CN202208671U - Brine waste zero emission recovering system - Google Patents
Brine waste zero emission recovering system Download PDFInfo
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- CN202208671U CN202208671U CN201120332719.7U CN201120332719U CN202208671U CN 202208671 U CN202208671 U CN 202208671U CN 201120332719 U CN201120332719 U CN 201120332719U CN 202208671 U CN202208671 U CN 202208671U
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- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 title claims abstract description 73
- 239000012267 brine Substances 0.000 title claims abstract description 72
- 239000002699 waste material Substances 0.000 title claims abstract description 59
- 150000003839 salts Chemical class 0.000 claims abstract description 31
- 239000006200 vaporizer Substances 0.000 claims description 62
- 239000002351 wastewater Substances 0.000 claims description 57
- 238000000034 method Methods 0.000 claims description 32
- 238000010438 heat treatment Methods 0.000 claims description 30
- 239000013078 crystal Substances 0.000 claims description 16
- 238000002156 mixing Methods 0.000 claims description 16
- 238000011084 recovery Methods 0.000 claims description 15
- 238000007872 degassing Methods 0.000 claims description 13
- 238000003756 stirring Methods 0.000 claims description 8
- 238000001914 filtration Methods 0.000 claims description 7
- 238000009835 boiling Methods 0.000 claims description 6
- 238000005374 membrane filtration Methods 0.000 claims description 3
- 235000014347 soups Nutrition 0.000 claims description 3
- 239000012528 membrane Substances 0.000 abstract description 25
- 238000001704 evaporation Methods 0.000 abstract description 6
- 230000007613 environmental effect Effects 0.000 abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 55
- 239000010408 film Substances 0.000 description 36
- 239000002585 base Substances 0.000 description 18
- 239000007789 gas Substances 0.000 description 12
- 238000009833 condensation Methods 0.000 description 11
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- 238000002425 crystallisation Methods 0.000 description 9
- 230000008025 crystallization Effects 0.000 description 9
- 239000007788 liquid Substances 0.000 description 8
- 238000002203 pretreatment Methods 0.000 description 8
- 239000002918 waste heat Substances 0.000 description 8
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 6
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 6
- 238000000746 purification Methods 0.000 description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
- 235000011089 carbon dioxide Nutrition 0.000 description 5
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- 239000001301 oxygen Substances 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 239000012141 concentrate Substances 0.000 description 4
- 238000001471 micro-filtration Methods 0.000 description 4
- 239000002244 precipitate Substances 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- 238000000108 ultra-filtration Methods 0.000 description 4
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- 239000002253 acid Substances 0.000 description 3
- 235000011132 calcium sulphate Nutrition 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 3
- 239000010970 precious metal Substances 0.000 description 3
- 239000002455 scale inhibitor Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
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- 101100194816 Caenorhabditis elegans rig-3 gene Proteins 0.000 description 2
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 239000001110 calcium chloride Substances 0.000 description 2
- 229910001628 calcium chloride Inorganic materials 0.000 description 2
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- 238000001728 nano-filtration Methods 0.000 description 2
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- 239000001506 calcium phosphate Substances 0.000 description 1
- 229910000389 calcium phosphate Inorganic materials 0.000 description 1
- 235000011010 calcium phosphates Nutrition 0.000 description 1
- 239000001175 calcium sulphate Substances 0.000 description 1
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- 150000001875 compounds Chemical class 0.000 description 1
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- QORWJWZARLRLPR-UHFFFAOYSA-H tricalcium bis(phosphate) Chemical compound [Ca+2].[Ca+2].[Ca+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O QORWJWZARLRLPR-UHFFFAOYSA-H 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/30—Wastewater or sewage treatment systems using renewable energies
- Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy
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- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
A brine waste zero emission recovering system is characterized by including a stirrer (1), a membrane pretreatment device (2), a pre-heat-exchange device (3), a degasser (4), a second membrane pretreatment device (5), a second heat exchanger (6), a second degasser (7) and evaporators (8), wherein the evaporators (8) are formed through connecting one or more evaporators in series; each evaporator (8) is formed by a mixer (801) at the bottom, an evaporating pipe (802) in the middle and a distributor (803) at the upper part; the mixers (801) are connected with a separator (9) outside the evaporators (8); and the separator (9) is connected with a crystallized salt drier (10) and a circulating pump respectively. Brine waste separated by the separator (9) is sent to a channel box at the top of the evaporator through the circulating pump, flows to the distributors (803), and then sent to the evaporating pipes (802) through the distributors (803). The brine waste zero emission recovering system can realize the efficient environmental protection and zero emission through lower project investment and operating cost.
Description
Technical field
The utility model relates to a kind of method of wastewater treatment, the treatment process of the inorganic or organic waste water of especially a kind of high density, specifically a kind of brine waste zero release recovery system.
Background technology
" zero release " be meant ad infinitum reduce pollutent with can source emission until the activity that is zero: promptly utilize cleaner production; 3R (Reduce; Reuse Recycle) and technology such as ecological industry, realizes the complete recycle to natural resources; Thereby do not give atmosphere, water body and soil are left over any waste.
At present, various industry like industries such as electric power, chemical industry, oil refining, medicine, can produce the waste water of some high densitys, and these waste water be difficult to adopt traditional waste water treatment process to carry out 100% and handle and reach the requirement of discharging.Industry many times is owing to the waste water of itself facility discharge is restricted, and strict environmental requirement needs more consummate waste water reuse system, the particularly water resources shortage in western dry.Be the protection environment now, reduce the water consumption, all there is the many reuses of construction water factory in enterprise.But these reuse water factories also produce a large amount of waste water that can not satisfy emission request simultaneously, thereby can not become zero release water factory truly when producing high-quality pure water.
Summary of the invention
The purpose of the utility model is high to the brine film processing of generally using at present, thickener and mold cost; Particularly pre-treatment or membrane treatment process can't once be realized the problem of zero release; If need utilize vaporizer to carry out secondary treatment again; The result is vaporizer maximization, many with precious metal, and cost for wastewater treatment is high, the problem that can't promote the use of.Design a kind of brine waste zero release recovery system.
A kind of brine waste zero release recovery system is characterized in that it comprises
One whisking appliance 1, this whisking appliance 1 is provided with dosing mouth, stirs so that brine waste and institute add soup, and the pH value that makes waste water is between 5～6;
One film pretreater 2, this film treater 2 can make the saliferous rate of the adjusted brine waste of process pH value less than 10%;
One preparatory heat-exchanger rig 3, this preparatory heat-exchanger rig are used to make the filtering waste water of process film treater to be heated near boiling point from normal temperature;
One degasser 4, this degasser 4 are used for sending the row degassing to through the waste water of pre-heaters 3 heating, to remove the gas that generates in the brine waste;
The brine waste that one second film pretreater 5, this second film pretreater 5 will pass through after degasser 4 degassings carries out the secondary membrane filtration, so that the saliferous rate of waste water is less than 5%;
One second interchanger 6, this second interchanger 6 are used for the filtering waste water of process secondary film pretreater is carried out second-heating, and the temperature that makes brine waste is at 90 ℃-100 ℃;
One second degasser 7, this second degasser 7 are used for the waste water through second-heating is outgased, and to remove the gas that wherein generates, the internal pressure of this second degasser 7 will be higher than vaporizer 8 dirty bottom internal pressures;
One vaporizer 8; This vaporizer 8 is by one or more vaporizers and compose in series, and this vaporizer 8 is made up of the sparger 803 on mixing tank 801, intermediary generating tube 802 and the top of bottom, and mixing tank 801 links to each other with vaporizer 8 outside separators 9; Separator 9 is connected with crystal salt moisture eliminator 10 and recycle pump respectively; Recycle pump pumps into separator 9 isolated brine wastes in the bobbin carriage at vaporizer top, flows in the sparger 803 again, and sparger 803 is sent into brine waste in the generating tube 802 again.
The method that matches with said apparatus may further comprise the steps:
A kind of brine waste zero release recovery and treatment method is characterized in that it may further comprise the steps:
The first step gets in the whipping appts brine waste, and dosing stirs, and adjusts its pH value between 5～6, is converted into dissolved CO to guarantee the carbonate in the brine waste
2, become steam after the heating;
Second step made through handling in the adjusted brine waste entering of the pH value film pretreatment unit, and the saliferous rate that makes waste water is less than 10%;
The 3rd step preheated above-mentioned sending in the heat-exchanger rig through the pretreated waste water of film, and controlled temperature is heated near boiling point from normal temperature;
In the 4th step, will pass through pre-warmed waste water and send in the degasser and outgas, to remove the gas that wherein generates;
In the 5th step, the brine waste that will pass through outgases handles is sent in the secondary film pretreatment unit and is handled, so that the saliferous rate of waste water is less than 5%;
The 6th step, will pass through the pretreated waste water of secondary film and send into the secondary heat exchange device and carry out second-heating, the temperature that makes brine waste is at 90 ℃-100 ℃ evaporating point;
In the 7th step, the waste water that will pass through second-heating is sent into and is carried out the secondary degassing in the degasser, and to remove the gas that wherein generates, the degasser internal pressure is wanted a little higher than base of evaporator mixing tank internal pressure;
The 8th step; Enter into through the waste water of the secondary degassing in the mixing tank of one or more base of evaporators with dense salt after the evaporator tube intercrystalline concentrates out the separated steam of base of evaporator and mix; (concentration of strong brine is 1%-15%), the steam of separating are introduced subordinate's vaporizer as the generating tube thermal source or introduce the secondary heat exchange device and be condensed into the water purification reuse after as the thermal source heated waste water; Dense saline solution mixed in the base of evaporator mixing tank gets into the separator precipitate and separate again, isolates the dry use of crystal salt dispensing; Isolated brackish water liquid is delivered to the bobbin carriage at vaporizer top through recycle pump;, sparger, drops to that the bobbin carriage of generating tube bottom is interior to be separated steam with crystal salt in being evenly distributed to brackish water on each pipe of vaporizer heat-exchanging tube bundle by the outer steam heating vaporization of pipe, crystallization; The outer steam of the described pipe steam that to be the surplus vapour of LP steam or factory that produces of waste-heat recovery device, MP steam go out through the LP steam or the upper level vaporizer composite liberation of pressure and temperature reducing, the effect of short steam is that its latent heat is passed in the strong brine in the tube bank; Steam discharge become behind the latent heat water of condensation draw from vaporizer tube bank bottom as secondary add become after the thermal source heated waste water of interchanger water of condensation industrial or by pump delivery to the boiler reuse.The product water water quality of Zero discharging system is very high, reaches the index of pure water fully, but direct reuse is used as boiler feedwater in the circulation cooling or after simple precision processing.This pure water is if be used for recirculated cooling water, and its circulation cycles of concentration can be up to 15 times, and circulating cooling system does not produce sewer basically.
Evaporator operation principle: before vapo(u)rization system starts,, make calcium sulfate that brackish water produces in working cycle etc. be deposited in crystal growth on the salt kind through in base of evaporator mixing tank feed liquid, adding calcium sulphate crystal (as the salt kind).Owing in vaporizer circulating and evaporating concentration process, produced new salt kind, and new salt kind produces continuously, therefore when vaporizer normally moves, do not need to add in addition the salt kind.
The base of evaporator strong brine is recycled to the vaporizer top after separating through the bottom continuously, the process divider inflow evaporator heat-exchanging tube bundle at the top, and in tube bank, drop to kerve.In moisture film decline process, a part of water is heated evaporation.Thereby sparger forms uniform thin film with strong brine and prevents tube wall incrustation in tube bank.The shell side that steam gets into well heater is delivered to the strong brine in the tube bank to heat, forms water of condensation at shell side after the steam release of heat.Water of condensation is used for heating preheated feed water or cooling back water of condensation carries out reuse.
For avoiding in vaporizer, forming fouling, the strong brine of saliferous kind is circulation continuously in heat exchanger tube.Because the water of strong brine film evaporation in the tube bank, the remaining over-saturated brine film that becomes, calcium sulfate, calcium phosphate, tripoli and other scale-forming compound begin deposition.Sedimentary material has promoted that crystalline forms in the dope, and sedimentable matter sticks on the salt kind surface, thereby prevents to precipitate the surface scale that scale forming matter is not managed.Quantity discharged through crystallization dope in the control base of evaporator groove is to keep in the strong brine suitable concentration being arranged.
The utility model utilizes de-salted water, vapour that waste water is preheated and heats or produce steam or get into (salt) water that gives up before the vaporizer with the water heating that the outer heating steam of I and II vaporizer heat transfer tube is condensed with secondary (being final stage) vaporizer heat-exchanging tube bundle.The water purification that also available heating heat exchanger is condensed is useless (salt) water of preheating again, reaches the purpose that makes full use of waste heat recovery.
The utility model utilize steam that one-level vaporizer heat-exchanging tube bundle produces through demist with separate after, send into the secondary evaporimeter heat-exchanging tube bundle as thermal source, make full use of waste heat; By that analogy, steam that the secondary evaporimeter heat-exchanging tube bundle produces through demist with separate after, send into three grades of vaporizer heat-exchanging tube bundles as thermal source.
Described interchanger is out that one is equipped with, and is equipped with clean-in-place system.
Described film pretreatment unit and secondary film pretreatment unit are ionic membrane, membrane bioreactor, r-o-, nanofiltration, ultrafiltration or micro-filtration.
The beneficial effect of the utility model:
The utility model integrated application chemical treatment, membrane sepn, physics such as evaporative crystallization and drying, chemistry, biological process are concentrated into very high density with the solid salinity in the middle of the waste water, and the salt water crystallization uses, and does not discharge system.Having realized that especially pre-treatment or membrane treatment process can't once realize the problem of zero release, promptly is to utilize vaporizer to carry out secondary treatment again, the result be vaporizer maximize, many with precious metal, cost for wastewater treatment is high, can't promote the use of.A kind of waste heat brine waste zero release recovery and treatment method that makes full use of of the utility model, make vaporizer get volume minimize, most economical.
The utility model can be handled saline sewage and other waste water, and reclaim high quality boiler feedwater and public water every day from high density brine waste and other waste water.Help factory with less project investment and working cost the most at last, realize the environmental protection zero emission requirement.
The utility model adopts embrane method/hot method to combine, and can significantly reduce the investment and working cost of system: compare with the traditional hot method, the utility model can make investment reduce 50%～85%, and working cost reduces 40%～80%, thereby makes the more economical practicality of liquid zero emission system.
Description of drawings
Fig. 1 is the process flow diagram of the utility model.
Embodiment
Below in conjunction with accompanying drawing and embodiment the utility model is further described.
As shown in Figure 1.
A kind of brine waste zero release recovery system; It comprises mainly by whisking appliance 1, film pretreater 2, heat-exchanger rig 3, degasser 4, the second film pretreater 5, second interchanger 6, second degasser 7, vaporizer 8, separator 9 and crystal salt moisture eliminator 10 are formed in advance; As shown in Figure 1; Wherein: whisking appliance 1 is provided with dosing mouth, stirs so that brine waste and institute add soup, and the pH value that makes waste water is between 5～6; This film treater 2 can make the saliferous rate of the adjusted brine waste of process pH value less than 10%; Heat-exchanger rig is used to make the filtering waste water of process film treater to be heated near boiling point from normal temperature in advance; Degasser 4 is used for sending the row degassing to through the waste water of pre-heaters 3 heating, to remove the gas that generates in the brine waste; The brine waste that the second film pretreater 5 will pass through after degasser 4 degassings carries out the secondary membrane filtration, so that the saliferous rate of waste water is less than 5%; Second interchanger 6 is used for the filtering waste water of process secondary film pretreater is carried out second-heating, and the temperature that makes brine waste is at 90 ℃-100 ℃; Second degasser 7 is used for the waste water through second-heating is outgased, and to remove the gas that wherein generates, the internal pressure of this second degasser 7 will be higher than vaporizer 8 dirty bottom internal pressures; Vaporizer 8; This vaporizer 8 is by one or more vaporizers and compose in series, and this vaporizer 8 is made up of the sparger 803 on mixing tank 801, intermediary generating tube 802 and the top of bottom, and mixing tank 801 links to each other with vaporizer 8 outside separators 9; Separator 9 is connected with crystal salt moisture eliminator 10 and recycle pump respectively; Recycle pump pumps into separator 9 isolated brine wastes in the bobbin carriage at vaporizer top, flows in the sparger 803 again, and sparger 803 is sent into brine waste in the generating tube 802 again.Whisking appliance 1 in the present embodiment, film pretreater 2, in advance, to add heat-exchanger rig be that high-performance heat exchanger 3, degasser 4, the second film pretreater 5, second interchanger 6, second degasser 7, vaporizer 8, separator 9 and crystal salt moisture eliminator 10 are the water treatment field specific equipment; All can directly purchase or order, also can adopt relevant water treatment standard self design from market.
The key of the brine waste zero release recovery and treatment method that matches with said apparatus is to adopt Chemical Pretreatment+membrane process pre-treatment+evaporative crystallization+exsiccant waste liq zero-discharge technology (ZLD); Can handle saline sewage and other waste water, reclaim high quality boiler feedwater and public water every day from high density brine waste and other waste water.Help factory with less project investment and working cost the most at last, realize the environmental protection zero emission requirement.
Concrete treatment process is:
After brine waste or waste water get into sewage zero-discharge (ZLD) device; Respectively through add acid add alkali stirring, membrance chemistry pre-treatment (removing 90% brine waste), with de-salted water preheating, the degassing processings, membrance chemistry pre-treatment (removing the brine waste 95% or more), again with the steam heating, processing outgases; Waste water gets into a plurality of parallel connections or placed in-line brine waste vaporizer then; Use the outside LP steam that provides (factory's exhaust steam, waste gas residual heat reclaim steam or MP steam through the steam of pressure and temperature reducing); With the strong brine evaporative crystallization in the vaporizer tube bank; Mix with the dense salt after the evaporator tube intercrystalline goes out the separated steam of base of evaporator, the steam separated is introduced interchanger and is condensed into the water purification reuse after as the thermal source heated waste water; Dense saline solution mixed in the base of evaporator mixing tank gets into the separator precipitate and separate again, isolates the dry use of crystal salt dispensing; Isolated brackish water liquid is delivered to the bobbin carriage at vaporizer top through recycle pump; By steam heating vaporization, crystallization outside the pipe, the bobbin carriage that drops to base of evaporator separates steam with crystal salt in sparger is evenly distributed to brackish water on each pipe of vaporizer heat exchange bundle; Manage outer steam and be surplus vapour of LP steam or factory that waste-heat recovery device produces or the MP steam LP steam through pressure and temperature reducing, the effect of short steam is that its latent heat is passed in the strong brine in the tube bank; Steam discharge become behind the latent heat water of condensation draw from vaporizer tube bank bottom as become after the preheater thermal source heated waste water water of condensation industrial or by pump delivery to the boiler reuse.
Concrete steps are:
The first step gets in the whipping appts brine waste, and dosing (like calcium chloride, sulfuric acid and Scale inhibitors) stirs, and adjusts its pH value between 5～6, is converted into dissolved CO to guarantee the carbonate in the brine waste
2, become steam after the heating;
Second step made through handling in the adjusted brine waste entering of the pH value film pretreatment unit, and the saliferous rate that makes waste water is less than 10% (being that the salinity more than 90% is removed in the brine waste);
The 3rd step preheated above-mentioned sending in the heat-exchanger rig through the pretreated waste water of film, and controlled temperature is heated near boiling point (about 80-90 ℃) from normal temperature (20 ℃);
In the 4th step, will pass through pre-warmed waste water and send in the degasser and outgas, to remove the gas (removing carbonic acid gas, oxygen and other noncondensable gas) that wherein generates;
In the 5th step, the brine waste that will pass through outgases handles is sent in the secondary film pretreatment unit and is handled, so that the saliferous rate of waste water is less than 5% (so far, the salinity more than 95% is removed in the brine waste);
The 6th step, will pass through the pretreated waste water of secondary film and send into the secondary heat exchange device and carry out second-heating, the temperature that makes brine waste is at 90 ℃ more than-100 ℃.
In the 7th step, the waste water that will pass through second-heating is sent in the degasser and is outgased, and to remove the gas (removing carbonic acid gas, oxygen and other noncondensable gas) that wherein generates, the degasser internal pressure is wanted a little higher than vaporizer dirt bottom internal pressure.
Enter into through the waste water of the secondary degassing in the mixing tank of one or more base of evaporators and to mix with dense salt after the evaporator tube intercrystalline concentrates out the separated steam of base of evaporator that (mass concentration of controlling mixed waste water is 1%-15%; Dense salt can be and be processed the crystal salt that waste water matches; Also can be and be processed the strong brine that waste water matches; The mass percent of strong brine can be arbitrary value; Only need the quality degree of depth of the mixed brine waste of control get final product, the steam of separating is introduced subordinate's vaporizer and is condensed into the water purification reuse as generating tube thermal source or introducing secondary heat exchange device after as the thermal source heated waste water; Dense saline solution mixed in the base of evaporator mixing tank gets into the separator precipitate and separate again, isolates the dry use of crystal salt dispensing; Isolated brackish water liquid is delivered to the bobbin carriage at vaporizer top through recycle pump;, sparger, drops to that the bobbin carriage of generating tube bottom is interior to be separated steam with crystal salt in being evenly distributed to brackish water on each pipe of vaporizer heat-exchanging tube bundle by the outer steam heating vaporization of pipe, crystallization; The outer steam of the described pipe steam that to be the surplus vapour of LP steam or factory that produces of waste-heat recovery device, MP steam go out through the LP steam or the upper level vaporizer composite liberation of pressure and temperature reducing, the effect of short steam is that its latent heat is passed in the strong brine in the tube bank; Steam discharge become behind the latent heat water of condensation draw from vaporizer tube bank bottom as secondary add become after the thermal source heated waste water of interchanger water of condensation industrial or by pump delivery to the boiler reuse.
Details are as follows:
One, adds acid and add the alkali stirring: in the charging stirred pot, add calcium chloride, sulfuric acid (or hydrochloric acid) and Scale inhibitors, stir homogenizing with whisking appliance.In jar, adjust to 5-6 to pH value, be converted into dissolved CO to guarantee carbonate with acid
2Steam can be removed from degasser.Scale inhibitor can prevent fouling in front end interchanger and the degasifier.
Two, membrance chemistry pre-treatment: embrane method pre-treatment concentration systems (utilizing ionic membrane, membrane bioreactor, r-o-, nanofiltration, ultrafiltration, membrane techniquies such as micro-filtration).
Utilize the selective separation of film realize the different components of feed liquid separation, purifying, concentrate.It can separate in molecular range with the different films that are of traditional filtering, and this process is a kind of physical process, the variation of phase need not take place and add auxiliary agent.The aperture of film is generally micron order; Difference (or being called molecular weight cut-off) according to its aperture; Can film be divided into microfiltration membrane, ultra-filtration membrane, nf membrane and reverse osmosis membrane, can be divided into mineral membrane and organic membrane, mineral membrane such as ceramic membrane and metallic membrane according to the difference of material.Organic membrane such as FM, aromatic polyamide, polyethersulfone, gather fluoropolymer or the like.Embrane method pre-treatment concentrating capacity is removed the waste water of saliferous 90%.
Three, de-salted water preheating: process has adjusted pH value and the pretreated charging of film is carried out preheating to charging with pump delivery in interchanger, and interchanger is out that one is equipped with, and is equipped with a clean-in-place system.The preheating thermal source heats from the zero(ppm) water in the vaporizer or produces steam or get into preceding useless (salt) water of vaporizer with the water heating that the outer heating steam of I and II vaporizer heat transfer tube is condensed with secondary (being final stage) vaporizer heat-exchanging tube bundle.The water purification that also available heating heat exchanger is condensed is useless (salt) water of preheating again, reaches the purpose that makes full use of waste heat recovery.
Four, the degassing is handled: the brine waste through preheating removes carbonic acid gas, oxygen and other noncondensable gas in degasser.Remove carbonic acid gas and prevent the carbonate fouling, remove the oxygen protection against corrosion.
Five, film secondary treatment: utilize the selective separation of film (microfiltration membrane, ultra-filtration membrane, nf membrane and reverse osmosis membrane) realize feed liquid the separating of different components, purifying, concentrate.The secondary treatment concentrating capacity reaches removes saliferous more than 95%.
Six, second-heating: the second-heating purpose be charging brackish water temperature near boiling point (more than 90 ℃), save vaporizer and use quantity of steam, reduce the volume of vaporizer, reduce precious metal, the saving cost.
Seven, the secondary degassing is handled: the brine waste through heating removes carbonic acid gas, oxygen and other noncondensable gas in degasser.The bottom of degasser is provided with an aqua storage tank, and feed water has about 5 minutes residence time at this.The degasser internal pressure is wanted a little higher than base of evaporator pressure.
Eight, brine waste vaporizer (comprising film-type evaporator, jet film vaporizer, solar still):
Enter in one or more base of evaporator mixing tanks with dense salt after the evaporator tube intercrystalline goes out the separated steam of base of evaporator through the waste water of the degassing and to mix, the steam introducing interchanger of separating is condensed into the water purification reuse after as the thermal source heated waste water; Dense saline solution mixed in the base of evaporator mixing tank gets into the separator precipitate and separate again, isolates the dry use of crystal salt dispensing; Isolated brackish water liquid is delivered to the bobbin carriage at vaporizer top through recycle pump; By steam heating vaporization, crystallization outside the pipe, the bobbin carriage that drops to base of evaporator separates steam with crystal salt in sparger is evenly distributed to brackish water on each pipe of vaporizer heat exchange bundle; Manage outer steam and be surplus vapour of LP steam or factory that waste-heat recovery device produces or the MP steam LP steam through pressure and temperature reducing, the effect of short steam is that its latent heat is passed in the strong brine in the tube bank; Steam discharge become behind the latent heat water of condensation draw from vaporizer tube bank bottom as become after the preheater thermal source heated waste water water of condensation industrial or by pump delivery to the boiler reuse.
The principle of work of secondary (or three grades) brine waste vaporizer is identical with one-level, by that analogy.
The utility model does not relate to all identical with the prior art prior art that maybe can adopt of part to be realized.
Claims (1)
1. brine waste zero release recovery system is characterized in that it comprises:
One whisking appliance (1), this whisking appliance (1) is provided with dosing mouth, stirs so that brine waste and institute add soup, and the pH value that makes waste water is between 5～6;
One film pretreater (2), this film treater (2) can make the saliferous rate of the adjusted brine waste of process pH value less than 10%;
One preparatory heat-exchanger rig (3), this heat-exchanger rig are used to make the filtering waste water of process film treater to be heated near boiling point from normal temperature;
One degasser (4), this degasser (4) are used for sending the row degassing to through the waste water of pre-heaters (3) heating, to remove the gas that generates in the brine waste;
The brine waste that one second film pretreater (5), this second film pretreater (5) will pass through after degasser (4) degassing carries out the secondary membrane filtration, so that the saliferous rate of waste water is less than 5%;
One second interchanger (6), this second interchanger (6) are used for the filtering waste water of process secondary film pretreater is carried out second-heating, and the temperature that makes brine waste is at 90 ℃-100 ℃;
One second degasser (7), this second degasser (7) are used for the waste water through second-heating is outgased, and to remove the gas that wherein generates, the internal pressure of this second degasser (7) will be higher than vaporizer (8) bottom mixing section internal pressure;
One vaporizer (8); This vaporizer (8) is by one or more vaporizers and compose in series; This vaporizer (8) is made up of the sparger (803) on mixing tank (801), intermediary generating tube (802) and the top of bottom; Mixing tank (801) links to each other with the outside separator (9) of vaporizer (8), and separator (9) is connected with crystal salt moisture eliminator (10) and recycle pump respectively, and recycle pump is sent into the isolated brine waste of separator (9) in the bobbin carriage at vaporizer top; Flow in the sparger (803), sparger (803) is sent into brine waste in the generating tube (802) more again.
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| CN201120332719.7U CN202208671U (en) | 2011-09-06 | 2011-09-06 | Brine waste zero emission recovering system |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102329036A (en) * | 2011-09-06 | 2012-01-25 | 江苏中圣高科技产业有限公司 | High-efficiency method for recovery treatment of saliferous wastewater under zero emission through residual heat utilization |
| CN103440810A (en) * | 2013-09-10 | 2013-12-11 | 同济大学建筑设计研究院(集团)有限公司 | Salt water experiment simulation system used for building ventilation and smoke discharge experiments and using method thereof |
| CN109942039A (en) * | 2019-03-28 | 2019-06-28 | 石山霞 | A kind of desalinization of soil by flooding or leaching Sewage treatment purification method |
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2011
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102329036A (en) * | 2011-09-06 | 2012-01-25 | 江苏中圣高科技产业有限公司 | High-efficiency method for recovery treatment of saliferous wastewater under zero emission through residual heat utilization |
| CN102329036B (en) * | 2011-09-06 | 2013-02-27 | 江苏中圣高科技产业有限公司 | High-efficiency method for recovery treatment of saliferous wastewater under zero emission through residual heat utilization |
| CN103440810A (en) * | 2013-09-10 | 2013-12-11 | 同济大学建筑设计研究院(集团)有限公司 | Salt water experiment simulation system used for building ventilation and smoke discharge experiments and using method thereof |
| CN103440810B (en) * | 2013-09-10 | 2016-04-13 | 同济大学建筑设计研究院(集团)有限公司 | For saline experiment simulation system and the using method of building ventilation smoke evacuation experiment |
| CN109942039A (en) * | 2019-03-28 | 2019-06-28 | 石山霞 | A kind of desalinization of soil by flooding or leaching Sewage treatment purification method |
| CN109942039B (en) * | 2019-03-28 | 2022-07-08 | 广州众康环保设备有限公司 | Method for recycling and purifying salt-washing wastewater |
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