CN115806367A - Organic wastewater treatment system - Google Patents
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- CN115806367A CN115806367A CN202211621818.6A CN202211621818A CN115806367A CN 115806367 A CN115806367 A CN 115806367A CN 202211621818 A CN202211621818 A CN 202211621818A CN 115806367 A CN115806367 A CN 115806367A
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Abstract
The invention provides an organic wastewater treatment system which comprises a head tank, a sewage reactor, a first inorganic salt solution pump, a vapor phase cooler, a heater, a raw water collecting tank, a raw water pump, a second inorganic salt solution pump, a thickener, a centrifugal machine, a dryer and a filter membrane, wherein all the parts are communicated through pipelines, the head tank is connected with the sewage reactor, the sewage reactor is connected with the heater through the first inorganic salt solution pump, the heater is connected with the thickener through the second inorganic salt solution pump, a vapor outlet of the sewage reactor is connected with the raw water collecting tank through the vapor phase cooler, and the raw water collecting tank is also connected with the filter membrane through the raw water pump. The invention realizes the complete decomposition of organic waste by supercritical water oxidation, the reuse of pure water prepared from sewage by a mechanical steam recompression technology or a multi-effect evaporation energy-saving mode, the complete decomposition of organic waste in the sewage into inorganic substances and the economic recovery of inorganic salt in the sewage.
Description
Technical Field
The invention belongs to the technical field of wastewater treatment, and particularly relates to an organic wastewater treatment system.
Background
High-salt high-concentration organic wastewater can be generated in the industries of petrochemical industry, medicine, food, papermaking, textile, printing and dyeing and the like. Part of organic waste has the properties of mutagenicity, teratogenicity and carcinogenesis, seriously threatens the health and ecological safety of human beings, and the toxic organic waste water has the characteristics of high concentration, deep color, more salt content, high toxicity, strong acidity (alkalinity) and difficult degradation. The high-efficiency treatment of high-salt high-concentration organic wastewater is always a great problem in academia.
Chinese patent CN 216972050U provides a processing apparatus of high salt organic waste water, adopts the vacuum evaporation mode to evaporate organic matter and water and then decomposes the organic matter with photocatalysis, and this patent is difficult to evaporate macromolecular organic matter completely, and some chelates in the waste water also can't evaporate out, and salt sediment still has organic waste.
Chinese patent CN 115159757A provides a supercritical water gasification reaction system for high-salinity organic wastewater, which adopts supercritical water oxidation technology to solve the problem of organic waste oxidative decomposition in high-salinity wastewater, but only one concept is provided for salt slag recovery treatment and water reuse treatment, and no feasible measures are provided.
Chinese patent CN 114605018A provides a method for treating high-salt organic wastewater containing phosphorus and fluorine and recovering salt, which adopts methods such as flash evaporation phase separation, melting, dissolving, insoluble substance conversion, adsorption and the like, the flash evaporation phase separation is difficult to completely evaporate macromolecular organic substances, and simultaneously evaporated organic substances are treated by an adsorption method, and the organic substances are only adsorbed without a subsequent treatment measure, thereby bringing secondary new pollutants.
Chinese patent CN 114853220A provides a method for treating high ammonia nitrogen and high salt organic wastewater COD, the method adopts electrocatalytic oxidation and Fenton oxidation to treat organic waste, the preparation difficulty of an electrocatalytic oxidation electrode is high, the manufacturing cost is high, the multi-stage oxidation investment is large, complete oxidation is difficult to realize, and finally, the discharged slag still contains incompletely decomposed organic waste.
Chinese patent CN 110386728A is an integrated process for treating high-salinity high-COD industrial wastewater by tubular free radical oxidation, the invention partially solves the problems of wet oxidation decomposition treatment and waste heat recovery of high-salinity wastewater, but the oxidation decomposition rate of organic matters in the high-salinity wastewater is difficult to be complete, so that salt products cannot be produced as by-products, and the zero emission of resource utilization of sewage-to-pure water cannot be realized; due to the existence of unoxidized organic matters, the evaporation cooling is preposed, so that the evaporation energy consumption is high, the operation cost is high, and the complete evaporation is difficult to realize.
The invention discloses a method for desalting industrial high-salt wastewater of Chinese patent CN 110759575A, which partially solves the problems of high water recovery rate and high salt recovery rate of high-concentration degradation-resistant high-salt industrial organic wastewater treatment, and because of adopting wet oxidative decomposition treatment, the organic matter oxidative decomposition rate is caused, thereby finally realizing the zero discharge problem of resource utilization of byproduct salt products and sewage prepared pure water, and the waste heat recovery is not mentioned; the special film treatment method is placed before MVR, and the maintenance and operation cost of the special film is high and the normal operation is difficult due to the existence of salt.
Chinese patent CN 114620889A is a treatment system and process for zero discharge of electroplating comprehensive wastewater, the invention realizes the zero discharge of electroplating comprehensive wastewater, but biochemical treatment needs to culture special strains, different strains of different sewage have high cost and great technical difficulty, the biochemical treatment is placed before membrane treatment, the survival environment of the strains is worse, an evaporation system is placed after membrane treatment, and organic filter cakes (new pollutants) are produced between the evaporation system and the membrane treatment, and the existence of residual organic matters can bring high maintenance and operation cost of special membranes and is difficult to normally operate.
In summary, a scheme which can effectively treat organic matters and simultaneously realize water resource recovery and has relatively low cost is lacked at present.
Disclosure of Invention
Aiming at the problems in the prior art, the invention aims to provide an organic wastewater treatment system, which can easily and completely decompose organic wastes through supercritical water oxidation, realize inorganic salt recovery through a mechanical steam recompression technology or a multi-effect evaporation energy-saving mode, realize pure water preparation through an advanced membrane treatment technology, fully utilize the characteristics of each process of a combined new process, and efficiently realize that the sewage is prepared into pure water for recycling, the organic wastes in the sewage are completely decomposed into inorganic matters, and the inorganic salts in the sewage are economically recovered, thereby solving the problem of sewage pollution treatment and the problem of water resource recycling.
In order to achieve the purpose, the invention adopts the technical scheme that:
the utility model provides an organic wastewater treatment system, including the elevated tank, the sewage reactor, first inorganic salt solution pump, the steam phase cooler, the heater, the former water collection tank, the raw water pump, the second inorganic salt solution pump, the stiff ware, centrifuge, the desiccator, the filter membrane, through the pipeline intercommunication between each part, the elevated tank is connected with the sewage reactor, sewage reactor and heater pass through first inorganic salt solution pump connection, connect through the second inorganic salt solution pump between heater and the stiff ware, the steam outlet and the former water collection tank of sewage reactor pass through the steam phase cooler and connect, former water collection tank still passes through the raw water pump with the filter membrane and connects.
As a further improvement of the above technical solution:
the processing system also comprises a centrifugal machine and a drying machine, wherein the thickener, the centrifugal machine and the drying machine are sequentially connected.
The treatment system also comprises a reverse osmosis membrane, and a water production outlet of the filter membrane is connected with a water production inlet of the reverse osmosis membrane.
The treatment system also comprises an evaporator, a mixture outlet of the heater is connected with the evaporator, and the bottom of the evaporator is connected with the thickener through a second inorganic salt solution pump.
The treatment system further comprises a vapor compressor, and an inlet of the vapor compressor is connected with a vapor outlet of the evaporator.
The solution in the heater is heated by steam, the outlet of the steam compressor and the external steam are both connected with the steam inlet of the heater, and the condensed water outlet of the heater is connected with the raw water collecting tank.
The treatment system further comprises a lock hopper, and the bottom of the sewage reactor, the lock hopper and the first inorganic salt solution pump are connected in sequence.
The treatment system also comprises a sewage pump and an organic sewage storage tank for collecting sewage, and the organic sewage storage tank is connected with the elevated tank through the sewage pump.
The treatment system also comprises a high-pressure water pump and a deionized water tank for collecting deionized water, and the deionized water tank is connected with the elevated tank through the high-pressure water pump.
The treatment system also comprises a gas compressor and a gas purification tank for purifying air or oxygen, wherein the gas purification tank, the gas compressor and the sewage reactor are sequentially connected.
The invention has the beneficial effects that: the supercritical water oxidation is easy to completely decompose organic wastes, the mechanical steam recompression technology or the multi-effect evaporation is more energy-saving to realize inorganic salt recovery, the advanced membrane treatment technology is adopted to realize pure water preparation, the characteristics of all procedures of the combined new process are fully utilized, the sewage pure water is efficiently prepared for recycling, the organic wastes in the sewage are completely decomposed into inorganic matters, and the inorganic salts in the sewage are economically recovered, so that the sewage pollution treatment problem is solved, and the water resource recycling problem is also solved.
Drawings
FIG. 1 is a schematic process flow diagram of one embodiment of the present invention.
Detailed Description
The following detailed description of embodiments of the invention refers to the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the preferred embodiment of the invention, are given by way of illustration and explanation only, not limitation.
For ease of description, spatially relative terms such as "over 8230," "upper surface," "above," and the like may be used herein to describe the spatial positional relationship of one device or feature to other devices or features as illustrated in the figures. It will be understood that the spatially relative terms are intended to encompass different orientations of the device in use or operation in addition to the orientation depicted in the figures. For example, if a device in the figures is turned over, devices described as "above" or "on" other devices or configurations would then be oriented "below" or "under" the other devices or configurations. Thus, the exemplary terms "at 8230; \8230; 'above" may include both orientations "at 8230; \8230;' above 8230; 'at 8230;' below 8230;" above ". The device may be otherwise variously oriented (rotated 90 degrees or at other orientations) and the spatially relative descriptors used herein interpreted accordingly.
An organic wastewater treatment system is shown in figure 1 and comprises a gas purification tank 1, a gas compressor 2, an organic wastewater storage tank 3, a sewage pump 4, a deionized water tank 5, a high-pressure water pump 6, a head tank 7, a sewage reactor 8, a lock hopper 9, a first inorganic salt solution pump 10, a vapor phase cooler 11, an inorganic salt solution heater 12, an inorganic salt solution evaporator 13, a vapor compressor 14, a raw water collection tank 15, a raw water pump 16, a second inorganic salt solution pump 17, a thickener 18, a centrifuge 19, a dryer 20, a filter membrane 21 and a reverse osmosis membrane 22.
The gas purification tank 1 is used for removing a small amount of water and impurities carried by air or oxygen, a first inlet 11 and a first outlet 12 are formed in the gas purification tank 1, and the first inlet 11 is an inlet for air or oxygen. The first outlet 12 is an outlet for air or oxygen.
The gas compressor 2 is used for increasing the pressure of air or oxygen to be higher than the supercritical water pressure, namely 22-28 MPa (G), the gas compressor 2 is provided with a second inlet 21 and a second outlet 22, and the second inlet 21 is a purified air or oxygen inlet. The second outlet 22 is an outlet for air or oxygen.
The organic sewage storage tank 3 is used for storing high-salt high-concentration organic sewage raw materials, a third inlet 31 and a third outlet 32 are formed in the organic sewage storage tank 3, and the third inlet 31 is an inlet for high-salt high-concentration organic sewage to enter the organic sewage storage tank 3; the third outlet 32 is an outlet through which the high-salt and high-concentration organic sewage flows out of the organic sewage storage tank 3.
The sewage pump 4 is used for conveying the high-salinity high-concentration organic sewage in the organic sewage storage tank 3 to the high-level tank 7. The sewage pump 4 is provided with a fourth inlet 41 and a fourth outlet 42, and the fourth inlet 41 is a high-salt high-concentration organic sewage inlet; the fourth outlet 42 is a high-salt and high-concentration organic sewage outlet.
The deionized water tank 5 is used for storing deionized water raw materials, a fifth inlet 51 and a fifth outlet 52 are arranged on the deionized water tank 5, the fifth inlet 51 is a deionized water inlet, and the fifth outlet 52 is a deionized water outlet.
The high-pressure water pump 6 is used for pressurizing the deionized water in the deionized water tank 5 and conveying the deionized water to the high-level tank 7, a sixth inlet 61 and a sixth outlet 62 are arranged on the high-pressure water pump 6, the sixth inlet 61 is a deionized water inlet, and the sixth outlet 62 is a deionized water outlet.
The elevated tank 7 is used for storing the mixed high-salt high-concentration organic sewage and deionized water, and is also used as a transportation channel for conveying the high-salt high-concentration organic sewage to the sewage reactor 8 by using the high-pressure deionized water. A seventh inlet 71 and a seventh outlet 72 are arranged on the elevated tank 7, and the seventh inlet 71 is an inlet for high-salt high-concentration organic sewage and high-pressure deionized water; the seventh outlet 72 is an outlet for a mixture of high-pressure deionized water and high-salt high-concentration organic wastewater.
The sewage reactor 8 is used for oxidizing and decomposing organic wastes in the high-salt and high-concentration organic sewage into CO 2 、H 2 O and other inorganic substances. The sewage reactor 8 is provided with two inlets and two outlets, the two inlets are respectively a mixture inlet 81 and a gas inlet 82, the two outlets are respectively a vapor phase outlet 84 and an inorganic salt phase outlet 83, and the vapor phase outlet 84 and the inorganic salt phase outlet 83 are respectively arranged at the top and the bottom of the sewage reactor 8. The mixture inlet 81 is an inlet for a mixture of high-salt high-concentration organic sewage and high-pressure deionized water; the gas inlet 82 is an air or oxygen inlet; vapor phase outlet 84 is a reaction product vapor phase outlet; the inorganic salt phase outlet 83 is a reaction product inorganic salt phase outlet.
The lock hopper 9 is used for maintaining the pressure of the sewage reactor 8 and discharging inorganic salt solution, a ninth inlet 91 and a ninth outlet 92 are formed in the lock hopper 9, and the ninth inlet 91 is an inorganic salt solution inlet; the ninth outlet 92 is an inorganic salt solution outlet.
The first inorganic salt solution pump 10 is used for conveying an inorganic salt solution to the heater 12, a tenth inlet 101 and a tenth outlet 102 are arranged on the first inorganic salt solution pump 10, and the tenth inlet 101 is an inorganic salt solution inlet; the tenth outlet 102 is an outlet for inorganic salt solution.
The vapor phase cooler 11 is used for cooling the vapor phase of the sewage reaction product into condensed water. The vapor phase cooler 11 is provided with an eleventh inlet 111 and an eleventh outlet 112, wherein the eleventh inlet 111 is a vapor phase inlet; the eleventh outlet 112 is a condensed water outlet.
The heater 12 is used to heat the inorganic salt solution. The heater 12 is provided with two inlets, which are a first solution inlet 121 and a first steam inlet 122, and three outlets, which are a condensed water outlet 123, a mixture outlet 124, and a first inorganic salt outlet 125. The first solution inlet 121 is an inorganic salt solution inlet. The mixture outlet 124 is located above the first inorganic salt outlet 125.
The evaporator 13 is used for evaporating water in the inorganic salt solution and concentrating the inorganic salt solution. The evaporator 13 is provided with an inlet 131 which is a thirteenth inlet and two outlets, namely a second steam outlet 132 and a second inorganic salt outlet 133. The second inorganic salt outlet 133 is a concentrated inorganic salt solution outlet.
The vapor compressor 14 is used for raising temperature and circulating delivery of vapor, and the vapor compressor 14 is provided with an inlet and an outlet, which are a fourteenth inlet 141 and a fourteenth outlet 142 respectively.
The raw water collecting tank 15 is used for collecting condensed water of sewage reaction and evaporative crystallization, and recycling and cooling are carried out. The raw water collecting tank 15 is provided with two inlets and one outlet, the two inlets are respectively a deionized water inlet 151 and a condensed water inlet 152, and the outlet is a raw water outlet 153.
The raw water pump 16 is used for conveying raw water to the filter membrane 21, and the raw water pump 16 is provided with a raw water inlet 161 and a raw water outlet 162.
The second inorganic salt solution pump 17 is used for conveying an inorganic salt solution to the thickener 18, a seventeenth inlet 171 and a seventeenth outlet 172 are arranged on the second inorganic salt solution pump 17, and the seventeenth inlet 171 is an inorganic salt solution inlet; the seventeenth outlet 172 is an inorganic salt solution outlet.
The thickener 18 separates thick magma from low-concentration semi-finished magma by using gravity settling principle, and the thickener 18 is provided with a solution inlet 181 and a thick magma outlet 182.
The centrifuge 19 is used for centrifuging the thick magma into semi-finished crystal grains. The centrifuge 19 is provided with a centrifuge inlet 191 and a centrifuge outlet 192. The centrifugal inlet 191 is a thick crystal slurry inlet, and the centrifugal outlet 192 is a semi-finished crystal grain outlet.
The dryer 20 is used to dry the semi-finished grains into solid grains. The dryer 20 is provided with a semi-finished product grain inlet 201 and a dried grain outlet 202.
The filter membrane 21 is an ultrafiltration membrane or a nanofiltration membrane, and is used for filtering the raw water to produce water by adopting ultrafiltration or nanofiltration membrane. The filter membrane 21 is provided with an inlet and two outlets, the inlet is a filter membrane inlet 211, and the filter membrane inlet 211 is a raw water inlet. The two outlets are respectively a water production outlet 212 and a first backwashing concentrated water outlet 213.
The reverse osmosis membrane 22 is used for filtering the water produced by the filter membrane 21 by adopting the reverse osmosis membrane to produce pure water. The reverse osmosis membrane 22 is provided with an inlet and two outlets, wherein the inlet is a water production inlet 221. The two outlets are respectively a water outlet 222 and a second backwashing concentrated water outlet 223. The water from the water outlet 222 is pure or deionized water.
The elevated tank 7 is positioned above the sewage reactor 8, and the sewage reactor 8 is positioned above the lock hopper 9.
The components are connected through pipelines, and the specific connection relationship is as follows: the high-salt high-concentration organic sewage enters the organic sewage storage tank 3 through the third inlet 31, the third outlet 32 is connected with the fourth inlet 41, and the fourth outlet 42 is connected with the seventh inlet 71.
External deionized water enters the deionized water tank 5 through a fifth inlet 51, a fifth outlet 52 is connected with a sixth inlet 61, a sixth outlet 62 is connected with a seventh inlet 71, and a seventh outlet 72 is connected with a mixture inlet 81.
External air or oxygen enters the gas purification tank 1 through the first inlet 11, and the first outlet 12 is connected to the second inlet 21. The second outlet 22 is connected to the gas inlet 82. The inorganic salt phase outlet 83 is connected to the ninth inlet 91, the vapor phase outlet 84 is connected to the eleventh inlet 111, and the eleventh outlet 112 is connected to the condensed water inlet 152.
The ninth outlet 92 is connected with the tenth inlet 101, and the tenth outlet 102, the first backwash concentrated water outlet 213 and the second backwash concentrated water outlet 223 are connected with the first solution inlet 121.
Both the external steam and the fourteenth outlet 142 are connected to the first steam inlet 122, the condensed water outlet 123 is connected to the condensed water inlet 152, the first inorganic salt outlet 125 is connected to the seventeenth inlet 171, and the mixture outlet 124 is connected to the thirteenth inlet 131.
The second steam outlet 132 is connected to the fourteenth inlet 141, and the second inorganic salt outlet 133 is connected to the seventeenth inlet 171.
The external deionized water and water outlet 222 is connected with the deionized water inlet 151, the raw water outlet 153 is connected with the raw water inlet 161, the raw water outlet 162 is connected with the filter membrane inlet 211, the seventeenth outlet 172 is connected with the solution inlet 181, the thick crystal slurry outlet 182 is connected with the centrifugal inlet 191, the centrifugal outlet 192 is connected with the semi-finished crystal grain inlet 201, and the water production outlet 212 is connected with the water production inlet 221.
Based on the structure, the invention firstly adopts supercritical water oxidation technology, combines the high COD characteristic of high-salt high-concentration organic wastewater and adopts an auto-thermal mode to completely decompose organic waste into CO 2 、H 2 And the generated steam phase is cooled to be used as raw water, the inorganic salt phase adopts a mechanical steam recompression technology or multi-effect evaporation to realize evaporation crystallization and drying of inorganic salt to recover inorganic salt, the supercritical water oxidation raw water and evaporation crystallization condensed water are all used as raw water of a water ultrafiltration membrane, a nanofiltration membrane and a reverse osmosis membrane, pure water preparation is completed through advanced membrane filtration to be recycled, backwashing concentrated water of the ultrafiltration membrane, the nanofiltration membrane and the reverse osmosis membrane returns to the mechanical steam recompression technology or the multi-effect evaporation process to recover the inorganic salt, so that the harmless treatment of sewage is completed, and the resource utilization of preparing pure water from sewage is also completed, so that the cyclic utilization of water resources is realized.
Based on the structure, the working principle and the process of the invention are as follows:
step 1: the high-salt high-concentration organic wastewater is collected and stored and is transferred to the upper tank 7.
In this step, the high-concentration and high-salinity sewage enters the organic sewage storage tank 3 through the third inlet 31, and then is conveyed to the high-level tank 7 through the sewage pump 4.
Step 2: deionized water is collected and stored and is transferred to the head tank 7, and the deionized water and the high-salt and high-concentration organic wastewater in the head tank 7 are sent to the wastewater reactor 8.
In this step, external deionized water enters the deionized water tank 5 through the fifth inlet 51, is conveyed by the high-pressure water pump 6, is sent into the head tank 7, and simultaneously pressurizes the high-salt and high-concentration sewage in the head tank 7 to 22-28 MPa (G), and enters the sewage reactor 8 after being mixed.
In this embodiment, when the pressure in the head tank 7 reaches or exceeds the critical pressure condition of supercritical water (i.e., 22-28 MPa (G)), the mixture of high-salt and high-concentration organic wastewater and deionized water enters the wastewater reactor 8 through the mixture inlet 81.
And 3, step 3: the outside air or oxygen is purified and pumped into the sewage reactor 8.
In the step, external air or oxygen enters the gas purification tank 1 through the first inlet 11 for purification, the purified air or oxygen is compressed to 22-28 MPa (G) through the gas compressor 2, and the compressed air or oxygen enters the sewage reactor 8.
In this embodiment, when the pressure of the air or oxygen pressurized by the gas compressor 2 reaches or exceeds the supercritical water critical pressure condition (i.e., 22 to 28MPa (G)), the air or oxygen enters the sewage reactor 8 through the gas inlet 82.
And 4, step 4: and reacting the sewage in the sewage reactor 8 to obtain inorganic salt solution and steam.
The temperature in the sewage reactor 8 is raised to 350-400 ℃ by adopting electric heating or other high-temperature heat sources, and the sewage reaction starts at the moment. Under the condition of supercritical water oxidation, organic wastes in the high-salt high-concentration organic sewage are quickly and completely decomposed into inorganic matters, a steam phase is discharged from a steam phase outlet 84, and an inorganic salt phase is discharged from an inorganic salt phase outlet 83. After the reaction in the sewage reactor 8 normally runs, the reaction in the sewage reactor 8 is an exothermic reaction, and the generated reaction heat can maintain the supercritical water oxidation reaction of the organic wastes in the sewage without external electric heating or heating by other high-temperature heat sources.
The inorganic salt solution and the steam generated in the sewage reactor 8 enter different devices to be treated respectively, wherein the steps 51 to 81 are the treatment step of the inorganic salt solution, and the steps 52 to 82 are the treatment step of the steam.
Step 51: evaporating and crystallizing the inorganic salt solution to obtain a concentrated inorganic salt solution.
Inorganic salt phase generated in the sewage reactor 8 is discharged from the inorganic salt phase outlet 83, enters the lock hopper 9 from the ninth inlet 91, and is discharged from the ninth outlet 92, and the inorganic salt solution in the lock hopper 9 is conveyed to the heater 12 by the first inorganic salt solution pump 10 to be heated. The inorganic salt solution enters the heater 12 from the first solution inlet 121.
The heater 12 is a dividing wall heater. The inorganic salt solution is heated by steam in a heater 12, wherein one part of the steam used for heating in the heater 12 comes from a low-pressure steam pipe network (0.5 MPa (G)) of the system, and the other part of the steam comes from secondary steam after temperature rise of a steam compressor 14. The external steam and the steam from the steam compressor 14 enter the heater 12 through the first steam inlet 122, the temperature of the external steam and the steam is reduced to condensate after the heat is released, and the condensate flows out of the condensate outlet 123 and enters the raw water collection tank 15 through the condensate inlet 152.
The inorganic salt solution in the heater 12 is heated, the inorganic salt solution is heated to generate steam and concentrated inorganic salt solution, the generated steam carries the inorganic salt out of the mixture outlet 124 and enters the evaporator 13 through the thirteenth inlet 131, and the concentrated inorganic salt solution generated in the heater 12 flows out of the first inorganic salt outlet 125 at the bottom and is sent into the thickener 18 from the solution inlet 181 through the second inorganic salt solution pump 17.
The inorganic salt solution and steam entering the evaporator 13 are further evaporated and crystallized in the evaporator 13 to form a semi-finished inorganic salt crystal slurry, and the semi-finished inorganic salt crystal slurry is discharged from the second inorganic salt outlet 133 and is sent into the thickener 18 from the solution inlet 181 through the second inorganic salt solution pump 17.
The vapor in the evaporator 13 is discharged from the second vapor outlet 132, enters the vapor compressor 14 from the fourteenth inlet 141, and the vapor compressor 14 compresses and heats the entering vapor and sends the compressed vapor to the heater 12.
Step 61: the semi-finished magma is separated in a thickener 18 to obtain a thick magma.
In this step, the semi-finished slurry is separated from the low-concentration semi-finished slurry in the thickener 18 by using the gravity settling principle, and then discharged from the thick slurry outlet 182 at the bottom of the thickener 18.
Step 71: semi-finished grains are prepared in centrifuge 19.
In this step, the thick magma enters the centrifuge 19 from the centrifugal inlet 191 at the upper part of the centrifuge 19, and the thick magma is further centrifuged to remove water under the action of centrifugal force, so as to obtain semi-finished product crystal grains.
Step 81: drying, granulating and packaging the semi-finished product crystal grains.
The semi-finished product crystal grains enter the dryer 20 from a semi-finished product crystal grain inlet 201 at the top of the dryer 20, and are deeply dried in the dryer 20 to obtain inorganic salt particles, and the inorganic salt particles flow out of a dried crystal grain outlet 202 at the bottom of the dryer 20 and are packaged.
Step 52: the steam from the vapor phase outlet 84 of the sewage reactor 8 meets the condensed water cooled by the vapor phase cooler 11 and the condensed water formed in the heater 12, and then enters the raw water collecting tank 15 through the condensed water inlet 152 of the raw water collecting tank 15 as raw water, and meanwhile, the external normal temperature deionized water enters the raw water collecting tank 15 through the deionized water inlet 151.
In this step, the temperature in the raw water collection tank 15 is adjusted to not higher than 37 ℃.
Step 62: the water in the raw water collection tank 15 is sent to the filter membrane 21 by the raw water pump 16.
Step 72: the produced water in the filter membrane 21 enters the reverse osmosis membrane 22 from the produced water outlet 212 through the produced water inlet 221, the generated backwashing concentrated water is discharged from the first backwashing concentrated water outlet 213, enters the heater 12 from the first solution inlet 121,
step 82: pure water (or deionized water) generated in the reverse osmosis membrane 22 is discharged to the system for recycling through the water outlet 222, enters the raw water collecting tank 15 through the deionized water inlet 151, and backwash concentrated water generated in the reverse osmosis membrane 22 is discharged through the second backwash concentrated water outlet 223 and enters the heater 12 through the first solution inlet 121.
Preferably, the backwash concentrated water generated by the filter membrane 21 and the backwash concentrated water generated by the reverse osmosis membrane 22 are merged and then discharged into the heater 12.
In the embodiment, the experiment is developed for the high-salt and high-concentration organic sewage with the high TOC content of 8000-200000 mg/L, the TOC in the inorganic salt particles is not measured, the total content of pure water metal ions is not higher than 10 microgram/L, so that the high-salt and high-concentration organic sewage can be seen, the organic sewage is almost completely decomposed, the membrane technology well completes membrane high-efficiency separation on the premise that supercritical water oxidation and evaporative crystallization sequentially carry out deep treatment on the high-salt and high-concentration organic sewage, the sewage is prepared into pure water for recycling, meanwhile, inorganic salt and miscellaneous salt crystal grains are byproduct, and the sewage recycling utilization is realized.
The mechanical steam recompression technology or multi-effect evaporation can well realize the evaporative crystallization of inorganic salt, but the organic matter with high suspended matter content and high boiling point in the sewage causes the problems of equipment blockage, low evaporation efficiency, high operation cost and the like, and the equipment paralysis can occur in severe cases, so that the large high boiling point molecular organic matter which is difficult to decompose by the common oxidation technology can be completely decomposed by adopting supercritical water oxidation at first, and the suspended matter is effectively removed. The advanced membrane technology can work efficiently on the premise that the COD (chemical oxygen demand) of raw water is not more than 50ppm, the concentration of filtered ions is not more than 100ppm, the membrane technology can run stably and efficiently for a long period under the condition, the service life of the membrane is greatly prolonged, so that most of inorganic salts are concentrated into concentrated solution by adopting a mechanical steam recompression technology or a multi-effect evaporation evaporative crystallization technology, then solid packaging is carried out after thickening, crystallization and drying, condensed water is used as raw water, and only soluble trace ions carried by the evaporated solution are contained (the content of the trace ions in the raw water is far less than 100 ppm).
Finally, it must be said here that: the above embodiments are only used for further detailed description of the technical solutions of the present invention, and should not be understood as limiting the scope of the present invention, and the insubstantial modifications and adaptations made by those skilled in the art according to the above descriptions of the present invention are within the scope of the present invention.
Claims (10)
1. The utility model provides an organic wastewater treatment system, a serial communication port, including elevated tank (7), sewage reactor (8), first inorganic salt solution pump (10), steam phase cooler (11), heater (12), former water collection tank (15), former water pump (16), second inorganic salt solution pump (17), stiff ware (18), centrifuge (19), desiccator (20), filter membrane (21), through the pipeline intercommunication between each part, elevated tank (7) and sewage reactor (8) are connected, sewage reactor (8) and heater (12) are connected through first inorganic salt solution pump (10), connect through second inorganic salt solution pump (17) between heater (12) and stiff ware (18), the steam outlet and former water collection tank (15) of sewage reactor (8) are connected through steam phase cooler (11), former water collection tank (15) still pass through former water pump (16) with filter membrane (21) and are connected.
2. The processing system of claim 1, wherein: the treatment system further comprises a centrifugal machine (19) and a drying machine (20), and the thickener (18), the centrifugal machine (19) and the drying machine (20) are sequentially connected.
3. The processing system of claim 1, wherein: the treatment system also comprises a reverse osmosis membrane (22), and a water production outlet (212) of the filter membrane (21) is connected with a water production inlet (221) of the reverse osmosis membrane (22).
4. The processing system of claim 1, wherein: the treatment system further comprises an evaporator (13), the mixture outlet (124) of the heater (12) is connected with the evaporator (13), and the bottom of the evaporator (13) is connected with the thickener (18) through a second inorganic salt solution pump (17).
5. The processing system of claim 4, wherein: the treatment system further comprises a vapor compressor (14), and an inlet of the vapor compressor (14) is connected with a vapor outlet of the evaporator (13).
6. The processing system of claim 5, wherein: the solution in the heater (12) is heated by steam, the outlet of the steam compressor (14) and external steam are both connected with the steam inlet of the heater (12), and the condensed water outlet (123) of the heater (12) is connected with the raw water collecting tank (15).
7. The processing system of claim 1, wherein: the treatment system further comprises a lock hopper (9), and the bottom of the sewage reactor (8), the lock hopper (9) and the first inorganic salt solution pump (10) are sequentially connected.
8. The processing system of claim 1, wherein: the treatment system also comprises a sewage pump (4) and an organic sewage storage tank (3) for collecting sewage, wherein the organic sewage storage tank (3) is connected with the elevated tank (7) through the sewage pump (4).
9. The processing system of claim 1, wherein: the treatment system further comprises a high-pressure water pump (6) and a deionized water tank (5) for collecting deionized water, and the deionized water tank (5) is connected with the elevated tank (7) through the high-pressure water pump (6).
10. The processing system of claim 1, wherein: the treatment system further comprises a gas compressor (2) and a gas purification tank (1) for purifying air or oxygen, and the gas purification tank (1), the gas compressor (2) and the sewage reactor (8) are connected in sequence.
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