CN206730539U - A kind of liquid evaporation enrichment facility - Google Patents
A kind of liquid evaporation enrichment facility Download PDFInfo
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- CN206730539U CN206730539U CN201720564503.0U CN201720564503U CN206730539U CN 206730539 U CN206730539 U CN 206730539U CN 201720564503 U CN201720564503 U CN 201720564503U CN 206730539 U CN206730539 U CN 206730539U
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- evaporator
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Abstract
The utility model provides a kind of liquid evaporation enrichment facility.At least arranged in device of the present utility model by two evaporator series, the feed input of preheater connects with waste liquid feed-line in device, the output end of preheater connects with the feed end of evaporator, the circulation line for carrying circulating pump thereon is provided between the feed input and output end of each evaporator, the cold fixed gas outlet side of previous stage evaporator connects with the steam inlet end of rear stage evaporator, the steam output end of final evaporator is connected with preheater steam inlet end, and the indirect steam that a jet pump introduces final evaporator is provided with device.The utility model takes full advantage of the energy in system, form a kind of new pressure and temperature balance, system will be back to after the heating pressurization of end effect steam, so as to realize recycling for steam, overcome the deficiencies in the prior art, energy-saving effect clearly, the investment operating cost for the equipment that degraded significantly.
Description
Technical field
A kind of liquid evaporation enrichment facility is the utility model is related to, needs to carry out at concentration in particularly a kind of industrial production
The technique of reason, and concentration is evaporated to life and industrial wastewater, distilled water and dense waste liquid are formed, further to twice laid
And harmless treatment is done, reclaim other industrial products in waste water, the device of water-filling resource of going forward side by side recycling.The utility model
Device includes process pipelines between evaporator, waste liquid preheater, condensate water pot and each evaporator of connection and miscellaneous equipment, work
Skill water pump and valve.
Background technology
Vaporising device and its system process have very important status in national product, are often undertaken in industrial production
Various forms of technique contents such as decomposition, extraction, separation, concentration, for example milk in food service industry, fruit juice, beverage is dense
Contracting and high-temperature sterilization；Such as need certain solution being maintained under specific concentration in the industrial production again and realize that certain is specific
Technology mode, it is required for a set of complete vapo(u)rization system to ensure and realize.Evaporation technology is also desalinization, at sewage simultaneously
Manage the key industry means of the industries such as reuse.Therefore the technology upgrading to vapo(u)rization system and equipment and energy-saving and emission-reduction are a sternnesses
With urgent problem.
In order to realize the purpose of energy-conservation in evaporation technology system, the general shape for using multifunctional evaporating equipment arranged in series
Formula, the application of multiple-effect evaporation is a traditional mode the most basic, and current application is still quite varied.Traditional multiple-effect
Last evaporator is connected with condenser in vapo(u)rization system, injects secondary steaming of the substantial amounts of clear water by last evaporator within the condenser
Vapour cools down, and then extracts incoagulable gas and air using vavuum pump, so as to the temperature and pressure difference between formation system, protects
Card system being capable of normal work.Indirect steam temperature and pressure in last evaporator is all than relatively low, but the latent heat of steam is again
It is very huge, have no idea directly to apply in traditional multi-effect evaporation system, to set some technological equipments to utilize clear water on the contrary
Go to cool down, clear water send cooling tower cooler after being heated, and is back to condenser after cooling again, forms a process to consume energy repeatedly.
Traditional multiple-effect evaporation howsoever increases effect number, but it is also a brass tacks that the indirect steam of end effect, which is unable to reuse, is caused
The waste of energy and the increase of system, the increasing of land use, therefore how effectively to turn into efficient using the indirect steam of end effect
The direction of energy-conservation, and improve evaporation service efficiency instantly, reduce the effective way of energy resource consumption, it is current traditional vapo(u)rization system
The technical bottleneck faced.
The content of the invention
The utility model, which provides, a kind of to be untied technical bottleneck that current traditional vapo(u)rization system faces, overcomes prior art not
The liquid evaporation enrichment facility of foot.
A kind of liquid evaporation enrichment facility of the utility model, including：Evaporator, preheater, pipeline, the connection power of connection
The pipeline of steam and the valve being arranged on each pipeline, at least arranged by two evaporator series in described device, evaporator
Condensed water outlet side connects with condensate water pot, and the feed input of preheater connects with waste liquid feed-line, the output of preheater
End is connected with the feed end of evaporator, and following with circulating pump thereon is provided between the feed input and output end of each evaporator
Endless tube road, wherein：The cold fixed gas outlet side of previous stage evaporator is connected with the steam inlet end of rear stage evaporator, and final stage is steamed
The steam output end of hair device connects with preheater steam inlet end, is provided with a jet pump in device, the input of jet pump and
Power steam connects, and injection pump output terminal connects with the steam inlet tube of one-level evaporator, jet pump bypass and final evaporator
Indirect steam output end connection.
Preferably, two-stage preheater, wherein one-level preheater are provided with liquid evaporation enrichment facility of the present utility model
Heating medium input connected with power steam pipe, the feed input of one-level preheater connects with waste liquid feed-line, quilt
The output end of heated material connects with the heated medium input of two level preheater, the heated medium output of two level preheater
End connects with the feed input of final evaporator.
Preferably, liquid evaporation enrichment facility of the present utility model, steamed in material output end and the final stage of two level preheater
The feed input for sending out device is connected with final evaporator feed pipe, and connectivity points are located on the circulating pump on final stage circulation line
Swim, inlet control valve door, the circulation of this grade of evaporator input and output end are provided with described final evaporator feed pipe
Connected between pipeline and previous stage evaporator input and the circulation line of output end with previous stage evaporation feed liquor pipe, and it is described
Inlet control valve, position of its connection are provided with feed pipe respectively positioned at the downstream of this grade of evaporator circulating pump and previous evaporation
Between the upstream of device circulating pump, the circulation line of one-level evaporator is located at the downstream of circulating pump connects dope discharge nozzle with threeway
And dope discharging control valve is provided with dope discharge nozzle.
Preferably, the one-level evaporation feed liquor output end in liquid evaporation enrichment facility of the present utility model also with itself
Secondary steam pipe connects.
Preferably, intelligent DCS control systems are used in liquid evaporation enrichment facility of the present utility model.
As most preferred embodiment, double effect evaporator is provided only with liquid evaporation enrichment facility of the present utility model.
Evaporator at least two-stage series connection arranges that it is carrier to set industrial jet pump, utilizes middle pressure steam in the utility model
For power, the indirect steam of final evaporator is mixed with middle pressure steam, a kind of new pressure and temperature balance is formed, is back to use
In one-level evaporator, so as to realize recycling for steam, to reach the purpose of energy-saving and emission-reduction.By final evaporator during work
Indirect steam outlet is connected with the suction room of steam jet pump, and middle pressure steam is connected with jet chamber, the controlled valve of middle pressure steam
Control, is sprayed with very high speed by nozzle, and under the jet-action of middle pressure steam, suction room forms low pressure, evaporates final stage
The indirect steam of device is inhaled into the chamber, and the steam of two kinds of different pressures and temperature then proceedes to promote, and enters mixing chamber,
In mixing chamber, the middle pressure steam of high-energy and the final evaporator indirect steam of low energy are sufficiently mixed, and energy is exchanged with each other,
Speed is gradually consistent, and static pressure is gone up, and is formed a kind of steam with new temperature and pressure equilibrium relation again, is sent to
In the heat exchange element of one-level evaporator, material is thus formed an efficiency high, the closed loop steam system saved.
In the utility model, one-level evaporator heat exchange is entered from the steam that steam jet pump mixing chamber is sent out except most of
In element, also a small part is entered in one-level preheater.Only because in middle pressure steam（That is power steam）Promotion under,
Although solving the problems, such as the rise of final stage indirect steam energy position using steam jet pump, the increase of quantity of steam is also resulted in simultaneously,
The utility model consumes the preheating of this some vapor using one-level preheater so that and whole vapo(u)rization system heat disengaging is balanced,
Ensure that energy makes full use of.
In order to ensure that vapo(u)rization system forms more stable pressure and temperature difference relation, evaporation technology process is continued,
It is steady to carry out, then need effectively to exclude mixed air in system and some other incoagulable gas.In the utility model
One-level evaporator incoagulable gas outlet and the secondary steam pipe of itself are together with forming certain swabbing action；Final stage is evaporated
The incoagulable gas outlet of device is with two level preheater together with the afterheat steam that fixed gas gas mixes by two level preheater
Cool down and heat pending liquid, incoagulable gas, air etc. are finally arranged to air from one-level preheater.
Evaporator at least two-stage series connection arranges that it is carrier to set industrial jet pump, utilizes middle pressure steam in the utility model
For power, the indirect steam of final evaporator is mixed with middle pressure steam, a kind of new pressure and temperature balance is formed, by end effect
System is back to after steam heating pressurization, so as to realize recycling for steam, overcomes the deficiencies in the prior art, it is energy-saving
Effect clearly, the investment operating cost for the equipment that degraded significantly.
Brief description of the drawings
Accompanying drawing 1 is the schematic diagram of a most preferred embodiment of the present utility model.
In figure：1 is waste liquid feed-line, and 2 be one-level preheater, and 3 be two level preheater feed pipe, and 4 be two level preheater,
5 be secondary evaporimeter feed pipe, and 6 be secondary evaporimeter inlet control valve, and 7 be secondary evaporimeter circulating pump, and 8 be dual evaporation
Device, 9 be secondary evaporimeter condensed water discharge pipe, and 10 be secondary evaporimeter condensate water pot, and 11 be one-level evaporation feed liquor pipe, and 12 are
One-level evaporation feed liquor control valve, 13 be one-level evaporator circulating pump, and 14 be one-level evaporator, and 15 be one-level evaporator condensation water
Discharge pipe, 16 be one-level evaporator condensation water pot, and 17 be one-level evaporator condensation water delivery pipe, and 18 be that one-level evaporator steam enters
Mouthful pipe, 19 be the cold fixed gas discharge pipe of one-level evaporator, and 20 be one-level evaporator secondary steam pipe, and 21 be steam jet pump, 22
It is power steam control valve for secondary evaporimeter secondary steam pipe, 23,24 be power steam delivery pipe, and 25 be that one-level preheater is cold
Condensate discharge pipe, 26 be two level preheater condensed water discharge pipe, and 27 be condensation water collection tank, and 28 be condensed water delivery pump, and 29 are
Condensed water feed-line, 30 be dense waste liquid delivery pipe, and 31 be one-level preheater air intake, and 32 be dope discharging control valve.
Embodiment
Accompanying drawing 1 is a most preferred embodiment being made up of double effect evaporator of the present utility model.Tied below the utility model
Most preferred embodiment is closed to explain in detail.
Arranged in the embodiment of accompanying drawing 1 by two evaporator series, wherein：The heated medium of double effect evaporator 14 and 8
It is each provided with being respectively provided with the circulation line of circulating pump 13 and 7 between input and efferent duct thereon.The condensed water row of each evaporator
Go out end to connect with water tank.Two-stage preheater 2 and 4, the one-level preheater air intake end 31 of one-level preheater 2 are provided with device
Being connected with the pipeline 18 for connecting power steam, the liquid input that is preheated of one-level preheater 2 connects with waste liquid feed-line 1, and one
Heated medium output end the two level preheater feed pipe 3 and the heated medium input of two level preheater 4 of level preheater 2
Connection.The heated medium output end of two level preheater 4 is with the heated medium input of secondary evaporimeter 8 at circulation line
Connected with secondary evaporimeter feed pipe 5, and two level inlet control valve door 6 is provided with secondary evaporimeter feeding pipe 5, and it connects
Logical point is in the upstream of secondary evaporimeter circulating pump 7.The input output end circulation line of secondary evaporimeter 8 and one-level evaporator
Connected between input output end circulation line with one-level evaporation feed liquor pipe 11, the position of connectivity points is located at the circulation of one-level evaporator
The upstream of pump 13, and one-level inlet control valve door 12 is provided with one-level evaporation feed liquor pipe 11.The heating of one-level evaporator 14
Medium output end connects with the heating medium input pipeline 20 of secondary evaporimeter 8.The heating medium output of secondary evaporimeter 8
Medium input pipeline 31 is heated with two level preheater 4 and is connected in end.There is a jet pump 21 in the present embodiment, jet pump 21
Shunt valve 22 connects with the indirect steam output end of secondary evaporimeter 8；The input of jet pump 21 pipeline 24 and power steam
Source connects；The output end of jet pump 21 is connected by pipe 18 with the heating medium input of one-level evaporator.One-level evaporator 14
Circulation line on connected at the downstream of one-level evaporator circulating pump 13 with three general dope discharge nozzles 30, and go out in dope
Dope discharging control valve 32 is provided with expects pipe 30.In the present embodiment the heating medium output end of one-level evaporator 14 also with itself
Secondary steam pipe connection, certain swabbing action can be formed at work using this structure.
In the utility model TVR vapo(u)rization systems and device, waste liquid is sent to one-level preheater by waste liquid feed-line 1
In 2, and then two level preheater 4, then the pending solution by secondary evaporimeter are fed to by two level preheater feed pipe 3
Feed pipe 5 enters secondary evaporimeter 8, opens secondary evaporimeter circulating pump 7, and waste liquid is sent to two level by top through circulation pipe and steamed
Device 8 is sent out, and is evenly distributed on each heat exchange element surface of secondary evaporimeter 8, while waste liquid is entered by one-level evaporation feed liquor pipe 11
Enter the liquid level for one-level evaporator 14, being loaded into and specifying, so load preliminary pending waste liquid, charging in the entire system
Process terminates.
Start one-level evaporator circulating pump 13, waste liquid is sent to one-level evaporator 14 through circulation pipe by top, and uniformly divides
Cloth is on each heat exchange element surface of one-level evaporator 14.It is pico- to open middle pressure steam control valve 23, and gradually increase valve opening,
Now because the waste liquid temperature in secondary evaporimeter 8 is very low, it is far from reaching boiling point, therefore temporarily without the production of indirect steam
It is raw, so, the incoagulable gas such as air in secondary evaporimeter is taken away by the suction of steam jet pump 21, forms certain vacuum
Degree.Middle pressure steam depressurizes after steam jet pump, has respectively entered in one-level preheater and one-level evaporator.
The waste liquid of one-level evaporator 14 is slowly heated by steam, indirect steam is generated after reaching boiling point, with heating
Continue, the yield of the indirect steam of one-level evaporator 14 constantly adds increase, is entered via one-level evaporator secondary steam pipe 20
In the heat exchange element of secondary evaporimeter 8, heat exchange is fully carried out with waste liquid, the waste liquid in secondary evaporimeter 8 is constantly heated, temperature
Degree constantly rise, pressure gradually increase, and are finally reached boiling point, produce indirect steam, entered by secondary evaporimeter secondary steam pipe 22
Enter the suction room to steam jet pump 21, the steam of two kinds of different pressures and temperature then proceedes to promote, and enters steam injection
The mixing chamber of pump 21, in mixing chamber, the middle pressure steam of high-energy and the secondary evaporimeter indirect steam of low energy are sufficiently mixed,
Energy is exchanged with each other, and speed is gradually consistent, and static pressure is gone up, and formed a kind of has new temperature and pressure equilibrium relation again
Steam, be sent to through one-level evaporator steam inlet tube 18 in the heat exchange element of one-level evaporator 14.In secondary evaporimeter
The mixed gas such as incoagulable gas, air, afterheat steam are entered under the driving of system pressure in two level preheater 4, mixing
Steam in device produces heat exchange with used heat and is cooled to condensed water, and incoagulable gas and air then arrange air.It is so whole
System is just normal to be started, and is controlled by DCS system, is automatically replenished feed liquid, evaporated in lasting, even running.
Steam is entered after the heat exchange element of one-level evaporator 14 and carries out sufficient heat exchange with waste liquid, and contribution steam is dived
Heat two is undergone phase transition, and forms condensed water, one-level evaporator condensation water pot 16 is entered by one-level evaporator condensation water discharge pipe 15
In.
Steam is entered after the heat exchange element of secondary evaporimeter 8 and carries out sufficient heat exchange with waste liquid, and contribution steam is dived
Heat two is undergone phase transition, and forms condensed water, secondary evaporimeter condensate water pot 10 is entered by secondary evaporimeter condensed water discharge pipe 9
In.
Steam enters after one-level preheater 2 and carries out sufficient heat exchange with waste liquid, and phase occurs for contribution steam latent heat two
Become, form condensed water, entered by one-level preheater condensed water discharge pipe 25 in secondary evaporimeter condensate water pot 10.
Condensed water, one-level evaporator condensation water, the secondary evaporimeter condensed water of two level preheater 4 are finally pooled to condensed water
In collecting tank 27, other workshop sections are delivered to when hot water uses by the condensed water feed-line 29 of condensed water delivery pump 28.
Waste liquid has and finally concentrated through one-level evaporator, reached needed for harmless treatment through secondary evaporimeter initial concentration again
Sent to after the concentration wanted by dope discharging control valve 32 through dense waste liquid delivery pipe 30 and do harmless treatment and recovery useful resources.Newly
Feed liquid enter system by DCS controls, progress continuous and stable production.Tthe utility model system itself zero-emission, efficient resource obtain
To recycle.
It the above is only one embodiment of the present utility model, multistage particularly as that can be set according to the requirement of technique
Evaporator, its specific set-up mode can refer to foregoing embodiment.
Claims (6)
1. a kind of liquid evaporation enrichment facility, including：Evaporator, preheater, the pipeline of connection, connect power steam pipeline and
The valve being arranged on each pipeline, it is characterised in that at least arranged in device by two evaporator series, the condensed water of evaporator
Outlet side connects with condensate water pot, and the feed input of preheater connects with waste liquid feed-line, the output end of preheater and steaming
The feed end connection of device is sent out, the circulation pipe for carrying circulating pump thereon is provided between the feed input and output end of each evaporator
Road, wherein：The cold fixed gas outlet side of previous stage evaporator connects with the steam inlet end of rear stage evaporator, final evaporator
Steam output end connected with preheater steam inlet end, a jet pump, the input and power of jet pump are provided with device
Vapor communication, injection pump output terminal connect with the steam inlet tube of one-level evaporator, jet pump bypass and the two of final evaporator
Secondary steam output end connection.
2. liquid evaporation enrichment facility according to claim 1, it is characterised in that two-stage preheater is provided with device, its
The heating medium input of middle one-level preheater connects with power steam pipe, and feed input and the waste liquid of one-level preheater convey
Pipeline connection, the output end of heated material connect with the heated medium input of two level preheater, the quilt of two level preheater
Heating medium output end connects with the feed input of final evaporator.
3. liquid evaporation enrichment facility according to claim 2, it is characterised in that the material output end of two level preheater with
The feed input of final evaporator is connected with final evaporator feed pipe, and connectivity points are located at the circulation on final stage circulation line
Pump upstream, is provided with inlet control valve door on described final evaporator feed pipe, this grade of evaporator input and output end
Connected between circulation line and previous stage evaporator input and the circulation line of output end with previous stage evaporation feed liquor pipe, and institute
Inlet control valve, position of its connection are provided with the feed pipe stated respectively positioned at the downstream of this grade of evaporator circulating pump and previous
Between the upstream of evaporator circulating pump, the circulation line of one-level evaporator is located at the downstream of circulating pump to be gone out with threeway connection dope
Expects pipe and dope discharging control valve is provided with dope discharge nozzle.
4. according to the liquid evaporation enrichment facility described in claim 1 or 2 or 3, it is characterised in that the one-level in the utility model
Evaporation feed liquor output end also connects with the secondary steam pipe of itself.
5. liquid evaporation enrichment facility according to claim 4, it is characterised in that using intelligent DCS controls system in device
System.
6. liquid evaporation enrichment facility according to claim 5, it is characterised in that double effect evaporator is provided with device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720564503.0U CN206730539U (en) | 2017-05-20 | 2017-05-20 | A kind of liquid evaporation enrichment facility |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720564503.0U CN206730539U (en) | 2017-05-20 | 2017-05-20 | A kind of liquid evaporation enrichment facility |
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| Publication Number | Publication Date |
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| CN206730539U true CN206730539U (en) | 2017-12-12 |
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| CN201720564503.0U Active CN206730539U (en) | 2017-05-20 | 2017-05-20 | A kind of liquid evaporation enrichment facility |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107019928A (en) * | 2017-05-20 | 2017-08-08 | 兰州节能环保工程有限责任公司 | A kind of liquid evaporation enrichment facility |
| CN108211389A (en) * | 2018-03-22 | 2018-06-29 | 兰州节能环保工程有限责任公司 | A kind of vaporising device and setting method with self-cleaning function |
-
2017
- 2017-05-20 CN CN201720564503.0U patent/CN206730539U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107019928A (en) * | 2017-05-20 | 2017-08-08 | 兰州节能环保工程有限责任公司 | A kind of liquid evaporation enrichment facility |
| CN108211389A (en) * | 2018-03-22 | 2018-06-29 | 兰州节能环保工程有限责任公司 | A kind of vaporising device and setting method with self-cleaning function |
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