CN108217797A - A kind of single-stage multiple-effect evaporation separator - Google Patents
A kind of single-stage multiple-effect evaporation separator Download PDFInfo
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- CN108217797A CN108217797A CN201810240424.3A CN201810240424A CN108217797A CN 108217797 A CN108217797 A CN 108217797A CN 201810240424 A CN201810240424 A CN 201810240424A CN 108217797 A CN108217797 A CN 108217797A
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- evaporator
- pipe
- waste liquid
- steam
- evaporation
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- 238000001704 evaporation Methods 0.000 title claims abstract description 47
- 230000008020 evaporation Effects 0.000 title claims abstract description 47
- 239000007788 liquid Substances 0.000 claims abstract description 86
- 230000006835 compression Effects 0.000 claims abstract description 20
- 238000007906 compression Methods 0.000 claims abstract description 20
- 239000002699 waste material Substances 0.000 claims description 57
- 239000007789 gas Substances 0.000 claims description 28
- 239000000706 filtrate Substances 0.000 claims description 23
- 239000007787 solid Substances 0.000 claims description 22
- 238000005520 cutting process Methods 0.000 claims description 15
- 239000012530 fluid Substances 0.000 claims description 14
- 150000003839 salts Chemical class 0.000 claims description 12
- 238000007599 discharging Methods 0.000 claims description 9
- 238000011144 upstream manufacturing Methods 0.000 claims description 6
- 238000004821 distillation Methods 0.000 claims description 5
- 235000019504 cigarettes Nutrition 0.000 claims description 3
- 239000002918 waste heat Substances 0.000 claims description 2
- 239000000463 material Substances 0.000 abstract description 4
- 230000007812 deficiency Effects 0.000 abstract description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 43
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 27
- 239000003546 flue gas Substances 0.000 description 27
- 238000009833 condensation Methods 0.000 description 12
- 230000005494 condensation Effects 0.000 description 12
- 239000012528 membrane Substances 0.000 description 8
- 238000000926 separation method Methods 0.000 description 8
- 238000000034 method Methods 0.000 description 7
- 230000000694 effects Effects 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- 239000013078 crystal Substances 0.000 description 5
- 238000002156 mixing Methods 0.000 description 5
- 239000002245 particle Substances 0.000 description 5
- 239000010865 sewage Substances 0.000 description 5
- 238000005119 centrifugation Methods 0.000 description 4
- 238000002425 crystallisation Methods 0.000 description 4
- 230000008025 crystallization Effects 0.000 description 4
- 235000014347 soups Nutrition 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- 230000001112 coagulating effect Effects 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 230000002045 lasting effect Effects 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 3
- 238000011282 treatment 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
- 238000009835 boiling Methods 0.000 description 2
- 239000012267 brine Substances 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 238000012432 intermediate storage Methods 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- PALNZFJYSCMLBK-UHFFFAOYSA-K magnesium;potassium;trichloride;hexahydrate Chemical compound O.O.O.O.O.O.[Mg+2].[Cl-].[Cl-].[Cl-].[K+] PALNZFJYSCMLBK-UHFFFAOYSA-K 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 239000011343 solid material Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000010025 steaming Methods 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
- 230000009471 action Effects 0.000 description 1
- 239000004480 active ingredient Substances 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 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
- 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
- 230000007423 decrease 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
- 239000000446 fuel Substances 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 230000006872 improvement Effects 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
- 229910017053 inorganic salt Inorganic materials 0.000 description 1
- 238000007689 inspection Methods 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
- 239000000615 nonconductor Substances 0.000 description 1
- 230000003204 osmotic effect Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000004064 recycling 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
- 239000000126 substance Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 239000000725 suspension Substances 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
- C02F1/048—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
- 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
- C02F1/16—Treatment of water, waste water, or sewage by heating by distillation or evaporation using waste heat from other processes
-
- 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
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Analytical Chemistry (AREA)
- Mechanical Engineering (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The present invention disclose it is a kind of overcome the shortage of prior art, single-stage but there is the device of multiple-effect evaporation simultaneously.A kind of single-stage multiple-effect evaporation separator of the present invention, pump and control valve including evaporator and vapour compression machine and connecting pipeline and the various liquid of conveying, dress center first and second two evaporators.The present invention overcomes the deficiencies in the prior art, and the operating cost for the equipment that degraded significantly comprehensively so that measures to effectively increase energy savings and reduce material consumption can be realized smoothly.
Description
Technical field
The present invention relates to a kind of single-stage multiple-effect evaporation separator, particularly a kind of multiple-effect evaporation separation dress with MVR
It puts.Include evaporator and vapour compression machine in the device of the invention and connect the pipeline in live steam source, distillation condensed water
Efferent duct, pending waste liquid intake line, dense discharging of waste liquid pipeline after processing and the various liquid of conveying pump and be set to
Control valve 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 containing the solid suspensions such as a large amount of calcium carbonate and excessive ash, will be rapid in evaporator
Fouling causes equipment to be unable to operate normally.
Traditional MVR vapo(u)rization systems are obtained due to it with the advantages of easy to operate, space is small, and good energy-conserving effect etc. is many
To being widely applied, but it is an independent unit, and processing performance is poor, and a set of MVR vapo(u)rization systems can only be same
It works under one temperature and CONCENTRATION STATE, due to being evaporated the waste liquid of processing with the increase of concentration, the elevation of boiling point also carries therewith
Height, needs vapour compression machine to be capable of providing larger vapo(u)rous Wen Sheng, and energy consumption dramatically increases.Meanwhile equipment is in high-temperature and high concentration
Working environment in run, easily generate Structure Phenomenon, cleaning is extremely difficult, and operating cost increases.
And centrifuge the stage, traditional material returned centrifuge is due to the grain to the concentration of supersaturated liquid, temperature and crystal
Degree requirement is very high, easily generates clogging, separation of solid and liquid is caused to be difficult to realize, if containing a certain amount of organic in waste liquid
Object, then centrifugal effect is worse.
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 present invention provide it is a kind of overcome the shortage of prior art, single-stage but there is the device of multiple-effect evaporation simultaneously.
A kind of single-stage multiple-effect evaporation separator of the present invention is fresh including evaporator and vapour compression machine and connection
The pipeline of vapour source, distillation condensate output transistor, pending waste liquid intake line, dense discharging of waste liquid pipeline after processing and
The pump of various liquid and the control valve being set on pipeline are conveyed, dress centers first and second two evaporators, each to evaporate
Device is evaporated fluid output port and is evaporated the connecting pipeline that is respectively arranged between fluid input port and carries circulating pump thereon, respectively
The secondary steam pipe efferent duct of evaporator is connected with the input pipe of vapour compression machine, the steam input pipe and vapour pressure of each evaporator
The steam output pipe of contracting machine and the pipeline unicom in connection live steam source, the circulating pump upstream of the first evaporator are introduced with being used for
Pending waste liquid feed pipe connection, with band thereon between the circulating pump downstream of the first evaporator and the circulating pump upstream of the second evaporator
There is the pipeline connection of the second evaporation feed liquor control valve, being evaporated fluid output port and being evaporated liquid for the second evaporator inputs
Connecting pipeline between end is located at the evaporation dope discharge nozzle for carrying discharging control valve at circulating pump downstream thereon with threeway connection.
Preferably, a kind of single-stage multiple-effect evaporation separator of the invention, the input pipe and steam of pending waste liquid are pre-
Hot device heated medium input pipe connection, the heated medium efferent duct of vapor preheater and the input terminal of surface condenser connect
Logical, the output terminal of surface condenser is connected with the feed pipe of the first evaporator, and the vapor preheater is added using flue residue heat
Heat, the fixed gas port of export of the fixed gas arrival end of surface condenser respectively with two evaporators connect.During present invention work,
The mixture effusion of some vapor, incoagulable gas and air is had in evaporator, because incoagulable gas and air are all heat
Non-conductor, in heater assemble after by hinder evaporation, reduce heat exchange efficiency.Therefore it is provided with surface condensation in the present invention
Device, using the mixture of some vapor, incoagulable gas and air overflowed in evaporator in surface condenser with it is pending
Waste liquid carries out indirect heat exchange, and steam is condensed, and forms condensed water discharge, and incoagulable gas and air mixture are then to air
Discharge by the use of pending waste liquid as the cooling medium of surface condenser, further saves energy consumption, this structure of the invention according to
Make the discharge of mixed gas more easy by cooling down the quick barometric gradient that formed, solve the prior art and steaming is escaped from evaporator
When the mixture of vapour, incoagulable gas and air is in line because system pressure difference not enough caused by direct difficulty.Pass through surface condenser
Just the incoagulable gas in evaporator and air are continuously discharged afterwards, ensure that the efficient of vapo(u)rization system, steady and continuous service,
And further save energy consumption.
Preferably, in a kind of single-stage multiple-effect evaporation separator of the invention, set on the circulating pump downstream of the second evaporator
It is connected between evaporation dope discharge nozzle and the feed inlet of absorptiometer at place, the feed inlet of absorptiometer is arranged on the tangential direction of intermediate tube
On, the dope discharge nozzle of absorptiometer is connected with the feed inlet of automatic cutting centrifuge, the solid salt discharge of automatic cutting centrifuge
Mouth is arranged with chute, the leakage fluid dram of automatic cutting centrifuge and the clear liquid overflow pipe of absorptiometer respectively with filtrate tank into
Expect end connection, the discharge end of filtrate tank is connected with pending waste tank.
The present invention is in the case where using a vapour compression machine, and at least two or more sets evaporators share steam compressed
Machine is unified after the indirect steam respectively generated concentration is converged to be sent into after same vapour compression machine heating pressurization by sub-cylinder
An evaporator is distributed to as the heat source stream being persistently evaporated.Meanwhile waste liquid is first into a wherein evaporator, into
Concentration is risen after the preliminary evaporation of row, goes out liquid later to another group of evaporator, such waste liquid in different evaporators step by step
It is concentrated by evaporation, similar to the technique of traditional multiple-effect evaporation.Using waste liquid, in low concentration, the elevation of boiling point is smaller, can be formed larger
Effective temperature difference it is big, so as to reduce heat exchange area, improve evaporation efficiency, thus overcome traditional MVR evaporation elements work shape
The application limitations such as state is single, heat exchange area is larger, the cleaning frequency is shorter, have greatly widened the use scope of MVR vapo(u)rization systems,
The service efficiency of equipment is improved, reduces equipment investment and operating cost.The present invention is two evaporators of setting, but in reality
Application in also can be according to technological requirement and the concrete condition of pending waste liquid, basic principle according to the present invention sets more steamings
Device is sent out, to realize the purpose of multiple-effect evaporation.
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, waste heat flue gas carries out indirect heat transfer to the partial condensation water that vapo(u)rization system is formed, and partial condensation water is by heating vapour
Change becomes steam, and the flue gas after heat exchange is returned outside exhaust system high-altitude and arranged, and steam is entered to heat waste liquid in vapor preheater and be risen
Temperature provides condition for initial management, has recycled available resources.
Traditional pusher centrifuge is easily produced since the granularity requirements to the concentration of supersaturated liquid, temperature and crystal are very high
Raw clogging, causes separation of solid and liquid to be difficult to realize.In evaporation stage, since carnallites various in waste liquid mix, do not have
The standby operating condition for forming certain particle size, even if the solid content in waste liquid is higher, but the solid of granulating is not very much, therefore usually
Centrifuge is caused to block under the action of powdery solid, centrifugation task can not be completed.To solve this technical barrier, in of the invention
There is provided absorptiometers and automatic cutting centrifuge.The saturation waste liquid after evaporative crystallization is further thickened using absorptiometer, is increased
Input concentration before centrifugation improves the solid content of feeding liquid, and good basic condition is created to centrifuge.The charging of absorptiometer
Mouth is arranged in the tangential direction of intermediate tube, and larger crystalline particle forms eddy flow state in entrance and thrown to wall, with liquid stream
Sink under motional inertia and gravity, from underflow is formed, scheming be sent from the discharge of cone bottom, and clear liquid then due to density compared with
It is small, it is moved in upper up-flow, discharges, entered in filtrate tank from top overflow port.The full-automatic cutting centrifuge of the present invention is carrying out
During separation of solid and liquid, for waste liquid since proportion difference, solids are thrown to barrel in high speed rotation, the filter membrane on barrel can root
There is different selections according to actual conditions difference, filtering accuracy can be thousands of, mesh even up to up to ten thousand, the crystalline particle of waste liquid
It being centrifuged with powder and is adhered to barrel filter membrane surface, hydrone and soluble ion can then pass through filter membrane, from
And form filtrate and enter filtrate tank, filtrate returns vapo(u)rization system circular treatment；Later, step scraper promotes, and will be adhered to barrel
The solid material cutting blanking of filter membrane surface, is exported by crystal salt and discharged, fallen and pack along salt chute, so as to thoroughly solve
Carnallite of having determined is difficult to the problem detached.
Technical solution provided by the invention overcomes the deficiencies in the prior art comprehensively, meanwhile, degraded equipment significantly
Operating cost so that measures to effectively increase energy savings and reduce material consumption can be realized smoothly.
Description of the drawings
The embodiment schematic diagram that two group evaporators and a shared Pistonless compressor is made of of the attached drawing 1 for the present invention.
Attached drawing 2 heats the schematic device of pending waste water for the present invention using fume afterheat.
The centrifugation systems and its operating mode schematic diagram of 3 present invention of attached drawing.
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 evaporation dope discharge nozzle, and 8 be high temperature
Flue snorkel, 9 be high-temperature flue gas collecting pipe, 10 be preheater condensate pump, 11 be flue gas heat-exchange unit vapour-discharge tube, 12
For vapor preheater, 13 be vapor preheater drip pipe, and 14 be preheater condensate water pot, and 15 be surface condenser, 16
It is vapor preheater outlet tube for surface condenser drip pipe, 17,18 be surface condenser outlet tube, and 19 be fixed gas
Mixing tube, 20 be A evaporator fixed gas outlets, and 21 be A evaporation feed liquor control valves, and 22 be A evaporator circulating pumps, and 23 be A
Evaporator, 24 be A evaporator circulation fluid inlet tubes, and 25 be A evaporator indirect steam outlets, and 26 be A evaporator steam inlets
Pipe, 27 be A evaporator condensation water discharge spouts, and 28 be evaporator condensation water pot, and 29 be evaporator condensation water pump, and 30 be both vapor compression
Machine steam inlet tube, 31 be vapour compression machine, and 32 be vapour compression machine steam outlet pipe, and 33 be sub-cylinder, 34 for B evaporators not
Solidifying gas outlet, 35 be B evaporator steam inlet pipes, and 36 be B evaporator condensation water discharge spouts, and 37 be B evaporators, and 38 steam for B
Device indirect steam outlet is sent out, 39 be B evaporation feed liquor control valves, and 40 be B evaporator circulating pumps, and 41 be live steam pipe network,
42 be absorptiometer, and 43 be clear liquid overflow pipe, and 44 coagulate the soup dope discharge nozzle, and 45 be centrifugation control valve, 46 for it is full-automatic cut from
Scheming, 47 export for solid crystal salt, and 48 be filtrate pipe, and 49 be solid salt chute, and 50 be filtrate tank, and 51 be filtrate pump, and 52 are
Return to vapo(u)rization system filtrate pipe.
Specific embodiment
The present invention is explained below in conjunction with the embodiment that attached drawing provides.
The embodiment provided by attached drawing is as it can be seen that include the first evaporator 23 and the second evaporator 37 in the present invention.First
Being evaporated fluid output port and being evaporated between fluid input port for 23 and second evaporator 37 of evaporator is respectively arranged with band thereon
There is the connecting pipeline of first circulation pump 22 and second circulation pump 40.It is condensed in the upstream threeway communicating surface of first circulation pump 22
The outlet tube 18 of device 15.With thereon with the second evaporator between the downstream of first circulation pump 22 and the upstream of second circulation pump 40
The pipeline connection of 37 inlet control valve 39.The secondary steam pipe efferent duct 25 and 38 of two evaporators respectively with vapour compression machine
31 input pipe 30 connects.As seen from Figure 1, the exhaust outlet 32 of vapour compression machine 31 is connected with a sub-cylinder 33.Sub-cylinder 33
The steam input terminal of the first evaporator 23 and the second evaporator 37 is respectively communicated with pipeline 26 and 35 respectively, on pipeline 26 and 35
Valve is also respectively provided with, while sub-cylinder 33 also connects live steam pipe 41, to meet device when originating work by power
Boiler provides power steam.On the connecting pipeline for being evaporated fluid output port and being evaporated between fluid input port of second evaporator
In the evaporation dope discharge nozzle 7 for carrying discharging control valve thereon with threeway connection at circulating pump downstream.First evaporator 23
It is connected respectively with pipeline 27 and 36 with the condensed water output terminal of the second evaporator 37 and the condensed water output terminal of sub-cylinder 33 cold
Condensate intermediate storage tank 28, the output terminal condensate line 6 of condensed water intermediate storage tank 28 sees reuse off, on condensate line 6
It is additionally provided with condensate pump 29.It is preheated by attached drawing 1 as it can be seen that being also set up in apparatus of the present invention there are one surface condenser 15
Pending waste liquid is to be sent into surface condenser 15 to handle by pipe 17, is then discharged into surface condenser outlet tube from output terminal
18, it is re-fed into the first evaporator 23 and is handled, and the outlet of the fixed gas of first and second evaporator is respectively with first and the
Two fixed gas outlets 20 and 34 connect with fixed gas mixing tube 19 and are sent into the mouth fixed gas mixing tube 19 of surface condenser 15
Interior, the condensate pipe 16 of surface condenser is connected in preheater condensate water pot 14.
To make full use of the energy, in the device of the invention, the pending waste liquid for being sent into surface condenser 15 first passes through steam
Preheater 12 carries out the pre-heat treatment, and the preheater is heated using flue residue heat, then is sent into condenser 15 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.The present invention this
Structure can make the energy be fully utilized.
A kind of single-stage multiple-effect evaporation crystallization of the present invention and separator, the input pipe and steam preheating of pending waste liquid
Device heated medium input pipe connects, and the heated medium efferent duct of vapor preheater is connected with the input terminal of surface condenser,
The output terminal of surface condenser is connected with the feed pipe of the first evaporator, and the vapor preheater is heated using flue residue heat,
The fixed gas port of export of the fixed gas arrival end of surface condenser respectively with two evaporators connects.Due to setting up surface condensation
Device makes, by just continuously discharging the incoagulable gas in evaporator and air after surface condenser, to ensure that vapo(u)rization system
Efficiently, steady and continuous service.
Absorptiometer 42 and automatic cutting centrifuge 46 are additionally provided in the embodiment of the present invention, referring to attached drawing 3, wherein, if
Evaporation dope discharge nozzle 7 at 40 downstream of circulating pump of the second evaporator 37 is coagulated the soup with being connected between the feed inlet of absorptiometer 42
The feed inlet of device is arranged in the tangential direction of intermediate tube, the dope discharge nozzle 44 of absorptiometer and automatic cutting centrifuge 46 into
Material mouth connects.The solid salt outlet 47 of automatic cutting centrifuge 46 is arranged with chute 49, and solid salt can be conveyed through chute 49
To corresponding region.The leakage fluid dram 48 of automatic cutting centrifuge 46 and the clear liquid overflow pipe 43 of absorptiometer 42 respectively with a filtrate tank
50 feed end connection.Filtrate pipe 52 of the discharge end of filtrate tank 50 with filtrate pump 51 and control valve is stored up with pending waste liquid
Tank connects.
The working condition 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.
Waste liquid enters the steam generation heat exchange that in vapor preheater 12 and flue gas generates, waste liquid through waste liquid liquid supply pipe 5
Tentatively heated, steam is condensed caused by flue gas, formed condensed water after pass through by vapor preheater drip pipe 13 into
Enter to preheater condensate water pot 14 and temporarily store.
Waste liquid after tentatively being heated is exited into from vapor preheater outlet tube 17 in surface condenser 15, with from
The mixture of the incoagulable gas and steam of A evaporator fixed gases outlet 20 and B evaporator fixed gases outlet 34 is not coagulating
Converge in gas mixing tube 19, concentration, which is entered in surface condenser 15, occurs heat exchange, and condensed water is formed after steam cooling through table
The condensed water mixing that face condenser drip pipe 16 is entered in preheater condensate water pot 14 and vapor preheater is formed,
Production reuse is sent with preheater condensate pump 10.Waste liquid is heated again, is discharged by surface condenser outlet tube 18, is entered A
It is then entered in B evaporators 37 by B evaporation feed liquors control valve 39 in evaporator 23.
A is respectively started after the work liquid level that waste liquid meets after process pipeline enters A, B evaporator needed for evaporation
Evaporator circulating pump 22, B evaporators circulating pump 40, waste liquid are evenly distributed to respective heat exchange element surface and are constantly recycled respectively
Flowing.Steam is supplied into sub-cylinder 33 through live steam pipe network 43, steam is evaporated via A evaporator steam inlets pipe 26 and B
Device steam inlet pipe 35 is had respectively entered in the heat exchange element of A evaporators 23 and B evaporators 37, and steam and waste liquid fully carry out heat
Steam is condensed after exchange, forms condensed water, is discharged respectively via A evaporator condensations water discharge spout 27 and B evaporator condensations water
Pipe 36 enters evaporator condensation water pot 28, then sees reuse off from distillation condensed water flow pipe 6 through evaporator condensation water pump 29, together
When clear water is continuously replenished into flue gas heat-exchange unit 2.Waste liquid is constantly heated in A evaporators 23, B evaporators 37, is then reached
Violent fluidized state generates a large amount of indirect steam, through A evaporator indirect steams outlet 25 and B evaporator indirect steams
Outlet 38, which is pooled in vapour compression machine steam inlet tube 30, enters vapour compression machine 31, using high-tension electricity drive motor
Rotation then drives vapour compression machine work, and indirect steam is warmed pressurization, and increases after heat content by vapour compression machine steam
Outlet 32, which is sent in sub-cylinder 33, replaces live steam to work, and hereafter no longer needs live steam, vapour compression machine 31 is not
Disconnected cycle compressed steam, evaporation continuation steadily carry out.
With the lasting progress of evaporation and concentration, waste liquid a portion condenses after being vaporized in evaporator, forms condensed water
Drain, decline so as to cause the liquid level in evaporator.At this point, B evaporation feed liquors control valve 39 is opened, it is useless in A evaporators 23
Liquid is entered in B evaporators 37, meanwhile, A evaporation feed liquors control valve is opened, the waste liquid in waste liquid tank via waste liquid by waste liquid
Liquid supply pipe 5 feeds supplement liquid level into A evaporators 23.With the lasting progress of politics and law, waste liquid is flowed also in lasting progress, thus
Realize that waste liquid stepped evaporation in different evaporators concentrates, similar to the technique of traditional multiple-effect evaporation.
Inorganic salts in waste liquid are constantly crystallized after being reached saturation due to evaporation and concentration, and forming salt is brilliant, are gone out in evaporation dope
It is discharged in expects pipe 7, enters absorptiometer 42 from the tangential direction of 42 feed inlet intermediate tube of absorptiometer, larger crystalline particle is in entrance
It forms eddy flow state and is thrown to wall, sink under motional inertia and gravity with liquid stream, from underflow is formed, by dope of coagulating the soup
The discharge of discharge nozzle 44 is sent from scheming, and clear liquid moves then since density is smaller in upper up-flow, from 43 overflow port of upper clear supernate overflow pipe
Discharge, enters in filtrate tank 50.
Waste liquid after coagulating the soup enters full-automatic cutting centrifuge 46 and carries out separation of solid and liquid, waste liquid in high speed rotation due to than
Weight is different, and solids is thrown to barrel, the filter membrane on barrel can be different according to actual conditions and have different selections, mistake
Filtering precision can be thousands of, and mesh even up to up to ten thousand, the crystalline particle and powder of waste liquid, which are centrifuged, is adhered to barrel filter membrane table
Face, hydrone and soluble ion can then pass through filter membrane, and so as to form filtrate, filtrate is entered via filtrate pipe 48
Tank 50, filtrate send vapo(u)rization system circular treatment back to by filtrate pump 51 through returning to vapo(u)rization system filtrate pipe 52；Later, step scraper pushes away
Into, will be adhered to barrel filter membrane surface solid material cutting blanking, by solid crystal salt outlet 47 discharge, along solid salt
Chute 49 falls and packs, so as to thoroughly solve the problems, such as that carnallite is difficult to detach.
Waste liquid forms condensed water and highly concentrated high saturated brine after the device of the present embodiment is concentrated by evaporation, then through further from
Solid packs reuse or as industrial preparation after heart separation, it is achieved thereby that a resource recycling, is discharged residual from device
Waste liquid, which is fed back at pending waste liquid storage, re-starts processing, therefore the device of the invention can realize liquid, solid pollutant
Zero-emission.
The introduction of above example can be crossed it is found that the present invention also can be according to the concrete condition and technological requirement of waste liquid in device
In add evaporator, to be suitble to the requirement of other waste liquid triple effects or more effect processing.
Claims (3)
1. a kind of single-stage multiple-effect evaporation separator, the pipe including evaporator and vapour compression machine and connection live steam source
Road, distillation condensate output transistor, pending waste liquid intake line, dense discharging of waste liquid pipeline after processing and the various liquid of conveying
The pump of body and the control valve being set on pipeline, it is characterised in that first and second two evaporators are at least set in device, respectively
Evaporator is evaporated fluid output port and is evaporated communicating pipe for being respectively arranged between fluid input port and carrying circulating pump thereon
Road, the secondary steam pipe efferent duct of each evaporator are connected with the input pipe of vapour compression machine, the steam input pipe of each evaporator with
The steam output pipe of vapour compression machine and the pipeline unicom in connection live steam source, the circulating pump upstream of the first evaporator is with using
In introducing pending waste liquid feed pipe connection, used between the circulating pump downstream of the first evaporator and the circulating pump upstream of the second evaporator
The pipeline connection of the second evaporation feed liquor control valve is carried thereon, and being evaporated for the second evaporator and is evaporated liquid at fluid output port
Connecting pipeline between body input terminal is located at circulating pump downstream to be gone out with threeway connection with the evaporation dope of discharging control valve thereon
Expects pipe.
A kind of 2. single-stage multiple-effect evaporation separator according to claim 1, it is characterised in that the input of pending waste liquid
Pipe is connected with vapor preheater heated medium input pipe, the heated medium efferent duct of vapor preheater and surface condenser
Input terminal connects, and the output terminal of surface condenser is connected with the feed pipe of the first evaporator, and the vapor preheater utilizes cigarette
Road waste-heat, the fixed gas port of export of the fixed gas arrival end of surface condenser respectively with two evaporators connect.
3. a kind of single-stage multiple-effect evaporation separator according to claim 1 or 2, it is characterised in that set on the second evaporator
Circulating pump downstream at evaporation dope discharge nozzle and the feed inlet of absorptiometer between connect, the feed inlet of absorptiometer is arranged on centre
In the tangential direction of pipe, the dope discharge nozzle of absorptiometer is connected with the feed inlet of automatic cutting centrifuge, automatic cutting centrifuge
Solid salt outlet be arranged with chute, the leakage fluid dram of automatic cutting centrifuge and the clear liquid overflow pipe of absorptiometer are respectively with one
The feed end connection of a filtrate tank, the discharge end of filtrate tank are connected with pending waste tank, return system circulation processing.
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| CN201810240424.3A CN108217797A (en) | 2018-03-22 | 2018-03-22 | A kind of single-stage multiple-effect evaporation separator |
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| CN201810240424.3A CN108217797A (en) | 2018-03-22 | 2018-03-22 | A kind of single-stage multiple-effect evaporation separator |
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