CN115304209A - Water-oil ammonia-sulfur separation device and process for phenol-ammonia wastewater treatment - Google Patents

Water-oil ammonia-sulfur separation device and process for phenol-ammonia wastewater treatment Download PDF

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CN115304209A
CN115304209A CN202210740179.9A CN202210740179A CN115304209A CN 115304209 A CN115304209 A CN 115304209A CN 202210740179 A CN202210740179 A CN 202210740179A CN 115304209 A CN115304209 A CN 115304209A
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water
oil
ammonia
communicated
sulfur
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CN115304209B (en
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宋如昌
李亚军
高玉安
宋涛
李海鹏
高宏寅
李秋觉
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Shaanxi Dongxinyuan Chemical Co ltd
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Shaanxi Dongxinyuan Chemical Co ltd
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
    • 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
    • C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
    • 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
    • C02F1/28—Treatment of water, waste water, or sewage by sorption
    • 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
    • C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
    • 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
    • C02F2101/16—Nitrogen compounds, e.g. ammonia
    • 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
    • C02F2101/30—Organic compounds
    • C02F2101/34—Organic compounds containing oxygen
    • C02F2101/345—Phenols
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/302—Nitrification and denitrification treatment

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  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physical Water Treatments (AREA)

Abstract

The application discloses a water-oil ammonia-sulfur separation device and a process for treating phenol-ammonia wastewater, wherein the separation device comprises a mother liquor tank heating system, a water-oil ammonia-sulfur vapor-state separation system, a water-oil liquid-state collection system, a boiler combustion system, a rectification high-efficiency deamination system, a temperature-changing regeneration oil removal system and a biochemical treatment system; the mother liquor tank heating system is respectively communicated with the water-oil ammonia-sulfur vapor-state separation system and the water-oil liquid-state collection system, and the input end of the variable-temperature regeneration oil removal system is communicated with the output end of the rectification high-efficiency deamination system; the biochemical treatment system is communicated with the output end of the variable-temperature regeneration oil removal system; the gas output end of the water-oil ammonia-sulfur-gas separation system is communicated to the input end of the boiler combustion system. The method realizes that the phenol-ammonia wastewater can reach biochemical water inlet indexes after being treated by water-oil ammonia-sulfur separation, ammonia distillation and water-oil separation processes, the treated wastewater meets the technical index requirement of indirect discharge of industrial wastewater, and meanwhile, the cost for treating the phenol-ammonia wastewater can be greatly reduced.

Description

Water-oil ammonia-sulfur separation device and process for phenol-ammonia wastewater treatment
Technical Field
The application relates to the technical field of coal chemical wastewater treatment and comprehensive utilization, in particular to a water-oil ammonia-sulfur separation device and a process for phenol-ammonia wastewater treatment.
Background
Phenol-ammonia wastewater generated in the medium-low temperature dry distillation process of coal has the characteristics of complex components, high pollutant concentration, high chromaticity, high toxicity, stable property and the like, the oil content of the wastewater is higher than 3500mg/L, the volatile phenol content is up to 5000mg/L, the ammonia nitrogen content is up to 5500mg/L, compared with coking wastewater, the semi-coke wastewater pollutants are similar in type but the concentration is about 10 times higher than that of the coking wastewater, the treatment cost is extremely high, and no mature wastewater treatment process exists at present. In recent years, the national environmental protection requirements are becoming stricter, and the problems of VOCs treatment, industrial wastewater treatment and the like in the coal chemical industry severely restrict the high-quality development of the industry and even face the major risk of shutdown.
The phenol-ammonia wastewater in the prior art contains a large amount of pollutants which are difficult to degrade and have high toxicity, and the biochemical water inlet index requirement is difficult to meet after the phenol-ammonia wastewater is treated by the traditional pretreatment process; the prior wastewater treatment adopts extraction dephenolization and ammonia distillation desulfurization processes, and has high wastewater treatment construction cost and high operation cost; in addition, in the prior art, when the water-oil ammonia sulfur mixed with gas and liquid is separated, the gas and liquid are separated by a common separator, and the gas and liquid are separated by the gravity effect after entering the separator, so that the separation effect is poor, and the subsequent water-oil ammonia sulfur separation is not thorough.
Disclosure of Invention
The application provides a water-oil ammonia-sulfur separation device and process for phenol-ammonia wastewater treatment, the problem that biochemical water inflow index requirements are difficult to achieve after traditional pretreatment process treatment in the prior art is solved, extraction dephenolization and ammonia evaporation desulfurization processes are adopted to lead to high wastewater treatment building cost and high operation cost, a common separator is adopted to carry out gas-liquid separation to lead to poor separation effect is solved, biochemical water inflow indexes can be achieved after phenol-ammonia wastewater treatment, the treated wastewater meets the technical index requirements of indirect industrial wastewater discharge, the water-oil ammonia-sulfur separation effect of gas-liquid mixing is good, and meanwhile, the phenol-ammonia wastewater treatment cost can be greatly reduced.
In a first aspect, the application provides a phenol-ammonia wastewater treatment device, which comprises a mother liquor tank heating system, a water-oil ammonia-sulfur vapor separation system, a water-oil liquid collection system, a boiler combustion system, a desulfurization system, a rectification high-efficiency deamination system, a variable-temperature regeneration oil removal system and a biochemical treatment system; the input end of the mother liquor tank heating system is communicated with a phenol-ammonia wastewater input pipeline; the input end of the water-oil ammonia-sulfur-vapor separation system is communicated with the vapor output end of the mother liquor tank heating system, and the liquid condensation end of the water-oil ammonia-sulfur-vapor separation system is communicated to the output end of the rectification high-efficiency deamination system; the input end of the water-oil liquid collecting system is communicated with the liquid output end of the mother liquor tank heating system; the input end of the rectification high-efficiency deamination system is communicated with the output end of the water-oil liquid collecting system; the input end of the temperature-changing regeneration oil removal system is communicated with the output end of the rectification high-efficiency deamination system; the input end of the biochemical treatment system is communicated with the output end of the variable-temperature regeneration oil removal system; the gas output end of the water-oil ammonia-sulfur-gas state separation system is communicated to the input end of the boiler combustion system; the input end of the desulfurization system is communicated with the output end of the boiler combustion system; the water-oil ammonia-sulfur vapor-state separation system comprises a first separator and a second separator; the input end of the first separator is communicated with the steam output end of the mother liquor tank heating system, and the output end of the first separator is communicated with the input end of the second separator; the output end of the second separator is communicated with the input end of the boiler combustion system; the liquid condensation end of the first separator is communicated to the output end of the rectification high-efficiency deamination system; the second separator comprises a cylinder body, a conical tube, a spiral plate and a tube body; the spiral plate is spirally arranged along the outer side surface of the conical tube and is fixedly connected with the outer side surface of the conical tube, the spiral plate and the conical tube are both arranged in the cylinder body, and the outer edge of the spiral plate is in sealing contact with the inner side surface of the cylinder body; the top end of the conical pipe is fixedly connected with the bottom end of the pipe body and communicated with the bottom end of the pipe body; the top end of the pipe body penetrates through the top end of the cylinder body and is rotatably connected with the cylinder body, and the pipe body is communicated to the input end of the boiler combustion system; the outer side of the top end of the cylinder body is communicated with the output end of the first separator, and the bottom end of the cylinder body is communicated to the output end of the rectification high-efficiency deamination system.
With reference to the first aspect, in a possible implementation manner, the mother liquor tank heating system includes a water-oil ammonia-sulfur separation mother liquor tank, a negative pressure gas collecting hood, and a semi-coke drying bed; the water-oil ammonia-sulfur separation mother liquor tank is arranged above the semi-coke drying bed; the negative pressure gas collecting hood is arranged above the water-oil ammonia-sulfur separation mother liquor tank and forms a closed space with the semi-coke drying bed; the input end of the water-oil ammonia-sulfur separation mother liquid tank is communicated with the phenol ammonia wastewater input pipeline, and the output end of the water-oil ammonia-sulfur separation mother liquid tank is communicated with the input end of the water-oil liquid collection system; and the output end of the negative pressure gas-collecting hood is communicated with the input end of the water-oil ammonia-sulfur vapor-state separation system.
With reference to the first aspect, in one possible implementation manner, the water-oil liquid state collection system includes a standing tank and an intermediate storage tank; the input end of the standing tank is communicated with the liquid output end of the mother liquor tank heating system, and the output end of the standing tank is communicated with the input end of the intermediate storage tank; the output end of the intermediate storage tank is communicated with the input end of the rectification high-efficiency deamination system; and the ammonia water end of the intermediate storage tank is connected to the phenol ammonia wastewater input pipeline in a backflow mode.
With reference to the first aspect, in a possible implementation manner, the second separator further includes a driving portion, a first ring body, and a second ring body; the first ring body is fixedly connected with the large opening end of the conical pipe; the second ring body is sleeved on the outer side of the first ring body, the first ring body is rotatably connected, and the outer side of the second ring body is fixedly connected with the inner side of the cylinder body; the output end of the driving part is meshed with the outer side of the pipe body and can drive the pipe body, the conical pipe and the spiral plate to rotate.
With reference to the first aspect, in one possible implementation manner, the boiler combustion system includes a boiler and a dust remover; the input end of the boiler is communicated with the gaseous output end of the water-oil ammonia-sulfur gaseous separation system, and the output end of the boiler is communicated with the input end of the dust remover; and the output end of the dust remover is communicated with the input end of the desulfurization system.
With reference to the first aspect, in one possible implementation manner, the desulfurization system includes a desulfurization tower; the input end of the desulfurizing tower is communicated with the output end of the boiler combustion system; and the gas output end of the desulfurizing tower is communicated to a chimney, and the liquid output end of the desulfurizing tower is used for preparing ammonium sulfate subsequently.
With reference to the first aspect, in one possible implementation manner, the rectification high-efficiency deamination system comprises an ammonia still and a water-oil tank; the input end of the ammonia still is communicated with the output end of the intermediate storage tank; the gas output end of the ammonia still is connected with the ammonia refining process and is used for preparing liquid ammonia; the liquid output end of the ammonia still is communicated with the input end of the water oil tank; the output end of the water oil tank is communicated with the input end of the temperature-changing regeneration oil removal system; and the liquid condensing end of the water-oil ammonia-sulfur-vapor separation system is communicated to the water-oil tank.
With reference to the first aspect, in one possible implementation manner, the temperature-varying regenerative oil removal system includes a water-oil separation tower and an intermediate water tank; the input end of the water-oil separation tower is communicated with the output end of the water-oil tank; the output end of the water-oil separation tower is communicated with the input end of the intermediate water tank; the output end of the intermediate water tank is communicated with the input end of the biochemical treatment system; the biochemical treatment system comprises a regulating tank, a biochemical tank and a sedimentation tank; the adjusting tank, the biochemical tank and the sedimentation tank are connected in sequence, and the output end of the middle water tank is communicated with the adjusting tank.
In a second aspect, the present application provides a process of a water-oil ammonia-sulfur separation device for phenol-ammonia wastewater treatment, comprising: primarily separating ammonia sulfur from water, namely conveying the phenol ammonia wastewater to a mother liquor tank heating system to primarily separate ammonia sulfur with a low boiling point and water oil with a high boiling point in the mother liquor tank heating system; separating the water-oil ammonia sulfur again, collecting the low-boiling-point ammonia sulfur in a gas-state form into a water-oil ammonia sulfur gas separation system, and separating the water oil attached to the low-boiling-point ammonia sulfur again; standing and separating water and oil, conveying the water and oil with high boiling point separated from the mother liquor tank heating system to a water and oil liquid collecting system, standing, layering the water and oil after standing, and removing upper part of light oil; ammonia distillation treatment, namely conveying the water-oil wastewater subjected to standing and light oil removal to a rectification high-efficiency deamination system to remove ammonium ions dissolved in water and oil; separating water from oil, conveying the water-oil wastewater subjected to ammonia evaporation treatment to a temperature-variable regeneration oil removal system, and adsorbing and removing oil in the water-oil wastewater; biochemical treatment, wherein the wastewater after water-oil separation is conveyed to a biochemical treatment system for biochemical reaction treatment, and finally reaches the secondary water reuse standard; gaseous ammonia sulfur separation, water oil ammonia sulfur separates the back once more, burns gaseous ammonia sulfur as combustion-supporting wind entering into the boiler, and ammonia reacts with nitrogen oxide under the boiler high temperature condition and plays the denitration effect, and the sulphide gets into desulfurization system along with the flue gas after the burning and retrieves and prepare ammonium sulfate.
One or more technical solutions provided in the present application have at least the following technical effects or advantages:
the method adopts a mother liquor tank heating system, a water-oil ammonia-sulfur vapor-state separation system, a water-oil liquid-state collection system, a boiler combustion system, a desulfurization system, a rectification high-efficiency deamination system, a temperature-changing regeneration oil removal system and a biochemical treatment system; the input end of the mother liquid tank heating system is communicated with a phenol-ammonia wastewater input pipeline, so that phenol-ammonia wastewater input into the mother liquid tank heating system is heated to separate water, oil and ammonia sulfur, the low-boiling point ammonia sulfur forms a vapor state and enters a water-oil-ammonia-sulfur vapor state separation system for subsequent separation, and the high-boiling point water and oil are still in a liquid state and can enter a water-oil-liquid state collection system for temporary storage, so that the separation of the water, oil and ammonia sulfur in the phenol-ammonia wastewater is realized;
the input end of the water-oil ammonia-sulfur-vapor separation system is further communicated with the vapor output end of the mother liquor tank heating system, the liquid condensation end of the water-oil ammonia-sulfur-vapor separation system is communicated with the output end of the rectification high-efficiency deamination system, and as ammonia sulfur is added with a part of water-oil vapor during heating and enters the water-oil ammonia-sulfur-vapor separation system, the added water oil can be further condensed and further separated from ammonia sulfur with low boiling point by arranging the water-oil ammonia-sulfur-vapor separation system, so that the purity of the ammonia sulfur is improved, the separated and condensed water oil enters the output end of the rectification high-efficiency deamination system and is mixed with the remaining oil-containing purified water after ammonia distillation, and the subsequent treatment is facilitated;
the input end of the water-oil liquid collecting system is communicated with the liquid output end of the mother liquor tank heating system, the water-oil liquid collecting system is arranged, heated water-oil with high boiling point can be temporarily stored and stood, the water-oil is layered after standing, most of light oil can be removed, and the rest water-oil is continuously subjected to subsequent ammonia distillation treatment;
the input end of the rectification high-efficiency deamination system is communicated with the output end of the water-oil liquid collecting system, and after ammonia sulfur with a low boiling point and water oil with a high boiling point are heated and separated, ammonium ions are easily dissolved in water and can enter the water-oil liquid collecting system along with the water oil, so that the ammonium ions in the water oil can be further removed by the rectification high-efficiency deamination system; the input end of the temperature-changing regeneration oil removal system is communicated with the output end of the rectification high-efficiency deamination system, and the temperature-changing regeneration oil removal system is arranged to further separate water from oil and adsorb the oil in the temperature-changing regeneration oil removal system; finally, the input end of the biochemical treatment system is communicated with the output end of the variable-temperature regeneration oil removal system, and the water after oil removal can reduce residual organic pollutants in the wastewater through the biochemical treatment system, so that the water finally reaches the secondary water reuse standard;
communicating the gaseous output end of the water-oil ammonia-sulfur-vapor separation system to the input end of a boiler combustion system; the input end of the desulfurization system is communicated with the output end of a boiler combustion system, ammonia sulfur with low boiling point can be used as combustion-supporting air to enter a boiler for combustion, ammonia reacts with nitric oxide under the high-temperature condition of the boiler to play a role in denitration, and the flue gas is discharged after reaching the standard; after the sulfide is combusted, the sulfide enters a desulfurization system along with flue gas to be recovered and prepared into ammonium sulfate;
the system is further provided with a water-oil ammonia-sulfur-vapor separation system which comprises a first separator and a second separator, wherein the second separator comprises a cylinder, a conical tube, a spiral plate and a tube body, a part of water-oil in the low-boiling ammonia-sulfur in the mother liquor tank heating system can enter the first separator in a gas-liquid coexisting form for gas-liquid separation, the separated liquid water-oil wastewater is conveyed to the output end of the rectification high-efficiency deamination system for subsequent treatment, and the first separator can not completely separate the gas and the liquid, so that the output end of the first separator can also output the water-oil ammonia-sulfur in the gas-liquid coexisting form, and then the water-oil ammonia-sulfur continuously enters the second separator, namely the cylinder, and then the gas and the liquid can sequentially spiral along with the spiral plate and then pass through the spiral plate, firstly, the separation time of gas and liquid in a separator can be prolonged, so that the gas-liquid separation effect is improved, secondly, the outer edge of the spiral plate is in sealed contact with the inner side surface of the cylinder, the centrifugal liquid has a folding effect, so that liquid drops can be prevented from splashing, and liquid drops entrained by secondary liquid drops in gas can be reduced; furthermore, due to the design of the conical tube, when gas and liquid just enter the barrel, the gas and liquid are spirally separated downwards outside the small opening end of the conical tube, the centrifugal force applied to the gas and liquid is smaller at the moment, and when the gas and liquid gradually reach the outer side of the large opening end of the conical tube, the centrifugal force applied to the gas and liquid is gradually increased as the outer diameter of the conical tube is gradually increased, so that the gas and liquid separation effect is improved again; the gas reaching the bottom end of the cylinder body upwards flows from the inside of the large-opening end of the conical pipe body and finally leaves the cylinder body through the top end of the pipe body, the liquid reaching the bottom end of the cylinder body flows out through the output port at the bottom end of the cylinder body, gas-liquid separation is finally achieved, and the whole gas-liquid separation effect is finally improved through the separation of the four times.
The technical problems that the biochemical water inlet index requirement is difficult to meet after the traditional pretreatment process treatment in the prior art, the wastewater treatment building cost is high and the operation cost is high due to the adoption of the extraction dephenolization and ammonia distillation desulfurization processes, and the separation effect is poor due to the adoption of a common separator for gas-liquid separation are solved, the biochemical water inlet index can be met after the phenol-ammonia wastewater treatment, the treated wastewater meets the technical index requirement of indirect industrial wastewater discharge, the gas-liquid mixed water-oil-ammonia-sulfur separation effect is good, and the technical effect of greatly reducing the phenol-ammonia wastewater treatment cost is achieved.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the embodiments of the present invention or the description in the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings can be obtained by those skilled in the art without creative efforts.
FIG. 1 is a schematic structural diagram of a phenol ammonia wastewater treatment device provided in an embodiment of the present application;
fig. 2 is a schematic front view of a second separator according to an embodiment of the present disclosure;
FIG. 3 is an isometric view of a second separator provided by an embodiment of the present application;
FIG. 4 is an isometric view of the second separator of FIG. 3 prior to assembly;
FIG. 5 is an isometric view of a tapered tube and a spiral plate provided in an embodiment of the present application;
FIG. 6 is an isometric view of a tapered tube, a spiral plate and a spiral diverter plate provided in an embodiment of the present application;
fig. 7 is a partially enlarged view of the area a in fig. 6.
Reference numerals: 1-mother liquor tank heating system; 11-a water-oil ammonia sulfur separation mother liquor tank; 12-negative pressure gas-collecting hood; 13-semi coke drying bed; 2-a water-oil ammonia-sulfur vapor separation system; 21-a first separator; 22-a second separator; 221-a barrel; 2211-inlet tube; 2212-liquid outlet pipe; 222-a tapered tube; 223-a spiral plate; 224-a tube body; 225-a drive section; 226-a first ring; 227-a second ring body; 228-a spiral splitter plate; 229-lower baffle; 23-a first induced draft fan; 24-a second induced draft fan; 3-a water-oil liquid collecting system; 31-a standing tank; 32-an intermediate storage tank; 33-a pump; 34-a return line; 4-a boiler combustion system; 41-a boiler; 42-a dust remover; 43-a third induced draft fan; 5-a desulfurization system; 51-a desulfurizing tower; 52-a chimney; 6-a rectification high-efficiency deamination system; 61-ammonia still; 62-water oil tank; 7-temperature changing regeneration oil removing system; 71-a water-oil separation column; 72-an intermediate water tank; 8-a biochemical treatment system; 81-adjusting tank; 82-biochemical pool; 83-a sedimentation tank; 9-phenol ammonia wastewater input pipeline.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, not all, embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In the description of the embodiments of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience in describing the embodiments of the present invention and simplifying the description, but do not indicate or imply that the referred devices or elements must have specific orientations, be configured in specific orientations, and operate, and thus, should not be construed as limiting the present invention. The terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance. Furthermore, the terms "mounted," "connected," and "connected" are to be construed broadly and may, for example, be fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. Specific meanings of the above terms in the embodiments of the present invention can be understood by those of ordinary skill in the art according to specific situations.
Referring to fig. 1, the water-oil ammonia-sulfur separation device for phenol-ammonia wastewater treatment provided in the embodiment of the present application includes a mother liquor tank heating system 1, a water-oil ammonia-sulfur vapor state separation system 2, a water-oil liquid state collection system 3, a boiler combustion system 4, a desulfurization system 5, a rectification high-efficiency deamination system 6, a variable-temperature regeneration degreasing system 7 and a biochemical treatment system 8; the input end of the mother liquor tank heating system 1 is communicated with a phenol ammonia wastewater input pipeline 9; the input end of the water-oil ammonia-sulfur-vapor separation system 2 is communicated with the vapor output end of the mother liquor tank heating system 1, and the liquid condensation end of the water-oil ammonia-sulfur-vapor separation system 2 is communicated with the output end of the rectification high-efficiency deamination system 6; the input end of the water-oil liquid collecting system 3 is communicated with the liquid output end of the mother liquor tank heating system 1; the input end of the rectification high-efficiency deamination system 6 is communicated with the output end of the water-oil liquid collecting system 3; the input end of the temperature-changing regeneration oil removal system 7 is communicated with the output end of the rectification high-efficiency deamination system 6; the input end of the biochemical treatment system 8 is communicated with the output end of the temperature-changing regeneration oil removal system 7; the gas output end of the water-oil ammonia-sulfur-gas state separation system 2 is communicated to the input end of a boiler combustion system 4; the input end of the desulfurization system 5 is communicated with the output end of the boiler combustion system 4. In the embodiment of the application, phenol-ammonia wastewater is firstly input into a mother liquor tank heating system 1 through a phenol-ammonia wastewater input pipeline 9, water, oil, ammonia and sulfur are separated through heating, ammonia and sulfur with low boiling point form a vapor state and enter a water, oil, ammonia, sulfur and vapor state separation system 2, then water and oil attached to the ammonia and sulfur with low boiling point are further separated again through the water, oil, ammonia and sulfur vapor state separation system 2, the ammonia and sulfur with low boiling point are further sent to a boiler combustion system 4 along with flue gas to be combusted, ammonia reacts with nitrogen oxides under the high-temperature condition of a boiler 41 to play a denitration role, the flue gas is discharged up to the standard, and sulfides enter a desulfurization system 5 along with the flue gas after being combusted to be recovered to prepare ammonium sulfate; high boiling water oil after through mother liquor groove heating system 1 separation carries the liquid collecting system 3 of water oil, carry out temporary storage and stewing, after the water oil layering of stewing, get rid of most light oil, then remaining water oil continues to carry the high-efficient deamination system 6 of rectification to evaporate ammonia and handles, get rid of the ammonium ion in the water oil, then through alternating temperature regeneration deoiling system 7, further separate water and oil, the waste water after finally getting rid of the deoiling reduces remaining organic pollutant in the waste water through biochemical treatment system 8, finally reach secondary water retrieval and utilization standard.
Referring to fig. 1, a mother liquor tank heating system 1 comprises a water-oil ammonia-sulfur separation mother liquor tank 11, a negative pressure gas collecting hood 12 and a semi-coke drying bed 13; the water-oil ammonia-sulfur separation mother liquor tank 11 is arranged above the semi-coke drying bed 13; the negative pressure gas collecting hood 12 is arranged above the water-oil ammonia-sulfur separation mother liquor tank 11 and forms a closed space with the semi-coke drying bed 13; the input end of the water-oil ammonia-sulfur separation mother liquor tank 11 is communicated with the phenol-ammonia wastewater input pipeline 9, and the output end of the water-oil ammonia-sulfur separation mother liquor tank 11 is communicated with the input end of the water-oil liquid collection system 3; the output end of the negative pressure gas-collecting hood 12 is communicated with the input end of the water-oil-ammonia-sulfur-vapor separation system 2. In the embodiment of the application, the semi-coke drying bed 13 is specifically adopted in the mother liquor tank heating system 1 to heat the phenol-ammonia wastewater in the water-oil-ammonia-sulfur separation mother liquor tank 11, the waste heat of the semi-coke closed drying bed is fully utilized to heat the phenol-ammonia wastewater, and meanwhile, the waste heat is absorbed by the waste heat utilization, so that the problem of high-temperature deformation of a top plate and a side plate of the drying bed is further effectively solved; the phenol-ammonia wastewater is gasified and evaporated at the high temperature of 300-450 ℃ by the waste heat of a closed drying bed, so that the separation of water, oil, ammonia and sulfur is realized, ammonia and sulfur with low boiling point form water vapor, and the water vapor, the drying flue gas and the cold coke water vapor are collected by a gas collecting hood under negative pressure and enter a water-oil-ammonia-sulfur vapor separation system 2 for subsequent water-oil-ammonia-sulfur further separation, and water and oil with high boiling point are conveyed to a water-oil-liquid collection system 3 for subsequent water-oil separation; the quality index of the wastewater in the phenol ammonia wastewater input pipeline through actual detection in the embodiment of the application is as follows: COD: more than 35000; NH (NH) 3 -N > 5000; total oil: more than 3500; volatile phenol: is more than 5000, and the unit is mg/L.
Referring to fig. 1, the water-oil liquid collection system 3 includes a rest tank 31 and an intermediate storage tank 32; the input end of the standing tank 31 is communicated with the liquid output end of the mother liquor tank heating system 1, and the output end of the standing tank 31 is communicated with the input end of the intermediate storage tank 32; the output end of the intermediate storage tank 32 is communicated with the input end of the rectification high-efficiency deamination system 6; the ammonia water end of the intermediate storage tank 32 is connected with the phenol ammonia wastewater input pipeline 9 in a backflow mode. In the embodiment of the present application, the liquid water-oil collecting system 3 further includes a standing tank 31 and an intermediate storage tank 32, wherein the heated high-boiling-point water-oil in the water-oil ammonia-sulfur separation mother liquor tank 11 firstly enters the standing tank 31 to stand so as to separate water from oil, so that most of light oil can be removed from the standing tank 31, and the water-oil with most of light oil removed further enters the intermediate storage tank 32 to be collected, which is convenient for subsequent ammonia distillation treatment, and when the system is specifically set, a communication pipeline and a pump 33 are arranged between the standing tank 31 and the intermediate storage tank, and a pump 33 is also arranged at the output end of the intermediate storage tank 32, so as to facilitate the transportation of water-oil; in addition, a return pipeline 34 is added on the intermediate storage tank 32 and connected to the phenol ammonia wastewater input pipeline 9, and when necessary, because part of ammonia water exists in the water and oil, the water and oil in the intermediate storage tank 32 can be returned to the water-oil ammonia-sulfur separation mother liquid tank 11 again, and the separation of ammonia sulfur and water oil is carried out again.
Referring to fig. 1, a water-oil-ammonia-sulfur-vapor separation system 2 includes a first separator 21 and a second separator 22; the input end of the first separator 21 is communicated with the steam output end of the mother liquor tank heating system 1, and the output end of the first separator 21 is communicated with the input end of the second separator 22; the output end of the second separator 22 is communicated with the input end of the boiler combustion system 4; the liquid condensation ends of the first separator 21 and the second separator 22 are communicated to the output end of the rectification high-efficiency deamination system 6. In the embodiment of the present application, the first separator 21 and the second separator 22 are provided to further improve the separation degree of the ammonia sulfur from the water and the oil, and in particular, when the first induced draft fan 23 is provided between the first separator 21 and the second separator 22, the gaseous ammonia sulfur in the first separator 21 is conveniently introduced into the second separator 22 for separation, and the second induced draft fan 24 is also provided between the second separator 22 and the boiler combustion system 4, so that the gaseous ammonia sulfur in the second separator 22 is conveniently introduced into the boiler combustion system 4 along with the flue gas for combustion treatment; the oily wastewater separated by the first separator 21 and the second separator 22 is conveyed to the output end of the rectification high-efficiency deamination system 6, so that the subsequent water-oil separation is facilitated.
Referring to fig. 2-5, the second separator 22 provided in the embodiment of the present application includes a cylinder 221, a conical tube 222, a spiral plate 223, and a tube body 224; the spiral plate 223 is spirally arranged along the outer side surface of the conical tube 222 and fixedly connected with the outer side surface of the conical tube 222, the spiral plate 223 and the conical tube 222 are both arranged inside the cylinder 221, and the outer edge of the spiral plate 223 is in sealing contact with the inner side surface of the cylinder 221; the top end of the conical tube 222 is fixedly connected with the bottom end of the tube body 224 and communicated with each other; the top end of the tube 224 penetrates through the top end of the barrel 221 and is rotatably connected with the barrel 221, and the tube 224 is communicated to the input end of the boiler combustion system; the outer side of the top end of the cylinder 221 is communicated with the output end of the first separator 21, and the bottom end of the cylinder 221 is communicated with the output end of the rectification high-efficiency deamination system. The gas and liquid output from the first separator 21 enter the second separator 22 again, the inlet pipe 2211 is arranged on the outer side of the top end of the cylinder 221, the liquid outlet pipe 2212 is arranged at the bottom end of the cylinder 221, namely, the gas and liquid firstly enter the cylinder 221 through the inlet pipe 2211, then the gas and liquid can sequentially spiral down along with the spiral plate 223, centrifugal force is generated in the spiral process to facilitate separation, the outer edge of the spiral plate 223 is in sealing contact with the inner side surface of the cylinder 221, the centrifugal liquid has a folding effect to avoid liquid drops from splashing, secondary liquid drops entrained in the gas are reduced, the gas and liquid also move around the outer side of the conical pipe 222 in the spiral process, and the centrifugal force applied to the gas and liquid is gradually increased along with the gradually increasing outer diameter of the conical pipe 222, so that the gas and liquid separation effect is improved again; the gas reaching the bottom end of the cylinder 221 goes upward from the inside of the large opening end of the tapered tube 222 and finally leaves the cylinder 221 through the top end of the tube body 224, and the liquid reaching the bottom end of the cylinder 221 flows out through the liquid outlet tube 2212 at the bottom end of the cylinder 221, so that gas-liquid separation is finally realized.
Referring to fig. 2, it is further provided in the embodiment of the present application that the second separator 22 further includes a driving portion 225, a first ring 226, and a second ring 227; the first ring 226 is fixedly connected to the large opening end of the tapered tube 222; the second ring 227 is sleeved on the outer side of the first ring 226, the first ring 226 is rotatably connected, and the outer side of the second ring 227 is fixedly connected with the inner side of the cylinder 221; the output end of the driving part 225 is engaged with the outer side of the tube 224, and can drive the tube 224, the tapered tube 222 and the spiral plate 223 to rotate. The motor is selected for use by the driving part 225, meshing transmission is realized between the output end of the motor and the outer side of the pipe body 224 through a gear, and the support for the large opening end of the conical pipe 222 is realized through the second ring body 227 and the first ring body 226, so that the conical pipe 222 is more stable in rotation.
Referring to fig. 2, 6-7, it is further provided in the present embodiment that the second separator 22 further comprises a spiral diverter plate 228 and a lower baffle plate 229; the spiral flow distribution plate 228 is fixedly connected to the top surface of the spiral plate 223 along the spiral direction of the spiral plate 223; lower baffle 229 is located below spiral plate 223 and is disposed inside the bottom end of barrel 221, and the outer diameter of lower baffle 229 is less than the inner diameter of barrel 221. The spiral flow distribution plate 228 is arranged, so that gas and liquid entering the cylinder 221 are divided into two flows by the spiral flow distribution plate 228 on the spiral plate 223, the two flows are respectively spirally downward for gas and liquid separation, meanwhile, the spiral plate 223 is driven to rotate along the reverse direction of the spiral motion of the gas and liquid by matching with the rotation of the driving part 225, and the spiral flow distribution plate 228 rotates in the reverse direction and has the trend of being driven in the reverse direction of the spiral direction to the gas and liquid, so that the integral separation time of the gas and liquid in the cylinder 221 is prolonged, and the gas and liquid separation effect is further improved; the lower baffle 229 is arranged, so that when the gas-liquid reaches the lower baffle 229, the gas-liquid is blocked and buffered, the gas is blocked and then enters the tapered tube 222 upwards, and finally leaves the cylinder 221, and after being blocked, the liquid overflows to the liquid outlet tube 2212 at the bottom end of the cylinder 221 along the outer edge of the lower baffle 229.
Referring to fig. 1, the boiler combustion system 4 includes a boiler 41 and a dust collector 42; the input end of the boiler 41 is communicated with the gaseous output end of the water-oil ammonia-sulfur gaseous separation system 2, and the output end of the boiler 41 is communicated with the input end of the dust remover 42; the output of the dust separator 42 communicates with the input of the desulfurization system 5. Gaseous ammonia sulfur that draws forth in this application embodiment from second separator 22 gets into boiler 41 burning as combustion-supporting wind, and ammonia reacts with nitrogen oxide under the high temperature condition of boiler 41 and plays the denitration effect, is carried to desulfurization system 5 by third draught fan 43 after the dust remover 42 removes dust afterwards and carries out subsequent desulfurization treatment. The ammonia gas enters the boiler 41 to participate in the denitration reaction, and the reaction principle is as follows:
Figure BDA0003717581170000121
referring to fig. 1, the desulfurization system 5 includes a desulfurization tower 51; the input end of the desulfurizing tower 51 is communicated with the output end of the combustion system 4 of the boiler 41; the gas output end of the desulfurizing tower 51 is communicated to a chimney 52, and the liquid output end of the desulfurizing tower 51 is used for preparing ammonium sulfate subsequently. In the embodiment of the application, the hydrogen sulfide enters the boiler 41 to be combusted into SO 2 、SO 3 Then the ammonium sulfate is recovered and prepared by a desulfurizing tower 51, and the reaction principle is as follows:
SO 2 +2NH 3 .H 2 O——→(NH 4 ) 2 SO 3 +H 2 O
2(NH 4 ) 2 SO 3 +O 2 ——→2(NH 4 ) 2 SO 4
the flue gas finally reaches the standard and is discharged through a chimney 52.
Referring to fig. 1, the rectification high-efficiency deamination system 6 comprises an ammonia still 61 and a water-oil tank 62; the input end of the ammonia still 61 is communicated with the output end of the intermediate storage tank 32; the gas output end of the ammonia still 61 is connected with the ammonia refining process and is used for preparing liquid ammonia; the liquid output end of the ammonia still 61 is communicated with the input end of the water-oil tank 62; the output end of the water oil tank 62 is communicated with the input end of the temperature-changing regeneration oil removal system 7; the liquid condensing end of the water-oil ammonia-sulfur-vapor separation system 2 is communicated to the water-oil tank 62. In the embodiment of the application, 99 percent of ammonia in the wastewater is ammonium ion (NH) in a compound state at 40 DEG C 3 + ) Dissolved in water, ammonia gas is difficult to separate completely from water at low temperatures because of the high solubility of ammonia. Based on the characteristic of ammonia dissolving temperature, the temperature is raised to over 140 ℃, the ammonia dissolving and ionization can be thoroughly destroyed, and gaseous ammonia gas is formed and volatilized. Therefore, in the embodiment of the application, the ammonia distillation tower 61 can realize stripping deamination, namely, the waste water is neutralized by taking steam as a heating mediumThe resultant ammonia is stripped from the waste water, so that the liquid ammonia product can be further separated and extracted, and the stripping reaction process can be represented by the following formula:
OH - +NH 4 + ＝NH 3 + +H 2 o (liquid phase) = NH 3 (gas phase) + H 2 O
The practical detection in the embodiment of the application is that the water quality indexes of the wastewater after passing through the ammonia still are as follows: COD: < 1500,NH 3 -N < 150 in mg/L.
Referring to fig. 1, the temperature-variable regeneration degreasing system 7 includes a water-oil separation tower 71 and an intermediate water tank 72; the input end of the water-oil separation tower 71 is communicated with the output end of the water-oil tank 62; the output end of the water-oil separation tower 71 is communicated with the input end of the intermediate water tank 72; the output of the intermediate water tank 72 is in communication with the input of the biochemical processing system 8. In the embodiment of the application, the water-oil separation tower 71 is a common water-oil separation tower 71, and after water and oil pass through the water-oil separation tower 71, the oil can be absorbed in the water-oil separation tower 71, so that the water and oil are separated, and finally, the wastewater after oil removal is conveyed to the intermediate water tank 72 for temporary storage; the practical detection in the embodiment of the application is that the water quality index of the wastewater after passing through the water-oil separation tower is as follows: COD: is less than 1500; NH (NH) 3 -N: < 150; total oil: is less than 60; volatile phenol: < 400, in mg/L.
Referring to fig. 1, the biochemical treatment system 8 includes a conditioning tank 81, a biochemical tank 82, and a sedimentation tank 83; the adjusting tank 81, the biochemical tank 82 and the sedimentation tank 83 are connected in sequence, and the output end of the intermediate water tank 72 is communicated with the adjusting tank 81. The biochemical tank 82 in the embodiment of the application comprises an anaerobic tank, an anoxic tank and an aerobic tank, and the biochemical treatment process adopts an A2O process, belongs to a biological denitrification process, and can convert ammonia nitrogen in sewage into nitrogen by nitrification and denitrification treatment of nitrogen-containing substances in the sewage through the biochemical action of bacteria, so that COD (chemical oxygen demand) and ammonia nitrogen in the sewage are effectively reduced. The waste water treated by the biochemical system reduces residual organic pollutants in the waste water, and finally reaches the recycling standard of secondary water; the practical wastewater quality index that detects in the sedimentation tank in the embodiment of this application is: COD: is less than 150; NH 3 -N < 25; total oil: is less than 5; volatile phenol: < 0.5, unitIs mg/L.
The embodiment of the application provides a technology of water oil ammonia sulfur separator of phenol ammonia wastewater treatment, includes:
primarily separating ammonia and sulfur in water and oil, namely conveying the phenol ammonia wastewater to a mother liquor tank heating system 1, wherein the mother liquor tank heating system 1 adopts a semi-coke drying bed 13 as a heating source, and the temperature is 300-450 ℃, so that the ammonia and sulfur with low boiling point and the water and oil with high boiling point are gasified and evaporated in the mother liquor tank heating system 1 to realize primary separation;
separating the water-oil ammonia sulfur again, namely collecting the low-boiling-point ammonia sulfur into a water-oil ammonia sulfur steam-state separation system 2 in a steam state, namely performing high-efficiency separation by adopting the first separator 21 and the second separator 22, and separating the water oil attached to the low-boiling-point ammonia sulfur again;
standing and separating water and oil, conveying the water and oil with high boiling point separated from the mother liquor tank heating system 1 to a water and oil liquid collecting system 3, standing, layering the water and oil after standing, and removing upper part of light oil;
performing ammonia distillation treatment, namely conveying the water-oil wastewater subjected to standing and light oil removal to a rectification high-efficiency deamination system 6, and removing ammonium ions dissolved in water oil;
water-oil separation, wherein the water-oil wastewater after ammonia evaporation treatment is conveyed to a temperature-changing regeneration oil removal system 7 to adsorb and remove oil in the water-oil wastewater;
biochemical treatment, wherein the wastewater after water-oil separation is conveyed to a biochemical treatment system 8 for biochemical reaction treatment, and finally reaches the secondary water reuse standard;
gaseous ammonia sulfur separation, water oil ammonia sulfur separates the back again, and the ammonia sulfur with gaseous ammonia is burnt as combustion-supporting wind entering into boiler combustion system 4, and ammonia reacts with nitrogen oxide under the high temperature condition and plays the denitration effect, and the sulphide gets into desulfurization system 5 along with the flue gas after the burning and retrieves and prepare ammonium sulfate.
The embodiments in the present specification are described in a progressive manner, and the same or similar parts among the embodiments may be referred to each other, and each embodiment focuses on the differences from the other embodiments.
The above embodiments are only used to illustrate the technical solutions of the present application, and are not intended to limit the present application; although the present application has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; such modifications or substitutions do not depart from the spirit and scope of the present disclosure.

Claims (10)

1. A water-oil ammonia-sulfur separation device for phenol-ammonia wastewater treatment is characterized by comprising a mother liquor tank heating system (1), a water-oil ammonia-sulfur steam-state separation system (2), a water-oil liquid-state collection system (3), a boiler combustion system (4), a desulfurization system (5), a rectification high-efficiency deamination system (6), a variable-temperature regeneration oil removal system (7) and a biochemical treatment system (8);
the input end of the mother liquor tank heating system (1) is communicated with a phenol-ammonia wastewater input pipeline (9);
the input end of the water-oil ammonia sulfur vapor separation system (2) is communicated with the vapor output end of the mother liquor tank heating system (1), and the liquid condensation end of the water-oil ammonia sulfur vapor separation system (2) is communicated to the output end of the rectification high-efficiency deamination system (6);
the input end of the water-oil liquid collecting system (3) is communicated with the liquid output end of the mother liquor tank heating system (1);
the input end of the rectification high-efficiency deamination system (6) is communicated with the output end of the water-oil liquid collecting system (3);
the input end of the temperature-changing regeneration oil removal system (7) is communicated with the output end of the rectification high-efficiency deamination system (6);
the input end of the biochemical treatment system (8) is communicated with the output end of the variable-temperature regeneration oil removal system (7);
the gaseous output end of the water-oil-ammonia-sulfur-vapor separation system (2) is communicated to the input end of the boiler combustion system (4);
the input end of the desulfurization system (5) is communicated with the output end of the boiler combustion system (4);
the water-oil-ammonia-sulfur-vapor separation system (2) comprises a first separator (21) and a second separator (22);
the input end of the first separator (21) is communicated with the steam output end of the mother liquor tank heating system (1), and the output end of the first separator (21) is communicated with the input end of the second separator (22);
the output end of the second separator (22) is communicated with the input end of the boiler combustion system (4);
the liquid condensation end of the first separator (21) is communicated to the output end of the rectification high-efficiency deamination system (6);
the second separator (22) comprises a cylinder (221), a conical tube (222), a spiral plate (223) and a tube body (224);
the spiral plate (223) is spirally arranged along the outer side surface of the conical tube (222) and fixedly connected with the outer side surface of the conical tube (222), the spiral plate (223) and the conical tube (222) are both arranged in the cylinder body (221), and the outer edge of the spiral plate (223) is in sealing contact with the inner side surface of the cylinder body (221);
the top end of the conical pipe (222) is fixedly connected with the bottom end of the pipe body (224) and communicated with the bottom end of the pipe body;
the top end of the pipe body (224) penetrates through the top end of the barrel (221) and is rotatably connected with the barrel (221), and the pipe body (224) is communicated to the input end of the boiler combustion system (4);
the outer side of the top end of the cylinder body (221) is communicated with the output end of the first separator (21), and the bottom end of the cylinder body (221) is communicated with the output end of the rectification efficient deamination system (6).
2. The water-oil ammonia-sulfur separation device for phenol-ammonia wastewater treatment according to claim 1, wherein the mother liquor tank heating system (1) comprises a water-oil ammonia-sulfur separation mother liquor tank (11), a negative pressure gas collecting hood (12) and a semi-coke drying bed (13);
the water-oil ammonia-sulfur separation mother liquor tank (11) is arranged above the semi-coke drying bed (13);
the negative pressure gas collecting hood (12) is arranged above the water-oil ammonia-sulfur separation mother liquor tank (11) and forms a closed space with the semi-coke drying bed (13);
the input end of the water-oil ammonia-sulfur separation mother liquor tank (11) is communicated with the phenol-ammonia wastewater input pipeline (9), and the output end of the water-oil ammonia-sulfur separation mother liquor tank (11) is communicated with the input end of the water-oil liquid collection system (3);
the output end of the negative pressure gas-collecting hood (12) is communicated with the input end of the water-oil ammonia-sulfur gas-state separation system (2).
3. The apparatus for separating ammonia and sulfur from water in phenol-ammonia wastewater treatment according to claim 1 or 2, wherein the water-oil liquid collection system (3) comprises a standing tank (31) and an intermediate storage tank (32);
the input end of the standing tank (31) is communicated with the liquid output end of the mother liquor tank heating system (1), and the output end of the standing tank (31) is communicated with the input end of the intermediate storage tank (32);
the output end of the intermediate storage tank (32) is communicated with the input end of the rectification high-efficiency deamination system (6);
and the ammonia water end of the intermediate storage tank (32) is connected to the phenol ammonia wastewater input pipeline (9) in a backflow mode.
4. The apparatus for separating ammonia and water from oil and ammonia in phenol-ammonia wastewater treatment according to claim 1, wherein the second separator (22) further comprises a driving part (225), a first ring body (226) and a second ring body (227);
the first ring body (226) is fixedly connected to the large opening end of the conical pipe (222);
the second ring body (227) is sleeved on the outer side of the first ring body (226), the first ring body (226) is rotatably connected, and the outer side of the second ring body (227) is fixedly connected with the inner side of the cylinder body (221);
the output end of the driving part (225) is meshed with the outer side of the pipe body (224) and can drive the pipe body (224), the conical pipe (222) and the spiral plate (223) to rotate.
5. The apparatus for separating ammonia and water from oil and ammonia in phenol-ammonia wastewater treatment according to claim 1, wherein the second separator (22) further comprises a spiral flow splitter plate (228) and a lower baffle plate (229);
the spiral flow distribution plate (228) is fixedly connected to the top surface of the spiral plate (223) along the spiral direction of the spiral plate (223);
the lower baffle (229) is arranged below the spiral plate (223) and inside the bottom end of the cylinder (221), and the outer diameter of the lower baffle (229) is smaller than the inner diameter of the cylinder (221).
6. The phenol-ammonia wastewater treatment water-oil ammonia-sulfur separation device according to claim 1, wherein the boiler combustion system (4) comprises a boiler (41) and a dust remover (42);
the input end of the boiler (41) is communicated with the gaseous output end of the water-oil-ammonia-sulfur-vapor separation system (2), and the output end of the boiler (41) is communicated with the input end of the dust remover (42);
the output end of the dust remover (42) is communicated with the input end of the desulfurization system (5).
7. The apparatus for separating ammonia and sulfur in water oil treated by phenol-ammonia wastewater according to claim 1, wherein the desulfurization system (5) comprises a desulfurization tower (51);
the input end of the desulfurizing tower (51) is communicated with the output end of the boiler combustion system (4);
the gas output end of the desulfurizing tower (51) is communicated to a chimney (52), and the liquid output end of the desulfurizing tower (51) is used for subsequently preparing ammonium sulfate.
8. The phenol-ammonia wastewater treatment water-oil ammonia-sulfur separation device according to claim 3, wherein the rectification high-efficiency deamination system (6) comprises an ammonia still (61) and a water-oil tank (62);
the input end of the ammonia still (61) is communicated with the output end of the intermediate storage tank (32);
the gas output end of the ammonia still (61) is connected with an ammonia refining process and is used for preparing liquid ammonia;
the liquid output end of the ammonia still (61) is communicated with the input end of the water-oil tank (62);
the output end of the water oil tank (62) is communicated with the input end of the temperature-changing regeneration oil removal system (7);
and the liquid condensation end of the water-oil ammonia-sulfur-vapor separation system (2) is communicated to the water-oil tank (62).
9. The water-oil ammonia-sulfur separation device for phenol-ammonia wastewater treatment according to claim 8, wherein the temperature-variable regeneration oil removal system (7) comprises a water-oil separation tower (71) and an intermediate water tank (72);
the input end of the water-oil separation tower (71) is communicated with the output end of the water-oil tank (62);
the output end of the water-oil separation tower (71) is communicated with the input end of the intermediate water tank (72);
the output end of the intermediate water tank (72) is communicated with the input end of the biochemical treatment system (8);
the biochemical treatment system (8) comprises a regulating tank (81), a biochemical tank (82) and a sedimentation tank (83);
the adjusting tank (81), the biochemical tank (82) and the sedimentation tank (83) are sequentially connected, and the output end of the middle water tank (72) is communicated with the adjusting tank (81).
10. A process of a water-oil ammonia-sulfur separation device for phenol-ammonia wastewater treatment, which is based on the water-oil ammonia-sulfur separation device for phenol-ammonia wastewater treatment of any one of claims 1 to 9, and is characterized by comprising the following steps:
primarily separating ammonia sulfur from water oil, namely conveying phenol ammonia wastewater to the mother liquor tank heating system (1) to primarily separate ammonia sulfur with low boiling point and water oil with high boiling point in the mother liquor tank heating system (1);
separating the water-oil ammonia sulfur again, collecting the low-boiling-point ammonia sulfur in a vapor state into the water-oil ammonia sulfur vapor state separation system (2), and separating the water oil attached to the low-boiling-point ammonia sulfur again;
standing and separating water and oil, conveying the water and oil with high boiling point separated from the mother liquor tank heating system (1) to the water and oil liquid collecting system (3), standing, layering the water and oil after standing, and removing the upper part of light oil;
performing ammonia distillation treatment, namely conveying the water-oil wastewater subjected to standing and light oil removal to the rectification high-efficiency deamination system (6), and removing ammonium ions dissolved in the water-oil;
water-oil separation, wherein the water-oil wastewater after ammonia evaporation treatment is conveyed to the temperature-changing regeneration oil removal system (7) to adsorb and remove oil in the water-oil wastewater;
carrying out biochemical treatment, wherein the wastewater subjected to water-oil separation is conveyed to the biochemical treatment system (8) for biochemical reaction treatment, and finally reaches the secondary water reuse standard;
and (3) separating gaseous ammonia and sulfur, separating water oil ammonia and sulfur again, taking the gaseous ammonia and sulfur as combustion-supporting air to enter the boiler combustion system (4) for combustion, reacting ammonia with nitrogen oxide under a high-temperature condition to play a denitration role, and enabling sulfide after combustion to enter the desulfurization system (5) along with flue gas to recover and prepare ammonium sulfate.
CN202210740179.9A 2022-06-28 2022-06-28 Water-oil ammonia-sulfur separation device and process for phenol-ammonia wastewater treatment Active CN115304209B (en)

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* Cited by examiner, † Cited by third party
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KR101386954B1 (en) * 2013-12-24 2014-04-29 (주)도드람환경연구소 Purifying apparatus for wastewater having organic waste
WO2016188326A1 (en) * 2015-05-27 2016-12-01 波鹰(厦门)科技有限公司 Semi coke wastewater treating and regenerative recycling method
CN114409197A (en) * 2022-01-29 2022-04-29 陕西东鑫垣化工有限责任公司 Coke quenching closed type drying water-oil ammonia-sulfur component recycling treatment process
CN114409170A (en) * 2022-01-29 2022-04-29 陕西东鑫垣化工有限责任公司 Water-oil ammonia-sulfur residue separation system and method for phenol-ammonia wastewater treatment

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR101386954B1 (en) * 2013-12-24 2014-04-29 (주)도드람환경연구소 Purifying apparatus for wastewater having organic waste
WO2016188326A1 (en) * 2015-05-27 2016-12-01 波鹰(厦门)科技有限公司 Semi coke wastewater treating and regenerative recycling method
CN114409197A (en) * 2022-01-29 2022-04-29 陕西东鑫垣化工有限责任公司 Coke quenching closed type drying water-oil ammonia-sulfur component recycling treatment process
CN114409170A (en) * 2022-01-29 2022-04-29 陕西东鑫垣化工有限责任公司 Water-oil ammonia-sulfur residue separation system and method for phenol-ammonia wastewater treatment

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