CN214936766U - Phenol ammonia sewage single tower processing system - Google Patents
Phenol ammonia sewage single tower processing system Download PDFInfo
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- CN214936766U CN214936766U CN202121270181.1U CN202121270181U CN214936766U CN 214936766 U CN214936766 U CN 214936766U CN 202121270181 U CN202121270181 U CN 202121270181U CN 214936766 U CN214936766 U CN 214936766U
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Abstract
The utility model discloses a phenol ammonia sewage single tower processing system, including the single tower of strip and with the pretreatment equipment of the single tower import intercommunication of strip, the liquid outlet of the single tower of strip has connected gradually extraction tower and phenol tower through the pipeline, and the gas-liquid export of the single tower of strip communicates ammonia segregation system after water tower reboiler and water tower cauldron extraction liquid heat transfer. The utility model discloses the system makes phenol ammonia sewage earlier through the treatment of pretreatment equipment, gets rid of impurity such as light oil, heavy oil, dust in the sewage, alleviates the burden of follow-up treatment equipment and avoids the pipe blockage, obtains pretreatment sewage. The pretreatment sewage is deacidified and deaminated by adopting a stripping single tower, and high-temperature ammonia-containing water vapor is extracted from a side line to be used as a heat source of a reboiler of a water tower, so that the energy consumption is reduced, and the ammonia-containing water vapor is subjected to three-stage fractional condensation to obtain high-concentration ammonia gas. The system device is simple and reasonable, can avoid pipeline blockage, realize high-purity recovery of phenol ammonia and the extracting agent, can fully utilize heat energy, and reduces equipment investment and operating cost.
Description
Technical Field
The utility model belongs to the technical field of waste water treatment, specifically be a phenol ammonia sewage single tower processing system.
Background
The coal pyrolysis wastewater treatment is a relatively difficult treatment recognized in the wastewater treatment industry, wherein the wastewater generated in the process of carbonizing a product coke by coal at a high temperature is called coal gasification phenol-ammonia wastewater or phenol-ammonia wastewater, the coal gasification phenol-ammonia wastewater or phenol-ammonia wastewater contains a large amount of different organic matters, COD (chemical oxygen demand) reaches 30000 or even higher, the COD is difficult to directly pass through biochemical treatment, and the biochemical treatment is carried out after the COD is reduced by pretreatment. At present, a pretreatment process route of oil removal, deacidification and deamination, extraction and dephenolization and solvent recovery in an air flotation tank is generally adopted in the industry, and finally biochemical treatment is carried out. However, from the actual operation condition of an industrial device, the effect is not ideal, and the top of the deacidification deamination tower in the traditional process adopts raw material sewage as a feed stream, and a large amount of free ammonia-containing substances in the raw material sewage cause the ammonia content in the acid gas to be higher under the blowing and stripping action of the acid gas extracted from the top of the deacidification deamination tower, so that a gas phase pipeline at the top of the deacidification deamination tower is frequently blocked; in addition, steam consumption of deacidification and deamination, extraction and dephenolization and solvent recovery is large, energy consumption is high, and operation cost is high.
Application number CN201611176828.8 discloses coal gasification waste water phenol ammonia recovery process in patent document, it is proposed that aqueous ammonia steam of sour water stripper side extraction is used as the heat source of phenol tower and solvent stripper reboiler in proper order, in order to reach energy-conserving purpose, but sour water stripper top steam ammonia content that 1.5Mpa medium pressure steam made the heat source setting is high, the temperature is relatively low, for satisfying the heat demand of phenol tower, it needs to improve sour water stripper operating pressure to 2Mpa in advance, thereby rise the temperature that the side extraction ammonia steam, make it possess the condition as phenol tower bottom heat source, this pressurization operation has increased the degree of difficulty and has not reached real energy-conserving purpose.
Patent document No. 202011355473.5 discloses a pretreatment method of coal chemical wastewater, which can save energy by collecting steam from the upper side of a deamination tower and using the steam as a heat source of a reboiler of a water tower of a solvent/phenol recovery system, but adopts a double-tower stripping process, i.e. deacidification ammonia is separately arranged, so that the device is more, the energy consumption is naturally higher, and the energy-saving effect is not obvious even if energy is saved.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the problems existing in the prior art and provide a phenol ammonia sewage single-tower treatment system. The utility model discloses system's device is simple reasonable, can avoid the pipeline to block up, realize the high-purity recovery of phenol ammonia and extractant, again can heat utilization abundant, reduce equipment investment and running cost.
In order to achieve the purpose, the utility model provides a phenol ammonia sewage single tower processing system, specifically as follows:
the single-tower treatment system for the phenol-ammonia sewage comprises a stripping single tower and pretreatment equipment communicated with an inlet of the stripping single tower, wherein a liquid outlet of the stripping single tower is sequentially connected with an extraction tower and a phenol tower through a pipeline, and a gas-liquid outlet of the stripping single tower is communicated with an ammonia gas fractional condensation system after heat exchange with produced liquid of a tower kettle of the water tower through a water tower reboiler.
Adopt above-mentioned technical scheme for the steam that contains ammonia that steam strip single-tower gas-liquid outlet was adopted provides the heat source for the water tower through the heat transfer of water tower reboiler, also make the water tower provide the cold source for containing ammonia through the heat transfer of water tower reboiler, the heat source that has both saved the water tower is supplied with, the cold source that also has saved containing ammonia steam is supplied with, 5 ~ 10 tons of refrigeration cycle water per hour can be practiced thrift in ton sewage treatment promptly, 50 ~ 100 kilograms of consumption of heating steam per hour can be practiced thrift in ton sewage treatment simultaneously, and like this after the hot-cold stream coupling, still save the investment of a heat exchanger.
Further, a gas outlet at the top of the stripping single tower is communicated with a tail gas treatment device, the tail gas treatment device is used for treating the extracted acidic gases such as carbon dioxide and hydrogen sulfide to avoid environmental pollution, and preferably, the tail gas treatment device is a sulfur production device, so that the environmental pollution can be avoided, and waste can be changed into valuable.
Further, the pretreatment equipment comprises one or more of an oil separation tank, a coalescer and macroporous resin.
Furthermore, a modified material is arranged in the pretreatment equipment, and the modified material has an oleophylic and hydrophobic effect, so that the separation of oil and water in the phenol ammonia wastewater is accelerated.
Furthermore, the pretreatment equipment is provided with a dosing port, a light oil outlet, a heavy oil outlet and a pretreatment water outlet.
By adopting the technical scheme, the phenol ammonia sewage pretreatment medicine is added into the pretreatment equipment through the medicine adding port, and the light oil, the heavy oil and the pretreatment sewage which are treated and separated by the pretreatment equipment are discharged through the light oil outlet, the heavy oil outlet and the pretreatment water outlet respectively. The phenol ammonia sewage can be treated by the pretreatment equipment, impurities such as light oil, heavy oil, dust and the like can be removed, the burden of subsequent treatment equipment is reduced, the pollution and blockage of pipelines are avoided, and the light oil and the heavy oil in the sewage can be used as byproducts to be barreled and reused.
Furthermore, the inlet of the stripping single tower comprises an upper feed inlet and a middle-upper feed inlet, the pretreatment water outlet of the pretreatment equipment is communicated with the upper feed inlet of the stripping single tower through a first cooler, and the pretreatment water outlet of the pretreatment equipment is communicated with the middle-upper feed inlet of the stripping single tower through a first heat exchanger.
By adopting the technical scheme, the pretreatment water discharged from the pretreatment water outlet on the pretreatment equipment is divided into cold feed and hot feed, wherein the cold feed is cooled by the first cooler and then fed from the upper feed inlet of the stripping single tower, and the hot feed is subjected to heat exchange with the produced liquid in the kettle of the stripping single tower by the first heat exchanger and then fed from the middle upper feed inlet of the stripping single tower. Through two feeding processes of cold and hot, a large amount of free ammonia-containing substances contained in phenol ammonia sewage directly serving as a feeding stream are reduced, and the phenomenon that a gas phase pipeline at the top of a stripping single tower is frequently blocked due to the fact that the content of ammonia in acid gas is high under the blowing and stripping action of the acid gas extracted from the top of the stripping single tower is avoided.
Wherein the operating pressure of the stripping single tower is 0.2-0.6 MPa. The operation pressure is small and easy to set and control.
The feeding temperature of the upper feeding hole of the single stripping tower is not more than 30 ℃, preferably 20-30 ℃, and more preferably 25-30 ℃, the lower the cold feeding temperature is, the better the separation efficiency of the tower is, the lower the ammonia content of the acid gas discharged from the top of the single stripping tower is, and when the cold feeding temperature is 25-30 ℃, the ammonia content of the acid gas discharged from the top of the single stripping tower is less than or equal to 500 ppm.
Wherein the feeding temperature of a feeding hole at the middle upper part of the stripping single tower is 125-150 ℃.
Wherein the volume ratio of the cold feed to the hot feed is 1: 1-1: 10.
Furthermore, the inlet of the single stripping tower also comprises a top feeding hole, and the top feeding hole is used for allowing external desalted water as a cooling material to enter the single stripping tower so as to greatly reduce the content of ammonia in the acid gas extracted from the top of the single stripping tower, so that the content of the ammonia in the acid gas is less than or equal to 300 ppm.
Further, the number of the extraction towers is preferably 1-3, an extract outlet is formed in the top of each extraction tower, a sewage feed inlet is formed in the upper portion of each extraction tower, an extractant inlet is formed in the lower portion of each extraction tower, a dephenolized sewage outlet is formed in the bottom of each extraction tower, a liquid outlet of each stripping single tower is communicated with a sewage feed inlet of the first extraction tower through the first heat exchanger and the second cooler, a dephenolized sewage outlet of the first extraction tower is communicated with a sewage feed inlet of the second extraction tower, and the like until a dephenolized sewage outlet of the last extraction tower exchanges heat with the produced liquid of the tower kettle through the second heat exchanger and then feeds the liquid from the feed inlet of the water tower.
Wherein the extraction stages of the extraction tower are 1-5, and the stages of the extraction towers can be the same or different.
Wherein the feeding temperature of a sewage feeding hole of the first extraction tower is 30-60 ℃.
The temperature of the extraction tower is 20-65 ℃, preferably 25-50 ℃, the pressure is normal pressure, and the pH value is 3-11.
Wherein the ratio of the feeding sewage to the dosage of the extracting agent in the extracting tower is 1: 1-1: 10, and the proportion of each extracting tower can be the same or different.
Wherein the extractant is fresh extractant which is in countercurrent contact with the sewage, and cross-flow cascade is formed between the extraction tower and the extraction tower. The fresh extractant is newly purchased extractant, regenerated extractant or mixture of the two.
Wherein the extracting agent is one or more of methyl isobutyl ketone and diisopropyl ether.
Furthermore, extract outlets of the extraction tower are communicated with a feed inlet of the phenol tower through a third heat exchanger, an extractant outlet is formed in the top of the phenol tower, a phenol outlet is formed in the bottom of the phenol tower, the extractant outlet is communicated with an extractant circulating groove through the third heat exchanger and a third cooler, and the extractant circulating groove is communicated with an extractant inlet in the lower portion of the extraction tower.
By adopting the technical scheme, the high-purity extractant is extracted from the extractant outlet of the phenol tower, and flows into the extractant circulating tank automatically after being subjected to heat exchange by the third heat exchanger and cooling by the third cooler, so that the extractant can be returned to the extraction tower for recycling; crude phenol is extracted from a phenol outlet at the bottom of the phenol tower and is taken as a byproduct to be sent out of the device.
Wherein the feeding temperature of the feeding port of the phenol tower is 70-130 ℃.
Wherein the reflux ratio of the phenol tower is 0.1-1.
The top temperature of the phenol tower is 60-120 ℃, the bottom temperature of the phenol tower is 150-210 ℃, the pressure of the phenol tower is-0.01-0.02 MPa, and the operation can be normal pressure operation or negative pressure operation. If the negative pressure operation is about 10 percent of energy saving.
Further, the water tower top is equipped with azeotrope export, upper portion is equipped with feed inlet and backward flow mouth, the bottom is equipped with the export of preliminary treatment water, the azeotrope export of water tower through first partial condensate cooler, backflow jar with the backward flow mouth intercommunication of water tower, the backflow jar passes through the third cooler with the extraction agent circulation groove intercommunication, the export of preliminary treatment water of water tower passes through second heat exchanger, water tower cauldron liquid cooler with the top feed inlet intercommunication of steam stripping single tower.
By adopting the technical scheme, the azeotrope of the extracting agent and the water is extracted from the azeotrope outlet of the water tower, and the azeotrope enters the reflux tank after being cooled by the first condensate cooler. Layering the extractant and the water in a reflux tank, extracting the extractant from the upper layer, and allowing the extractant to enter an extractant circulating tank through a third cooler to be recovered; the lower layer produced water is used as reflux liquid and returns to the tower through a reflux port of the water tower, and the extraction agent is fully recovered through the arrangement. In addition, the outlet of the pretreated water is communicated with the top feed inlet of the stripping single tower through a second heat exchanger and a water tower bottom cooler, so that a small part of the pretreated effluent is used as a cooling material at the top of the stripping single tower, the content of ammonia in the acidic gas extracted from the top of the stripping single tower is greatly reduced, the content is less than or equal to 300ppm, and the use of external desalted water as the top feed of the stripping single tower is reduced or even avoided.
Wherein the feeding temperature of the feeding port of the water tower is 50-100 ℃.
Wherein the tower top temperature of the water tower is 60-100 ℃.
Wherein the temperature of a tower kettle of the water tower is 101-110 ℃.
Further, the ammonia gas fractional condensation system comprises a first-stage fractional condenser, a first-stage flash evaporator, a second-stage fractional condenser, a second-stage flash evaporator and a third-stage fractional condenser which are sequentially connected, and liquid outlets of the first-stage fractional condenser, the second-stage fractional condenser and the third-stage fractional condenser are communicated with the pretreatment equipment through a second fractional condensation liquid cooler.
Furthermore, the operating pressure of the first-stage partial condenser is 0.4-0.5 MPa, the temperature is 125-140 ℃, the pressure of the second-stage partial condenser is 0.3-0.4 MPa, the temperature is 80-100 ℃, the pressure of the third-stage partial condenser is 0.2-0.3 MPa, and the temperature is 30-60 ℃; the parameter setting ensures that the content of hydrogen sulfide in ammonia gas is less than or equal to 300ppm and the content of ammonia gas is more than or equal to 98 percent.
The utility model discloses following beneficial effect has:
1. the utility model relates to a phenol ammonia sewage single tower processing system can get rid of impurity such as light oil, heavy oil, dust after with phenol ammonia sewage treatment through the setting of pretreatment equipment, alleviates the burden of follow-up treatment facility, avoids the dirty stifled of pipeline, can also carry out the barrelling with light oil, heavy oil in the sewage as the by-product and recycle. And the heat exchange of the ammonia-containing water vapor extracted from the gas-liquid outlet of the stripping single tower is performed through the water tower reboiler to provide a heat source for the water tower, and the heat exchange of the water tower through the water tower reboiler is performed to provide a cold source for the ammonia-containing water vapor, so that the heat source supply of the water tower is saved, the cold source supply of the ammonia-containing water vapor is also saved, 5-10 tons of cooling circulating water per hour can be saved in ton sewage treatment, meanwhile, the consumption of heating steam per hour of 50-100 kilograms per hour can be saved in ton sewage treatment, the steam consumption is at least saved by 15%, and the investment of one heat exchanger is saved after the hot-cold streams are coupled. In addition, the larger the flow of the ammonia-containing water vapor extracted from the side line is, the better the water quality purification effect is, but in order to reduce the increase of the energy consumption of the tower, the flow of the ammonia-containing water vapor extracted from the side line of the stripping single tower is set to be 5-20% of the total feeding flow of the stripping single tower, so that the ammonia content in the total feeding flow is larger, the water quality purification effect is good, and the tower consumption is low. Solves the problems of easy blockage of pipelines, high energy consumption and high operating cost.
2. The utility model relates to a phenol ammonia sewage single tower processing system, it is cold through the single tower of strip, two hot strands of feeding, and simultaneously with the export of preliminary treatment water through the second heat exchanger, water tower cauldron liquid cooler and the top feed inlet intercommunication of the single tower of strip, make a small part of preliminary treatment water outlet as the feeding of the single tower top of strip, a large amount of free state ammoniated substance that messenger phenol ammonia sewage directly contains as the incoming stream reduces, the acidic gas who has avoided adopting at the single tower top of strip blows off under the effect, the ammonia content in the acidic gas is great, make the problem of the frequent jam of the single tower top of strip gaseous pipeline, and make the ammonia volume of collecting big, it obtains high-concentration ammonia to handle through tertiary segregation.
Drawings
FIG. 1 is a schematic diagram of a single tower treatment system for phenol-ammonia wastewater.
In the figure: 1. stripping in a single column; 2. an extraction tower; 3. a tail gas treatment device; 4. a phenol column; 5. a water tower; 6. pretreatment equipment; 7. a first cooler; 8. a first heat exchanger; 9. a second cooler; 10. a third heat exchanger; 11. a third cooler; 12. an extractant circulation tank; 13. a first condensate cooler; 14. a reflux tank; 15. a water tower reboiler; 16. a second heat exchanger; 17. a first-stage dephlegmator; 18. a secondary dephlegmator; 19. a third-stage dephlegmator; 20. a primary flash evaporator; 21. a secondary flash evaporator; 22. a second condensate cooler; 23. a water tower bottom liquid cooler.
Detailed Description
The present invention will be described in detail with reference to the accompanying drawings and examples.
Example 1
A phenol-ammonia sewage single-tower treatment system is shown in figure 1 and comprises a stripping single tower 1 and pretreatment equipment 6 communicated with an inlet of the stripping single tower 1, wherein a liquid outlet of the stripping single tower 1 is sequentially connected with an extraction tower 2 and a phenol tower 4 through pipelines, and a gas-liquid outlet of the stripping single tower 1 is communicated with an ammonia gas fractional condensation system after exchanging heat with a tower kettle produced liquid of a water tower 5 through a water tower reboiler 15.
Specifically, as shown in fig. 1, an air outlet at the top of the stripping single tower 1 is communicated with a tail gas treatment device 3, the tail gas treatment device 3 is used for treating acidic gases such as extracted carbon dioxide and hydrogen sulfide to avoid environmental pollution, and preferably, the tail gas treatment device 3 is a sulfur production device, so that not only can the environment be prevented from being polluted, but also waste can be changed into valuable.
Specifically, as shown in fig. 1, the pretreatment equipment 6 is provided with a chemical feeding port, a light oil outlet, a heavy oil outlet and a pretreatment water outlet. The phenol ammonia sewage pretreatment medicine is added into the pretreatment equipment 6 through the medicine adding port, and the light oil, the heavy oil and the pretreatment sewage which are treated and separated by the pretreatment equipment 6 are discharged through the light oil outlet, the heavy oil outlet and the pretreatment water outlet respectively. In addition, the pretreatment equipment 6 is internally provided with a modified material which has oleophylic and hydrophobic functions, so that the oil and water separation in the phenol ammonia wastewater is accelerated.
Specifically, as shown in fig. 1, the inlet of the stripping single tower 1 comprises an upper feed inlet, a middle upper feed inlet and a top feed inlet, the pretreatment water outlet of the pretreatment equipment 6 is communicated with the upper feed inlet of the stripping single tower 1 through a first cooler 7, and the pretreatment water outlet of the pretreatment equipment 6 is also communicated with the middle upper feed inlet of the stripping single tower 1 through a first heat exchanger 8. The top feed inlet is used for feeding external desalted water serving as a cooling material into the single stripping tower 1 so as to greatly reduce the content of ammonia in the acid gas extracted from the top of the single stripping tower 1.
Specifically, as shown in fig. 1, the number of the extraction towers 2 is two, the extraction towers 2 are all provided with extract outlets at the tops, sewage feed inlets are arranged at the upper parts, extractant inlets are arranged at the lower parts, dephenolized sewage outlets are arranged at the bottoms, the liquid outlet of the single stripping tower 1 is communicated with the sewage feed inlet of the first extraction tower 2 through a first heat exchanger 8 and a second cooler 9, the dephenolized sewage outlet of the first extraction tower 2 is communicated with the sewage feed inlet of the second extraction tower 2, and the dephenolized sewage outlet of the second extraction tower 2 is fed from the upper feed inlet of the water tower 5 after exchanging heat with the produced liquid in the tower bottom of the water tower 5 through a second heat exchanger 16.
Specifically, as shown in fig. 1, the extract outlets of the extraction tower 2 are all communicated with the feed inlet of the phenol tower 4 through a third heat exchanger 10, the top of the phenol tower 4 is provided with an extractant outlet, the bottom of the phenol tower 4 is provided with a phenol outlet, the extractant outlet of the phenol tower 4 is communicated with an extractant circulation tank 12 through the third heat exchanger 10 and a third cooler 11, and the extractant circulation tank 12 is communicated with the extractant inlet of the extraction tower 2.
Specifically, as shown in fig. 1, an azeotrope outlet is arranged at the top of the water tower 5, a feed inlet and a reflux port are arranged at the upper part of the water tower 5, and a pretreated water outlet is arranged at the bottom of the water tower 5, the azeotrope outlet of the water tower 5 is communicated with the reflux port of the water tower 5 through a first condensate cooler 13 and a reflux tank 14, and the reflux tank 14 is communicated with an extractant circulating tank 12 through a third cooler 11; the pretreated water outlet is communicated with the top feed inlet of the stripping single tower 1 through a second heat exchanger 16 and a water tower bottom liquid cooler 23.
Specifically, as shown in fig. 1, the ammonia partial condensation system comprises a first partial condenser 17, a first flash evaporator 20, a second partial condenser 18, a second flash evaporator 21 and a third partial condenser 19 which are connected in sequence, and liquid outlets of the first partial condenser 17, the second partial condenser 18 and the third partial condenser 19 are communicated with the pretreatment equipment 6 through a second partial condensation liquid cooler 22.
The utility model relates to a phenol ammonia sewage single tower processing system concrete working process as follows:
s1 pretreatment:
the phenol ammonia sewage firstly enters the pretreatment equipment 6 at a temperature of 25-60 ℃, and then is treated by the pretreatment equipment 6 to respectively obtain light oil, heavy oil and pretreatment sewage.
S2 deacidification ammonia treatment:
the pretreatment sewage obtained in the step of S1 pretreatment is divided into cold and hot feed, wherein the cold feed is cooled to 20-30 ℃ by a first cooler 7 and then enters the stripping single tower 1 from a feed inlet at the upper part of the stripping single tower 1;
the hot feed exchanges heat with the produced liquid at the liquid outlet of the stripping single tower 1 through a first heat exchanger 8 to 125-150 ℃, enters the stripping single tower 1 from the feed inlet at the middle upper part of the stripping single tower 1, and the volume ratio of the cold feed to the hot feed is 1: 1-1: 10;
a feed port at the top of the stripping single tower 1 adopts pretreated effluent or desalted water outside as tower top feed, and the volume percentage of the tower top feed accounts for 1-25% of the water yield of a liquid outlet of the stripping single tower 1;
injecting 5-32% caustic soda solution into the stripping single tower 1 below the middle upper feed port of the stripping single tower 1 to convert solid ammonia into gaseous ammonia for removal;
acid gases such as carbon dioxide, hydrogen sulfide and the like are extracted from a gas outlet at the top of the stripping single tower 1 and then are sent to a tail gas treatment device 3;
high-temperature ammonia-containing water vapor is extracted from the side line of a gas-liquid outlet of the stripping single tower 1, heat exchange is carried out through a water tower reboiler 15, the ammonia-containing water vapor is used for providing a heat source for the water tower 5 through the heat exchange of the water tower reboiler 15, and a cold source is provided for the ammonia-containing water vapor through the heat exchange of the water tower reboiler 15, wherein the operating pressure of the stripping single tower 1 is 0.2-0.6 MPa; the flow of ammonia-containing water vapor extracted from the side line of the single stripping tower 1 accounts for 5-20% of the total feed flow of the single stripping tower 1; the pressure of the side line extraction of the stripping single tower 1 is 0.4-0.5 MPa, and the temperature is 120-150 ℃;
after condensing the ammonia-containing water vapor part gas which exchanges heat in a water tower reboiler 15, sequentially entering a first-stage partial condenser 17, a first-stage flash evaporator 20, a second-stage partial condenser 18, a second-stage flash evaporator 21 and a third-stage partial condenser 19 for gradually cooling and decompressing to obtain high-purity ammonia gas (the content of hydrogen sulfide in the ammonia gas is less than or equal to 300ppm, and the purity of the ammonia gas is more than or equal to 98%), cooling the liquid separated by the first-stage partial condenser 17, the second-stage partial condenser 18 and the third-stage partial condenser 19 by a second partial condensate cooler 22, and then sending the liquid into the pre-treatment equipment 6, wherein the operating pressure of the first-stage partial condenser 17 is 0.4-0.5 MPa, and the temperature is 125-140 ℃; the pressure of the secondary partial condenser 18 is 0.3-0.4 MPa, and the temperature is 80-100 ℃; the pressure of the third-stage partial condenser 19 is 0.2-0.3 MPa, and the temperature is 30-60 ℃;
neutral deacidifying and deaminizing sewage with pH 7 is obtained from the liquid outlet of the tower bottom of the stripping single tower 1.
S3 dephenolization treatment:
cooling deacidification and deamination sewage obtained in the step of treating deacidification ammonia by a first heat exchanger 8 and a second cooler 9 to 30-60 ℃, then feeding the sewage from a sewage feed inlet at the upper part of a first extraction tower 2, feeding an extracting agent from an extracting agent inlet at the lower part of the first extraction tower 2, carrying out countercurrent extraction on the deacidification and deamination sewage and the extracting agent, respectively obtaining a first extract and first dephenolization sewage at an extract outlet at the top of the first extraction tower 2 and a dephenolization sewage outlet at a tower kettle, feeding the first dephenolization sewage from a sewage feed inlet at the upper part of a second extraction tower 2, feeding the extracting agent from an extracting agent inlet at the lower part of the second extraction tower 2, continuously carrying out countercurrent extraction on the first dephenolization sewage and the extracting agent, respectively obtaining a second extract and second dephenolization sewage at an extract outlet at the top of the second extraction tower 2 and a dephenolization sewage outlet at a tower kettle, and repeating the steps until the dephenolization sewage is extracted from a dephenolization sewage outlet at the tower kettle of the last extraction tower 2, and each extract is extracted from the extract outlet at the top of each extraction tower 2;
wherein the temperature of the extraction tower 2 is 20-65 ℃, the pressure is normal pressure, and the pH value is 3-11; the ratio of the dosage of each extractant to the sewage fed into the extraction tower 2 is 1:1 to 1: 10.
S4 extraction agent regeneration treatment:
exchanging heat between each extract obtained in the step of S3 dephenolizing and gas extracted from the top of the phenol tower 4 through a third liquid heat exchanger 10 to 70-130 ℃, and allowing the extract to enter the phenol tower 4, wherein the reflux ratio of the phenol tower 4 is controlled to be 0.1-1;
cooling the high-purity extractant extracted from the extractant outlet at the top of the phenol tower 4 to 30-60 ℃ by a third cooler 11, allowing the high-purity extractant to automatically flow to an extractant circulating tank 12, and returning the extractant to the extraction tower 2 for recycling;
crude phenol is extracted from a phenol outlet of a tower kettle of the phenol tower 4 and is taken as a byproduct to be sent out of the device;
wherein the control pressure of the phenol tower 4 is-0.01-0.02 MPa; the temperature of the top of the phenol tower 4 is 60-120 ℃; the temperature of the tower kettle is 150-210 ℃.
S5 extractant recovery treatment:
the dephenolized sewage obtained by the dephenolizing treatment in the S3 is subjected to heat exchange with pretreated effluent collected from a pretreated water outlet of a tower kettle of the water tower 5 through a second heat exchanger 16 to 50-100 ℃, and then enters the tower from a feed inlet at the upper part of the water tower 5;
an azeotrope of the extracting agent and water is extracted from an azeotrope outlet of the water tower 5, and the azeotrope enters a reflux tank 14 after being condensed by a first condensate cooler 13;
in the reflux tank 14, the extractant and the water are layered, the upper layer extracted extractant enters the extractant circulating tank 12 through the third cooler 11 to be recovered, and the lower layer extracted water is used as reflux and returns to the tower through a reflux port of the water tower 5, so that the extractant is fully recovered;
extracting pretreated effluent from a pretreated water outlet of a tower kettle 5 of the water tower;
most of the pretreated effluent is sent to a subsequent biochemical treatment system, and a small part of the pretreated effluent is sent to a preceding stripping single tower 1 to be used as the feeding material at the top of the stripping single tower 1, so that the content of ammonia in the acidic gas collected at the top of the stripping single tower 1 is greatly reduced, the content is less than or equal to 300ppm, and meanwhile, the use of external desalted water as the feeding material at the top of the stripping single tower 1 is reduced or even avoided;
wherein the tower top temperature of the water tower 5 is 60-100 ℃, and the tower kettle temperature is 101-110 ℃.
To sum up, the utility model discloses the system makes phenol ammonia sewage earlier through pretreatment equipment 6 processing, gets rid of impurity such as light oil, heavy oil, dust in the sewage, alleviates follow-up treatment equipment's burden, obtains pretreatment sewage. The pretreatment sewage is deacidified and deaminated by a stripping single tower 1, acid gas is collected from the top of the tower, and high-temperature ammonia-containing water vapor is collected from the lateral line; high-temperature ammonia-containing water vapor is used as a heating heat source of the water tower reboiler 15, so that energy consumption is reduced, and high-concentration ammonia gas is obtained through three-stage segregation of the ammonia-containing water vapor. The extracted liquid at the bottom of the stripping single tower 1 enters an extraction tower 2 for dephenolization, and the extraction tower 2 adopts a countercurrent contact and cascade extraction method to respectively extract an extract and dephenolized sewage at the top and the bottom of the extraction tower 2; the extract enters a phenol tower 4 to regenerate the extractant, and the regenerated extractant is recycled to obtain a crude phenol byproduct; dephenolized sewage enters a water tower 5, the water tower 5 recovers an extracting agent dissolved in the dephenolized sewage, the recovered extracting agent is recycled, meanwhile, a tower kettle of the water tower 5 recovers pretreated effluent meeting the water inflow requirement of a biochemical system, the system device is simple and reasonable, not only can avoid pipeline blockage and realize high-purity recovery of phenol ammonia and the extracting agent, but also can fully utilize heat energy and reduce equipment investment and operating cost.
It should be finally noted that the above embodiments are only used for illustrating the technical solutions of the embodiments of the present invention and not for limiting the same, and although the embodiments of the present invention are described in detail with reference to the preferred embodiments, those skilled in the art should understand that the technical solutions of the embodiments of the present invention can still be modified or replaced with equivalents, and these modifications or equivalent replacements cannot make the modified technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.
Claims (10)
1. The single-tower treatment system for the phenol-ammonia sewage is characterized by comprising a stripping single tower (1) and pretreatment equipment (6) communicated with an inlet of the stripping single tower (1), wherein a liquid outlet of the stripping single tower (1) is sequentially connected with an extraction tower (2) and a phenol tower (4) through pipelines, and a gas-liquid outlet of the stripping single tower (1) is communicated with an ammonia segregation system after heat exchange with a produced liquid in a tower kettle of a water tower (5) through a water tower reboiler (15).
2. The phenol-ammonia wastewater single-tower treatment system according to claim 1, wherein an air outlet at the top of the stripping single tower (1) is communicated with a tail gas treatment device (3), and the tail gas treatment device (3) is used for treating the acidic gas extracted from the stripping single tower (1) to avoid environmental pollution.
3. The single-tower treatment system for phenol-ammonia wastewater as claimed in claim 1, wherein the pretreatment equipment (6) is internally provided with a modified material, and the modified material has oleophilic and hydrophobic effects to accelerate the separation of oil and water in phenol-ammonia wastewater.
4. The single-tower treatment system for phenol-ammonia wastewater according to any one of claims 1 to 3, wherein the pretreatment equipment (6) is provided with a dosing port, a light oil outlet, a heavy oil outlet and a pretreatment water outlet, phenol-ammonia wastewater pretreatment chemicals are added into the pretreatment equipment (6) through the dosing port, and light oil, heavy oil and pretreatment wastewater treated and separated by the pretreatment equipment (6) are discharged through the light oil outlet, the heavy oil outlet and the pretreatment water outlet of the pretreatment equipment (6), respectively.
5. The phenol-ammonia wastewater single-tower treatment system according to claim 4, wherein the inlet of the stripping single tower (1) comprises an upper feed port and a middle upper feed port, the pretreatment water outlet of the pretreatment device (6) is communicated with the upper feed port of the stripping single tower (1) through a first cooler (7), and the pretreatment water outlet of the pretreatment device (6) is also communicated with the middle upper feed port of the stripping single tower (1) through a first heat exchanger (8).
6. The phenol-ammonia wastewater single-tower treatment system according to claim 5, wherein the inlet of the stripping single tower (1) further comprises a top feed inlet for introducing external desalted water into the stripping single tower (1) as a cooling material so as to greatly reduce the content of ammonia in the acid gas extracted from the top of the stripping single tower (1).
7. The phenol-ammonia wastewater single-tower treatment system according to claim 6, wherein an extract outlet is arranged at the top of the extraction tower (2), a wastewater feed inlet is arranged at the upper part of the extraction tower, an extractant inlet is arranged at the lower part of the extraction tower, and a dephenolized wastewater outlet is arranged at the bottom of the extraction tower, the liquid outlet of the stripping single-tower (1) is communicated with the wastewater feed inlet of the extraction tower (2) through the first heat exchanger (8) and the second cooler (9), and the dephenolized wastewater outlet of the extraction tower (2) is communicated with the feed inlet of the water tower (5) through the second heat exchanger (16).
8. The phenol-ammonia wastewater single-tower treatment system according to claim 7, wherein an extract outlet of the extraction tower (2) is communicated with a feed inlet of the phenol tower (4) through a third heat exchanger (10), an extractant outlet is formed in the top of the phenol tower (4), a phenol outlet is formed in the bottom of the phenol tower (4), the extractant outlet of the phenol tower (4) is communicated with an extractant circulating tank (12) through the third heat exchanger (10) and a third cooler (11), and the extractant circulating tank (12) is communicated with an extractant inlet in the lower part of the extraction tower (2).
9. The single-tower phenol-ammonia wastewater treatment system according to claim 8, wherein an azeotrope outlet is arranged at the top of the water tower (5), a feed inlet and a reflux inlet are arranged at the upper part of the water tower (5), a pretreatment water outlet is arranged at the bottom of the water tower (5), the azeotrope outlet of the water tower (5) is communicated with the reflux inlet of the water tower (5) through a first condensate cooler (13) and a reflux tank (14), the reflux tank (14) is communicated with the extractant circulating tank (12) through the third cooler (11), and the pretreatment water outlet of the water tower (5) is communicated with the top feed inlet of the stripping single tower (1) through the second heat exchanger (16) and a water tower still liquid cooler (23).
10. The single-tower treatment system for the phenol-ammonia wastewater as claimed in claim 1, which comprises a first dephlegmator (17), a first flash evaporator (20), a second dephlegmator (18), a second flash evaporator (21) and a third dephlegmator (19) which are connected in sequence, wherein liquid outlets of the first dephlegmator (17), the second dephlegmator (18) and the third dephlegmator (19) are communicated with the pretreatment equipment (6) through a second dephlegmator cooler (22).
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| CN202121270181.1U CN214936766U (en) | 2021-06-07 | 2021-06-07 | Phenol ammonia sewage single tower processing system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113213686A (en) * | 2021-06-07 | 2021-08-06 | 天津同创恒泰科技有限公司 | Single-tower treatment system and method for phenol ammonia sewage |
| CN115974321A (en) * | 2022-12-30 | 2023-04-18 | 陕西延长中煤榆林能源化工有限公司 | Sewage treatment system and method for heavy oil catalytic thermal cracking DCC device |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113213686A (en) * | 2021-06-07 | 2021-08-06 | 天津同创恒泰科技有限公司 | Single-tower treatment system and method for phenol ammonia sewage |
| CN115974321A (en) * | 2022-12-30 | 2023-04-18 | 陕西延长中煤榆林能源化工有限公司 | Sewage treatment system and method for heavy oil catalytic thermal cracking DCC device |
| CN115974321B (en) * | 2022-12-30 | 2024-04-30 | 陕西延长中煤榆林能源化工股份有限公司 | Sewage treatment system and method of heavy oil catalytic pyrolysis DCC device |
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