pre-treatment method for sea salt water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100602406A CN100513324C (en) | 2006-04-10 | 2006-04-10 | Pre-treatment method for sea salt water |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101054220A CN101054220A (en) | 2007-10-17 |
| CN100513324C true CN100513324C (en) | 2009-07-15 |
Family
ID=38794301
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2006100602406A Expired - Fee Related CN100513324C (en) | 2006-04-10 | 2006-04-10 | Pre-treatment method for sea salt water |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100513324C (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2011092803A (en) * | 2009-10-27 | 2011-05-12 | Panasonic Electric Works Co Ltd | Water processing device |
| AU2011252769A1 (en) * | 2010-05-13 | 2012-12-06 | Clean Teq Holdings Ltd. | Water treatment process |
| CN102020383B (en) * | 2010-12-01 | 2012-04-04 | 杭州水处理技术研究开发中心有限公司 | Bipolar membrane-reverse osmosis method sea water desalination and integrated treatment method |
| WO2014193955A1 (en) * | 2013-05-29 | 2014-12-04 | Lehigh University | Brackish water desalination using tunable anion exchange bed |
| CN104230087B (en) * | 2014-09-30 | 2016-06-01 | 东莞市英硫净水服务有限公司 | The desalination treatment process of a kind of haline water |
| CN106219830A (en) * | 2016-06-01 | 2016-12-14 | 东莞汇金环境科技有限公司 | A kind of electroplated heavy metals wastewater zero discharge system and method |
-
2006
- 2006-04-10 CN CNB2006100602406A patent/CN100513324C/en not_active Expired - Fee Related
Non-Patent Citations (2)
| Title |
|---|
| 油田用阻垢剂及其筛选. 徐僖，郑邦乾，朱清泉.大庆石油地质与开发，第3卷第3期. 1984 |
| 油田用阻垢剂及其筛选. 徐僖，郑邦乾，朱清泉.大庆石油地质与开发，第3卷第3期. 1984 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101054220A (en) | 2007-10-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Li et al. | Intermediate concentrate demineralization techniques for enhanced brackish water reverse osmosis water recovery–A review | |
| Ogunbiyi et al. | Sustainable brine management from the perspectives of water, energy and mineral recovery: A comprehensive review | |
| Ezechi et al. | Boron in Produced VVater: Challenges and Improvements: A Comprehensive Review | |
| CN105939970B (en) | System and method for removing minerals from brine using electrodialysis | |
| CN101928088B (en) | Method for treating reverse osmosis concentrated water of petrochemical enterprises | |
| CN104843927A (en) | Desulfurization waste water zero discharging process and system | |
| CN105439341B (en) | A kind of brine waste processing system and processing method | |
| CN103214115B (en) | Water treatment method of strong acid cation exchange resin incomplete regeneration | |
| EP2268583A2 (en) | Sulfate removal from water sources | |
| CN101767888A (en) | Wastewater recycling treatment process | |
| CN100513324C (en) | Pre-treatment method for sea salt water | |
| CN105084587A (en) | Treatment method and equipment of high-salt waste water | |
| CN102438957A (en) | Method for treatment and purification of seawater to recover high purity sodium chloride for industrial usage | |
| CN207130086U (en) | A kind of salt-containing waste water treating device | |
| CN107915354A (en) | A kind of desulfurization wastewater zero-emission and resource utilization device and method | |
| CN113955888A (en) | Integrated treatment system and process for recycling concentrated brine in coking wastewater | |
| CN107381881A (en) | The method of wastewater treatment and processing unit of desulfurization wastewater zero-emission | |
| CN203728664U (en) | Wastewater recovery system | |
| CN105540971A (en) | Process for crushed coal pressurized gasification industrial wastewater deep processing and high recovery rate | |
| WO2013091129A1 (en) | Membrane filtration process for industrial process water treatment and recovery | |
| CN205442916U (en) | Contain salt effluent disposal system | |
| CN113087259B (en) | Process for non-softening concentration of high-salt wastewater based on nanofiltration of recycled salt | |
| CN107055886B (en) | A kind of depth graded divides salt technique | |
| CN102897947A (en) | Reverse osmosis (RO) desalting treatment method and treatment system with ultrahigh water recovery rate for waste water containing high sulfate radicals | |
| CN209923115U (en) | Salt recovery system and processing system for salt-containing wastewater |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20090715 Termination date: 20180410 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |