CN108069482B - Wastewater treatment process and system - Google Patents
Wastewater treatment process and system Download PDFInfo
- Publication number
- CN108069482B CN108069482B CN201610991599.9A CN201610991599A CN108069482B CN 108069482 B CN108069482 B CN 108069482B CN 201610991599 A CN201610991599 A CN 201610991599A CN 108069482 B CN108069482 B CN 108069482B
- Authority
- CN
- China
- Prior art keywords
- waste water
- wastewater
- evaporator
- compressor
- stripping tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/041—Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/10—Treatment of water, waste water, or sewage by heating by distillation or evaporation by direct contact with a particulate solid or with a fluid, as a heat transfer medium
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/101—Sulfur compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention provides a wastewater treatment process and a system, wherein the system comprises a wastewater preheater, a wastewater heater, 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, a wastewater heater, an evaporator, a stripping tower, a steam compressor, a heat exchanger, a non-condensable gas compressor and a condensed water collector, wherein the wastewater heater is arranged on the bottom of the stripping tower; wherein the waste water inlet line is connected with the waste water inlet of the waste water heater through the waste water preheater, the waste water outlet of the waste water heater is connected with the waste water inlet of the evaporator, the gas outlet of the waste water heater is connected with the non-condensable gas inlet of the heat exchanger through the non-condensable gas compressor, the steam outlet of the evaporator is connected with the inlet of the steam compressor, the outlet of the steam compressor is divided into two paths, one path of the outlet is connected with the heat source steam inlet of the evaporator, the other path of the outlet is connected with the heat source steam inlet of the heat exchanger, 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 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 gas inlet of the waste water heater, the concentrated solution discharge port at the bottom of the stripping tower is connected with The inlet is connected, and the discharge port of the condensed water collector is connected with the waste water preheater.
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 noncondensable gas replenishing pipeline is arranged on a connecting pipeline between a gas outlet of the wastewater heater and an inlet of the noncondensable 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 wastewater heater can adopt a shell-and-tube heat exchanger or a plate-and-shell heat exchanger, and preferably adopts a plate-and-shell heat exchanger. The wastewater heater is provided with a gas-water separation bag, so that separation between condensed water and non-condensed gas in the heater is realized.
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 evaporator is a falling film evaporator, and 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 wastewater treatment 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;
the method comprises the following steps of (1) using a waste water heater for treating preheated raw material waste water and stripping gas at the top of a stripping tower, wherein the preheated raw material waste water and the stripping gas at the top of the stripping tower exchange heat in the waste water heater to obtain heated raw material waste water, condensed water and non-condensable gas;
using an evaporator for treating the raw wastewater heated by the wastewater heater to obtain a 1 st material flow of a gas phase, a 2 nd material flow of a liquid phase 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, said 3 rd stream being divided into a 31 st substream and a 32 nd substream, wherein the 31 st substream is returned to the evaporator;
using a non-condensable gas compressor for treating non-condensable gas from the waste water heater, resulting in a 4 th stream in the gas phase;
using a heat exchanger for treating the 32 nd substream from the vapor compressor and the 4 th stream from the non-condensable gas compressor, the 5 th stream of the gas phase obtained after treatment and the condensed water;
using a stripping tower for treating a 2 nd material flow from the evaporator and a 5 th material flow from the heat exchanger to obtain a stripping tower top gas and a stripping tower concentrated solution, wherein the stripping tower top gas is used as a heat source and enters a wastewater heater;
a condensate collector is used for receiving condensate from the evaporator, condensate from the waste water heater and condensate from the heat exchanger.
In the treatment process, raw material wastewater enters a wastewater heater to exchange heat with condensate and concentrated solution of a stripping tower in a wastewater preheater to reach a saturation temperature, then enters an evaporator after entering the wastewater heater to exchange heat with stripping gas of the stripping tower to reach the saturation temperature, is evaporated in the evaporator, the latent heat of the steam is increased after the obtained steam is compressed by a steam compressor, the compressed steam is respectively used as heat sources of the evaporator and a heat exchanger, the concentrated solution at the bottom of the evaporator enters the stripping tower to be stripped and evaporated, the heated non-condensable gas is used as carrier gas to enter the stripping tower to strip and evaporate the concentrated wastewater, the introduction of the non-condensable gas in the stripping tower improves 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 wastewater heater to serve as a heating heat source of the wastewater heater, 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 heater 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 80-98 ℃, preferably 85-95 ℃, and then enters a wastewater heater, and is subjected to heat exchange with stripping gas at the top of the stripping tower in the wastewater heater to 85-100 ℃, preferably 90-100 ℃, 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 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 ℃.
In the treatment process, the non-condensable gas can be any one or more of air, nitrogen and oxygen.
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 can realize 50-95% of water resource recycling. 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, and the heat required in the stripping tower is brought into the stripping tower by the noncondensable gas, so that the noncondensable gas and the wastewater are directly subjected to heat transfer, the thermal efficiency of the system is improved, and the problem of evaporation, scaling and blockage is effectively avoided.
3. The heat exchanger is arranged in the wastewater treatment process, so that excessive latent heat of the compressed steam is transferred to the non-condensable gas through heat exchange, 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.
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 including a wastewater preheater 2, a wastewater heater 4, 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 a wastewater heater 4 through a wastewater preheater 2, a wastewater outlet of the wastewater heater 4 is connected with a wastewater inlet of an evaporator 5, a gas outlet of the wastewater heater 4 is connected with a non-condensable gas inlet of a 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 gas outlet of the wastewater heater 4 and the inlet of the non-condensable gas compressor 14, 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 the inlet of the steam compressor 8, an outlet of the steam compressor 8 is divided into two paths, one path is connected with a heat source steam inlet of the evaporator 5, the other path is connected with a heat source steam inlet of the heat exchanger 24, a concentrated solution discharge port at the bottom of the evaporator 5 is connected with the wastewater, the non-condensable gas outlet of the heat exchanger 24 is connected with the gas phase inlet of the stripping tower 11, the gas phase outlet of the stripping tower 11 is connected with the heat source gas inlet of the wastewater heater 4, the concentrated solution discharge port at the bottom of the stripping tower 11 is connected with the wastewater preheater 2 through a pipeline, the condensed water outlet of the evaporator 5, the condensed water outlet of the heat exchanger 24 and the condensed water discharge port of the wastewater heater 4 are respectively connected with the condensed water inlet of the condensed water collector 20 through pipelines, and the discharge port of the condensed water collector 20 is connected with the wastewater preheater 2.
The invention also provides a wastewater treatment process, which adopts the system and comprises the following steps:
the method comprises the following steps of using a waste water preheater 2 for receiving and processing raw material waste water 1, condensed water 21 and a concentrated solution 16 of a stripping tower, wherein the raw material waste water 1, the condensed water 21 and the concentrated solution 16 of the stripping tower exchange heat in the waste water preheater 2 to obtain preheated raw material waste water 3, cooled condensed water 22 and a cooled concentrated solution 17 after processing;
a waste water heater 4 is used for treating preheated raw material waste water 3 and stripping gas 12 from the top of the stripping tower, and the preheated raw material waste water 3 and the stripping gas 12 exchange heat in the waste water heater 4 to obtain heated raw material waste water 27, condensed water 25 and non-condensable gas 13;
using an evaporator 5 for treating the raw wastewater 27 heated by the wastewater heater, wherein the 1 st material flow 6 in gas phase, the 2 nd material flow 10 in liquid phase and the condensed water 18 are obtained after treatment;
using a vapor compressor 8 for treating the 1 st stream 6 of the gas phase from the evaporator, resulting after the treatment in a 3 rd stream of the gas phase, the 3 rd stream of the gas phase being divided into a 31 st substream 9 and a 32 nd substream 26;
using a non-condensable gas compressor 14 for treating the non-condensable gas 13 from the waste water heater 4, resulting in a 4 th stream 28 in the gas phase after treatment;
using a heat exchanger 24 for treating a 32 nd substream 26 from the vapor compressor and a 4 th stream 28 of the gas phase from the non-condensable gas compressor, a 5 th stream 15 of the gas phase obtained after the treatment and the condensation water 19;
using a stripping column 11 for treating a 2 nd stream 10 from the evaporator and a 5 th stream 15 from the heat exchanger to obtain a stripping column overhead gas 12 and a stripping column concentrated solution 18, wherein the stripping gas 12 at the top of the stripping column enters a wastewater heater as a heat source;
a condensate collector is used which receives the evaporator condensate 18, the waste water heater 4 condensate 25 and the condensate 19 from the heat exchanger.
In the method, the raw material wastewater 1 is subjected to heat exchange with the condensed water 21 and the concentrated solution 16 of the stripping tower in the wastewater preheater 2 to reach a saturation temperature, then is subjected to heat exchange with the stripping gas 12 of the stripping tower to reach the saturation temperature, and then enters the evaporator 5, and is evaporated in the evaporator 5, the obtained steam is compressed by the steam compressor 8, the latent heat of the steam is increased, the compressed steam is respectively used as heat sources of the evaporator 5 and the heat exchanger 24, the concentrated solution at the bottom of the evaporator 5 enters the stripping tower 11 for stripping evaporation, the heated non-condensable gas is used as a carrier gas to enter the stripping tower 11 for stripping evaporation and concentration of the wastewater, the introduction of the non-condensable gas into the stripping tower 11 improves the mass transfer efficiency of the stripping tower 11, and the scaling and blocking of the wastewater in the stripping tower. Steam evaporated by steam stripping in the stripping tower 11 and the introduced non-condensable gas are mixed and enter the wastewater heater 4 to be used as a heating source of the wastewater heater 4, the steam is condensed into condensed water, the non-condensable gas enters the non-condensable gas compressor 14 from a non-condensable gas outlet of the heater 4 to be compressed, and the compressed non-condensable gas enters the stripping tower 11 through heating circulation. And the concentrated solution 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 ratio of the height 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
Adopt the system of figure 1, the evaporimeter adopts the device of figure 2, used waste water is FCC desulfurization waste water, mainly contains sodium sulfite, sodium sulfate and calcium carbonate salt in the waste water, and raw materials waste water contains salt concentration and is 6wt%, and raw materials waste water treatment capacity is 20t/h, and normal atmospheric temperature waste water preheats through preheater 2, heater 4 heats to 100 ℃, gets into in the evaporimeter 5. The compression ratio of the vapor compressor 8 is 1.4, and nitrogen is used as supplementary non-condensable gas. 15wt% of concentrated solution 10 is discharged from the bottom of the evaporator 5, and 24wt% of concentrated solution 17 is discharged after the concentrated solution 10 is subjected to steam stripping, evaporation and concentration by the stripping tower 11. The temperature of the condensed water 21 after heat recovery is about 45 ℃, and the recovery amount of the condensed water is 11.1 t/h.
Claims (25)
1. A wastewater treatment system comprises a wastewater preheater, a wastewater heater, an evaporator, a stripping tower, a steam compressor, a heat exchanger, a non-condensable gas compressor and a condensed water collector; wherein the waste water inlet line is connected with the waste water inlet of the waste water heater through the waste water preheater, the waste water outlet of the waste water heater is connected with the waste water inlet of the evaporator, the gas outlet of the waste water heater is connected with the non-condensable gas inlet of the heat exchanger through the non-condensable gas compressor, the steam outlet of the evaporator is connected with the inlet of the steam compressor, the outlet of the steam compressor is divided into two paths, one path of the outlet is connected with the heat source steam inlet of the evaporator, the other path of the outlet is connected with the heat source steam inlet of the heat exchanger, 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 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 gas inlet of the waste water heater, the concentrated solution discharge port at the bottom of the stripping tower is connected with The inlet is connected, and the discharge port of the condensed water collector is connected with the waste water preheater;
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 wastewater treatment system according to 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 wastewater treatment system according to claim 1, wherein: and a non-condensable gas replenishing pipeline is arranged on a connecting pipeline between a gas outlet of the wastewater heater and an inlet of the non-condensable gas compressor.
4. The wastewater treatment system according to claim 1, wherein: the non-condensable gas compressor is a volume type compressor, a turbine type compressor or a thermal type compressor.
5. The wastewater treatment system according to 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 wastewater treatment system according to claim 1 or 5, characterized in that: the waste water preheater and the heat exchanger adopt plate heat exchangers.
7. The wastewater treatment system according to claim 1, wherein: the waste water heater adopts a shell-and-tube heat exchanger or a plate-and-shell heat exchanger.
8. The wastewater treatment system according to claim 1 or 7, characterized in that: the waste water heater adopts a plate-shell type heat exchanger.
9. The wastewater treatment system according to claim 1, wherein: the stripping tower adopts a packed tower or a spray tower.
10. The wastewater treatment system according to claim 1, wherein: the stripping tower adopts a spray tower.
11. The system of claim 1, wherein: the branch material inlet pipe is detachably arranged on the liquid inlet groove.
12. 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.
13. The system of claim 12, wherein: and the impingement baffle is provided with a via hole.
14. The system of claim 12, wherein: the height ratio of the impingement plate to the depth of the liquid inlet groove is 1/3-3/5.
15. 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.
16. The system of claim 15, wherein: the overflow baffle is a cylinder, and the cross section of the overflow baffle is in an inverted L-shaped shape.
17. The system of claim 1, wherein: the evaporation tubes are uniformly arranged in the shell.
18. 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.
19. A wastewater treatment process using the wastewater treatment system according to any one of claims 1 to 18, the process comprising:
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;
the method comprises the following steps of (1) using a waste water heater for treating preheated raw material waste water and stripping gas at the top of a stripping tower, wherein the preheated raw material waste water and the stripping gas at the top of the stripping tower exchange heat in the waste water heater to obtain heated raw material waste water, condensed water and non-condensable gas;
using an evaporator for treating the raw wastewater heated by the wastewater heater to obtain a 1 st material flow of a gas phase, a 2 nd material flow of a liquid phase 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, said 3 rd stream being divided into a 31 st substream and a 32 nd substream, wherein the 31 st substream is returned to the evaporator;
using a non-condensable gas compressor for treating non-condensable gas from the waste water heater, resulting in a 4 th stream in the gas phase;
using a heat exchanger for treating the 32 nd substream from the vapor compressor and the 4 th stream from the non-condensable gas compressor, the 5 th stream of the gas phase obtained after treatment and the condensed water;
using a stripping tower for treating a 2 nd material flow from the evaporator and a 5 th material flow from the heat exchanger to obtain a stripping tower top gas and a stripping tower concentrated solution, wherein the stripping tower top gas is used as a heat source and enters a wastewater heater;
a condensate collector is used for receiving condensate from the evaporator, condensate from the waste water heater and condensate from the heat exchanger.
20. The process of claim 19, wherein: the raw material wastewater enters a wastewater heater after exchanging heat with condensed water and concentrated solution of a stripping tower in the wastewater preheater to 80-98 ℃, and then enters an evaporator after exchanging heat with stripping gas at the top of the stripping tower in the wastewater heater to 85-100 ℃.
21. The process according to claim 19 or 20, wherein: the raw material wastewater enters a wastewater heater after exchanging heat with condensed water and concentrated solution of a stripping tower in the wastewater preheater to 85-95 ℃, and then enters an evaporator after exchanging heat with stripping gas at the top of the stripping tower in the wastewater heater to 90-100 ℃.
22. The process of claim 19, wherein: the logarithmic heat exchange temperature difference between the steam and the waste water in the evaporator is 3-10 ℃, and meanwhile, the vaporization rate of the waste water in the evaporator is 5-50%.
23. The process according to claim 19 or 22, wherein: the logarithmic heat exchange temperature difference between the steam and the waste water in the evaporator is 4-8 ℃, and meanwhile, the vaporization rate of the waste water in the evaporator is 10-40%.
24. The process of claim 19, 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 ℃.
25. The process of claim 19, wherein: the non-condensable gas is any one or more of air, nitrogen and oxygen.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610991599.9A CN108069482B (en) | 2016-11-11 | 2016-11-11 | Wastewater treatment process and system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610991599.9A CN108069482B (en) | 2016-11-11 | 2016-11-11 | Wastewater treatment process and system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108069482A CN108069482A (en) | 2018-05-25 |
| CN108069482B true CN108069482B (en) | 2020-01-10 |
Family
ID=62153519
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610991599.9A Active CN108069482B (en) | 2016-11-11 | 2016-11-11 | Wastewater treatment process and system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108069482B (en) |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH1176761A (en) * | 1997-09-05 | 1999-03-23 | Jgc Corp | Treatment of ammonia-containing waste water |
| CN101811743A (en) * | 2010-04-09 | 2010-08-25 | 兰州节能环保工程有限责任公司 | Circulation evaporator |
| 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 |
| CN104986816A (en) * | 2015-02-16 | 2015-10-21 | 吴大川 | Process and apparatus for carrying out wastewater desorption and falling film evaporation on coking sewage |
| CN205061601U (en) * | 2015-08-25 | 2016-03-02 | 兰州节能环保工程有限责任公司 | Energy -efficient sewage treatment plant |
-
2016
- 2016-11-11 CN CN201610991599.9A patent/CN108069482B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH1176761A (en) * | 1997-09-05 | 1999-03-23 | Jgc Corp | Treatment of ammonia-containing waste water |
| CN101811743A (en) * | 2010-04-09 | 2010-08-25 | 兰州节能环保工程有限责任公司 | Circulation evaporator |
| 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) |
| CN104986816A (en) * | 2015-02-16 | 2015-10-21 | 吴大川 | Process and apparatus for carrying out wastewater desorption and falling film evaporation on coking sewage |
| 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 |
| CN205061601U (en) * | 2015-08-25 | 2016-03-02 | 兰州节能环保工程有限责任公司 | Energy -efficient sewage treatment plant |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108069482A (en) | 2018-05-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103387308B (en) | Multi-effect membrane distillation-multistage flash evaporation seawater desalination system | |
| CN101139119B (en) | Machine for desalination of sea water by using pressure gas flash evaporation method | |
| CN102557168B (en) | Heat-pipe low-temperature multi-effect sea water desalinating system and process flow | |
| CN101786754A (en) | Zero-emission treatment process for salt-containing wastewater | |
| WO2006094437A1 (en) | A method and an multi-effect evaporation for waste water of alkylene oxides | |
| CN105461134A (en) | Technology and device applied to recycling of high-salinity wastewater in coal chemical industry | |
| CN110422899A (en) | A kind of heat pump flash vaporization concentration systems | |
| CN104310514A (en) | Efficient mechanical vapor recompression seawater desalination method | |
| CN106629937B (en) | Wastewater treatment process and system | |
| CN110451596A (en) | A kind of carrier gas extraction HPE vapo(u)rization system | |
| CN106630338B (en) | Method and device for treating organic wastewater | |
| CN108069479B (en) | Wastewater treatment method and system | |
| CN201660457U (en) | Novel multiple-effect distilled sea water desalination device | |
| CN112960717A (en) | System for utilize oil field oil well output fluid waste heat to accomplish oil field water distillation and purification | |
| CN104724776A (en) | Device and method for mixing secondary steam into pressurized water in pressurized evaporation | |
| CN105110396A (en) | Method and device for continuously separating low-boiling point substances in wastewater produced by extraction of natural gas and shale gas | |
| CN103316588A (en) | Multiple-effect membrane distillation device and method | |
| CN106630336B (en) | Method and device for treating wastewater containing organic matters | |
| CN207891096U (en) | Photo-thermal method depressurizes the device and system of multiple-effect membrane distillation processing desulfurization wastewater | |
| CN117164037A (en) | Concentrated crystallization of high salt wastewater contains salt desalination water processing apparatus through heat pump | |
| CN108069482B (en) | Wastewater treatment process and system | |
| CN106629936B (en) | Process and system for treating wastewater | |
| CN208440312U (en) | A kind of processing system of desulfurization wastewater | |
| CN106621424A (en) | Wastewater treater | |
| CN112408528B (en) | Anti-fouling blocking and self-cleaning MVR evaporation concentration system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |