CN208413904U - It is a kind of can simultaneously a variety of waste liquids of crystallization treatment device - Google Patents

Abstract

The utility model disclose it is a kind of can a variety of waste liquids of crystallization treatment simultaneously device.The vaporising device of the utility model includes evaporator and vapour compression machine, connecting pipeline, the control valve for conveying the pump of various liquid and being set on pipeline, a point column are provided with evaporator identical with waste liquid number of species to be processed and crystal seed conveying mechanism in described device, the secondary steam pipe efferent duct of each evaporator is connected to the input pipe of a vapour compression machine, the steam input pipe of each evaporator is with the steam output pipe of vapour compression machine and is connected to the pipeline connection in live steam source, the lower half of the evaporation cavity of each evaporator is respectively connected to a crystal seed conveying mechanism respectively, salt crystalline substance collection device is respectively arranged at the lower cone of each evaporator.The utility model is the work heat source of each evaporator using secondary steam after compression, while taking full advantage of flue residue heat, can sufficiently recycle resource, while can be effectively treated to waste liquid.

Description

It is a kind of can simultaneously a variety of waste liquids of crystallization treatment device

Technical field

The utility model relates to a kind of method and device thereof of evaporation process, and exactly, the utility model relates to one kind can Condensing crystallizing handles device used in the method and this method of a variety of waste liquids simultaneously.The evaporation process side of the utility model Method has similarity with the evaporation process method mutually having, and includes the MVR of evaporator and vapour compression machine composition in its device The pipeline of pipeline, live steam source between vaporising device, and connection secondary steam and vapour compression machine, distillation condensed water output Pipe, waste liquid intake line to be processed, dense discharging of waste liquid pipeline after processing, and convey the pump of various liquid and be set to pipeline On control valve.

Background technique

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 being achieved as National Environmental administers the increasing of policy and inspection Some gratifying achievements, still, waste water outlet are the embarrassment reality for having to face, and the public still feels that water pollution adds Play, the pressure of environmental improvement is still very big, the not change of essence.On the one hand, the waste water origin cause of formation of China's outlet 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 and ingredient mistake of outlet pollutant In single, the substance of the limitation does not bring standard into, and major pollutants row value as defined in standard only only accounts for Injury to human body cannot be much connected to each other with environmental demand, led to sewage effluent pollution environment, deteriorated water quality.Certainly, 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 level of sewage treatment.

Currently, 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 effective component separation for realizing orientation different from the molecular weight of liquid Effect, but effective osmotic pressure cannot be formed after the degree that inorganic salt concentration in sewage reaches certain, therefore make Narrow range, cost of investment is excessively high in addition, is not able to satisfy industrial needs at present；Evaporative crystallization is to form sewage evaporation to steam Distilled water and strong brine, strong brine either still use MVR vapo(u)rization system using the system of traditional multiple-effect again through being separated by solid-liquid separation, Treated, and water quality is very good, and solid waste can concentrate pack, processing result ratio more thoroughly, still, calcium, magnesium in waste water, Silicon ion content is very high, and contains the solid suspensions such as a large amount of calcium carbonate and excessive ash, it will ties rapidly in evaporator Dirt, therefore need to shut down scale removal afterwards for a period of time in equipment operation, it otherwise will cause equipment and be unable to operate normally.

Since it is with easy to operate, space occupied is small, energy-saving effect is good etc. many obtains a little traditional MVR vapo(u)rization system It is widely applied, but it is an independent unit, processing performance is poor, a set of MVR vapo(u)rization system can only handle one Kind medium.However there are many sewage species that some enterprises generate, and each sewage water is not very greatly, if to each Kind sewage requires mating different vapo(u)rization system, classification processing, the generated investment of such method of operation and administration fee Enterprise is allowed to can't bear the heavy load.

Boiler is usually widely used in the industrial production to generate steam to meet process requirement, outlet 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.

Summary of the invention

The utility model, which provides, a set of solves the insufficient technical solution of the prior art.The technical solution of the utility model Gram the deficiencies in the prior art can be taken, meanwhile, the operating cost for the equipment that degraded significantly enables measures to effectively increase energy savings and reduce material consumption to be able to suitable Benefit is realized.

The utility model it is a kind of can the devices of a variety of waste liquids of crystallization treatment simultaneously be to work as follows: will be different Waste liquid to be processed, which is introduced respectively in different evaporators, is evaporated concentration and crystallization treatment, and the secondary steam of each evaporator is sent into One vapour compression machine compress after making its heat content increase and is used further to heat each evaporator.

The utility model can simultaneously a variety of waste liquids of crystallization treatment method in, at least part waste liquid to be processed is being sent into It is heated before evaporator first with flue residue heat.

The utility model one kind can the vaporising devices of a variety of waste liquids of crystallization treatment include: simultaneously evaporator and both vapor compression Machine, and pipeline, the distillation condensate output transistor, waste liquid intake line to be processed, after processing dense in connection live steam source Discharging of waste liquid pipeline, and the various liquid of conveying pump and the control valve that is set on pipeline, in described device a point column be provided with The identical evaporator of waste liquid number of species to be processed and crystal seed conveying mechanism, the secondary steam pipe efferent duct of each evaporator is with one The input pipe of a vapour compression machine is connected to, and the steam input pipe of each evaporator and the steam output pipe of vapour compression machine and is connected to The pipeline connection in live steam source, each evaporator are respectively arranged with connection evaporated liquid output end and evaporated liquid input terminal Between and circulation connecting pipeline that have circulating pump thereon, different waste liquid intake line to be processed respectively evaporated respectively with one The feed pipe of device is connected to, and the lower half of the evaporation cavity of each evaporator is respectively connected to a crystal seed conveying mechanism respectively, each evaporator Lower cone at be respectively arranged with salt crystalline substance collection device, each salt crystalline substance collection device has the discharging of discharging control valve respectively and thereon Delivery pipe connection.

Preferably, the utility model can simultaneously a variety of waste liquids of crystallization treatment vaporising device in point column be provided with wait locate The identical surface condenser of waste liquid number of species is managed, each waste liquid to be processed is respectively fed to each evaporation after surface condenser is handled Device.When utility model works, the mixture evolution of some vapor, incoagulable gas and air is had in each evaporator, because All it is the non-conductor of heat for incoagulable gas and air, evaporation will be hindered after assembling in heater, reduces heat exchange efficiency.Cause It is provided with surface condenser in this utility model, utilizes some vapor, incoagulable gas and the air overflowed in evaporator Mixture carries out indirect heat exchange with waste liquid to be processed in surface condenser, and steam is condensed, and forms condensed water discharge, without Solidifying property gas and air mixture are then discharged to atmosphere, using waste liquid to be processed as the cooling medium of surface condenser, into one Step saves energy consumption, this structure of the utility model holds that the discharge of mixed gas more by the cooling barometric gradient that quickly formed Easily, solve the prior art escaped from evaporator steam, incoagulable gas and air mixture it is in line when because of system pressure difference Not enough cause direct difficulty.By after surface condenser just by evaporator incoagulable gas and air be continuously discharged, protect The efficient of vapo(u)rization system has been demonstrate,proved, steady and continuous service, and further save energy consumption.

Preferably, the utility model can simultaneously a variety of waste liquids of crystallization treatment vaporising device in, be sent into each surface condensation At least a part of preheater that first passes through respectively of the waste liquid to be processed of device carries out the pre-heat treatment, and the preheater utilizes more than flue Heat heating.

Preferably, the utility model can simultaneously a variety of waste liquids of crystallization treatment vaporising device, the lower cone of each evaporator A vertical tube is respectively set in body, is sequentially communicated salt crystalline substance cylinder respectively along vertical tube short transverse, is provided with discharging control valve Discharge nozzle, be provided with washing control valve flushing pipe and rinse general pipeline.

The utility model can simultaneously a variety of waste liquids of crystallization treatment vaporising device most preferred embodiment in, point column be provided with Two evaporators and two crystal seed conveying mechanisms.

More evaporators identical with waste liquid number of species to be processed are arranged in the utility model point column, such as divide column setting three For platform evaporator to handle three kinds of waste liquids to be processed, each evaporator uses same vapour compression machine, by the evaporation of formula, point column arrangement Secondary steam caused by device, which carries out returning again after heating pressurization together, to be conveyed to each evaporator group and uses as heat source.Respectively Evaporator is evaporated enrichment to processed liquid therein is introduced, and at it close or equal to after saturated concentration, passes through crystalline substance Kind conveying mechanism introduces crystal seed into waste liquid, promotes its crystallization.

Flue gas waste heat-recovering device is arranged in the utility model, configures flue gas heat-exchange unit, is sent into after flue gas collection is summarized Into flue gas heat-exchange unit, the partial condensation water that at least part vapo(u)rization system is formed is carried out using the waste heat flue gas of flue indirect Heat transfer, partial condensation water is heated vaporization and becomes steam, and the flue gas after heat exchange returns exhaust system high-altitude outlet, the steam of formation into Enter at least part waste liquid heat temperature raising into vapor preheater, pre-add can also be carried out to each waste liquid to be processed used certainly Heat treatment.This way and structure of the utility model are that initial management provides condition, while can also sufficiently recycle money Source.

The utility model settles structure in the tubular salt crystalline substance that each evaporator lower disposed is referred to as salt crystalline substance cylinder, gives up in evaporator Inorganic salts in liquid are constantly crystallized after being reached saturation due to evaporation and concentration, and forming salt is brilliant, because of the downward subsiding movement of gravity relationship, Salt crystalline substance cylinder is gradually dropped into from cone, the supersaturated waste water containing salt crystalline substance discharges from salt crystalline substance cylinder lower part, and centrifugation systems is sent to be consolidated Liquid separation.The utility model 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, Rinse salt filtrate enter after salt crystalline substance cylinder along barrel rise with the countercurrent washing of salt crystalline substance, generate the phenomenon that being similar to boiling, by gypsum, Small grain of salt crystals, which is brought into again in evaporator, continues to participate in circulation, and saturation inorganic salts are attached as core using this tiny crystal grains Grow up, while soluble impurity can be dissolved and be removed, advantageously form the crystalline particle with certain volume, granularity improves, Facilitate centrifuge efficient operation.The balanced exchange and distribution of heat will be carried out while rinsing salt filtrate and salt crystalline substance antikinesis, So that the crystallization strong brine temperature of discharging reduces, reduces thermal loss, be conducive to be centrifugated.Experiments have shown that it is dense to discharge Salt water and the volume ratio for rinsing salt filtrate are set as between 1:1.2-1.3, that is to say, that the flow of flushing liquor is slightly greater than Flushing process from bottom to top can be better achieved in this way, and sufficiently carry out heat exchange for the load of strong brine, and output passes through Discharge valve on pipeline realizes accurate adjustment control with hydraulic control valve is rinsed.Flushing liquor in the utility model is from steaming The mixture of salt filtrate and waste liquid after sending out device discharging centrifugation, concentration is close to saturation, and temperature is lower than dense salt in evaporator Water is ideal scouring media.

Crystal grain inoculation system is arranged in the utility model, be interrupted by crystal seed tank into evaporator or continuous conveying add with Calcium sulfate or the substance of selectivity are basic additive, i.e., artificially control nucleus quantity, when the inorganic salts of waste water tend to saturation, Inorganic salts are attached on the crystal grain the surface of the seed of these additions and constantly grow up, and the particle of crystallization remains suspended in water, will not It is attached to heat exchange element surface scale, so that evaporation can continually and steadily be run.

Detailed description of the invention

Attached drawing 1 be the utility model be divided to column be arranged two groups of evaporators can a variety of waste liquids of crystallization treatment simultaneously device implementation It illustrates and is intended to.

Attached drawing 2 is the device connection schematic diagram that fume afterheat heated waste water is utilized in the utility model embodiment.

Attached drawing 3 is that salt crystalline substance rinses and sink mechanism embodiment schematic diagram.

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 secondary 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 secondary 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 evaporator 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 flushing pipe, and 54 be flushing liquor control valve, and 55 be undershoot Pipe is washed, 56 is rinse general pipeline, and 57 be evacuation port.

Specific embodiment

The utility model is explained below in conjunction with the Installation practice 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 secondary steam of evaporator 23 and the second evaporator 37 outlet 25 and 38 is connected to the air inlet 30 of vapour compression machine 31.Vapour pressure The exhaust outlet 32 of contracting machine 31 is connected to 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 on pipeline 26 and 35 as seen from the figure, while sub-cylinder 33 is also connected to fresh steaming Steam pipe 43 provides power steam by power boiler to meet device when originating work.First evaporator 23 and the second evaporator 37 condensed water water outlet uses condensate pipe 27 and 36 to be connected to condensate water pot 28 respectively, also divides on pipeline 27 and 36 as seen from the figure Valve is not provided with it.The evaporated liquid output end of first evaporator 23 and the second evaporator 37 and evaporated liquid input terminal point The pipeline connection that circulating pump 40 and 22 Yong be had thereon, the upstream of circulating pump 40 respectively with the pipe that inputs waste liquid to be processed Road connection.

Waste liquid to be processed is inputted in the device of the utility model can directly use connection waste liquid cylinder pipeline connection, but in this reality With in novel most preferred embodiment, being to be provided with surface condenser 15 in a device, the first waste liquid to be processed is through surface condenser Each evaporator is respectively fed to after processing again.The fixed gas of evaporator and the mixture concentration of steam are entered in surface condenser and are sent out Heat exchange forms condensed water after steam is cooling and is discharged through surface condenser drip pipe, final incoagulable gas and sky Gas mixture is emptied to atmosphere.It, will resistance after assembling in heater because incoagulable gas and air are all the non-conductors of heat Hinder evaporation, reduce heat exchange.The utility model by setting surface condenser, can by evaporator incoagulable gas and air connect Continuous discharge, ensure that the efficient of vapo(u)rization system, steady and continuous service.

To make full use of the energy, in the device of the utility model, the first waste liquid to be processed for being sent into surface condenser 15 is first The pre-heat treatment is carried out by preheater, the preheater is heated using flue residue heat, then is sent into condenser with waste-solution line 17 15, it is respectively fed in first or second evaporator 23 or 37 again after the processing of surface condenser 15, referring to attached drawing 2.Attached drawing provides The utility model embodiment in second of waste liquid to be processed without preparatory processing, be directly admitted to by the second liquid supply pipe 7 It is handled in second evaporator 37.It should be noted that can also be arranged again for the second evaporator according to specific circumstances a set of The waste-heat facility of surface condenser and its front end before first evaporator 23 as shown in Fig. 1, to second wait locate Reason waste liquid is heated in advance.

The evaporation cavity lower part of second evaporator of the vaporising device of the vapo(u)rization system of the utility model is provided with by dosing mouth 51, crystal seed tank 50, crystal seed delivery pump 49 and thereon with crystal seed inoculation mouth control valve 47 crystal seed delivery pipe constitute crystal seed it is defeated Send mechanism.It should be noted that the details of the first evaporator 23 and crystal seed conveying mechanism is not indicated in fig. 1, in specific device It can according to need the crystal seed conveying mechanism being arranged to the first evaporator as being arranged on the second evaporator in attached drawing 2.Each Salt crystalline substance collection device is respectively arranged at the lower cone 46 of evaporator or 45.By taking the second evaporator 37 as an example, referring to attached drawing 3, Be arranged on the lower cone 45 of its evaporator by being sequentially communicated salt crystalline substance cylinder 52 respectively along vertical height direction on vertical tube, setting thereon It is equipped with the discharge nozzle 42 of discharging control valve 41, be provided with the upper flushing pipe 53 of washing control valve and rinses general pipeline 56 and is constituted Salt crystalline substance collection device.The upstream of upper flushing pipe 53 is provided with lower flushing pipe 55 and washing control valve 54.First evaporator 23 Set salt crystalline substance collection device is identical, steaming with salt crystalline substance collection device set by the second evaporator 37 on lower cone 46 Sending out device discharging delivery pipe 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: being aggregated into height from high-temperature flue snorkel 8 from different smokejack exhaust gas It enters in flue gas heat-exchange unit 2 after warm flue gas collecting pipe 9, while being sent through flue gas heat-exchange unit water inlet pipe 4 into flue gas heat-exchange unit 2 Enter clear water, the condensed water that the clear water that the present embodiment is supplied to flue gas heat-exchange unit is generated from evaporation, with certain temperature and Heat content.In flue gas heat-exchange unit 2, clear water and high-temperature flue gas sufficiently exchange heat, clear water is vaporized to form steam after by flue gas heat-exchange unit Vapour-discharge tube 11 is discharged, and enters in vapor preheater 12.It is controlled by flue gas heat-exchange unit water inlet control valve 3 into flue gas and is changed Clear water amount in hot device 2, 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 Gas exhaust system outlet.

The first waste liquid to be processed 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 caused by flue gas is condensed, and 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 exits into surface condenser 15 from vapor preheater outlet tube 17, With incoagulable gas and steam from the first evaporator fixed gas outlet 20 and the second evaporator fixed gas outlet 34 Mixture converges in fixed gas mixing tube 19, and concentration, which enters in surface condenser 15, occurs heat exchange, shape after steam is cooling It is entered in preheater condensate water pot 14 at condensed water through surface condenser drip pipe 16 and vapor preheater is formed Condensed water mixing, send production reuse 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 waste liquid to be processed in its storage tank with the second liquid supply pipe 7 directly from being introduced into the second evaporator 37 and carrying out Reason.

Meet needed for evaporation after waste liquid is entered by different pipelines has respectively entered the first, second evaporator 23 and 37 The first evaporator circulating pump 22, the second evaporator circulating pump 40 are respectively started after work liquid level, waste liquid is evenly distributed respectively It is constantly circulated to respective heat exchange element surface.Steam, steam warp are supplied into sub-cylinder 33 through live steam pipe network 43 First evaporator 23 and second is had respectively entered by the first evaporator steam inlet pipe 26 and the second evaporator steam inlet pipe 35 In the heat exchange element of evaporator 37, steam is condensed after steam and waste liquid sufficiently carry out heat exchange, forms condensed water, respectively via First evaporator condensation water discharge spout 27 and the second evaporator condensation water discharge spout 36 enter evaporator condensation water pot 28, then pass through Evaporator condensation water pump 29 sees reuse off from distillation condensed water flow pipe 6, while clear water is continuously replenished into flue gas heat-exchange unit 2. Waste liquid is constantly heated in 23 second evaporator 37 of the first evaporator, then reaches violent fluidized state, is generated a large amount of Secondary steam is pooled to vapour pressure through the first evaporator secondary steam outlet 25 and the second evaporator secondary steam outlet 38 Enter vapour compression machine 31 in contracting machine steam inlet tube 30, is rotated using high-tension electricity drive motor, then drive vapour pressure The work of contracting machine, secondary steam is warmed pressurization, and increases and be sent to a point gas by vapour compression machine steam outlet pipe 32 after heat content It replaces live steam to work in cylinder 33, hereafter no longer needs live steam, the constantly circulation compressed steam of vapour compression machine 31, evaporation Continued smooth carries out.

Respectively with the lasting progress of evaporation and concentration, concentration increases liquid in two evaporators, full reaching It will form salt crystalline substance 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 can promote the crystallization process in it, salt crystalline substance gradually drops into salt crystalline substance cylinder 52 from evaporator lower cone 45, come It is entered in salt crystalline substance cylinder 52 from the flushing liquor rinsed in general pipeline 56 from upper flushing pipe 53 and lower flushing pipe 54, flushing liquor enters Along barrel rising and the countercurrent washing of salt crystalline substance 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 circulation, and saturation inorganic salts, which are adhered to using this tiny crystal grains as core, grows up, while can Soluble impurity is dissolved and is removed, the crystalline particle with certain volume is advantageously formed, granularity improves, and facilitates centrifuge efficient Work.The balanced exchange and distribution of heat will be carried out while rinsing salt filtrate and salt crystalline substance antikinesis, so that the crystallization of discharging Strong brine temperature reduces, and reduces thermal loss, is conducive to be centrifugated.Usually by discharging strong brine amount and salt filtrate can be rinsed Volume ratio be set as between 1:1.2-1.3, pass through the second evaporator discharging control valve 41 and flushing liquor control valve 55 be real Now accurate adjustment control.The flushing liquor for the second evaporator in the present embodiment is after the discharging centrifugation of the second evaporator The mixture of salt filtrate and waste liquid, for concentration close to saturation, temperature is that ideal flushing is situated between lower than strong brine in evaporator Matter.Similarly, identical operating condition is experiencing 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 For sending out device, the utility model can also be by will have certain particle size from crystal seed tank 50 with calcium sulfate or selectivity Substance be basic additive, inoculum is quantitatively conveyed to B evaporator 37 by crystal seed delivery pipe 48 with crystal seed delivery pump 49, can Taking human as the granule size of control nucleus quantity and crystal, primary condition is provided to be separated by solid-liquid separation.When the inorganic salts of waste water become When being saturated and generating crystallization trend, inorganic salts, which are just attached on the crystal grain seed of these additions, constantly grows up, and keeps suspending In water, 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, further solid fills after centrifuge separation Bag reuse or as industrial preparation, so that a resource recycling is realized, the advanced technologies case of liquid waste processing zero-emission.

For enterprise production in generate a greater variety of waste liquids to be processed, can divide respectively according to specific circumstances column setting with The identical evaporator of waste liquid number of species to be processed, to be handled simultaneously.

Claims (5)

1. one kind can a variety of waste liquids of crystallization treatment simultaneously device, including evaporator and vapour compression machine, and the fresh steaming of connection The pipeline of vapour source, distillation condensate output transistor, waste liquid intake line to be processed, dense discharging of waste liquid pipeline after processing and defeated The control valve for sending the pump of various liquid and being set on pipeline, it is characterised in that a point column are provided with and waste liquid kind to be processed in device The identical evaporator of class quantity and crystal seed conveying mechanism, the secondary steam pipe efferent duct of each evaporator with a vapour compression machine Input pipe connection, the steam input pipe of each evaporator and the steam output pipe of vapour compression machine and be connected to live steam source Pipeline connection, each evaporator be respectively arranged with connection evaporated liquid output end and evaporated liquid input terminal between and thereon Circulation connecting pipeline with circulating pump, different waste liquid intake lines to be processed respectively connect with the feed pipe of an evaporator respectively Logical, the lower half of the evaporation cavity of each evaporator is respectively connected to a crystal seed conveying mechanism respectively, the lower cone punishment of each evaporator It is not provided with salt crystalline substance collection device, each salt crystalline substance collection device is connected to the discharging delivery pipe for having discharging control valve thereon respectively.

2. it is according to claim 1 can simultaneously a variety of waste liquids of crystallization treatment device, it is characterised in that be provided in device Surface condenser identical with waste liquid number of species to be processed, each waste liquid to be processed are respectively fed to respectively after surface condenser is handled Evaporator.

3. it is according to claim 2 can simultaneously a variety of waste liquids of crystallization treatment device, it is characterised in that it is cold to be sent into each surface At least a part of preheater that first passes through respectively of the waste liquid to be processed of condenser carries out the pre-heat treatment, and the preheater utilizes flue Waste-heat.

4. it is according to claim 1 or 2 or 3 can simultaneously a variety of waste liquids of crystallization treatment device, it is characterised in that Ge Gezheng A vertical tube is respectively set in the lower cone of hair device, is sequentially communicated salt crystalline substance cylinder respectively along vertical tube short transverse, is provided with The discharge nozzle of discharging control valve, the flushing pipe for being provided with washing control valve and flushing general pipeline.

5. it is according to claim 4 can simultaneously a variety of waste liquids of crystallization treatment device, it is characterised in that set respectively in device It is equipped with two evaporators and two crystal seed conveying mechanisms.