CN108217794A - It is a kind of can simultaneously a variety of waste liquids of crystallization treatment method and device - Google Patents
It is a kind of can simultaneously a variety of waste liquids of crystallization treatment method and device Download PDFInfo
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- CN108217794A CN108217794A CN201810241372.1A CN201810241372A CN108217794A CN 108217794 A CN108217794 A CN 108217794A CN 201810241372 A CN201810241372 A CN 201810241372A CN 108217794 A CN108217794 A CN 108217794A
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- evaporator
- waste liquid
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- heat
- crystallization treatment
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- 239000007788 liquid Substances 0.000 title claims abstract description 92
- 239000002699 waste material Substances 0.000 title claims abstract description 74
- 238000002425 crystallisation Methods 0.000 title claims abstract description 30
- 230000008025 crystallization Effects 0.000 title claims abstract description 30
- 238000000034 method Methods 0.000 title claims abstract description 25
- 238000011282 treatment Methods 0.000 title claims abstract description 23
- 230000006835 compression Effects 0.000 claims abstract description 23
- 238000007906 compression Methods 0.000 claims abstract description 23
- 150000003839 salts Chemical class 0.000 claims description 47
- 239000013078 crystal Substances 0.000 claims description 30
- 239000000126 substance Substances 0.000 claims description 30
- 238000007599 discharging Methods 0.000 claims description 25
- 238000001704 evaporation Methods 0.000 claims description 23
- 230000008020 evaporation Effects 0.000 claims description 23
- 230000007246 mechanism Effects 0.000 claims description 10
- 238000010438 heat treatment Methods 0.000 claims description 6
- 238000005406 washing Methods 0.000 claims description 6
- 239000012530 fluid Substances 0.000 claims description 5
- 238000010025 steaming Methods 0.000 claims description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 41
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 27
- 239000003546 flue gas Substances 0.000 description 27
- 239000007789 gas Substances 0.000 description 21
- 238000011010 flushing procedure Methods 0.000 description 11
- 239000000203 mixture Substances 0.000 description 10
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 10
- 239000012267 brine Substances 0.000 description 9
- 238000009833 condensation Methods 0.000 description 9
- 230000005494 condensation Effects 0.000 description 9
- 239000010865 sewage Substances 0.000 description 8
- 239000000706 filtrate Substances 0.000 description 7
- 239000002351 wastewater Substances 0.000 description 7
- 239000002245 particle Substances 0.000 description 6
- 238000005119 centrifugation Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 239000007787 solid Substances 0.000 description 4
- 238000007792 addition Methods 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 238000004821 distillation Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 238000011081 inoculation Methods 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- 239000000654 additive Substances 0.000 description 2
- 230000000996 additive effect Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 235000019504 cigarettes Nutrition 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 229910052602 gypsum Inorganic materials 0.000 description 2
- 239000010440 gypsum Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000615 nonconductor Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 208000027418 Wounds and injury Diseases 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000004480 active ingredient Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- GJYLKIZKRHDRER-UHFFFAOYSA-N calcium;sulfuric acid Chemical compound [Ca].OS(O)(=O)=O GJYLKIZKRHDRER-UHFFFAOYSA-N 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 239000012153 distilled water Substances 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 208000014674 injury Diseases 0.000 description 1
- 239000002054 inoculum Substances 0.000 description 1
- 229910017053 inorganic salt Inorganic materials 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 230000002045 lasting effect Effects 0.000 description 1
- 239000010808 liquid waste Substances 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 238000007726 management method Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000013011 mating Effects 0.000 description 1
- 230000003204 osmotic effect Effects 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000009991 scouring Methods 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- -1 silicon ion Chemical class 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
- 238000003911 water pollution Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/042—Prevention of deposits
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/043—Details
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/002—Construction details of the apparatus
- C02F2201/007—Modular design
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/14—Maintenance of water treatment installations
Abstract
The present invention disclose it is a kind of can a variety of waste liquids of condensing crystallizing processing simultaneously method and this method used in device.The method of the present invention is to introduce different pending waste liquids in different evaporators respectively to be evaporated concentration and crystallization treatment, and the indirect steam of each evaporator is sent into a vapour compression machine and carries out being used further to heat each evaporator after compression makes its heat content increase.The present invention can simultaneously a variety of waste liquids of crystallization treatment method in, at least the pending waste liquid in part is heated before evaporator is sent into first with flue residue heat.The present invention is the work heat source of each evaporator using indirect steam after compression, while takes full advantage of flue residue heat, you can fully recycles resource, while waste liquid can be effectively treated.
Description
Technical field
The present invention relates to the methods and its device of a kind of evaporation process, and exactly, the present invention relates to one kind to concentrate simultaneously
Device used in the method and this method of a variety of waste liquids of crystallization treatment.The evaporation process method of the present invention and the steaming mutually having
Hair processing method have similarity, and include in its device evaporator and vapour compression machine composition MVR vaporising devices and
Pipeline, distillation condensate output transistor, the pending waste liquid of pipeline, live steam source between connection indirect steam and vapour compression machine
Intake line, the pump of dense discharging of waste liquid pipeline after processing and the various liquid of conveying and the control valve that is set on pipeline.
Background technology
In China, the wretched insufficiency of water resource and shortage are an objective reality situations, while the repetition of water resource is sharp
Acid test is faced with with pollution control.Although as National Environmental administers the increasing of policy and inspection, achieve
Some gratifying achievements, it is the embarrassment reality for having to face still, outside waste water to arrange, and the public still feels that water pollution adds
Play, the pressure of environmental improvement is still very big, without the change of essence.On the one hand, the waste water origin cause of formation arranged outside China is extremely complex,
Difficulty of governance is larger；On the other hand, generally believe that the standard limited value of lag is excessively loose, the type of outer pollution discharging object and ingredient mistake
In single, the substance of the limitation does not bring standard into, and major pollutants row value only only accounts for as defined in standard
Injury to human body cannot be much connected to each other with environmental demand, led to sewage effluent pollution environment, deteriorated water quality.Certainly, it is national
The construction about standard is paid much attention to, this means that once new standard is put into effect, and the sewage of original qualified discharge will be closed no longer
Lattice, each manufacturing enterprise need actively to carry out technology upgrading, improve the technical merit of sewage disposal.
At present, the main method of Industrial Waste Water Treatments has the treatment process such as film concentration and evaporative crystallization.Film concentration is a kind of
The technology of efficiently purifying concentration, it reaches concentration using the active ingredient separation for realizing orientation different from the molecular weight of liquid
Effect, but cannot form effective osmotic pressure, therefore make after the degree that inorganic salt concentration in sewage reaches certain
Narrow range, cost of investment is excessively high in addition, cannot meet industrial needs at present；Evaporative crystallization is to form sewage evaporation
Distilled water and strong brine, strong brine is again through separation of solid and liquid, either using the system of traditional multiple-effect still using MVR evaporations system
System, water quality that treated is very excellent, and solid waste can concentrate pack, handling result ratio more thoroughly, still, calcium in waste water,
Magnesium, silicon ion content are very high, and contain the solid suspensions such as a large amount of calcium carbonate and excessive ash, it will rapid in evaporator
Fouling, therefore need in equipment operation to shut down scale removal afterwards for a period of time, it is no that it will cause equipment to be unable to operate normally.
Traditional MVR vapo(u)rization systems due to its with it is easy to operate, space is small, good energy-conserving effect etc. is many to be obtained a little
It is widely applied, but it is an independent unit, processing performance is poor, a set of MVR vapo(u)rization systems can only handle one
Kind medium.However there are many sewage species that some enterprises generate, and each sewage water is not very big, if to each
Kind sewage is required for mating different vapo(u)rization system, classification processing, investment and administration fee caused by such method of operation
Enterprise is allowed to can't bear the heavy load.
Boiler is usually widely used in the industrial production to generate steam to meet technique needs, outer row after fuel combustion
Flue gas still has quite high temperature, and by boiler smoke, discharging directly into atmosphere, this partial heat energy do not have after desulfurization process at present
It is utilized effectively.
Invention content
The insufficient technical solution of the prior art is solved the present invention provides a set of.Technical scheme of the present invention gram can take existing
There is the deficiency of technology, meanwhile, the operating cost for the equipment that degraded significantly so that measures to effectively increase energy savings and reduce material consumption can be realized smoothly.
The present invention it is a kind of can simultaneously a variety of waste liquids of crystallization treatment method, be to introduce different pending waste liquids respectively
Concentration and crystallization treatment are evaporated in different evaporators, the indirect steam of each evaporator is sent into a vapour compression machine and is carried out
Compression is used further to heat each evaporator after making its heat content increase.
The present invention can simultaneously a variety of waste liquids of crystallization treatment method in, at least the pending waste liquid in part be sent into evaporate
It is heated before device first with flue residue heat.
Be used to implement a kind of of the method for the present invention the vaporising devices of a variety of waste liquids of crystallization treatment can include simultaneously：Evaporator and
Vapour compression machine and the pipeline in connection live steam source distill condensate output transistor, pending waste liquid intake line, through place
The pump of dense discharging of waste liquid pipeline after reason and the various liquid of conveying and the control valve being set on pipeline, point row in described device
It is provided with the evaporator identical with pending waste liquid number of species and crystal seed conveying mechanism, the secondary steam pipe output of each evaporator
The input pipe connection of mono- vapour compression machine of Guan Junyu, the steam input pipe of each evaporator and the steam output pipe of vapour compression machine
And the pipeline unicom in connection live steam source, each evaporator are respectively arranged with connection and are evaporated fluid output port and are evaporated liquid
It is between body input terminal and thereon carry circulating pump cycle connecting pipeline, different pending waste liquid intake lines respectively respectively with
The feed pipe connection of one evaporator, the lower half of the evaporation cavity of each evaporator respectively connect respectively with a crystal seed conveying mechanism,
Salt crystalline substance collection device is respectively arranged at the lower cone of each evaporator, each salt crystalline substance collection device controls respectively with thereon with discharging
The discharging delivery pipe connection of valve.
Preferably, it is of the invention can simultaneously in the vaporising device of a variety of waste liquids of crystallization treatment a point row be provided with it is pending useless
The identical surface condenser of liquid number of species, each pending waste liquid are respectively fed to each evaporator after surface condenser is handled.This
During invention work, the mixture effusion of some vapor, incoagulable gas and air is had in each evaporator, because of incoagulability gas
Body and air are all the non-conductors of heat, and evaporation will be hindered after assembling in heater, reduces heat exchange efficiency.Therefore in the present invention
There is provided surface condensers, cold on surface using the mixture of some vapor, incoagulable gas and air overflowed in evaporator
Indirect heat exchange is carried out with pending waste liquid in condenser, steam is condensed, and forms condensed water and discharges, and incoagulable gas and air
Mixture is then discharged to air, by the use of pending waste liquid as the cooling medium of surface condenser, further saves energy consumption, this hair
Bright this structure makes the discharge of mixed gas more easy by the quick barometric gradient that formed of cooling, solve the prior art from
Escaped in evaporator steam, incoagulable gas and air mixture it is in line when because system pressure difference not enough caused by direct difficulty.
By just continuously discharging the incoagulable gas in evaporator and air after surface condenser, the efficient of vapo(u)rization system ensure that,
Steady and continuous service, and further save energy consumption.
Preferably, it is of the invention simultaneously in the vaporising device of a variety of waste liquids of crystallization treatment, each surface condenser to be sent into
At least part of preheater that first passes through respectively of pending waste liquid carries out the pre-heat treatment, and the preheater is added using flue residue heat
Heat.
Preferably, it is of the invention can a variety of waste liquids of crystallization treatment simultaneously vaporising device, the lower cone point of each evaporator
Not She Zhi a vertical tube, be sequentially communicated salt crystalline substance cylinder respectively along vertical tube short transverse, be provided with going out for discharging control valve
Expects pipe, the flush pipe for being provided with washing control valve and flushing manifold.
The present invention can simultaneously a variety of waste liquids of crystallization treatment vaporising device most preferred embodiment in, be divided to arrange be provided with two
Evaporator and two crystal seed conveying mechanisms.
The present invention point row set the more evaporators identical with pending waste liquid number of species, such as divide row setting three steamings
For hair device to handle three kinds of pending waste liquids, each evaporator uses same vapour compression machine, by the evaporator institute of formula, point row arrangement
The indirect steam of generation, which carries out returning again after heating pressurization together, to be conveyed to each evaporator group and is used as heat source.Each evaporation
Device is evaporated enrichment to introducing processed liquid therein, defeated by crystal seed after it is close or equal to saturated concentration
Mechanism is sent to introduce crystal seed into waste liquid, promotes its crystallization.
Present invention setting flue gas waste heat-recovering device, is configured flue gas heat-exchange unit, and cigarette is sent to after flue gas collection is summarized
In gas heat exchanger, the partial condensation water that at least part vapo(u)rization system is formed is passed indirectly using the waste heat flue gas of flue
Heat, partial condensation water become steam by heating vaporization, and the flue gas after heat exchange is returned outside exhaust system high-altitude and arranged, and the steam of formation enters
Into vapor preheater by least part waste liquid heat temperature raising, each pending waste liquid used can also be preheated certainly
Processing.This way and structure of the present invention is that initial management provides condition, while also can fully recycle resource.
The tubular salt crystalline substance that the present invention is referred to as salt crystalline substance cylinder in each evaporator lower disposed settles structure, in evaporator in waste liquid
Inorganic salts reach saturation due to evaporation and concentration after constantly crystallize, forming salt is brilliant, because of the downward subsiding movement of gravity relationship, from cone
Body gradually drops into salt crystalline substance cylinder, and the supersaturated waste water containing salt crystalline substance discharges from salt crystalline substance cylinder lower part, and centrifugation systems is sent to carry out solid-liquid point
From.The present invention is sent into using the salt filtrate after centrifugation as flushing liquor from the different location multiplex roles of salt crystalline substance cylinder lower part, rinses salt filter
Liquid rises after entering salt crystalline substance cylinder along barrel and salt crystalline substance countercurrent washing, the phenomenon that being similar to boiling is generated, by gypsum, small knot
Brilliant salt particle, which is brought into again in evaporator, continues to participate in cycle, and saturation inorganic salts are adhered to using this tiny crystal grains as core grows up,
Soluble impurity can be dissolved and removed simultaneously, advantageously form the crystalline particle with certain volume, granularity improves, and facilitates centrifugation
Machine efficient operation.Rinse salt filtrate and the balanced exchange and the distribution that will carry out heat while salt crystalline substance antikinesis so that discharging
Crystallization strong brine temperature reduce, reduce thermal loss, be conducive to centrifuge.Experiments have shown that will discharging strong brine amount with
The volume ratio for rinsing salt filtrate is set as 1:Between 1.2-1.3, that is to say, that the flow of flushing liquor is slightly more than strong brine
Load can be better achieved flushing process from bottom to top, and fully carry out heat exchange in this way, and output passes through on pipeline
Discharge valve realizes accurate adjustment control with hydraulic control valve is rinsed.Flushing liquor in the present invention comes from evaporator discharging centrifugation
Salt filtrate afterwards and the mixture of waste liquid, concentration is close to saturation, and temperature is less than strong brine in evaporator, is ideal
Scouring media.
Present invention setting crystal grain inoculation system is interrupted into evaporator by crystal seed tank or continuous conveying addition is with sulfuric acid
Calcium or the substance of selectivity are basic additive, i.e., artificially control nucleus quantity, inorganic when the inorganic salts of waste water tend to saturation
Salt is attached on the crystal grain the surface of the seed of these additions and constantly grows up, and the particle of crystallization is remained suspended in water, will not be adhered to
In heat exchange element surface scale, so that evaporation can continually and steadily be run.
Description of the drawings
Attached drawing 1 for the present invention be divided to row set two groups of evaporators can and meanwhile the device embodiments of a variety of waste liquids of crystallization treatment show
It is intended to.
Attached drawing 2 is the device connection diagram that fume afterheat heated waste water is utilized in the embodiment of the present invention.
Attached drawing 3 rinses and sink mechanism embodiment schematic diagram for salt crystalline substance.
In figure：In figure：1 is low-temperature flue gas delivery pipe, and 2 be flue gas heat-exchange unit, and 3 be flue gas heat-exchange unit water inlet control valve, and 4 are
Flue gas heat-exchange unit water inlet pipe, 5 be waste liquid liquid supply pipe, and 6 be distillation condensed water flow pipe, and 7 be useless for second to the second evaporator
Second liquid supply pipe of liquid, 8 be high-temperature flue snorkel, and 9 be high-temperature flue gas collecting pipe, and 10 be preheater condensate pump, and 11 are
Flue gas heat-exchange unit vapour-discharge tube, 12 be vapor preheater, and 13 be vapor preheater drip pipe, and 14 condense for preheater
Water pot, 15 be surface condenser, and 16 be surface condenser drip pipe, and 17 be vapor preheater outlet tube, and 18 be surface
Condenser outlet tube, 19 be fixed gas mixing tube, and 20 be the first evaporator fixed gas outlet, and 21 be the first evaporation feed liquor
Control valve, 22 be the first evaporator circulating pump, and 23 be the first evaporator, and 24 be the first evaporator discharging control valve, and 25 be first
Evaporator indirect steam outlet, 26 be the first evaporator steam inlet pipe, and 27 be the first evaporator condensation water discharge spout, and 28 are
Evaporator condensation water pot, 29 be evaporator condensation water pump, and 30 be vapour compression machine steam inlet tube, and 31 be vapour compression machine, 32
It is sub-cylinder for vapour compression machine steam outlet pipe, 33,34 be the second evaporator fixed gas outlet, and 35 steam for the second evaporator
Vapor inlet pipe, 36 be the second evaporator condensation water discharge spout, and 37 be the second evaporator, and 38 export for the second evaporator indirect steam
Pipe, 39 be the second evaporation feed liquor control valve, 40 be the second evaporator circulating pump, 41 be the second evaporator discharging control valve, 42
It is live steam pipe network for B evaporators discharging delivery pipe, 43,44 be the first evaporator discharging delivery pipe, and 45 be the second evaporator
Lower cone, 46 be the first evaporator lower cone, and 47 be crystal seed inoculation mouth control valve, and 48 be crystal seed delivery pipe, and 49 convey for crystal seed
Pump, 50 be crystal seed tank, and 51 be dosing mouth, and 52 be salt crystalline substance cylinder, and 53 be upper flush pipe, and 54 be flushing liquor control valve, and 55 be undershoot
Pipe is washed, 56 is rinse manifold, and 57 be evacuation port.
Specific embodiment
The present invention is explained below in conjunction with the device embodiment that attached drawing provides.
In the embodiment of attached drawing 1,37 two evaporators of the first evaporator 23 and the second evaporator are provided with by being divided to arrange, first
The indirect steam outlet 25 and 38 of 23 and second evaporator 37 of evaporator is connected with the air inlet 30 of vapour compression machine 31.Vapour pressure
The exhaust outlet 32 of contracting machine 31 is connected with sub-cylinder 33.Sub-cylinder 33 is respectively communicated with 23 He of the first evaporator with pipeline 26 and 35 respectively
Second evaporator 37 is also respectively provided with valve, while sub-cylinder 33 also connects fresh steaming on pipeline 26 and 35 as seen from the figure
Steam pipe 43 provides power steam when originating work to meet device by power boiler.First evaporator 23 and the second evaporator
37 condensed water water outlet connects condensate water pot 28 with condensate pipe 27 with 36 respectively, also divides on pipeline 27 and 36 as seen from the figure
Valve is not provided with it.The fluid output port that is evaporated of first evaporator 23 and the second evaporator 37 divides with being evaporated fluid input port
The pipeline connection of circulating pump 40 and 22 Yong be carried thereon, in the upstream of circulating pump 40 respectively with inputting the pipe of pending waste liquid
Road connects.
Pending waste liquid is inputted in the device of the invention can directly use connection waste liquid cylinder pipeline connection, but the present invention's
To be provided with surface condenser 15 in a device in most preferred embodiment, the first pending waste liquid after surface condenser is handled again
It is respectively fed to each evaporator.The fixed gas of evaporator and the mixture concentration of steam enter in surface condenser and heat friendship occur
It changes, form condensed water after steam cooling discharges through surface condenser drip pipe, final incoagulable gas and air mixing
Object is emptied to air.Because incoagulable gas and air be all heat non-conductor, in heater assemble after will hinder evaporation,
Reduce heat exchange.The present invention can continuously be discharged the incoagulable gas in evaporator and air by setting surface condenser, be ensured
Efficient, the steady and continuous service of vapo(u)rization system.
To make full use of the energy, in the device of the invention, the first pending waste liquid for being sent into surface condenser 15 first passes through
Preheater carries out the pre-heat treatment, and the preheater is heated using flue residue heat, then is sent into condenser 15, warp with waste-solution line 17
It is respectively fed to again in first or second evaporator 23 or 37 after the processing of surface condenser 15, referring to attached drawing 2.This hair that attached drawing provides
Second of pending waste liquid is directly admitted to the second evaporator without advance processing by the second liquid supply pipe 7 in bright embodiment
It is handled in 37.It it should be noted that according to specific circumstances can also be a set of as in attached drawing 1 for the setting of the second evaporator again
The waste-heat facility of surface condenser and its front end before shown first evaporator 23, to second pending waste liquid into
Row heating in advance.
The evaporation cavity lower part of second evaporator of the vaporising device of the vapo(u)rization system of the present invention is provided with by dosing mouth 51, crystalline substance
It plants tank 50, crystal seed delivery pump 49 and carries the crystal seed conveyer that the crystal seed delivery pipe of crystal seed inoculation mouth control valve 47 is formed thereon
Structure.It should be noted that do not represent the first evaporator 23 and the details of crystal seed conveying mechanism in fig. 1, it can also in specific device
It is set as needed to the first evaporator such as the crystal seed conveying mechanism set on the second evaporator in attached drawing 2.In each evaporation
Salt crystalline substance collection device is respectively arranged at the lower cone 46 or 45 of device.By taking the second evaporator 37 as an example, referring to attached drawing 3, in its steaming
What is set on the lower cone 45 of hair device is sequentially communicated salt crystalline substance cylinder 52 by vertical tube upper edge vertical height direction, is provided with respectively
The discharge nozzle 42 of discharging control valve 41, the upper flush pipe 53 for being provided with washing control valve and the salt for rinsing the compositions of manifold 56
Brilliant collection device.The upstream of upper flush pipe 53 is provided with lower flush pipe 55 and washing control valve 54.The lower cone of first evaporator 23
Salt crystalline substance collection device on body 46 set by set salt crystalline substance collection device and the second evaporator 37 is identical, evaporator
The delivery pipe that discharges is 44, and discharging control valve thereon is 24, is illustrated referring to attached drawing 1.
The course of work of the present embodiment is as follows：Come from different smokejack exhaust gas and be aggregated into height from high-temperature flue snorkel 8
It enters in flue gas heat-exchange unit 2 after warm flue gas collecting pipe 9, while is sent through flue gas heat-exchange unit water inlet pipe 4 into flue gas heat-exchange unit 2
Enter clear water, the clear water that the present embodiment is supplied to flue gas heat-exchange unit comes from the condensed water that evaporation generates, have certain temperature and
Heat content.In flue gas heat-exchange unit 2, clear water and high-temperature flue gas fully exchange heat, and clear water is vaporized to be formed after steam by flue gas heat-exchange unit
Vapour-discharge tube 11 is discharged, and is entered in vapor preheater 12.It is controlled into flue gas and changed by flue gas heat-exchange unit water inlet control valve 3
Clear water amount in hot device 2, so as to ensure that stablizing for steam is discharged.Flue gas after heat exchange sends cigarette back to by low-temperature flue gas delivery pipe 1
It is arranged outside gas exhaust system.
The first pending waste liquid enters the steam that in vapor preheater 12 and flue gas generates through waste liquid liquid supply pipe 5
Heat exchange occurs, waste liquid is tentatively heated, and steam is condensed caused by flue gas, is formed after condensed water through cold by vapor preheater
Condensate delivery pipe 13 enters preheater condensate water pot 14 and temporarily stores.
The first waste liquid after tentatively being heated is exited into from vapor preheater outlet tube 17 in surface condenser 15,
With the incoagulable gas from the first evaporator fixed gas outlet 20 and the second evaporator fixed gas outlet 34 and steam
Mixture converges in fixed gas mixing tube 19, and concentration, which is entered in surface condenser 15, occurs heat exchange, shape after steam cooling
It is entered in preheater condensate water pot 14 through surface condenser drip pipe 16 into condensed water and vapor preheater is formed
Condensed water mixes, and production reuse is sent with preheater condensate pump 10.Waste liquid I is heated again, by surface condenser outlet tube 18
Discharge, enters in the first evaporator 23 and goes to complete concentration.
Second of pending waste liquid is introduced into the second liquid supply pipe 7 in the second evaporator 37 directly from its storage tank carry out from
Reason
Meet the work needed for evaporation after waste liquid is entered by different pipelines has respectively entered first, second evaporator 23 and 37
The first evaporator circulating pump 22, the second evaporator circulating pump 40 are respectively started after liquid level, waste liquid is evenly distributed to each respectively
From heat exchange element surface constantly circulate.Steam is supplied into sub-cylinder 33 through live steam pipe network 43, steam is via
One evaporator steam inlet pipe 26 and the second evaporator steam inlet pipe 35 have respectively entered the first evaporator 23 and the second evaporation
In the heat exchange element of device 37, steam is condensed after steam and waste liquid fully carry out heat exchange, condensed water is formed, respectively via first
27 and second evaporator condensation water discharge spout 36 of evaporator condensation water discharge spout enters evaporator condensation water pot 28, then through evaporation
Device condensate pump 29 sees reuse off, while clear water is continuously replenished into flue gas heat-exchange unit 2 from distillation condensed water flow pipe 6.Waste liquid
It is constantly heated in 23 second evaporator 37 of the first evaporator, then reaches violent fluidized state, generated a large amount of secondary
Steam is pooled to vapour compression machine through the first evaporator indirect steam outlet 25 and the second evaporator indirect steam outlet 38
Enter vapour compression machine 31 in steam inlet tube 30, rotated using high-tension electricity drive motor, then drive vapour compression machine
Work, indirect steam is warmed pressurization, and increases and be sent to sub-cylinder 33 by vapour compression machine steam outlet pipe 32 after heat content
It is interior that live steam is replaced to work, hereafter no longer need live steam, the constantly cycle compressed steam of vapour compression machine 31, evaporation continuation
It is steady to carry out.
Respectively with the lasting progress of evaporation and concentration, concentration increases liquid in two evaporators, full reaching
Meeting forming salt is brilliant with after, and because of the downward subsiding movement of gravity relationship.By taking the second evaporator 37 as an example, at this moment to the second evaporator 37
Interior conveying crystal seed, you can promote the crystallization process in it, salt crystalline substance is gradually dropped into from evaporator lower cone 45 in salt crystalline substance cylinder 52, is come
It is entered in salt crystalline substance cylinder 52 from upper flush pipe 53 and lower flush pipe 54 from the flushing liquor rinsed in manifold 56, flushing liquor enters
Along barrel rising and salt crystalline substance countercurrent washing after salt crystalline substance cylinder 52, the phenomenon that being similar to boiling is generated, by gypsum, small crystal salt
Grain, which is brought into again in evaporator, continues to participate in cycle, and saturation inorganic salts are adhered to using this tiny crystal grains as core grows up, while can
Soluble impurity is dissolved and is removed, advantageously forms the crystalline particle with certain volume, granularity improves, and facilitates centrifuge efficient
Work.Rinse salt filtrate and the balanced exchange and the distribution that will carry out heat while salt crystalline substance antikinesis so that the crystallization of discharging
Strong brine temperature reduces, and reduces thermal loss, is conducive to centrifuge.It usually can be by discharging strong brine amount with rinsing salt filtrate
Volume ratio be set as 1:Between 1.2-1.3, by the second evaporator discharging control valve 41 and flushing liquor control valve 55 and real
Now accurate adjustment control.After the flushing liquor for the second evaporator in the present embodiment comes from the discharging centrifugation of the second evaporator
Salt filtrate and the mixture of waste liquid, concentration are less than strong brine in evaporator close to saturation, temperature, are that ideal flushing is situated between
Matter.Similarly, experiencing identical operating mode in the first evaporator.
In order to it is more efficient, be rapidly formed crystalline particle, prevent waste liquid equipment surface formed schmutzband, with second steam
Send out device for, the present invention can also by will come from crystal seed tank 50 with calcium sulfate or selectivity the object with certain particle size
Matter is basic additive, and inoculum is quantitatively conveyed to B evaporators 37 by crystal seed delivery pipe 48 with crystal seed delivery pump 49, can be with people
The granule size of nucleus quantity and crystal in order to control provides primary condition for separation of solid and liquid.When the inorganic salts of waste water tend to be full
With and when generating crystallization trend, inorganic salts, which are just attached on the crystal grain seed of these additions, constantly grows up, and remain suspended in water
In, without being adhered to heat exchange element surface scale, so that evaporation can continually and steadily be run.
Condensed water and highly concentrated high saturated brine are formed after being concentrated by evaporation in the present embodiment, solid fills after further centrifuging
Bag reuse or as industrial preparation a, it is achieved thereby that resource recycling, the advanced technologies case of liquid waste processing zero-emission.
For enterprise produce in generate a greater variety of pending waste liquids, can divide respectively according to specific circumstances row setting with
The identical evaporator of pending waste liquid number of species, to be carried out at the same time processing.
Claims (7)
1. it is a kind of can simultaneously a variety of waste liquids of crystallization treatment method, different pending waste liquids is introduced into different evaporators respectively
Inside it is evaporated concentration and crystallization treatment, it is characterised in that the indirect steam of each evaporator is sent into a vapour compression machine and is pressed
Contracting is used further to heat each evaporator after making its heat content increase.
2. it is according to claim 1 can simultaneously a variety of waste liquids of crystallization treatment method, it is characterised in that at least partly treat
It disposes waste liquid and is heated before evaporator is sent into first with flue residue heat.
3. realize claims 1 or 2 method can simultaneously a variety of waste liquids of crystallization treatment vaporising device, including evaporator and steaming
Vapour compressor and the pipeline in connection live steam source distill condensate output transistor, pending waste liquid intake line, through processing
The pump of rear dense discharging of waste liquid pipeline and the various liquid of conveying and the control valve being set on pipeline, it is characterised in that in device
Row is divided to be provided with the evaporator identical with pending waste liquid number of species and crystal seed conveying mechanism, the secondary steam pipe of each evaporator
Input pipe of the efferent duct with a vapour compression machine connects, and the steam input pipe of each evaporator and the steam of vapour compression machine are defeated
Outlet pipe and the pipeline unicom in connection live steam source, each evaporator are respectively arranged with connection and are evaporated fluid output port with being steamed
Cycle connecting pipeline that is between hair fluid input port and carrying circulating pump thereon, different pending waste liquid intake lines difference
Respectively the feed pipe with an evaporator connects, and the lower half of the evaporation cavity of each evaporator respectively connects respectively with a crystal seed conveying mechanism
It is logical, salt crystalline substance collection device is respectively arranged at the lower cone of each evaporator, each salt crystalline substance collection device respectively with carrying discharging thereon
The discharging delivery pipe connection of control valve.
4. it is according to claim 3 can simultaneously a variety of waste liquids of crystallization treatment vaporising device, it is characterised in that set in device
The surface condenser identical with pending waste liquid number of species is equipped with, each pending waste liquid is sent respectively after surface condenser is handled
Enter each evaporator.
5. it is according to claim 4 can simultaneously a variety of waste liquids of crystallization treatment vaporising device, it is characterised in that be sent into each table
At least part of preheater that first passes through respectively of the pending waste liquid of face condenser carries out the pre-heat treatment, and the preheater utilizes
Flue residue heat heats.
6. according to claim 3 or 4 or 5 can a variety of waste liquids of crystallization treatment simultaneously vaporising device, it is characterised in that it is each
The lower cone of a evaporator sets a vertical tube respectively, is sequentially communicated salt crystalline substance cylinder respectively along vertical tube short transverse, sets thereon
The discharge nozzle that is equipped with discharging control valve, the flush pipe for being provided with washing control valve and rinse manifold.
7. it is according to claim 6 can a variety of waste liquids of crystallization treatment simultaneously vaporising device, it is characterised in that in device point
Row are provided with two evaporators and two crystal seed conveying mechanisms.
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| CN110092520A (en) * | 2019-05-17 | 2019-08-06 | 中国神华煤制油化工有限公司 | Waste water desalter and waste water desalination process |
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