CN117209103B - Method for preparing boiler makeup water by combining steam condensate water and micro-polluted raw water - Google Patents
Method for preparing boiler makeup water by combining steam condensate water and micro-polluted raw water Download PDFInfo
- Publication number
- CN117209103B CN117209103B CN202311473828.4A CN202311473828A CN117209103B CN 117209103 B CN117209103 B CN 117209103B CN 202311473828 A CN202311473828 A CN 202311473828A CN 117209103 B CN117209103 B CN 117209103B
- Authority
- CN
- China
- Prior art keywords
- water
- raw water
- reverse osmosis
- introducing
- reclaimed
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 346
- 238000000034 method Methods 0.000 title claims abstract description 55
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 76
- 238000001914 filtration Methods 0.000 claims abstract description 59
- 238000005342 ion exchange Methods 0.000 claims abstract description 35
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 29
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 17
- 238000005189 flocculation Methods 0.000 claims abstract description 17
- 230000016615 flocculation Effects 0.000 claims abstract description 13
- 238000005345 coagulation Methods 0.000 claims abstract description 10
- 230000015271 coagulation Effects 0.000 claims abstract description 10
- 238000006243 chemical reaction Methods 0.000 claims description 15
- 239000000701 coagulant Substances 0.000 claims description 13
- 239000002455 scale inhibitor Substances 0.000 claims description 13
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 12
- 150000003839 salts Chemical class 0.000 claims description 12
- 239000003638 chemical reducing agent Substances 0.000 claims description 11
- 239000007788 liquid Substances 0.000 claims description 11
- 229920000742 Cotton Polymers 0.000 claims description 10
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 claims description 10
- 239000003830 anthracite Substances 0.000 claims description 10
- 230000000844 anti-bacterial effect Effects 0.000 claims description 10
- 239000003899 bactericide agent Substances 0.000 claims description 10
- 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 claims description 9
- 239000006004 Quartz sand Substances 0.000 claims description 9
- 230000001590 oxidative effect Effects 0.000 claims description 9
- 239000003729 cation exchange resin Substances 0.000 claims description 8
- 238000007599 discharging Methods 0.000 claims description 8
- 238000011049 filling Methods 0.000 claims description 8
- 238000002156 mixing Methods 0.000 claims description 7
- 229920000642 polymer Polymers 0.000 claims description 6
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 claims description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 4
- YDONNITUKPKTIG-UHFFFAOYSA-N [Nitrilotris(methylene)]trisphosphonic acid Chemical compound OP(O)(=O)CN(CP(O)(O)=O)CP(O)(O)=O YDONNITUKPKTIG-UHFFFAOYSA-N 0.000 claims description 4
- 238000010612 desalination reaction Methods 0.000 claims description 4
- DWAQJAXMDSEUJJ-UHFFFAOYSA-M Sodium bisulfite Chemical compound [Na+].OS([O-])=O DWAQJAXMDSEUJJ-UHFFFAOYSA-M 0.000 claims description 3
- 229920002401 polyacrylamide Polymers 0.000 claims description 3
- 235000010267 sodium hydrogen sulphite Nutrition 0.000 claims description 3
- AKHNMLFCWUSKQB-UHFFFAOYSA-L sodium thiosulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=S AKHNMLFCWUSKQB-UHFFFAOYSA-L 0.000 claims description 3
- 235000019345 sodium thiosulphate Nutrition 0.000 claims description 3
- ZZZCUOFIHGPKAK-UHFFFAOYSA-N D-erythro-ascorbic acid Natural products OCC1OC(=O)C(O)=C1O ZZZCUOFIHGPKAK-UHFFFAOYSA-N 0.000 claims description 2
- UNXHWFMMPAWVPI-UHFFFAOYSA-N Erythritol Natural products OCC(O)C(O)CO UNXHWFMMPAWVPI-UHFFFAOYSA-N 0.000 claims description 2
- 239000004386 Erythritol Substances 0.000 claims description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims description 2
- NJFOQBKWXBUYOM-UHFFFAOYSA-N P(=O)(O)OP(=O)O.C(=O)(O)C=C Chemical compound P(=O)(O)OP(=O)O.C(=O)(O)C=C NJFOQBKWXBUYOM-UHFFFAOYSA-N 0.000 claims description 2
- 229920000388 Polyphosphate Polymers 0.000 claims description 2
- 229930003268 Vitamin C Natural products 0.000 claims description 2
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 claims description 2
- UNXHWFMMPAWVPI-ZXZARUISSA-N erythritol Chemical compound OC[C@H](O)[C@H](O)CO UNXHWFMMPAWVPI-ZXZARUISSA-N 0.000 claims description 2
- 229940009714 erythritol Drugs 0.000 claims description 2
- 235000019414 erythritol Nutrition 0.000 claims description 2
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 2
- 229920001495 poly(sodium acrylate) polymer Polymers 0.000 claims description 2
- 229920000193 polymethacrylate Polymers 0.000 claims description 2
- 239000001205 polyphosphate Substances 0.000 claims description 2
- 235000011176 polyphosphates Nutrition 0.000 claims description 2
- 239000011734 sodium Substances 0.000 claims description 2
- 229910052708 sodium Inorganic materials 0.000 claims description 2
- NNMHYFLPFNGQFZ-UHFFFAOYSA-M sodium polyacrylate Chemical compound [Na+].[O-]C(=O)C=C NNMHYFLPFNGQFZ-UHFFFAOYSA-M 0.000 claims description 2
- PNFSYNAUAPBVGF-UHFFFAOYSA-M sodium;phenyl sulfate Chemical compound [Na+].[O-]S(=O)(=O)OC1=CC=CC=C1 PNFSYNAUAPBVGF-UHFFFAOYSA-M 0.000 claims description 2
- 235000019154 vitamin C Nutrition 0.000 claims description 2
- 239000011718 vitamin C Substances 0.000 claims description 2
- 150000001735 carboxylic acids Chemical class 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 238000004519 manufacturing process Methods 0.000 abstract description 5
- 238000004064 recycling Methods 0.000 abstract description 3
- 239000002918 waste heat Substances 0.000 abstract description 3
- 238000011033 desalting Methods 0.000 description 11
- 239000002253 acid Substances 0.000 description 10
- 239000012528 membrane Substances 0.000 description 9
- 239000010865 sewage Substances 0.000 description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 238000005406 washing Methods 0.000 description 8
- 239000003513 alkali Substances 0.000 description 7
- 239000003957 anion exchange resin Substances 0.000 description 6
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 6
- -1 trichloroamide Chemical compound 0.000 description 6
- 239000002585 base Substances 0.000 description 5
- 238000004140 cleaning Methods 0.000 description 5
- 230000000052 comparative effect Effects 0.000 description 5
- 238000012856 packing Methods 0.000 description 5
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 4
- 238000011001 backwashing Methods 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 239000013505 freshwater Substances 0.000 description 4
- 238000001471 micro-filtration Methods 0.000 description 4
- 230000008929 regeneration Effects 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- 239000004793 Polystyrene Substances 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000003456 ion exchange resin Substances 0.000 description 3
- 229920003303 ion-exchange polymer Polymers 0.000 description 3
- 150000002500 ions Chemical class 0.000 description 3
- 229920002223 polystyrene Polymers 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 238000007664 blowing Methods 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000007872 degassing Methods 0.000 description 2
- 230000004907 flux Effects 0.000 description 2
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 2
- 239000004810 polytetrafluoroethylene Substances 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000000153 supplemental effect Effects 0.000 description 2
- 239000008399 tap water Substances 0.000 description 2
- 235000020679 tap water Nutrition 0.000 description 2
- ISPYQTSUDJAMAB-UHFFFAOYSA-N 2-chlorophenol Chemical compound OC1=CC=CC=C1Cl ISPYQTSUDJAMAB-UHFFFAOYSA-N 0.000 description 1
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 description 1
- 241000894006 Bacteria Species 0.000 description 1
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical class [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 description 1
- LZZYPRNAOMGNLH-UHFFFAOYSA-M Cetrimonium bromide Chemical compound [Br-].CCCCCCCCCCCCCCCC[N+](C)(C)C LZZYPRNAOMGNLH-UHFFFAOYSA-M 0.000 description 1
- STZZWJCGRKXEFF-UHFFFAOYSA-N Dichloroacetonitrile Chemical compound ClC(Cl)C#N STZZWJCGRKXEFF-UHFFFAOYSA-N 0.000 description 1
- 239000003109 Disodium ethylene diamine tetraacetate Substances 0.000 description 1
- ZGTMUACCHSMWAC-UHFFFAOYSA-L EDTA disodium salt (anhydrous) Chemical compound [Na+].[Na+].OC(=O)CN(CC([O-])=O)CCN(CC(O)=O)CC([O-])=O ZGTMUACCHSMWAC-UHFFFAOYSA-L 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 239000004698 Polyethylene Substances 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 1
- 150000001450 anions Chemical class 0.000 description 1
- 229920005601 base polymer Polymers 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000003115 biocidal effect Effects 0.000 description 1
- 239000003139 biocide Substances 0.000 description 1
- 150000001732 carboxylic acid derivatives Chemical class 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 229960004106 citric acid Drugs 0.000 description 1
- 239000012459 cleaning agent Substances 0.000 description 1
- 230000003750 conditioning effect Effects 0.000 description 1
- 238000005536 corrosion prevention Methods 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 238000002242 deionisation method Methods 0.000 description 1
- 235000019301 disodium ethylene diamine tetraacetate Nutrition 0.000 description 1
- GVGUFUZHNYFZLC-UHFFFAOYSA-N dodecyl benzenesulfonate;sodium Chemical compound [Na].CCCCCCCCCCCCOS(=O)(=O)C1=CC=CC=C1 GVGUFUZHNYFZLC-UHFFFAOYSA-N 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000000909 electrodialysis Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
- RPTFBKSUERYYRQ-UHFFFAOYSA-N n-benzyl-n-methyldodecan-1-amine;hydrobromide Chemical compound Br.CCCCCCCCCCCCN(C)CC1=CC=CC=C1 RPTFBKSUERYYRQ-UHFFFAOYSA-N 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 150000007519 polyprotic acids Polymers 0.000 description 1
- 238000011045 prefiltration Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 229940080264 sodium dodecylbenzenesulfonate Drugs 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 239000002352 surface water Substances 0.000 description 1
- 230000026676 system process Effects 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
Landscapes
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Treatment Of Water By Ion Exchange (AREA)
Abstract
The invention relates to the technical field of water treatment, and discloses a method for preparing boiler makeup water by combining steam condensate water and micro-polluted raw water. The method comprises the following steps: step one, carrying out heat exchange treatment on raw water I, process steam condensate and turbine steam condensate in the heat exchange unit to obtain raw water II and heated raw water I; step two, introducing the heated raw water I into the micro flocculation filtration unit for coagulation filtration treatment to obtain reclaimed water II; step three, sequentially carrying out reverse osmosis treatment on the reclaimed water II through a reverse osmosis device and a carbon remover of the reverse osmosis unit to obtain reclaimed water III; and step four, introducing the reclaimed water III and the raw water II into the mixed bed ion exchange unit for ion exchange treatment to obtain boiler makeup water. The method provided by the invention can realize the efficient, reliable and economic process flow of the water production of the boiler makeup water, simultaneously reduce the energy consumption and realize the aims of waste heat utilization, reclaimed water recycling and water saving.
Description
Technical Field
The invention relates to the technical field of water treatment, in particular to a method for preparing boiler makeup water by combining steam condensate water and micro-polluted raw water.
Background
The boiler water for industrial and mining enterprises needs to remove impurities and most of salts in the water, for example, the water quality of boiler water supply is required to have Fe ion concentration of less than 30 mug/L, cu ion concentration of less than or equal to 5 mug/L, conductivity of less than or equal to 0.3 mug/cm and TOC of less than or equal to 500 mug/L in GB/T12145-2016 of steam quality of thermal generator set and steam power equipment. Therefore, the treated effluent water discharged from the factory after the standard discharge of tap water, fresh water and sewage can not meet the requirements, and the water can reach the standard after filtration and ion exchange treatment.
Due to the limitation of water production cost and process complexity, tap water or fresh water in a factory is conventionally generally used as raw water for preparing boiler water, and the raw water is treated by adopting a desalting water production process combining a positive bed, a negative bed and a mixed bed through mechanical filtration to obtain boiler makeup water. However, ion exchange resins are easily saturated in such processes, often requiring frequent cleaning and regeneration, and require the use of large amounts of strong acids and bases in regeneration, thus requiring high corrosion protection of the equipment.
In recent years, in order to pursue water saving and zero emission, many factories have started to use or partially use reclaimed water as raw water for preparing boiler water, and reverse osmosis has started to be used as a main step of desalting.
CN102942276a discloses a process for producing water from boiler makeup water, raw water is heated by a heater, then flocculant and bactericide are added, then the raw water enters a self-cleaning filter and a microfiltration system, enters a security filter, then enters a first-stage reverse osmosis through a first-stage booster pump, produced water enters a decarburization device, then enters an intermediate water tank, alkali is added, then enters a second-stage reverse osmosis through a second-stage high-pressure pump, concentrated water enters a microfiltration water tank, produced water enters an electric desalting device after entering the second-stage water tank, concentrated water enters the intermediate water tank, and produced water enters a desalting water tank to be used as boiler makeup water. The raw water of the process is blended by 30% of reclaimed water and 70% of fresh water, and the treated raw water meets the water requirement of a boiler. However, this process requires the use of a number of agents for cleaning and acid-base conditioning, such as citric acid and NaOH for the acid and base washing agents in microfiltration, organic phosphorus for the scale inhibitor, hydrochloric acid for the acid conditioner, sodium bisulfite for the reducing agent, bromine derivatives for the bactericide, naOH for the alkali conditioner, disodium ethylenediamine tetraacetate, sodium dodecylbenzenesulfonate, and citric acid for the chemical cleaning agent in the second stage. In addition, the electric desalting device (electrodialysis) does not need to regenerate ion exchange resin, but needs to use a high-voltage direct-current power supply, so that the equipment price is relatively high, the operation requirement is high, and the desalting effect is not ideal.
CN114873776a discloses a deep desalination system process of boiler makeup water, comprising: the pretreatment system comprises a clean water tank, a raw water pump, a pipeline mixer, a mechanical filter, an active carbon filter and a security filter, the reverse osmosis system comprises a high-pressure pump, a reverse osmosis device and an intermediate water tank, the mixed bed desalination system comprises an intermediate water pump, a mixed ion exchanger, a pure water tank and a pure water pump, a backwashing system and a chemical cleaning system. The boiler makeup water deep desalting system consists of a pretreatment system, a reverse osmosis system and a three-stage purifying system of a mixed bed desalting system, wherein the pretreatment system can effectively remove sediment suspended matters and particles in water, the reverse osmosis system can remove dissolved salts and bacteria in the water, and the mixed bed desalting system can remove residual ionic matters in the water, so that the purity of water quality is ensured, and the water consumption requirement is met. However, this patent does not specify the source of raw water for the make-up water for the boiler. And it is also not reasonable to backwash water by using clean water pond water (raw water) in mechanical filtration backwash water, because a large amount of water which has not been processed and has a certain turbidity and suspended solids can be remained in the filter after backwash, and mixed into the subsequent filtered water to enter the next stage of filter unit, affecting the operation of the subsequent unit.
In summary, most of the treatment processes of boiler makeup water at present need to frequently use strong base and strong acid for resin regeneration, consume a large amount of strong acid and strong base, and have high requirements on corrosion prevention of equipment. For factory enterprises with large boiler makeup water demand, the surplus of fresh water can not meet the requirements; from the standpoint of water saving and emission reduction, it is necessary to use reclaimed water as supplementary raw water, and at this time, because the salt content in the water is increased, it is necessary to adopt prefilter processes such as microfiltration and reverse osmosis to remove most of soluble and insoluble components besides mechanical filtration, and then ion exchange or electric desalting is adopted to completely remove salt. The processes are often long in flow, various in medicament types, multistage in pressurization and high in energy consumption. So the treatment method of boiler water makeup water which is efficient, reliable, convenient to operate, economical and energy-saving is also needed in the field of industrial enterprises at present.
Disclosure of Invention
The invention aims to solve the problems of high corrosion resistance requirement on equipment, complex process and high energy consumption caused by the fact that a large amount of strong acid and strong alkali are consumed in the process of preparing boiler makeup water in the prior art.
In order to achieve the above object, the present invention provides a method for preparing boiler makeup water by combining steam condensate and micro-polluted raw water, which is performed in a system including a heat exchange unit, a micro-flocculation filtration unit, a reverse osmosis unit, and a mixed bed ion exchange unit, comprising:
step one, carrying out heat exchange treatment on raw water I, process steam condensate and turbine steam condensate in the heat exchange unit to obtain raw water II and heated raw water I;
according to the flowing direction of the liquid, the heat exchange unit sequentially comprises a primary plate heat exchanger and a secondary plate heat exchanger;
step two, introducing the heated raw water I into the micro flocculation filtration unit for coagulation filtration treatment, wherein the step two comprises the following steps:
s1, introducing the heated raw water I into a primary pipeline mixer to perform micro flocculation reaction with a coagulant and a flocculant, and obtaining reclaimed water I after first filtration;
s2, introducing the reclaimed water I into a secondary pipeline mixer to perform a mixing reaction with a reducing agent, a scale inhibitor and a non-oxidizing bactericide, and performing second filtration to obtain reclaimed water II;
(3) The reclaimed water II is subjected to reverse osmosis treatment by a reverse osmosis device and a carbon remover of the reverse osmosis unit in sequence to obtain reclaimed water III;
(4) Introducing the reclaimed water III and the raw water II into the mixed bed ion exchange unit for ion exchange treatment to obtain boiler makeup water;
wherein the turbidity of the raw water I is not higher than 15NTU.
Compared with the prior art, the invention has at least the following beneficial effects:
(1) The invention adopts the slightly polluted surface water such as reservoir water or lake water and the like as raw water, utilizes steam condensate water as a heating heat source and as reclaimed water for supplementing boiler supplemental water, can realize the efficient, reliable and economic boiler supplemental water production process flow, simultaneously reduces energy consumption, and realizes the aims of waste heat utilization, reclaimed water reuse and water saving;
(2) The turbidity removal method adopts micro flocculation filtration, reaction and precipitation steps in the process steps of coagulation, reaction, precipitation and filtration used in the conventional turbidity removal process are omitted, and the process flow is simplified;
(3) The pre-desalting adopts the range-increasing reverse osmosis, so that an intermediate water tank and an intermediate water pump required by the conventional secondary reverse osmosis are saved, the flow is further simplified, and the running cost is saved;
(4) According to the invention, the mixed bed is used for ion exchange, strong acid and alkali waste liquid is not generated during regeneration, namely acid and alkali generated in the mixed bed are neutralized in the mixed bed, so that strong acid and alkali waste liquid is not generated, further treatment of the strong acid and alkali waste liquid is not needed, and compared with the traditional ion exchange deionization process adopting an anion bed, a cation bed and the mixed bed, the process flow is further simplified, and the treatment cost is reduced;
(5) The invention respectively treats the surface raw water and the steam condensate water and then combines the surface raw water and the steam condensate water for ion exchange, realizes the quality-separated water production, realizes the recycling of wastewater and reduces the treatment cost.
Drawings
Fig. 1 is a schematic flow chart of a preferred method for preparing boiler makeup water by combining steam condensate and slightly polluted raw water.
Description of the reference numerals
1.2, 3 and 4 represent water pumps.
Detailed Description
The endpoints and any values of the ranges disclosed herein are not limited to the precise range or value, and are understood to encompass values approaching those ranges or values. For numerical ranges, one or more new numerical ranges may be found between the endpoints of each range, between the endpoint of each range and the individual point value, and between the individual point value, in combination with each other, and are to be considered as specifically disclosed herein.
As described above, the present invention provides a method for preparing boiler makeup water by combining steam condensate and micro-polluted raw water, which is performed in a system including a heat exchange unit, a micro-flocculation filtration unit, a reverse osmosis unit, and a mixed bed ion exchange unit, comprising:
step one, carrying out heat exchange treatment on raw water I, process steam condensate and turbine steam condensate in the heat exchange unit to obtain raw water II and heated raw water I;
according to the flowing direction of the liquid, the heat exchange unit sequentially comprises a primary plate heat exchanger and a secondary plate heat exchanger;
step two, introducing the heated raw water I into the micro flocculation filtration unit for coagulation filtration treatment, wherein the step two comprises the following steps:
s1, introducing the heated raw water I into a primary pipeline mixer to perform micro flocculation reaction with a coagulant and a flocculant, and obtaining reclaimed water I after first filtration;
s2, introducing the reclaimed water I into a secondary pipeline mixer to perform a mixing reaction with a reducing agent, a scale inhibitor and a non-oxidizing bactericide, and performing second filtration to obtain reclaimed water II;
(3) The reclaimed water II is subjected to reverse osmosis treatment by a reverse osmosis device and a carbon remover of the reverse osmosis unit in sequence to obtain reclaimed water III;
(4) Introducing the reclaimed water III and the raw water II into the mixed bed ion exchange unit for ion exchange treatment to obtain boiler makeup water;
wherein the turbidity of the raw water I is not higher than 15NTU.
Preferably, the turbidity of the raw water I is 5-11NTU.
Preferably, the conditions are controlled such that the temperature of the raw water II is 20-30 ℃ and the temperature of the heated raw water I is 10-20 ℃. In this preferred case, the turbidity removal effect can be made better.
More preferably, the temperature of the raw water I is 0-10 ℃.
It should be noted that, the method of the present invention further includes: and selecting a flow regulating device according to the temperatures of the raw water I, the process steam condensate and the turbine steam condensate, and the finally required raw water II and the heated raw water I, so that the final temperature of the raw water II is 20-30 ℃, and the temperature of the heated raw water I is 10-20 ℃.
The raw water is defined as "source water" for preparing boiler makeup water, which is conventional in the art.
Preferably, the reducing agent is selected from at least one of sodium thiosulfate, sodium bisulfite, erythritol, sodium phenylsulfate, and vitamin C.
More preferably, the reducing agent is used in an amount of 5-15mg by weight per 1L of the reclaimed water I.
Preferably, the scale inhibitor is an organic polyphosphate and/or a carboxylic acid based polymer.
More preferably, the scale inhibitor is used in an amount of 3 to 10mg by weight per 1L of the reclaimed water I.
More preferably, the scale inhibitor is at least one selected from the group consisting of aminotrimethylene phosphonic acid, carboxyethylene diphosphonic acid, sodium polyacrylate, and sodium polymethacrylate.
Preferably, the non-oxidizing bactericide is at least one selected from chlorophenol, dichlorocyanomethane, trichloroamide, cetyltrimethylammonium bromide and dodecylmethylbenzylammonium bromide.
More preferably, the non-oxidizing biocide is used in an amount of 5-10mg by weight per 1L of the reclaimed water I.
The coagulant is at least one of polyaluminum chloride, aluminum hydroxide, aluminum sulfate and ferric trichloride.
Preferably, the flocculant is polyacrylamide.
Preferably, in the second step, the coagulant is used in an amount of 10 to 50mg per 1L of the warmed raw water I.
Preferably, in the second step, the flocculant is used in an amount of 3 to 10mg per 1L of the warmed raw water I.
In the invention, the coagulation filtration treatment adopts a micro-flocculation filtration process, wherein the coagulant and the flocculant are added into the primary pipeline mixer to be mixed and then directly subjected to the first filtration without a mixing reaction device and a sedimentation tank.
Preferably, the raw water I is at least one of reservoir water, lake water and underground water.
Preferably, the first filtration adopts a multi-medium filter, and quartz sand and anthracite are filled in the multi-medium filter; wherein the relative density of the quartz sand is 2.6-2.65g/mL and the volume average diameter is 0.5-1.2mm, and the relative density of the anthracite is 1.4-1.6g/mL and the volume average diameter is 0.8-1.8mm. In this preferred case, the turbidity removal effect can be made better.
Preferably, the filling height of the quartz sand is 700-900mm, and the filling height of the anthracite is 300-500mm.
Further preferably, the filling height of the quartz sand is 800mm, and the filling height of the anthracite coal is 400mm.
Preferably, the multi-media filter is backwashed using water and compressed air.
Preferably, the second filtration is performed in a fine filter having a fine filter medium with a filter accuracy of 0.1 to 20 μm.
According to a preferred embodiment, the precision filter medium is one of polytetrafluoroethylene membrane filter element, polyethylene membrane filter element, polypropylene membrane filter element and acetate membrane filter element.
According to a preferred embodiment, the method further comprises: and (3) backwashing the multi-medium filter and/or the precision filter by using at least a part of the reclaimed water II, wherein backwash drainage is discharged through a sewage pipeline.
More preferably, a part of the reclaimed water II is used for backwashing the multi-medium filter and/or the precision filter, and backwash drainage is discharged through a sewage pipeline; sequentially passing the rest part of reclaimed water II through a reverse osmosis device and a carbon remover of the reverse osmosis unit to carry out reverse osmosis treatment; wherein the weight ratio of the part of the reclaimed water II to the rest of the reclaimed water II is 1:12-16.
Preferably, the filtration flux of the reverse osmosis device is 5-50L/m 2 H, the filtration pressure is 0.2-1.5MPa.
According to a preferred embodiment, a reverse osmosis membrane in the reverse osmosis device is washed using a reverse osmosis membrane washing device.
Preferably, the carbon remover adopts a blowing degassing mode to remove free carbon dioxide in water, specifically, the water is introduced from the upper part of the equipment, flows through the surface of the packing layer through a spraying device, and enters from a lower air opening and reversely passes through the packing layer, and the air mixed with the carbon dioxide is discharged from the top of the equipment.
According to a preferred embodiment, the method further comprises: and introducing the reclaimed water II into the reverse osmosis device to obtain concentrated water, directly introducing the concentrated water into a concentrated water reverse osmosis unit to obtain produced water and range-increasing reverse osmosis concentrated water with the salt content of 2-2.5wt%, introducing the produced water into the carbon remover, introducing the range-increasing reverse osmosis concentrated water into a concentrated water tank, and collecting and discharging the concentrated water.
It should be noted that the extended-range reverse osmosis concentrated water is obtained from the concentrated-water reverse osmosis unit, wherein the extended-range reverse osmosis is different from the traditional two-stage reverse osmosis, and means that the concentrated water of the reverse osmosis device directly enters the concentrated-water reverse osmosis unit of the subsequent stage, without arranging an intermediate water tank and an intermediate booster pump, the extended-range reverse osmosis concentrated water with the water yield and the salt content of 2-2.5wt% is obtained, and the reclaimed water II is introduced into the carbon remover for further treatment after passing through the reverse osmosis device of the reverse osmosis unit and the extended-range reverse osmosis concentrated water, which is equivalent to prolonging the treatment flow of the reverse osmosis device.
Preferably, the salt content of the concentrated water is 0.9-1.1wt%.
According to a preferred embodiment, the method further comprises: before the ion exchange treatment, filtering the raw water II through a cotton pipe filter and an activated carbon filter in sequence, and then introducing the filtered raw water II into the mixed bed ion exchange unit to perform the ion exchange treatment;
wherein, the filtering precision of the cotton filter element in the cotton pipe filter is 4-6 mu m.
According to a preferred embodiment, the mixed bed ion exchange unit comprises an intermediate water tank, a mixed bed and a desalination water tank in the direction of liquid flow.
According to a preferred embodiment, the mixed bed is provided with a dosage volume ratio of 1-2:1 and a cation exchange resin.
Preferably, the anion exchange resin and/or the cation exchange resin is a polymer polybasic base polymer having a network-type three-dimensional structure or a polymer polybasic acid polymer having a network-type three-dimensional structure.
More preferably, the polymer skeletons of the anion exchange resin and the cation exchange resin are polystyrene type ion exchange resins.
According to a preferred embodiment, the method further comprises: before the heat exchange treatment, the process steam condensate and the turbine steam condensate are mixed in a condensate water tank and then introduced into the heat exchange unit for heat exchange treatment.
A preferred embodiment is provided below in conjunction with fig. 1, comprising:
step one, carrying out heat exchange treatment on raw water I in a primary plate heat exchanger and a secondary plate heat exchanger in a heat exchange unit sequentially from a raw water tank, and a process steam condensate and a turbine steam condensate which are mixed by a condensate water tank to obtain raw water II and heated raw water I;
step two, introducing the heated raw water I into the micro flocculation filtration unit for coagulation filtration treatment, wherein the step two comprises the following steps:
s1, introducing the heated raw water I into a primary pipeline mixer to perform micro flocculation reaction with a coagulant and a flocculant, and performing first filtration through the multi-medium filter to obtain reclaimed water I;
s2, introducing the reclaimed water I into a secondary pipeline mixer to perform a mixing reaction with a reducing agent, a scale inhibitor and a non-oxidizing bactericide, and performing second filtration through the precise filter to obtain reclaimed water II;
introducing a part of reclaimed water II from a reverse washing water tank into the multi-medium filter and the precision filter for reverse washing, and discharging the reverse washing liquid to a sewage station through a sewage pipeline;
and the rest part of reclaimed water II is subjected to reverse osmosis treatment by a reverse osmosis device and a carbon remover of the reverse osmosis unit in sequence to obtain reclaimed water III;
wherein the weight ratio of the part of the reclaimed water II to the rest of the reclaimed water II is 1:12-16;
introducing reclaimed water II into the reverse osmosis device to obtain concentrated water, directly introducing the concentrated water into a concentrated water reverse osmosis unit without being stored in an intermediate water tank and pressurized by a high-pressure water pump to obtain produced water and increased-range reverse osmosis concentrated water with the salt content of 2-2.5wt%, introducing the produced water into the carbon remover, introducing the increased-range reverse osmosis concentrated water into a concentrated water tank, and collecting and discharging the concentrated water;
and step four, filtering the raw water II sequentially through a cotton pipe filter and an activated carbon filter, and then sequentially carrying out ion exchange treatment on the raw water II and the reclaimed water III together in an intermediate water tank, a mixed bed and a desalted water tank in the mixed bed ion exchange unit to obtain boiler makeup water and leading the boiler makeup water to a using point.
The invention is not particularly limited to the cotton tube filter, the activated carbon filter and other parameter conditions of the ion exchange treatment, and can be carried out by selecting parameters which are conventional in the industry.
The present invention will be described in detail by way of examples, and unless otherwise specified, all materials used are commercially available.
Coagulant: is polyaluminum chloride, and has a weight average molecular weight of 1500-2000;
flocculant: is polyacrylamide, and has a weight average molecular weight of 1200-1800 ten thousand;
reducing agent: sodium thiosulfate with the dosage of 10mg/L;
scale inhibitor: is amino trimethylene phosphonic Acid (ATMP) with the dosage of 5mg/L;
non-oxidizing bactericides: sodium cetyl acrylate with the dosage of 8mg/L;
cation exchange resin: is polystyrene sulfonic cation exchange resin, which is purchased from Barleite (Purolite) company and is model C-100E;
anion exchange resin: is a polystyrene chloride ion type anion exchange resin, and is purchased from Hasi company of Tao Shiluo, U.S.A., and has the model number of AMBERJET4200Cl;
quartz sand: a relative density of 2.64g/mL and a volume average diameter of 1.0mm;
anthracite coal: a relative density of 1.5g/mL and a volume average diameter of 1.5mm;
raw water I: for reservoir water, the water quality parameters are shown in Table 1;
TABLE 1
Without specific explanation, the following examples were carried out using the flow scheme shown in FIG. 1, with a flow rate of raw water I of 200t/h, a process steam condensate of 80t/h and a turbine steam condensate of 165t/h.
Example 1
The embodiment is used for explaining a method for preparing boiler makeup water by combining steam condensate water and micro-polluted raw water, which is provided by the invention, and comprises the following steps:
step one, using a lifting pump and a booster pump to sequentially perform heat exchange treatment on raw water I from a raw water tank, and a process steam condensate (55 ℃) and a turbine steam condensate (66 ℃) which are mixed by a condensate water tank by a primary plate heat exchanger and a secondary plate heat exchanger in a heat exchange unit to obtain raw water II with the temperature of 23 ℃ and heated raw water I with the temperature of 15 ℃;
step two, introducing the heated raw water I into the micro flocculation filtration unit for coagulation filtration treatment, wherein the step two comprises the following steps:
s1, introducing the heated raw water I into a primary pipeline mixer to perform micro flocculation reaction with a coagulant and a flocculant, and performing first filtration through the multi-medium filter to obtain reclaimed water I;
wherein the amount of the coagulant is 20mg and the amount of the flocculant is 5mg for every 1L of the heated raw water I;
quartz sand with the filling height of 800mm and anthracite with the filling height of 400mm are respectively filled in the multi-medium filter;
s2, introducing the reclaimed water I into a secondary pipeline mixer to perform a mixing reaction with a reducing agent, a scale inhibitor and a non-oxidizing bactericide, and performing second filtration by using the precise filter with the filtration precision of 3 mu m to obtain reclaimed water II;
wherein, the precise filter medium in the precise filter adopts a polytetrafluoroethylene membrane filter element;
introducing a part of reclaimed water II from a reverse washing water tank into the multi-medium filter and the precision filter for reverse washing, and discharging the reverse washing liquid to a sewage station through a sewage pipeline;
and the rest part of reclaimed water II is subjected to reverse osmosis treatment by a reverse osmosis device and a carbon remover of the reverse osmosis unit in sequence to obtain reclaimed water III;
introducing reclaimed water II into the reverse osmosis device to obtain concentrated water (with the salt content of 1 wt%) and directly introducing the concentrated water into a concentrated water reverse osmosis unit for filtration to obtain produced water and extended-range reverse osmosis concentrated water with the salt content of 2.5wt%, introducing the produced water into the carbon remover, introducing the extended-range reverse osmosis concentrated water into a concentrated water tank for collection, and discharging;
wherein the weight ratio of the amount of the reclaimed water II to the rest reclaimed water II is 1:16;
the filtration flux of the reverse osmosis device is 40L/m 2 H, the filtering pressure is 0.4MPa, and the reverse osmosis membrane in the reverse osmosis device is cleaned periodically by using a reverse osmosis membrane cleaning device;
the carbon remover adopts a blowing degassing mode to remove free carbon dioxide in water, specifically, the water is introduced from the upper part of the equipment, flows through the surface of the packing layer by a spraying device, air enters from a lower air opening and reversely passes through the packing layer, and the air mixed with the carbon dioxide is discharged from the top of the equipment;
and step four, filtering the raw water II sequentially through a cotton pipe filter (the filtering precision is 5 mu m) and an activated carbon filter, sequentially introducing the raw water II and the reclaimed water III into an intermediate water tank, a lifting pump, a mixed bed (filled with anion exchange resin and cation exchange resin with the volume ratio of 2:1) and a desalted water tank in the mixed bed ion exchange unit, performing ion exchange treatment, and obtaining boiler makeup water (named P1) and introducing the boiler makeup water to a using point.
Example 2
This example was conducted in a similar manner to example 1, except that the conditions were controlled such that the temperatures of the raw water II and the warmed raw water I were 33 ℃ and 9 ℃ respectively, to finally obtain boiler makeup water, designated as P2.
Example 3
This example was conducted in a similar manner to example 1 except that in the first filtration, the packing heights of the silica sand and anthracite coal in the multi-media filter were 500mm and 200mm, respectively, and finally boiler makeup water was obtained, designated as P3.
Comparative example 1
This comparative example was conducted in a similar manner to example 1 except that the process steam condensate and turbine steam condensate were not used and the heat exchange treatment was not conducted, specifically:
(a) The raw water I is directly introduced into the micro flocculation filtration unit for coagulation filtration treatment, and the method comprises the following steps:
s1, introducing the raw water I into a primary pipeline mixer to perform coagulation reaction with a coagulant and a flocculant, and obtaining reclaimed water I after first filtration (a multi-medium filter);
s2, introducing the reclaimed water I into a secondary pipeline mixer to perform a mixing reaction with a reducing agent, a scale inhibitor and a non-oxidizing bactericide, and obtaining reclaimed water II after second filtration (a precise filter);
(b) Introducing a part of reclaimed water II from a reclaimed water tank into the multi-medium filter and the precision filter for backwashing, and discharging backwash liquid to a sewage station through a sewage pipeline;
and the rest part of reclaimed water II is subjected to reverse osmosis treatment by a reverse osmosis device and a carbon remover of the reverse osmosis unit in sequence to obtain reclaimed water III;
introducing reclaimed water II into the reverse osmosis device to obtain concentrated water, directly introducing the concentrated water into a concentrated water reverse osmosis unit for filtering to obtain produced water and increased-range reverse osmosis concentrated water with the salt content of 2.5wt%, introducing the produced water into the carbon remover, introducing the increased-range reverse osmosis concentrated water into a concentrated water tank for collection, and discharging;
(c) And introducing the reclaimed water III into the mixed bed ion exchange unit for ion exchange treatment to obtain boiler makeup water, wherein the boiler makeup water is named as DP1.
Comparative example 2
This comparative example was conducted in a similar manner to example 1 except that raw water II was directly fed into a mixed bed ion exchange unit for ion exchange treatment without filtration through a cotton pipe filter and an activated carbon filter, and the specific operations of step four include:
and step four, directly introducing the raw water II and the reclaimed water III into an intermediate water tank, a lifting pump, a mixed bed (filled with anion exchange resin and cation exchange resin with the volume ratio of 2:1) and a desalted water tank in the mixed bed ion exchange unit in sequence for ion exchange treatment, and finally obtaining boiler makeup water, which is named as DP2.
Test example 1
The water quality of the boiler makeup water obtained finally in examples and comparative examples was measured, and the specific results are shown in Table 2.
TABLE 2
The result shows that the method provided by the invention can realize the efficient, reliable and economic boiler makeup water preparation process flow, simultaneously reduce the energy consumption and realize the aims of waste heat utilization, reclaimed water recycling and water saving.
The preferred embodiments of the present invention have been described in detail above, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, a number of simple variants of the technical solution of the invention are possible, including combinations of the individual technical features in any other suitable way, which simple variants and combinations should likewise be regarded as being disclosed by the invention, all falling within the scope of protection of the invention.
Claims (7)
1. A method for preparing boiler makeup water by combining steam condensate and micro-polluted raw water, characterized in that the method is carried out in a system comprising a heat exchange unit, a micro-flocculation filtration unit, a reverse osmosis unit and a mixed bed ion exchange unit, and comprises the following steps:
step one, carrying out heat exchange treatment on raw water I, process steam condensate and turbine steam condensate in the heat exchange unit to obtain raw water II and heated raw water I;
according to the flowing direction of the liquid, the heat exchange unit sequentially comprises a primary plate heat exchanger and a secondary plate heat exchanger;
step two, introducing the heated raw water I into the micro flocculation filtration unit for coagulation filtration treatment, wherein the step two comprises the following steps:
s1, introducing the heated raw water I into a primary pipeline mixer to perform micro flocculation reaction with a coagulant and a flocculant, and obtaining reclaimed water I after first filtration; the coagulant is at least one of polyaluminum chloride, aluminum sulfate and ferric trichloride; the flocculant is polyacrylamide;
s2, introducing the reclaimed water I into a secondary pipeline mixer to perform a mixing reaction with a reducing agent, a scale inhibitor and a non-oxidizing bactericide, and performing second filtration to obtain reclaimed water II; the second filtering is performed in a precise filter, and a precise filter medium with the filtering precision of 0.1-20 mu m is arranged in the precise filter;
step three, sequentially carrying out reverse osmosis treatment on the reclaimed water II through a reverse osmosis device and a carbon remover of the reverse osmosis unit to obtain reclaimed water III;
step four, introducing the reclaimed water III and the raw water II into the mixed bed ion exchange unit for ion exchange treatment to obtain boiler makeup water;
wherein the turbidity of the raw water I is not higher than 15NTU;
in the first step, controlling the conditions so that the temperature of the raw water II is 20-30 ℃ and the temperature of the heated raw water I is 10-20 ℃;
the first filtering adopts a multi-medium filter, and quartz sand and anthracite are filled in the multi-medium filter; wherein the relative density of the quartz sand is 2.6-2.65g/mL and the volume average diameter is 0.5-1.2mm, and the relative density of the anthracite is 1.4-1.6g/mL and the volume average diameter is 0.8-1.8mm; the filling height of the quartz sand is 700-900mm, and the filling height of the anthracite is 300-500mm;
the method further comprises the steps of: before the ion exchange treatment, filtering the raw water II through a cotton pipe filter and an activated carbon filter in sequence, and then introducing the filtered raw water II into the mixed bed ion exchange unit to perform the ion exchange treatment;
wherein, the filtering precision of the cotton filter element in the cotton pipe filter is 4-6 mu m.
2. The method of claim 1, wherein the reducing agent is selected from at least one of sodium thiosulfate, sodium bisulfite, erythritol, sodium phenylsulfate, and vitamin C; and/or the scale inhibitor is an organic polyphosphate and/or a carboxylic acid polymer.
3. The method of claim 1 or 2, wherein the scale inhibitor is selected from at least one of aminotrimethylene phosphonic acid, carboxyethylene diphosphonic acid, sodium polyacrylate, sodium polymethacrylate.
4. The method according to claim 1 or 2, wherein in the second step, the coagulant is used in an amount of 10-50mg per 1L of the warmed raw water I; and/or
In the second step, the flocculant is used in an amount of 3-10mg per 1L of the heated raw water I.
5. The method according to claim 1 or 2, wherein the method further comprises: and introducing the reclaimed water II into the reverse osmosis device to obtain concentrated water, directly introducing the concentrated water into a concentrated water reverse osmosis unit to obtain produced water and range-increasing reverse osmosis concentrated water with the salt content of 2-2.5wt%, introducing the produced water into the carbon remover, introducing the range-increasing reverse osmosis concentrated water into a concentrated water tank, and collecting and discharging the concentrated water.
6. The method of claim 1 or 2, wherein the mixed bed ion exchange unit comprises an intermediate water tank, a mixed bed and a desalination water tank in the direction of liquid flow.
7. The method according to claim 1 or 2, wherein the mixed bed is provided with a dosage volume ratio of 1-2:1 and a cation exchange resin.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311473828.4A CN117209103B (en) | 2023-11-08 | 2023-11-08 | Method for preparing boiler makeup water by combining steam condensate water and micro-polluted raw water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311473828.4A CN117209103B (en) | 2023-11-08 | 2023-11-08 | Method for preparing boiler makeup water by combining steam condensate water and micro-polluted raw water |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN117209103A CN117209103A (en) | 2023-12-12 |
| CN117209103B true CN117209103B (en) | 2024-02-23 |
Family
ID=89039290
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202311473828.4A Active CN117209103B (en) | 2023-11-08 | 2023-11-08 | Method for preparing boiler makeup water by combining steam condensate water and micro-polluted raw water |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN117209103B (en) |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2008121941A (en) * | 2006-11-09 | 2008-05-29 | Miura Co Ltd | Method of operating steam boiler device |
| CN102838227A (en) * | 2012-08-16 | 2012-12-26 | 浙江东发环保工程有限公司 | System and method for treating industrial park recycled water to form power plant boiler supplemental water |
| CN103011456A (en) * | 2012-12-12 | 2013-04-03 | 贵州开磷（集团）有限责任公司 | Method for recycling condensate water in phosphoric acid concentration system |
| CN204125245U (en) * | 2014-07-31 | 2015-01-28 | 河南永银化工实业有限公司 | The de-salted water preparation system of reuse water of condensation and heat thereof |
| CN105000707A (en) * | 2015-07-02 | 2015-10-28 | 青岛龙发热电有限公司 | Preparation method of boiler water |
| CN114873776A (en) * | 2022-04-24 | 2022-08-09 | 广西下田锰矿有限责任公司 | Boiler makeup water deep desalting system and method |
-
2023
- 2023-11-08 CN CN202311473828.4A patent/CN117209103B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2008121941A (en) * | 2006-11-09 | 2008-05-29 | Miura Co Ltd | Method of operating steam boiler device |
| CN102838227A (en) * | 2012-08-16 | 2012-12-26 | 浙江东发环保工程有限公司 | System and method for treating industrial park recycled water to form power plant boiler supplemental water |
| CN103011456A (en) * | 2012-12-12 | 2013-04-03 | 贵州开磷（集团）有限责任公司 | Method for recycling condensate water in phosphoric acid concentration system |
| CN204125245U (en) * | 2014-07-31 | 2015-01-28 | 河南永银化工实业有限公司 | The de-salted water preparation system of reuse water of condensation and heat thereof |
| CN105000707A (en) * | 2015-07-02 | 2015-10-28 | 青岛龙发热电有限公司 | Preparation method of boiler water |
| CN114873776A (en) * | 2022-04-24 | 2022-08-09 | 广西下田锰矿有限责任公司 | Boiler makeup water deep desalting system and method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN117209103A (en) | 2023-12-12 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| RU2342330C2 (en) | System and method for treatment of acid sewage waters | |
| CN102942276B (en) | Boiler feedwater treatment method and treatment system related to reuse of reclaimed water | |
| CN101798150B (en) | Treatment method of wastewater with high salt content and treatment device thereof | |
| Al-Rehaili | Comparative chemical clarification for silica removal from RO groundwater feed | |
| CN105236661A (en) | System and method for preparing ultrapure water with zero wastewater discharge | |
| CN105439341A (en) | Salt-containing wastewater treatment system and treatment method | |
| CN205528161U (en) | Water treatment recovery unit during copper is smelted | |
| CN105645663A (en) | A water treatment method combining flocculation, counter-current ozone air floatation and biofiltration in order and a device used in the method | |
| CN105585183A (en) | Copper smelting reclaimed water treatment and recovery device and zero emission method | |
| CN104108813A (en) | Refining and chemical sewage desalting integrated treatment process and device | |
| CN101544430B (en) | Secondary treatment method of coking wastewater | |
| CN213295024U (en) | Ultrapure water preparation device | |
| CN113045059A (en) | Treatment system and treatment process for realizing zero discharge of wastewater by full-membrane method | |
| CN109422383A (en) | A kind of Treated sewage reusing treatment process | |
| CN117209103B (en) | Method for preparing boiler makeup water by combining steam condensate water and micro-polluted raw water | |
| CN210825779U (en) | Water saving system of ultrapure water system | |
| CN210237367U (en) | Arid cold area landfill leachate processing apparatus | |
| CN111875142A (en) | Zero discharge system and process for salt-containing wastewater of power plant | |
| CN106809993A (en) | A kind of Ultrapure water treatment technology | |
| CN215559437U (en) | Wastewater treatment system | |
| CN203498181U (en) | System for recycling waste acid and waste alkali | |
| CN215559636U (en) | Wastewater treatment system | |
| CN210764790U (en) | Semiconductor pure water treatment system | |
| CN112979022A (en) | Preparation and cleaning process of ultrapure water device in laboratory | |
| CN112939368A (en) | Circulating water sewage treatment and recycling method with high desalting rate |
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 | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |