CN106629937B - Wastewater treatment process and system - Google Patents
Wastewater treatment process and system Download PDFInfo
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- CN106629937B CN106629937B CN201510730117.XA CN201510730117A CN106629937B CN 106629937 B CN106629937 B CN 106629937B CN 201510730117 A CN201510730117 A CN 201510730117A CN 106629937 B CN106629937 B CN 106629937B
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Abstract
The invention provides a wastewater treatment process and a system, wherein the system comprises a wastewater preheater, an evaporator, a stripping tower, a steam compressor, a heat exchanger, a non-condensable gas compressor and a condensed water collector. The invention also provides a wastewater treatment process utilizing the system, and the wastewater treatment process and the system have the advantages of safety, reliability, simple equipment, low operation cost, obvious energy-saving effect and the like, and can realize 50-95% of water resource recycling.
Description
Technical Field
The invention relates to the technical field of environmental protection and energy conservation, in particular to a method and a device for concentrating and treating wastewater containing salt and high molecular organic matters.
Background
The high-salt-content wastewater refers to wastewater with the total salt content TDS being more than or equal to 1 percent and generally belongs to refractory wastewater. The common high salinity wastewater mainly comes from wastewater discharged by replacing seawater, industrial production wastewater and the like. The desalting treatment process of the high-salt-content wastewater mainly comprises an electrodialysis method, a reverse osmosis method, an ion exchange method and an evaporation method. The organic wastewater mainly comes from the fields of chemical industry, road deicing, food processing and the like, and also comprises printing and dyeing wastewater, petroleum exploitation and processing wastewater, papermaking wastewater, pesticide industry wastewater and the like. The total amount of high-salt organic wastewater is huge and increasing year by year. If the wastewater is not treated before being discharged, high-concentration soluble inorganic salts and refractory toxic organic matters in the wastewater can cause serious environmental pollution and damage to soil, surface water and underground water. Therefore, in the present day when water resources are in short supply, research and development of effective high-salt organic wastewater treatment technology are necessary.
In recent years, the treatment of recycled wastewater by mechanical vapor recompression evaporation technology has been proposed abroad. The mechanical vapor recompression technology is an advanced energy-saving technology for reducing the demand on external energy. The energy-saving principle is as follows: the secondary steam generated in the system is compressed by the compressor, so that the pressure, the temperature and the enthalpy value of the secondary steam are increased, an external heat source which is required to be adopted in the original system is replaced, and the latent heat of the secondary steam is fully utilized, thereby achieving the purpose of saving energy in the technical process. At present, the mechanical vapor recompression system is mainly applied to the recovery and treatment of wastewater containing salt, oilfield reinjection water, pharmaceutical wastewater and the like.
Disclosure of Invention
The invention aims to provide a wastewater treatment process and a wastewater treatment system, and the wastewater treatment process and the wastewater treatment system have the advantages of safety, reliability, simple equipment, low operation cost, obvious energy-saving effect and the like.
The invention provides a wastewater treatment system, which comprises a wastewater preheater, an evaporator, a stripping tower, a steam compressor, a heat exchanger, a non-condensable gas compressor and a condensed water collector, wherein the evaporator is connected with the wastewater preheater; wherein waste water inlet line is connected with the waste water entry of evaporimeter through waste water pre-heater, the steam outlet of evaporimeter links to each other with vapor compressor's entry, vapor compressor's export and the heat source steam inlet connection of heat exchanger, the condensate outlet of heat exchanger and the condensate inlet connection of condensate collector, the noncondensable gas export of evaporimeter links to each other through the noncondensable gas entry of noncondensable gas compressor and heat exchanger, the noncondensable gas export of heat exchanger and the gaseous phase entry linkage of strip tower, the gaseous phase export of strip tower and the heat source steam inlet connection of evaporimeter, the concentrate discharge port of evaporimeter bottom is connected with the waste water entry of strip tower through the pipeline, the concentrate discharge port of strip tower bottom is connected with waste water pre-heater through the pipeline, the condensate discharge port of evaporimeter is connected with the condensate collector through the pipeline, the discharge port of condensate collector is connected with waste.
In the wastewater treatment system, a steam supplementing pipeline is arranged on a connecting pipeline between a steam outlet of the evaporator and an inlet of the steam compressor.
In the wastewater treatment system, a non-condensable gas supplementing pipeline is arranged on a connecting pipeline between a non-condensable gas outlet of the evaporator and an inlet of the non-condensable gas compressor.
In the wastewater treatment system, the non-condensable gas compressor can be a volume type compressor, a turbine type compressor or a thermal type compressor.
In the wastewater treatment system, the wastewater preheater and the heat exchanger can adopt a shell-and-tube heat exchanger, a heat pipe type heat exchanger, a plate type heat exchanger or a plate-and-shell type heat exchanger, and preferably adopt a plate type heat exchanger.
In the wastewater treatment system, the stripping tower can adopt a packed tower and a spray tower, and preferably adopts the spray tower.
In the wastewater treatment system, the evaporator can be any one of a rising-film evaporator, a falling-film evaporator, a horizontal tube evaporator and a plate evaporator.
In the wastewater treatment system of the present invention, the falling film evaporator comprises: the evaporator comprises a shell, a tube plate, an evaporation tube and a liquid supply device, wherein the tube plate is arranged at the upper part of the shell; the evaporation tubes are arranged in the shell vertically, and the upper ends of the evaporation tubes penetrate through the tube plate; the upper end of the evaporation tube is provided with a flow guide device; the liquid supply device comprises a liquid inlet groove and a material separating pipe, the liquid inlet groove is vertically arranged on the upper portion of the outer wall of the shell and surrounds the whole shell, the liquid inlet groove is uniformly provided with a plurality of material separating ports, the material separating ports are arranged on the upper side wall of the liquid inlet groove, the lower end of the material separating pipe vertically penetrates through the material separating ports and extends into the liquid inlet groove, and the lower end of the material separating pipe is close to the bottom of the liquid inlet groove; the shell is provided with a plurality of overflow channels communicated with the liquid inlet groove.
Wherein, divide the material pipe detachably to install on the feed liquor groove.
Wherein, be equipped with a plurality of impingement baffles in the feed liquor groove, it is a plurality of impingement baffle align to grid is in the bottom of feed liquor groove.
Wherein, the impingement baffle is provided with a via hole.
Wherein, the height ratio of the impingement plate to the depth of the liquid inlet groove is 1/3-3/5.
The inner wall of the shell is provided with an overflow baffle which is fixed on the inner wall of the shell, and the overflow baffle, the inner wall of the shell and the tube plate form a liquid distribution channel.
The overflow baffle is a cylinder, and the cross section of the overflow baffle is in an inverted L-shaped shape.
Wherein the evaporation tubes are uniformly arranged in the housing.
In the wastewater treatment system, the vapor compressor can adopt a centrifugal compressor, a screw compressor, a reciprocating compressor and a high-pressure centrifugal fan; the compression ratio of the compressor is 1.3-2.0, preferably 1.4-1.7.
The invention also provides a wastewater treatment process, which adopts the system and comprises the following steps:
the method comprises the following steps of (1) using a waste water preheater for treating raw material waste water, condensed water and concentrated solution of a stripping tower, wherein the raw material waste water, the condensed water and the concentrated solution of the stripping tower exchange heat in the waste water preheater to obtain preheated raw material waste water, cooled condensed water and cooled concentrated solution;
using an evaporator for treating raw wastewater preheated by a wastewater preheater to obtain a 1 st material flow of a gas phase, a 2 nd material flow of a liquid phase, noncondensable gas and condensed water;
using a vapor compressor for treating the 1 st stream from the evaporator to obtain a 3 rd stream in the vapor phase after treatment;
using a non-condensable gas compressor for treating the non-condensable gas from the evaporator to obtain a 4 th stream in the gas phase;
using a heat exchanger for treating the 3 rd stream from the vapor compressor and the 4 th stream from the non-condensable gas compressor, the 5 th stream of the gaseous phase and the 6 th stream of the liquid phase obtained after the treatment;
using a condensate collector for receiving the condensate from the evaporator and a 6 th stream from the heat exchanger, and treating to obtain a 7 th stream in a liquid phase;
a stripping column is used which is used to treat the 2 nd stream from the evaporator and the 5 th stream from the heat exchanger, resulting after treatment in a 8 th stream in the gas phase and a 9 th stream in the liquid phase.
In the treatment process, raw material wastewater enters an evaporator after exchanging heat with condensed water and concentrated solution of a stripping tower in a wastewater preheater to reach a temperature close to saturation temperature, the raw material wastewater is evaporated in the evaporator, the obtained steam is compressed by a steam compressor, the latent heat of the steam is increased, the compressed steam is used as a heat source of a heat exchanger to heat non-condensable gas, the concentrated solution at the bottom of the evaporator enters the stripping tower to be subjected to stripping evaporation, the heated non-condensable gas is used as carrier gas to enter the stripping tower to strip, evaporate and concentrate the wastewater, the non-condensable gas is introduced into the stripping tower to improve the mass transfer and heat transfer efficiency of the stripping tower, and the scaling and blocking of the wastewater in the stripping tower can be. Steam evaporated by steam stripping in the stripping tower and introduced non-condensable gas are mixed and enter the evaporator to serve as a heating heat source of the evaporator, the steam is condensed into condensed water, the non-condensable gas enters the non-condensable gas compressor from a non-condensable gas outlet of the evaporator to be compressed, and the compressed non-condensable gas enters the stripping tower through heating circulation. And the concentrated solution at the bottom of the stripping tower enters a wastewater preheater to exchange heat with wastewater to recover heat.
In the treatment process, the raw material wastewater is subjected to heat exchange with condensed water and concentrated solution of a stripping tower in a wastewater preheater to 90-102 ℃, preferably 95-100 ℃, and then enters an evaporator.
In the treatment process, the logarithmic heat exchange temperature difference between the steam and the wastewater in the evaporator is 3-10 ℃, preferably 4-8 ℃, and meanwhile, the vaporization rate of the wastewater in the evaporator is 5-50%, preferably 10-40%.
In the treatment process, the non-condensable gas exchanges heat with steam compressed by a steam compressor in a heat exchanger, and the temperature after heat exchange is 110-115 ℃.
In the treatment process of the invention, the non-condensable gas can be air, nitrogen, oxygen, steam and the like.
In the treatment process, when the system is started, steam outside the system is required to be used as a heat source for starting the system, and the steam can be introduced into the system through a steam supplementing pipeline; if the steam generated in the system during the operation process can not maintain the steam quantity consumed by the system heat, the steam can be introduced through a steam replenishing pipeline; if the steam generated during operation of the system is greater than the amount of steam consumed to maintain system heat, the excess steam may be removed from the system via a make-up steam line.
In the treatment process, when the device is started, the non-condensable gas is required to be introduced into the stripping tower from the non-condensable gas supplementing pipeline.
In the treatment process, the evaporator can adopt any one of a climbing-film evaporator, a falling-film evaporator, a horizontal tube evaporator and a plate evaporator.
In the treatment process of the invention, the falling film evaporator comprises: the evaporator comprises a shell, a tube plate, an evaporation tube and a liquid supply device, wherein the tube plate is arranged at the upper part of the shell; the evaporation tubes are arranged in the shell vertically, and the upper ends of the evaporation tubes penetrate through the tube plate; the upper end of the evaporation tube is provided with a flow guide device; the liquid supply device comprises a liquid inlet groove and a material separating pipe, the liquid inlet groove is vertically arranged on the upper portion of the outer wall of the shell and surrounds the whole shell, the liquid inlet groove is uniformly provided with a plurality of material separating ports, the material separating ports are arranged on the upper side wall of the liquid inlet groove, the lower end of the material separating pipe vertically penetrates through the material separating ports and extends into the liquid inlet groove, and the lower end of the material separating pipe is close to the bottom of the liquid inlet groove; the shell is provided with a plurality of overflow channels communicated with the liquid inlet groove.
Wherein, divide the material pipe detachably to install on the feed liquor groove.
Wherein, be equipped with a plurality of impingement baffles in the feed liquor groove, it is a plurality of impingement baffle align to grid is in the bottom of feed liquor groove.
Wherein, the impingement baffle is provided with a via hole.
Wherein, the height ratio of the impingement plate to the depth of the liquid inlet groove is 1/3-3/5.
The inner wall of the shell is provided with an overflow baffle which is fixed on the inner wall of the shell, and the overflow baffle, the inner wall of the shell and the tube plate form a liquid distribution channel.
The overflow baffle is a cylinder, and the cross section of the overflow baffle is in an inverted L-shaped shape.
Wherein the evaporation tubes are uniformly arranged in the housing.
Other techniques in the treatment process of the present invention, such as water pumping, heat exchange, condensate collection, etc., are well known to those skilled in the art.
Compared with the prior art, the wastewater treatment process and the system have the following advantages:
1. in the wastewater treatment process, the wastewater evaporation concentration recovery adopts a combined process of steam mechanical recompression and non-condensable gas stripping, and 50-95% of water resource recycling can be realized. By controlling the concentration ratio of the waste water in the evaporator, the waste water is prevented from scaling in the evaporator, and the concentrated solution is further concentrated in the stripping tower.
2. In the wastewater treatment process, the compressed noncondensable gas is introduced into the stripping tower, so that the heat transfer and mass transfer coefficients of wastewater evaporation concentration are improved, and the heat required in the stripping tower is brought into the tower by the noncondensable gas, so that the noncondensable gas and the wastewater directly transfer heat, and the problem of scaling and blockage in the conventional double-effect steam mechanical recompression process is effectively avoided.
3. The heat exchanger is arranged in the wastewater treatment process, so that the latent heat of the compressed steam is transferred to the non-condensable gas through heat exchange, the heat directly enters the wastewater, and the utilization efficiency of the steam compression heat energy is improved.
4. In the wastewater treatment process and system, the falling film evaporator with lateral feeding is used, so that the structure is simple and compact, and the height of equipment is effectively reduced; the liquid circulation is large, and the operation and the maintenance are convenient; the equipment has the advantages of high liquid distribution rate, uniform film distribution, difficult blockage and easy cleaning, and can increase the arrangement quantity of the evaporation tubes and the heat exchange area of the evaporator.
5. The waste water treatment process and system of the invention have the characteristics of safety, reliability, simple equipment, low investment and the like.
Drawings
FIG. 1 is a schematic view of a wastewater treatment process and system according to the present invention.
Figure 2 is a front view in half section of a falling film evaporator for use in the present invention.
Figure 3 is a top plan view, partly in section, of a falling film evaporator for use in the present invention.
Figure 4 is a schematic view of the impingement plate of a falling film evaporator for use in the present invention.
Detailed Description
The following examples further illustrate specific aspects of the present invention, but are not limited to the following examples.
As shown in fig. 1, the present invention provides a wastewater treatment system, the treatment apparatus comprising a wastewater preheater 2, an evaporator 5, a stripping tower 11, a vapor compressor 8, a heat exchanger 24, a non-condensable gas compressor 14, and a condensed water collector 20; wherein a wastewater feeding pipeline is connected with a wastewater inlet of an evaporator 5 through a wastewater preheater 2, a steam outlet of the evaporator 5 is connected with an inlet of a steam compressor 8, a steam supplementing pipeline 7 is arranged on a connecting pipeline between the steam outlet of the evaporator 5 and an inlet of the steam compressor 8, an outlet of the steam compressor 8 is connected with a heat source steam inlet of a heat exchanger 24, a condensed water outlet of the heat exchanger 24 is connected with a condensed water inlet of a condensed water collector 20, a non-condensable gas outlet of the evaporator 5 is connected with a non-condensable gas inlet of the heat exchanger 24 through a non-condensable gas compressor 14, a non-condensable gas supplementing pipeline 23 is arranged on a connecting pipeline between the non-condensable gas outlet of the effective evaporator 5 and an inlet of the non-condensable gas compressor 14, a non-condensable gas outlet of the heat exchanger 24 is connected with a gas phase inlet of a stripping tower 11, a gas phase outlet of the stripping tower 11 is connected with the heat source steam inlet of the evaporator 5, a concentrated solution discharge port at, the concentrated solution discharge port at the bottom of the stripping tower 11 is connected with the waste water preheater 2 through a pipeline, the condensed water discharge port of the evaporator 5 is connected with the condensed water collector 20 through a pipeline, and the discharge port of the condensed water collector 20 is connected with the waste water preheater 2.
The invention also provides a wastewater treatment process, which adopts the system and comprises the following steps:
using a waste water preheater 2 for treating raw material waste water 1, condensed water 21 and a concentrated solution 15 of a stripping tower, wherein the raw material waste water 1, the condensed water 21 and the concentrated solution 15 of the stripping tower exchange heat in the waste water preheater 2 to obtain a preheated raw material waste water 3, a cooled condensed water 22 and a cooled concentrated solution 17;
using an evaporator 5 for treating the raw wastewater 3 preheated by the wastewater preheater, wherein a 1 st material flow 6 in a gas phase, a 2 nd material flow 10 in a liquid phase, a non-condensable gas 13 and condensed water 18 are obtained after treatment;
using a vapor compressor 8 for treating the 1 st stream 6 from the evaporator, resulting in a 3 rd stream 9 in the vapor phase after treatment;
using a non-condensable gas compressor 14 for treating the non-condensable gas 13 coming from the evaporator, a 4 th stream 16 in the gas phase being obtained after the treatment;
using a heat exchanger 24 for treating the 3 rd stream 9 from the vapor compressor and the 4 th stream 16 from the non-condensable gas compressor, the 5 th stream of the gaseous phase and the 6 th stream 19 of the liquid phase obtained after the treatment;
using a condensate collector for receiving the evaporator condensate 18 and the heat exchanger stream 6 19, resulting after treatment in a liquid phase stream 7 21;
a stripping column 11 is used which serves to treat the 2 nd stream from the evaporator and the 5 th stream of the heat exchanger, resulting after treatment in a 8 th stream 12 in the gas phase and a 9 th stream 15 in the liquid phase.
In the method, raw material wastewater 1 is subjected to heat exchange with condensed water 21 and concentrated liquor 15 of a stripping tower in a wastewater preheater 2 to reach a temperature close to saturation temperature, then enters an evaporator 5, is evaporated in the evaporator 5, latent heat of the steam is increased after the obtained steam is compressed by a steam compressor 8, then the compressed steam 9 is used as heat source steam of a heat exchanger 24 to heat non-condensable gas, the heated non-condensable gas enters a stripping tower 11 to be stripped and evaporated to obtain concentrated liquor 10 from the bottom of the evaporator 5, and stripping concentrated wastewater of the non-condensable gas is introduced into the stripping tower, so that the mass transfer and heat transfer efficiency of the stripping tower 11 is improved, and the scaling and blocking of the wastewater in the stripping tower 11 can be effectively avoided. Steam evaporated by stripping in the stripping tower 11 and introduced non-condensable gas are mixed and enter the evaporator 5 to serve as a heating source of the evaporator 5, the steam is condensed into condensed water 18, the non-condensable gas 13 enters the non-condensable gas compressor 14 from a non-condensable gas outlet of the evaporator 5 to be compressed, and the compressed non-condensable gas 16 enters the stripping tower 11 through heating circulation. And the concentrated solution 15 at the bottom of the stripping tower 11 enters a wastewater preheater 2 to exchange heat with wastewater to recover heat.
As shown in fig. 2, 3 and 4, the side-feed falling-film evaporator of the present invention comprises: shell 11, tube plate 1, evaporating tubes 3, liquid supply device 20. The shell 11 is cylindrical, the tube plate 1 is arranged at the upper part of the shell 11, and the upper surface of the tube plate 1 and the top end part of the shell 11 form a film distribution chamber. The evaporation tube 3 is provided in plurality, and the plurality of evaporation tubes 3 are vertically arranged in the housing 11, and preferably, the evaporation tubes are uniformly arranged. The upper end of the evaporation tube 3 penetrates through the tube plate 1, a plurality of evaporation tube holes are formed in the tube plate 1, and the upper end of the evaporation tube 3 extends out of the evaporation tube holes and is hermetically connected with the tube plate 1 by welding or expansion connection and other methods. The upper end of the evaporation tube 3 is provided with a flow guide device 2. The liquid supply device 20 comprises a liquid inlet groove 6 and a plurality of branch material pipes 7, in the embodiment, the liquid inlet groove 6 is an annular shell groove with an inner side opened, the inner diameter of the annular shell groove is the same as the outer diameter of the shell 11, the liquid inlet groove 6 is vertically arranged on the upper part of the outer wall of the shell 11 through welding and surrounds the whole shell 11, and the outer side wall of the shell 11 is used as a shared side wall on one side of the opening of the liquid inlet groove 6. Feed liquor groove 6 evenly is equipped with a plurality of branch and expects mouthful 13, and the quantity that divides material mouthful 13 is the same with branch material pipe 7 for the installation divides material pipe 7, specifically to this embodiment, divides the quantity that divides material mouthful to be 8. Divide feed inlet 13 to set up the upper wall in feed liquor groove 6, divide the vertical bottom that passes of feed inlet 13 of feed inlet pipe 7 to stretch into feed inlet groove 6, and divide the lower extreme export of feed inlet pipe 7 to be close to the bottom of feed inlet groove 6. The material dividing pipes 7 are communicated with a feeding main pipe 10, and materials are supplied into the feeding grooves 6 through the material dividing pipes 7 by the feeding main pipe 10. The shell 11 is provided with a plurality of overflow channels 5 communicated with the liquid inlet groove 6, the overflow channels 5 are weir mouths close to the upper side wall of the liquid inlet groove 6, and the common structures are a rectangular weir, a V-shaped weir and a round-bottom rectangular weir.
Further, the branch material inlet pipe 7 is detachably mounted on the liquid inlet groove 6 through a flange. Specifically, a flange 71 is welded and installed on the outer side wall of the material separating pipe 7, and the flange 71 is connected with the upper side wall of the liquid inlet groove 6 through a bolt assembly and can be detached as required.
Further, be equipped with a plurality of impingement baffles 8 in feed liquor groove 6, a plurality of impingement baffles 8 align to grid is in the bottom of feed liquor groove 6, and in this embodiment, 8 quantity of impingement baffles are 16. Preferably, the upper edge of the impingement plate 8 is higher than the lower outlet of the material separating pipe 7. Referring to fig. 4, the baffle plate 8 is provided with a through hole 81, and the through hole 81 preferably has a circular cross section with a diameter of 5-30 mm, preferably 10-20 mm. Preferably, the height ratio of the impingement plate 8 to the depth of the liquid inlet tank 6 is 1/3-3/5, for example, the height of the impingement plate 8 is 1/3, 3/7, 1/2 and 3/5 of the depth of the liquid inlet tank 6.
Further, an overflow baffle 4 is arranged on the inner wall of the shell 11, the overflow baffle 4 is a cylinder, and the outer diameter of the overflow baffle 4 is smaller than the inner diameter of the shell 11. The overflow baffle 4 is fixed on the inner wall of the shell 11 through a plurality of rectangular supporting plates 12, the lower edge of the overflow baffle 4 is higher than the upper surface of the tube plate 1, and the overflow baffle 4, the inner wall of the shell 11 and the tube plate 1 form a liquid distribution channel. The cross-sectional width of the liquid distribution channel is less than the minimum distance between the inner wall of the shell 11 and the evaporation tube 3.
Example 1
By adopting the system shown in figure 1, the evaporator adopts the device shown in figure 2, the used wastewater is ammonium sulfate wastewater, the concentration of the raw material wastewater is 20wt%, the treatment capacity of the raw material wastewater is 15t/h, the normal temperature wastewater is preheated to 99 ℃ by the preheater 2 and enters the evaporator 5. The compression ratio of the steam compressor 8 is 1.5, and air is adopted as supplementary non-condensable gas. The concentrated solution 10 discharged from the bottom of the evaporator 5 is 32wt%, and the concentrated solution 15 discharged from the concentrated solution 10 after being subjected to steam stripping, evaporation and concentration by a stripping tower is 45 wt%. The temperature of the condensed water 21 after heat recovery is about 45 ℃, and the recovery amount of the condensed water is 8.3 t/h.
Claims (27)
1. A wastewater treatment system comprising a wastewater preheater, an evaporator, a stripper, a steam compressor, a heat exchanger, a non-condensable gas compressor, and a condensate collector; wherein the waste water feed line is connected with the waste water inlet of the evaporator through the waste water preheater, the steam outlet of the evaporator is connected with the inlet of the steam compressor, the outlet of the steam compressor is connected with the heat source steam inlet of the heat exchanger, the condensed water outlet of the heat exchanger is connected with the condensed water inlet of the condensed water collector, the non-condensable gas outlet of the evaporator is connected with the non-condensable gas inlet of the heat exchanger through the non-condensable gas compressor, the non-condensable gas outlet of the heat exchanger is connected with the gas phase inlet of the stripping tower, the gas phase outlet of the stripping tower is connected with the heat source steam inlet of the evaporator, the concentrated solution discharge port at the bottom of the evaporator is connected with the waste water inlet of the stripping tower through a pipeline, the concentrated solution discharge port at the bottom of the stripping tower is connected with the waste water preheater through a pipeline, the condensed water discharge port of the;
wherein, the evaporimeter adopt falling film evaporator, falling film evaporator include: the evaporator comprises a shell, a tube plate, an evaporation tube and a liquid supply device, wherein the tube plate is arranged at the upper part of the shell; the evaporation tubes are arranged in the shell vertically, and the upper ends of the evaporation tubes penetrate through the tube plate; the upper end of the evaporation tube is provided with a flow guide device; the liquid supply device comprises a liquid inlet groove and a material separating pipe, the liquid inlet groove is vertically arranged on the upper portion of the outer wall of the shell and surrounds the whole shell, the liquid inlet groove is uniformly provided with a plurality of material separating ports, the material separating ports are arranged on the upper side wall of the liquid inlet groove, the lower end of the material separating pipe vertically penetrates through the material separating ports and extends into the liquid inlet groove, and the lower end of the material separating pipe is close to the bottom of the liquid inlet groove; the shell is provided with a plurality of overflow channels communicated with the liquid inlet groove.
2. The system of claim 1, wherein: and a steam supplementing pipeline is arranged on a connecting pipeline between the steam outlet of the evaporator and the inlet of the steam compressor.
3. The system of claim 1, wherein: and a non-condensable gas supplementing pipeline is arranged on a non-condensable gas outlet of the evaporator and an inlet connecting pipeline of the non-condensable gas compressor.
4. The system of claim 1, wherein: the non-condensable gas compressor is a volume type compressor, a turbine type compressor or a thermal type compressor.
5. The system of claim 1, wherein: the waste water preheater and the heat exchanger adopt a shell-and-tube heat exchanger, a heat pipe type heat exchanger, a plate type heat exchanger or a shell-and-tube heat exchanger.
6. The system of claim 1 or 5, wherein: the waste water preheater and the heat exchanger adopt plate heat exchangers.
7. The system of claim 1, wherein: the stripping tower adopts a packed tower or a spray tower.
8. The system of claim 1 or 7, wherein: the stripping tower adopts a spray tower.
9. The system of claim 1, wherein: the branch material inlet pipe is detachably arranged on the liquid inlet groove.
10. The system of claim 1, wherein: a plurality of impingement plates are arranged in the liquid inlet groove and are uniformly arranged at the bottom of the liquid inlet groove.
11. The system of claim 10, wherein: and the impingement baffle is provided with a via hole.
12. The system of claim 10, wherein: the height ratio of the impingement plate to the depth of the liquid inlet groove is 1/3-3/5.
13. The system of claim 1, wherein: the inner wall of the shell is provided with an overflow baffle which is fixed on the inner wall of the shell, and the overflow baffle, the inner wall of the shell and the tube plate form a liquid distribution channel.
14. The system of claim 13, wherein: the overflow baffle is a cylinder, and the cross section of the overflow baffle is in an inverted L-shaped shape.
15. The system of claim 1, wherein: the evaporation tubes are uniformly arranged in the shell.
16. The system of claim 1, wherein: the vapor compressor adopts a centrifugal compressor, a screw compressor, a reciprocating compressor and a high-pressure centrifugal fan.
17. A wastewater treatment process using the system of any one of claims 1-16, wherein: the process comprises the following steps:
the method comprises the following steps of (1) using a waste water preheater for treating raw material waste water, condensed water and concentrated solution of a stripping tower, wherein the raw material waste water, the condensed water and the concentrated solution of the stripping tower exchange heat in the waste water preheater to obtain preheated raw material waste water, cooled condensed water and cooled concentrated solution;
using an evaporator for treating raw wastewater preheated by a wastewater preheater to obtain a 1 st material flow of a gas phase, a 2 nd material flow of a liquid phase, noncondensable gas and condensed water;
using a vapor compressor for treating the 1 st stream from the evaporator to obtain a 3 rd stream in the vapor phase after treatment;
using a non-condensable gas compressor for treating the non-condensable gas from the evaporator to obtain a 4 th stream in the gas phase;
using a heat exchanger for treating the 3 rd stream from the vapor compressor and the 4 th stream from the non-condensable gas compressor, the 5 th stream of the gaseous phase and the 6 th stream of the liquid phase obtained after the treatment;
using a condensate collector for receiving the condensate from the evaporator and a 6 th stream from the heat exchanger, and treating to obtain a 7 th stream in a liquid phase;
a stripping column is used which is used to treat the 2 nd stream from the evaporator and the 5 th stream from the heat exchanger, resulting after treatment in a 8 th stream in the gas phase and a 9 th stream in the liquid phase.
18. The process of claim 17, wherein: the raw material wastewater enters an evaporator after heat exchange in a wastewater preheater to 90-102 ℃.
19. The process of claim 17 or 18, wherein: the raw material wastewater enters an evaporator after heat exchange in a wastewater preheater to 95-100 ℃.
20. The process of claim 17, wherein: the logarithmic heat exchange temperature difference between the steam and the waste water in the evaporator is 3-10 ℃.
21. The process of claim 17 or 20, wherein: the logarithmic heat exchange temperature difference between the steam and the waste water in the evaporator is 4-8 ℃.
22. The process of claim 17, wherein: the vaporization rate of the waste water in the evaporator is 5-50%.
23. The process of claim 17 or 22, wherein: the vaporization rate of the waste water in the evaporator is 10-40%.
24. The process of claim 17, wherein: when the system is started, steam outside the system is used as a heat source for starting the system, and the steam is introduced into the system through a steam supplementing pipeline; if the steam generated in the system in the operation process can not maintain the steam quantity consumed by the system heat, introducing the steam through a steam replenishing pipeline; if the steam generated during operation of the system is greater than the amount of steam consumed to maintain the system heat, the excess steam is removed from the system via the make-up steam line.
25. The process of claim 17, wherein: when the apparatus is started, the non-condensable gas needs to be introduced into the stripping tower from the non-condensable gas make-up line.
26. The process of claim 17, wherein: the non-condensable gas exchanges heat with the steam compressed by the steam compressor in the heat exchanger, and the temperature of the non-condensable gas after heat exchange is 110-115 ℃.
27. The process of claim 17, wherein: the non-condensable gas is air, nitrogen, oxygen or steam.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510730117.XA CN106629937B (en) | 2015-11-02 | 2015-11-02 | Wastewater treatment process and system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510730117.XA CN106629937B (en) | 2015-11-02 | 2015-11-02 | Wastewater treatment process and system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106629937A CN106629937A (en) | 2017-05-10 |
| CN106629937B true CN106629937B (en) | 2020-05-19 |
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| CN201704161U (en) * | 2010-05-14 | 2011-01-12 | 兰州节能环保工程有限责任公司 | Sewage evaporation treatment device |
| CN202880981U (en) * | 2012-11-08 | 2013-04-17 | 内蒙古伊泰煤制油有限责任公司 | Cyclic utilization system of Fischer-Tropsch synthesis wastewater in coal indirect liquefaction production |
| CN203530277U (en) * | 2013-07-31 | 2014-04-09 | 山东丽村生物科技有限公司 | Mixed oil evaporation device |
| CN203613059U (en) * | 2013-10-15 | 2014-05-28 | 中国石油化工股份有限公司 | Multiple-effect evaporation treatment device for alkali-contained waste water with high COD (chemical oxygen demand) |
| CN104787954A (en) * | 2015-04-08 | 2015-07-22 | 天津市创举科技有限公司 | Wastewater pretreatment technology |
| CN204522328U (en) * | 2015-03-23 | 2015-08-05 | 河北乐恒化工设备制造有限公司 | Three grades with function of mechanical steam recompression continuous falling liquid film circulating and evaporating concentration systems |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN201704161U (en) * | 2010-05-14 | 2011-01-12 | 兰州节能环保工程有限责任公司 | Sewage evaporation treatment device |
| CN202880981U (en) * | 2012-11-08 | 2013-04-17 | 内蒙古伊泰煤制油有限责任公司 | Cyclic utilization system of Fischer-Tropsch synthesis wastewater in coal indirect liquefaction production |
| CN203530277U (en) * | 2013-07-31 | 2014-04-09 | 山东丽村生物科技有限公司 | Mixed oil evaporation device |
| CN203613059U (en) * | 2013-10-15 | 2014-05-28 | 中国石油化工股份有限公司 | Multiple-effect evaporation treatment device for alkali-contained waste water with high COD (chemical oxygen demand) |
| CN204522328U (en) * | 2015-03-23 | 2015-08-05 | 河北乐恒化工设备制造有限公司 | Three grades with function of mechanical steam recompression continuous falling liquid film circulating and evaporating concentration systems |
| CN104787954A (en) * | 2015-04-08 | 2015-07-22 | 天津市创举科技有限公司 | Wastewater pretreatment technology |
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