CN106630338A - Treatment method and treatment apparatus for organic wastewater - Google Patents
Treatment method and treatment apparatus for organic wastewater Download PDFInfo
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- CN106630338A CN106630338A CN201510730154.0A CN201510730154A CN106630338A CN 106630338 A CN106630338 A CN 106630338A CN 201510730154 A CN201510730154 A CN 201510730154A CN 106630338 A CN106630338 A CN 106630338A
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Abstract
The present invention provides a treatment method and a treatment apparatus for organic wastewater. The treatment apparatus comprises a wastewater preheater, an evaporator, an ejector, a fouling device, a steam compressor and a condensation water collection separator. The present invention further provides a method for treating organic wastewater by using the treatment apparatus. According to the present invention, the treatment method and the treatment apparatus have advantages of safety, reliability, simple equipment, low operation cost, energy saving, significant effect, and the like.
Description
Technical field
The present invention relates to a kind for the treatment of method and apparatus of organic wastewater of environmental protection and field of energy-saving technology, the method and apparatus for specifically processing oil-refining chemical pbz polymer organic compound waste water.
Background technology
Organic wastewater is mainly derived from the fields such as chemical industry, road deicing, food processing, also including dyeing waste water, oil exploitation and processing waste water, paper waste and pesticide industry waste water etc..The total amount of high salt organic waste water is huge and increases year by year.If do not processed it before discharge, the soluble inorganic salt of Coal Gas Washing Cycling Water and the toxic organic compound of difficult degradation can cause serious environmental pollution, and soil and surface water, underground water are damaged.Therefore, in today of water scarcity, it is very necessary to research and develop effective high salt Technologies for Organic Wastewater Treatment.At present, the treatment technology of high salt organic waste water is more, mainly there is physical-chemical process, bioanalysis and combinations thereof technique.
In recent years, foreign countries propose and reclaim waste water with the process of function of mechanical steam recompression evaporation technique.Mechanical vapor recompression technology is a Technolqgy for Energy Economizing for reducing energy demand to external world.Its energy-saving principle is：By the indirect steam produced in system through compressor compresses so as to which pressure and temperature rises, enthalpy increases, and instead of the external heat source that must be adopted in original system, and the latent heat of indirect steam is fully used, so as to reach the purpose of technical process energy-conservation.
At present, function of mechanical steam recompression system mainly has application in terms of the waste water recycling devices such as saline sewage, oil field reinjection water, pharmacy waste water.Application is yet there are no in terms of pbz polymer organic compound waste water recycling device.Due to the macromolecule organic containing easy coking, fouling in organic wastewater, in the evaporimeter of function of mechanical steam recompression system, with the continuous evaporation of moisture content, organic wastewater is through concentration, boiling point will increase, macromolecule organic will coking, fouling in dope, and be attached on the heat-transfer surface of evaporimeter, evaporator heat exchange efficiency is had a strong impact on, and then the blocking of evaporimeter, pipeline can be caused.
Patent CN102641603A and CN102553274A individually disclose the plate-type evaporator with Mechanical Vapor Compression and tubular evaparator device, at 60 DEG C or so, the vacuum in patent CN102553274A in evaporimeter is 0.05～0.098MPa to operation temperature general control in patent CN102641603A in plate-type evaporator.Two kinds of low temperature are evaporated in vacuo mode, reduce the boiling point of material, and the method is suitable for the evaporation and concentration of heat sensitive material and easy fouling material.
Patent CN104001339A discloses a kind of MVR plate evaporations system, evaporates the indirect steam for producing temperature and pressure Jing after compressor compression and improves, and improves the grade of steam so that low temperature position steam can be reused.Multiple-effect evaporation portion can be set in the method vapo(u)rization system so that MVR plate evaporation system applications are wider, but with the increase of evaporation effect number in vapo(u)rization system, the energy efficiency coefficient of Mechanical Vapor Compression will be reduced so that the energy consumption of vapo(u)rization system increases.
CN202315333U, CN203170039U disclose a kind of steam mechanical Compression Evaporation equipment, the utility model is effectively utilized the indirect steam of evaporimeter generation, indirect steam latent heat after pressure-raising increases, using the steam latent heat heated waste water after pressure-raising, reach the purpose for reclaiming water resource, the method has obvious energy-saving effect, but equipment evaporimeter in application process has fouling.
The content of the invention
It is an object of the invention to provide a kind for the treatment of method and apparatus of organic wastewater, method of wastewater treatment of the present invention and device have the advantages that safe and reliable, equipment is simple, operating cost is low, energy-saving effect is obvious.
The invention provides a kind of processing meanss of organic wastewater, described device includes waste water preheater, evaporimeter, injector, fouling device, vapour compression machine and condensate water collecting separator；Wherein wastewater feed pipeline Jing waste water preheater is connected with the waterwater entrance of evaporimeter，Steam (vapor) outlet at the top of evaporimeter is connected with the gas phase entrance of injector，The condensation water outlet Jing pipelines of evaporimeter are connected with condensate water collecting separator，The concentrate floss hole Jing pipelines of base of evaporator are connected with the entrance of fouling device，Steam (vapor) outlet at the top of fouling device is connected with the heat source stream entrance of evaporimeter，The condensation water outlet Jing pipelines of fouling device are connected with condensate water collecting separator，The gaseous phase outlet of condensate water collecting separator is connected with the entrance of vapour compression machine，The outlet of vapour compression machine is connected with the heat source stream entrance of fouling device，The liquid discharge outlet of condensate water collecting separator point two-way，Wherein all the way Jing pipelines are connected with waste water preheater，Another road is connected with the liquid phase entrance of injector，The condensate water collecting separator that is exported to of injector connects，The concentrate floss hole Jing pipelines of fouling device are connected with the waterwater entrance of evaporimeter，Fouling device bottom is provided with dirt floss hole.
In the processing meanss of organic wastewater of the present invention, supplementary steam pipe line is set in the outlet of the vapour compression machine and the heat source stream entrance connecting pipeline of fouling device.
In the processing meanss of organic wastewater of the present invention, the waste water preheater can adopt shell-and-tube heat exchanger, heat-pipe heat exchanger, plate type heat exchanger or lamella heat exchanger, it is preferred to use plate type heat exchanger.
In the processing meanss of organic wastewater of the present invention, described injector is hydraulic ejector, and the gas phase inlet vacuum degree of injector is 10 ~ 40kPa, and injector outlet gas-liquid mixture pressure is 100 ~ 120kPa (A).
In the processing meanss of organic wastewater of the present invention, described evaporimeter can adopt any one in climbing film evaporator, falling film evaporator, horizontal tube evaporator and plate-type evaporator.
In the processing meanss of organic wastewater of the present invention, described falling film evaporator includes：Housing, tube sheet, evaporation tube, fluid Supplying apparatus, the tube sheet is arranged on the top of the housing；The evaporation tube is multiple, and multiple evaporation tubes are vertically arranged in the housing, and the upper end of the evaporation tube passes through the tube sheet；The upper end of the evaporation tube is provided with guiding device；The fluid Supplying apparatus include lead channel and point feed pipe, the lead channel is vertically arranged in the outer wall top of the housing, and around the whole housing, the lead channel is uniformly provided with multiple points of charging apertures, described point of charging aperture is arranged on the upper side wall of the lead channel, the lower end of described point of feed pipe passes vertically through point charging aperture and stretches in the lead channel, and the lower end of described point of feed pipe is near the bottom of the lead channel；The housing is provided with multiple overflow ducts connected with the lead channel.
Wherein, described point of feed pipe is removably mounted in the lead channel.
Wherein, multiple impingement baffles are provided with the lead channel, multiple impingement baffles are evenly arranged in the bottom of the lead channel.
Wherein, the impingement baffle is provided with via.
Wherein, the height of the impingement baffle and the depth ratio of the lead channel are 1/3～3/5.
Wherein, the inwall of the housing is provided with an overflow baffle, and the overflow baffle is fixed on the inwall of the housing, and the overflow baffle forms cloth liquid passage with the inner walls and tube sheet.
Wherein, the overflow baffle is cylinder, and section is in class inverted " L " font.
Wherein, the evaporation tube is evenly arranged in the housing.
In the processing meanss of organic wastewater of the present invention, described fouling device is jacket type structure, heated by heat source stream in chuck, the heat source stream is the steam steam again Jing after mechanical compress that evaporator evaporation is produced, and fouling device inner homogeneous arrange 2～6 scraping blades, are preferably provided with 2～4 scraping blades, the scraping blade is driven in fouling device internal rotating by motor, in process of production, scraping blade continuously rotates, and rotary speed is 200r/min～360r/min.
In the processing meanss of organic wastewater of the present invention, described vapour compression machine can adopt the one kind in centrifugal compressor, screw compressor, reciprocating compressor, centrifugal high pressure fan；The compression ratio of the vapour compression machine is 1.3～2.0, preferably 1.4～1.7.
The present invention also provides a kind of processing method of organic wastewater, and using said apparatus of the present invention, methods described includes：
Using waste water preheater, it is used to process raw material waste water and condensate, and raw material waste water and condensate are exchanged heat in waste water preheater, the condensate of the raw material waste water after being preheated after process and condensation；
Using evaporimeter, it is used to process the raw material waste water come after waste water preheater preheating of hanging oneself, and the 1st stream, the 2nd stream of liquid phase and the condensate of gas phase are obtained after process；
Using injector, it is used to process the 1st stream of flash-pot and the condensate of the saturation temperature from condensate water collecting separator, and the 3rd stream of gas-liquid mixed phase is obtained after process；
Using condensate water collecting separator, it is used to receive the 3rd stream of the condensate for carrying out flash-pot, the condensate of fouling device and injector, the 4th stream of gas phase and the condensate of saturation temperature are obtained after process, the condensate of the saturation temperature is divided into two-way, waste water preheater is wherein entered all the way, and another road enters injector；
Using vapour compression machine, it is used to process the 4th stream from condensate water collecting separator, and the 5th stream of gas phase is obtained after process, and the 5th stream enters fouling device as the heat source stream of fouling device；
Using fouling device, it is used to process the 2nd stream of flash-pot, and the 6th stream, the 7th stream of liquid phase, dirt and the condensate of gas phase are obtained after process；6th stream enters evaporimeter as the heat source stream of evaporimeter, and the 7th stream enters evaporimeter after mixing with the raw material waste water after preheating.
In the inventive method, raw material waste water is mixed in evaporimeter in waste water preheater by exchanging heat to the concentrate discharged with fouling device close to after saturation temperature with condensate, it is evaporated in evaporimeter, after the steam for obtaining is compressed again by vapour compression machine, the latent heat of steam is improved, with compressed steam as fouling device evaporation thermal source.
In the inventive method, raw material waste water is in waste water preheater by exchanging heat to 95 DEG C～102 DEG C with condensate, it is preferred that 98 DEG C～100 DEG C, then it is mixed in evaporimeter with the concentrate of fouling device, organic concentration is as unsaturated concentration with the mixed liquor for ensureing to be evaporated in evaporimeter.
In the inventive method, logarithm heat transfer temperature difference in the evaporimeter between steam and waste water is 3 DEG C～10 DEG C, it is preferred that 4 DEG C～8 DEG C, meanwhile, the vaporization rate of waste water evaporation is 5%～50%, preferably 10%～40% in the evaporimeter, it is close saturation but unsaturated concentration to make to be emitted into organic concentration in the liquid of fouling device after evaporation and concentration, meanwhile, evaporation in vacuo degree is 10 ~ 40kPa in evaporimeter, so as to more effectively avoid organic matter that coking is produced in evaporimeter.
In the inventive method, the operation temperature of the fouling device be the boiling temperature for concentrating waste water to higher than 1 DEG C～5 DEG C of boiling temperature, operating pressure is normal pressure.
In the inventive method, the operation temperature of described condensate water collecting separator is 100 DEG C～105 DEG C, and operating pressure is the saturated vapor pressure of condensate.
In the inventive method, when device goes into operation, need to be gone into operation thermal source as device with the extraneous steam of device.Steam can be by supplementary steam pipe line introducing device；If device is in running, when the steam of the generation of the processing meanss can not maintain device heat consumption quantity of steam, steam can be introduced by steam pipe line is supplemented；If device is in running, when the steam that wastewater treatment equipment is produced is more than device heat consumption quantity of steam is maintained, discharge steam can be by supplementary steam pipe line discharger.
In the inventive method, described falling film evaporator includes：Housing, tube sheet, evaporation tube, fluid Supplying apparatus, the tube sheet is arranged on the top of the housing；The evaporation tube is multiple, and multiple evaporation tubes are vertically arranged in the housing, and the upper end of the evaporation tube passes through the tube sheet；The upper end of the evaporation tube is provided with guiding device；The fluid Supplying apparatus include lead channel and point feed pipe, the lead channel is vertically arranged in the outer wall top of the housing, and around the whole housing, the lead channel is uniformly provided with multiple points of charging apertures, described point of charging aperture is arranged on the upper side wall of the lead channel, the lower end of described point of feed pipe passes vertically through point charging aperture and stretches in the lead channel, and the lower end of described point of feed pipe is near the bottom of the lead channel；The housing is provided with multiple overflow ducts connected with the lead channel.
Wherein, described point of feed pipe is removably mounted in the lead channel.
Wherein, multiple impingement baffles are provided with the lead channel, multiple impingement baffles are evenly arranged in the bottom of the lead channel.
Wherein, the impingement baffle is provided with via.
Wherein, the height of the impingement baffle and the depth ratio of the lead channel are 1/3～3/5.
Wherein, the inwall of the housing is provided with an overflow baffle, and the overflow baffle is fixed on the inwall of the housing, and the overflow baffle forms cloth liquid passage with the inner walls and tube sheet.
Wherein, the overflow baffle is cylinder, and section is in class inverted " L " font.
Wherein, the evaporation tube is evenly arranged in the housing.
Other technologies in the inventive method, the content as known to water pump, heat heat exchange, condensate water collecting etc. are those skilled in the art.
Compared with prior art, the treating method and apparatus of organic wastewater of the present invention have the advantage that：
1st, in the treating method and apparatus of organic wastewater of the present invention, waste water is concentrated by evaporation to reclaim and is reclaimed using steam mechanical recompression forced circulation technique, is capable of achieving 85%～99% water resource and is recycled.
2nd, in the treating method and apparatus of organic wastewater of the present invention, vapor recompression system mainly passes through Secondary-steam heating waste water in the present invention, allow wastewater temperature to reach, be even above the temperature of its easy fouling, to realize reaching the purpose of the organic matter in removing waste water, and the present invention increased fouling device after forced circulation pump, useless Organic substance in water is made in the inner surface fouling of fouling device and is removed, it is to avoid recycling waste water fouling in evaporimeter so that device long period steady running.
3rd, in the treating method and apparatus of organic wastewater of the present invention, charging waste water and recycling waste water are mixed into into evaporimeter, so as to reach the purpose of dilution recycling waste water, simultaneously, vapo(u)rization system arranges the steam that injector is drawn evaporator evaporation, so that evaporimeter can run under vacuum, so as to more effectively reduce the risk of fouling of evaporator.
4th, in the treating method and apparatus of organic wastewater of the present invention, steam mechanical recompression forced circulation technique has been effectively combined the advantage of the economic benefits and social benefits steam mechanical compression process of forced circulation vapor recompression technique and routine, fouling device is set, realize the conversion of fouling locus, both the purpose of energy-conservation had been reached, also fouling of evaporator problem can be effectively prevented, it is ensured that the high efficient heat exchanging effect of evaporimeter, it is to avoid the problems such as equipment scaling, coking and blocking.
5th, it is simple and compact for structure by using the falling film evaporator with lateral charging in the treating method and apparatus of organic wastewater of the present invention, effectively reduce the height of equipment；Liquid flow flux is big, operation, easy to maintenance；Using the equipment liquid distribution rate it is high, cloth film is uniform, be not easily blocked, be readily cleaned, and can increase the arrangement quantity of evaporation tube, increases the heat exchange area of evaporimeter.
6th, the treating method and apparatus of organic wastewater of the present invention have that safe and reliable, equipment is simple, it is low to invest, the features such as.
Description of the drawings
Fig. 1 is the schematic flow sheet of the treating method and apparatus of organic wastewater of the present invention.
Fig. 2 is the half-sectional structure front view of falling film evaporator used by the present invention.
Fig. 3 is the top view that the part of falling film evaporator used by the present invention is cutd open.
Fig. 4 is the impingement baffle schematic diagram of falling film evaporator used by the present invention.
Specific embodiment
The concrete condition of the present invention is further illustrated below by specific embodiment, but is not limited to following embodiments.
The invention provides a kind of processing meanss of organic wastewater, described device includes waste water preheater 2, evaporimeter 6, injector 8, fouling device 14, vapour compression machine 12 and condensate water collecting separator 10；Wherein wastewater feed pipeline Jing waste water preheater 2 is connected with the waterwater entrance of evaporimeter 6，The steam (vapor) outlet at the top of evaporimeter 6 is connected with the gas phase entrance of injector 7，The condensation water outlet Jing pipelines of evaporimeter 6 are connected with condensate water collecting separator 10，The concentrate floss hole Jing pipelines of the bottom of evaporimeter 6 are connected with the entrance of fouling device 14，The steam (vapor) outlet at the top of fouling device 14 is connected with the heat source stream entrance of evaporimeter 6，The condensation water outlet Jing pipelines of fouling device 14 are connected with condensate water collecting separator 10，The gaseous phase outlet of condensate water collecting separator 10 is connected with the entrance of vapour compression machine 12，The outlet of vapour compression machine 12 is connected with the heat source stream entrance of fouling device 14，The liquid discharge outlet of condensate water collecting separator 10 point two-way，Wherein all the way Jing pipelines are connected with waste water preheater 2，Another road is connected with the liquid phase entrance of injector 8，The condensate water collecting separator 10 that is exported to of injector 8 connects，The concentrate floss hole Jing pipelines of fouling device 14 are connected with the waterwater entrance of evaporimeter 6，The bottom of fouling device 14 is provided with dirt floss hole.
The present invention also provides a kind of processing method of organic wastewater, and using said apparatus of the present invention, methods described includes：
Using waste water preheater 2, it is used to process raw material waste water 1 and condensate 28, and raw material waste water 1 and condensate 28 are exchanged heat in waste water preheater 2, the condensate 29 of the raw material waste water 3 after being preheated after process and condensation；
Using evaporimeter 6, it is used to process the raw material waste water 3 come after waste water preheater preheating of hanging oneself, and the 2nd stream 15 and condensate 21 of the 1st stream 7, liquid phase of gas phase are obtained after process；
Using injector 8, it is used to process the condensate 27 of the 1st stream 7 of flash-pot and the saturation temperature from condensate water collecting separator 10, and the 3rd stream 9 of gas-liquid mixed phase is obtained after process；
Using condensate water collecting separator 10, it is used to receive the 3rd stream 9 of the condensate 21 of flash-pot, the condensate 24 of fouling device and injector, the 4th stream 11 of gas phase and the condensate 25 of saturation temperature are obtained after process, 25 points of two-way of condensate of the saturation temperature, wherein 28 waste water preheater 2 is entered all the way, another road 27 enters injector 8；
Using vapour compression machine 12, it is used to process the 4th stream 11 from condensate water collecting separator 10, and the 5th stream 13 of gas phase is obtained after process, and the 5th stream 13 enters fouling device 14 as the heat source stream of fouling device 14；
Using fouling device 14, it is used to process the 2nd stream 15 of flash-pot 6, and the 7th stream 4, dirt 18 and the condensate 24 of the 6th stream 16, liquid phase of gas phase are obtained after process；6th stream 16 enters evaporimeter 6 as the heat source stream of evaporimeter 6, and the 7th stream 4 enters evaporimeter 6 after mixing with the raw material waste water 3 after preheating.
In the processing method of organic wastewater of the present invention, raw material waste water 1 is preheated to close to saturation temperature in waste water preheater 2 with condensate 28, then the concentrate 4 discharged with fouling device 14 mixes, mixed material 5 is entered in evaporimeter 6, it is evaporated in evaporimeter 6, the evaporated vapor 7 that evaporation is obtained enters injector, realize that pressure energy is converted into kinetic energy and is changed into swiftly flowing stream in injector 8 from the supercharging condensate 27 from condensate water collecting separator 10, so as to realize that the gas phase entrance in injector 8 forms vacuum, the purpose for being drawn steam 7 is reached.The gas-liquid mixture 9 excluded by injector 8 enters condensate water collecting separator 10, the condensate 24 of condensate 21, fouling device with evaporimeter mixes, separates, isolated steam 11 enters vapour compression machine 12, the steam 13 obtained Jing after vapour compression machine 12 compresses enters fouling device as the heat source stream of fouling device, isolated 25 points of two-way of condensate, wherein 28 it is pumped up into waste water preheater 2 all the way, exchange heat with raw material waste water 1, realize heat recovery, the recoverable of condensate 29 of cooling, another road 27 enters injector 8.The Jing pumps of concentrate 15 for obtaining of evaporimeter 6 are squeezed in fouling device 14, concentrate 15 is evaporated again and fouling in fouling device 14, the steam 16 produced in fouling device 14 enters evaporimeter 6 as the heat source stream of evaporimeter 6, become condensate 21 after condensation, condensate 21 is entered in condensate water collecting separator 10.The dirt Jing scraping blades of attachment are removed in the wall of fouling device 13, and the dirt 18 for obtaining is discharged by the dirt floss hole of fouling device 14, through being pumped to incinerator as fuel or going the device of other harmless treatments to carry out subsequent treatment.Concentrate 4 after fouling device 14 further concentration is mixed into evaporimeter 6 with the raw material waste water 3 after preheating.
As shown in Figures 2 and 3, the falling film evaporator of lateral charging of the invention, including：Housing 11, tube sheet 1, evaporation tube 3, fluid Supplying apparatus 20.Housing 11 is cylindrical shape, and tube sheet 1 is arranged on the top of housing 11, and the upper surface of tube sheet 1 constitutes cloth film room with the part on the top of housing 11.Evaporation tube 3 is multiple, and multiple evaporation tubes 3 are vertically arranged in housing 11, and preferred evaporation tube is evenly distributed.The upper end of evaporation tube 3 passes through tube sheet 1, arranges multiple evaporation pores on tube sheet 1, and the upper end of evaporation tube 3 is stretched out from evaporation pore, and the method such as connects and be tightly connected with tube sheet 1 using welding or rising.Guiding device 2 is provided with the upper end of evaporation tube 3.Fluid Supplying apparatus 20 include lead channel 6 and multiple points of feed pipes 7, in the present embodiment, lead channel 6 is the toroidal shell groove of an interior side opening, the internal diameter of toroidal shell groove is identical with the external diameter of housing 11, lead channel 6 is vertically arranged in the outer wall top of housing 11 by welding, and around whole housing 11, the side of the opening of lead channel 6 is using the lateral wall of housing 11 as shared side wall.Lead channel 6 is uniformly provided with multiple points of charging apertures 13, and the quantity of point charging aperture 13 is identical with point feed pipe 7, and for installing a point feed pipe 7, specific to the present embodiment, the quantity of point charging aperture is 8.Charging aperture 13 is divided to be arranged on the upper side wall of lead channel 6, the lower end of point feed pipe 7 passes vertically through point charging aperture 13 and stretches in lead channel 6, and the lower end outlet of point feed pipe 7 is near the bottom of lead channel 6.Divide feed pipe 7 to be used to be connected with charging house steward 10, material is provided in feed well 6 by a point feed pipe 7 from charging house steward 10.Housing 11 is provided with multiple overflow ducts 5 connected with lead channel 6, and overflow ducts 5 are the crest of weir near the upper side wall of lead channel 6, and conventional structure has rectangular weir, V-type weir and round bottom rectangular weir.
Further, feed pipe 7 is divided to be removably mounted in lead channel 6 by flange.Specifically, one ring flange 71 of lateral wall welded and installed of feed pipe 7, ring flange 71 is divided to link together by bolt assembly with the upper side wall of lead channel 6, can be dismantled as needed.
Further, multiple impingement baffles 8 are provided with lead channel 6, multiple impingement baffles 8 are evenly arranged in the bottom of lead channel 6, in the present embodiment, the quantity of impingement baffle 8 is 16.Preferably, lower end outlet of the upper edge of impingement baffle 8 higher than point feed pipe 7.With reference to shown in Fig. 4, impingement baffle 8 is provided with via 81, and the section of via 81 is preferably circular, its a diameter of 5-30 millimeter, preferred 10-20 millimeters.Preferably, the height of impingement baffle 8 and the depth ratio of lead channel 6 are 1/3 ~ 3/5, and such as height of impingement baffle 8 is 1/3,3/7,1/2 and the 3/5 of feed liquor groove depth 6.
Further, the inwall of housing 11 is provided with an overflow baffle 4, and overflow baffle 4 is cylinder, and the external diameter of overflow baffle 4 is less than the internal diameter of housing 11.Overflow baffle 4 is fixed on the inwall of housing 11, and the lower edge of overflow baffle 4 by multiple rectangle gripper shoes 12 higher than the upper surface of tube sheet 1, and overflow baffle 4 forms cloth liquid passage with the inwall of housing 11 and tube sheet 1.The cross-sectional width of cloth liquid passage is less than the inwall of housing 11 and the minimum range of evaporation tube 3.
Embodiment 1
Using the device described in Fig. 1, the falling film evaporator is using the device described in Fig. 2, organic wastewater used is the fine production waste water of propylene, kelvin nitrogen content is 4050mg/L in the fine waste water of propylene, and waste water boiling point is 100 DEG C, when waste water evaporates more than the moisture content of 80wt%, raw material wastewater treatment capacity is 15t/h, normal temperature waste water is preheated to 99 DEG C through preheater 2, and the concentrate with 104 DEG C mixes, in evaporimeter 6.Raw material waste water is 3 with concentrate wastewater flow ratio:1～1.5.Evaporating temperature of the waste water in evaporimeter 6 is 100 DEG C, and injector gas phase steam inlet vacuum degree is 15 kPa, and the compression ratio of vapour compression machine 12 is 1.5.Evaporating temperature in fouling device 14 is 104 DEG C, and 2 scraping blades are arranged in fouling device 14, and scraping blade rotary speed is 360r/min, and dirt is arranged by dirt pump is continuously outer.Condensate temperature Jing after heat recovery is 45 DEG C or so, and condensate-water polishing amount is 11t/h.
Claims (21)
1. a kind of processing meanss of organic wastewater, described device includes waste water preheater, evaporimeter, injector, fouling device, vapour compression machine and condensate water collecting separator；Wherein wastewater feed pipeline Jing waste water preheater is connected with the waterwater entrance of evaporimeter，Steam (vapor) outlet at the top of evaporimeter is connected with the gas phase entrance of injector，The condensation water outlet Jing pipelines of evaporimeter are connected with condensate water collecting separator，The concentrate floss hole Jing pipelines of base of evaporator are connected with the entrance of fouling device，Steam (vapor) outlet at the top of fouling device is connected with the heat source stream entrance of evaporimeter，The condensation water outlet Jing pipelines of fouling device are connected with condensate water collecting separator，The gaseous phase outlet of condensate water collecting separator is connected with the entrance of vapour compression machine，The outlet of vapour compression machine is connected with the heat source stream entrance of fouling device，The liquid discharge outlet of condensate water collecting separator point two-way，Wherein all the way Jing pipelines are connected with waste water preheater，Another road is connected with the liquid phase entrance of injector，The condensate water collecting separator that is exported to of injector connects，The concentrate floss hole Jing pipelines of fouling device are connected with the waterwater entrance of evaporimeter，Fouling device bottom is provided with dirt floss hole.
2. according to the device described in claim 1, it is characterised in that：Supplementary steam pipe line is set in steam (vapor) outlet at the top of the fouling device and the heat source stream entrance connecting pipeline of evaporimeter.
3. according to the device described in claim 1, it is characterised in that：The waste water preheater is using any one in shell-and-tube heat exchanger, heat-pipe heat exchanger, plate type heat exchanger or lamella heat exchanger.
4. according to the device described in claim 1, it is characterised in that：The waste water preheater adopts plate type heat exchanger.
5. according to the device described in claim 1, it is characterised in that：Described evaporimeter is using any one in climbing film evaporator, falling film evaporator, horizontal tube evaporator and plate-type evaporator.
6. according to the device described in claim 1, it is characterised in that：Described falling film evaporator includes：Housing, tube sheet, evaporation tube, fluid Supplying apparatus, the tube sheet is arranged on the top of the housing；The evaporation tube is multiple, and multiple evaporation tubes are vertically arranged in the housing, and the upper end of the evaporation tube passes through the tube sheet；The upper end of the evaporation tube is provided with guiding device；The fluid Supplying apparatus include lead channel and point feed pipe, the lead channel is vertically arranged in the outer wall top of the housing, and around the whole housing, the lead channel is uniformly provided with multiple points of charging apertures, described point of charging aperture is arranged on the upper side wall of the lead channel, the lower end of described point of feed pipe passes vertically through point charging aperture and stretches in the lead channel, and the lower end of described point of feed pipe is near the bottom of the lead channel；The housing is provided with multiple overflow ducts connected with the lead channel.
7. according to the device described in claim 1, it is characterised in that：Described point of feed pipe is removably mounted in the lead channel.
8. according to the device described in claim 1, it is characterised in that：Multiple impingement baffles are provided with the lead channel, multiple impingement baffles are evenly arranged in the bottom of the lead channel.
9. according to the device described in claim 1, it is characterised in that：The impingement baffle is provided with via.
10. according to the device described in claim 1, it is characterised in that：The height of the impingement baffle is 1/3～3/5 with the depth ratio of the lead channel.
11. according to the device described in claim 1, it is characterised in that：The inwall of the housing is provided with an overflow baffle, and the overflow baffle is fixed on the inwall of the housing, and the overflow baffle forms cloth liquid passage with the inner walls and tube sheet.
12. according to the device described in claim 1, it is characterised in that：The overflow baffle is cylinder, and section is in class inverted " L " font.
13. according to the device described in claim 1, it is characterised in that：Described fouling device is jacket type structure, heated by heat source stream in chuck, the heat source stream is that fouling device evaporates the steam for producing steam again Jing after mechanical compress, fouling device inner homogeneous arrange 2～6 scraping blades, the scraping blade is driven in fouling device internal rotating by motor, in process of production, scraping blade continuously rotates, and rotary speed is 200r/min～360r/min.
14. according to the device described in claim 1, it is characterised in that：Described vapour compression machine is using the one kind in centrifugal compressor, screw compressor, reciprocating compressor, centrifugal high pressure fan.
15. according to the device described in claim 1, it is characterised in that：The compression ratio of described vapour compression machine is 1.3～2.0, preferably 1.4～1.7.
A kind of 16. methods of the process containing organic wastewater, using arbitrary described device in claim 1-16, methods described includes：
Using waste water preheater, it is used to process raw material waste water and condensate, and raw material waste water and condensate are exchanged heat in waste water preheater, the condensate of the raw material waste water after being preheated after process and condensation；
Using evaporimeter, it is used to process the raw material waste water come after waste water preheater preheating of hanging oneself, and the 1st stream, the 2nd stream of liquid phase and the condensate of gas phase are obtained after process；
Using injector, it is used to process the 1st stream of flash-pot and the condensate of the saturation temperature from condensate water collecting separator, and the 3rd stream of gas-liquid mixed phase is obtained after process；
Using condensate water collecting separator, it is used to receive the 3rd stream of the condensate for carrying out flash-pot, the condensate of fouling device and injector, the 4th stream of gas phase and the condensate of saturation temperature are obtained after process, the condensate of the saturation temperature is divided into two-way, waste water preheater is wherein entered all the way, and another road enters injector；
Using vapour compression machine, it is used to process the 4th stream from condensate water collecting separator, and the 5th stream of gas phase is obtained after process, and the 5th stream enters fouling device as the heat source stream of fouling device；
Using fouling device, it is used to process the 2nd stream of flash-pot, and the 6th stream, the 7th stream of liquid phase, dirt and the condensate of gas phase are obtained after process；6th stream enters evaporimeter as the heat source stream of evaporimeter, and the 7th stream enters evaporimeter after mixing with the raw material waste water after preheating.
17. in accordance with the method for claim 17, it is characterised in that：Raw material waste water, by exchanging heat to 95 DEG C～102 DEG C with condensate, is then mixed in evaporimeter in waste water preheater with the concentrate of fouling device, and organic concentration is as unsaturated concentration with the mixed liquor for ensureing to be evaporated in evaporimeter.
18. in accordance with the method for claim 18, it is characterised in that：Raw material waste water is in waste water preheater by exchanging heat to 98 DEG C～100 DEG C with condensate.
19. in accordance with the method for claim 17, it is characterised in that：Logarithm heat transfer temperature difference in the evaporimeter between steam and waste water is 3 DEG C～10 DEG C, and the vaporization rate of waste water evaporation is 5%～50% in the evaporimeter.
20. in accordance with the method for claim 20, it is characterised in that：Logarithm heat transfer temperature difference in the evaporimeter between steam and waste water is 4 DEG C～8 DEG C, and the vaporization rate of waste water evaporation is 10%～40% in the evaporimeter.
21. in accordance with the method for claim 21, it is characterised in that：It is extremely higher than 1 DEG C～5 DEG C of boiling temperature that the operation temperature of the fouling device is the boiling temperature of concentration waste water, and operating pressure is normal pressure.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112221169A (en) * | 2019-07-15 | 2021-01-15 | 合众思(北京)环境工程有限公司 | MVR evaporation crystallization system |
| CN113432480A (en) * | 2021-06-22 | 2021-09-24 | 中国科学院广州能源研究所 | Heat exchange enhancement type anti-scaling device and method |
| CN115520935A (en) * | 2022-09-29 | 2022-12-27 | 中冶焦耐(大连)工程技术有限公司 | Method and system for recovering high-temperature condensed water of coking plant |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102527070A (en) * | 2012-03-09 | 2012-07-04 | 南京科盛环保科技有限公司 | Free energy heat pump multiple-effect evaporation device and process |
| CN204138369U (en) * | 2014-08-26 | 2015-02-04 | 张大千 | A kind of luwa evaporator processing oil waste liquid |
| CN104787823A (en) * | 2015-04-17 | 2015-07-22 | 黑龙江鑫达晟机械科技有限公司 | Yeast wastewater zero discharge treatment method |
| CN104986910A (en) * | 2015-07-23 | 2015-10-21 | 江苏德邦工程有限公司 | Mechanical steam recompression falling film evaporation process method and system |
-
2015
- 2015-11-02 CN CN201510730154.0A patent/CN106630338B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102527070A (en) * | 2012-03-09 | 2012-07-04 | 南京科盛环保科技有限公司 | Free energy heat pump multiple-effect evaporation device and process |
| CN204138369U (en) * | 2014-08-26 | 2015-02-04 | 张大千 | A kind of luwa evaporator processing oil waste liquid |
| CN104787823A (en) * | 2015-04-17 | 2015-07-22 | 黑龙江鑫达晟机械科技有限公司 | Yeast wastewater zero discharge treatment method |
| CN104986910A (en) * | 2015-07-23 | 2015-10-21 | 江苏德邦工程有限公司 | Mechanical steam recompression falling film evaporation process method and system |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112221169A (en) * | 2019-07-15 | 2021-01-15 | 合众思(北京)环境工程有限公司 | MVR evaporation crystallization system |
| CN113432480A (en) * | 2021-06-22 | 2021-09-24 | 中国科学院广州能源研究所 | Heat exchange enhancement type anti-scaling device and method |
| CN115520935A (en) * | 2022-09-29 | 2022-12-27 | 中冶焦耐(大连)工程技术有限公司 | Method and system for recovering high-temperature condensed water of coking plant |
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