CN219259758U - Device for recycling phenol and ammonia from waste water of phenol-ammonia production from semi-coke - Google Patents
Device for recycling phenol and ammonia from waste water of phenol-ammonia production from semi-coke Download PDFInfo
- Publication number
- CN219259758U CN219259758U CN202222922861.8U CN202222922861U CN219259758U CN 219259758 U CN219259758 U CN 219259758U CN 202222922861 U CN202222922861 U CN 202222922861U CN 219259758 U CN219259758 U CN 219259758U
- Authority
- CN
- China
- Prior art keywords
- ammonia
- phenol
- inlet
- unit
- adsorption
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Physical Water Treatments (AREA)
Abstract
The utility model relates to the technical field of wastewater treatment, in particular to a device for recycling phenol and ammonia from waste water of phenol and ammonia produced by semi-coke, which comprises a deamination unit, an ammonia water impurity removal unit, a low-temperature salting-out unit, an adsorption dephenolization unit, a regenerant rectification recovery unit and a catalytic oxidation unit, wherein the deamination unit is fixedly communicated with the ammonia water impurity removal unit and the low-temperature salting-out unit through pipelines respectively, the ammonia water impurity removal unit and the adsorption dephenolization unit are fixedly communicated with the regenerant rectification recovery unit through pipelines respectively, the low-temperature salting-out unit is fixedly communicated with the adsorption dephenolization unit through pipelines, and the adsorption dephenolization unit is fixedly communicated with the catalytic oxidation unit through pipelines. The utility model has reasonable and compact structure and convenient use, ensures that the adsorption resin can be regenerated by using a low-boiling point solvent, not only greatly reduces investment cost and energy consumption, but also can recover high-purity ammonia water and crude phenol, has the COD of effluent less than 50mg/L, and has the characteristics of safety, labor saving, simplicity and high efficiency.
Description
Technical Field
The utility model relates to the technical field of wastewater treatment, in particular to a device for recycling phenol and ammonia from waste water generated in phenol-ammonia production by semi-coke.
Background
Semi-coke wastewater is coal chemical wastewater which has complex components, high toxicity and difficult degradation, and the treatment of semi-coke wastewater belongs to the worldwide difficult problem. The phenol-ammonia wastewater obtained in the semi-coke production process has complex components and high ammonia nitrogen and COD contents, wherein the COD is mainly caused by phenolic substances, the total phenol content can reach 4000mg/L to 6000mg/L, and the COD reaches 40000mg/L to 70000mg/L. Phenol-ammonia wastewater produced by semi-coke of certain enterprises is dark purple, COD is 46360mg/L, total phenol is 4387.5mg/L, ammonia nitrogen is 1144.5mg/L, oil is 1535.4mg/L, and electric conductivity is 13.21mS/cm.
In the existing phenol-ammonia wastewater system for semi-coke production, the process for treating the phenol-ammonia wastewater is an ammonia distillation and extraction dephenolization process, namely, the wastewater is subjected to oil removal and air floatation pretreatment to remove oil, then deacidified, and then subjected to ammonia distillation to remove most ammonia nitrogen and recycle to obtain ammonia water. The wastewater after deamination is dephenolized by an extraction process, and commonly used extracting agents are carbon tetrachloride, chloroform, cyclohexane, benzene, xylene, ketone organic solvents such as methyl isobutyl ketone and the like, and the extracting agents such as carbon tetrachloride, chloroform, benzene and the like have high toxicity and are generally used less. The phenol extract phase is back extracted with alkali liquor to obtain sodium phenolate, or directly distilled and separated to obtain crude phenol, and the organic solvent recovered by back extraction or distillation is returned to the extraction process. The raffinate goes to a subsequent biochemical unit and an ozone catalytic oxidation unit to further remove COD. The process has the following defects: (1) The process comprises deacidification, deamination, extraction dephenolization, biochemistry and catalytic oxidation units, and has long process flow, high equipment investment, and particularly high investment of extraction dephenolization towers and biochemical units. (2) The low volatile organic compounds in the wastewater can enter ammonia water during deamination, the purity of the ammonia water is poor, and the ammonia water needs further impurity removal and purification. (3) Due to the solubility of the extractant, the dephenolized raffinate carries the extractant, the COD is very high, and the extractant needs to be distilled and recovered, so that the cost is further increased. (4) The sodium phenolate obtained by the opposite extraction of the phenol extraction can obtain crude phenol by further acidification, and when the extracting agent is recovered by evaporation of the phenol extraction phase, the extracting agent such as methyl isobutyl ketone has high boiling point and high evaporation energy consumption.
Disclosure of Invention
The utility model provides a device for recycling phenol and ammonia from waste water generated in phenol and ammonia production by semi-coke, which overcomes the defects of the prior art, and can effectively solve the problems of high investment cost and energy consumption of adsorption resin regeneration and complex recycling treatment process existing in the prior art of treating the waste water generated in phenol and ammonia production by semi-coke.
The technical scheme of the utility model is realized by the following measures: the device comprises a deamination unit, an ammonia water impurity removal unit, a low-temperature salting-out unit, an adsorption dephenolization unit, a regenerant rectification recovery unit and a catalytic oxidation unit, wherein the deamination unit is fixedly communicated with the ammonia water impurity removal unit and the low-temperature salting-out unit through pipelines respectively, the ammonia water impurity removal unit and the adsorption dephenolization unit are fixedly communicated with the regenerant rectification recovery unit through pipelines respectively, the low-temperature salting-out unit is fixedly communicated with the adsorption dephenolization unit through pipelines, and the adsorption dephenolization unit is fixedly communicated with the catalytic oxidation unit through pipelines.
The following are further optimizations and/or improvements to the above-described inventive solution:
the ammonia removal unit comprises an ammonia removal tower, a first feed preheater and a first tower top condenser, the ammonia impurity removal unit comprises an ammonia impurity removal adsorption column, the low-temperature salting-out unit comprises a low Wen Yanxi device and a phase separator, the adsorption dephenolization unit comprises an adsorption dephenolization column, the regenerant rectification recovery unit comprises a rectification tower, a second feed preheater and a second tower top condenser, the catalytic oxidation unit comprises a catalytic oxidation reactor, a first feed preheater cold fluid inlet is fixedly communicated with a first feed pipeline of phenol ammonia wastewater, a second feed pipeline of phenol ammonia wastewater is fixedly communicated between a first feed preheater cold fluid outlet and a second inlet at the upper part of the ammonia removal tower, a first hot gas discharge pipeline is fixedly communicated between a first tower top outlet and a first tower top condenser hot fluid inlet, a hot fluid discharge pipeline is fixedly communicated between a first tower bottom outlet and the first feed preheater hot fluid inlet, a hot ammonia water discharge pipeline is fixedly communicated between a first tower top condenser hot fluid outlet and an upper inlet of an ammonia water impurity removal adsorption column, a first regenerated liquid recovery pipeline is fixedly communicated between a bottom outlet of the ammonia water impurity removal adsorption column and a cold fluid inlet of a second feeding preheater, a pure ammonia water discharge pipeline is fixedly communicated with a lower outlet of the ammonia water impurity removal adsorption column, a cooled ammonia water discharge pipeline is fixedly communicated between a cold fluid outlet of the second feeding preheater and a second inlet of the upper part of the rectifying tower, a second hot gas discharge pipeline is fixedly communicated between a top outlet of the rectifying tower and the hot fluid inlet of the second feeding preheater, a third hot gas discharge pipeline is fixedly communicated between a hot fluid outlet of the second feeding preheater and the hot fluid inlet of the second tower top condenser, a second tower top reflux pipeline is fixedly communicated between the hot fluid outlet of the second tower top condenser and the first inlet of the upper part of the rectifying tower, the outlet at the bottom of the rectifying tower is fixedly communicated with a first crude phenol discharge pipeline, a hot fluid inlet pipeline is fixedly communicated between a hot fluid outlet of the first feed preheater and a middle inlet of the low Wen Yanxi device, a low-temperature discharge pipeline is fixedly communicated between a middle outlet of the low Wen Yanxi device and a middle inlet of the phase separator, a liquid discharge pipeline after phase separation is fixedly communicated between an upper outlet of the phase separator and an upper inlet of the adsorption dephenolization column, a liquid discharge pipeline after dephenolization is fixedly communicated between a lower outlet of the adsorption dephenolization column and a top inlet of the catalytic oxidation reactor, a water discharge pipeline is fixedly communicated with a bottom outlet of the catalytic oxidation reactor, a second crude phenol discharge pipeline is fixedly communicated with a bottom outlet of the phase separator, and a second regeneration liquid recovery pipeline is fixedly communicated between a top outlet of the adsorption dephenolization column and the first regeneration liquid recovery pipeline.
An adsorption dephenolization regenerant inlet pipeline is fixedly communicated between the second tower top reflux pipeline and the bottom inlet of the adsorption dephenolization column.
The impurity-removing adsorption regenerant inlet pipeline is fixedly communicated between the adsorption dephenolization regenerant inlet pipeline and the ammonia water impurity-removing adsorption column top inlet.
The second feed pipe of the phenolic ammonia wastewater is fixedly communicated with a first medicament adding pipeline, and the top inlet of the low Wen Yanxi device is fixedly communicated with a second medicament adding pipeline.
The inlet at the lower part of the deamination tower is fixedly communicated with a first low-pressure steam pipeline, and the inlet at the lower part of the rectifying tower is fixedly communicated with a second low-pressure steam pipeline.
The low Wen Yanxi device is internally provided with a stirrer and a freezing jacket, a liquid inlet of the freezing jacket is fixedly communicated with a chilled water inlet pipeline, and a liquid outlet of the freezing jacket is fixedly communicated with a chilled water outlet pipeline.
A first tower top reflux pipeline is fixedly communicated between the hot ammonia water discharge pipeline and a first inlet at the upper part of the deamination tower.
The utility model has the following beneficial technical effects:
(1) Controlling the salt concentration, pH and temperature of the wastewater by utilizing the salting-out effect of salt on phenols, and separating out most of phenols in the wastewater to obtain a crude phenol product; the wastewater after phenol precipitation is further adsorbed by polyacrylate resin, and the COD of the wastewater can be reduced to below 200 mg/L; the combination of low Wen Yanxi and adsorption dephenolization replaces the extraction dephenolization and biochemical operation, so that the investment is greatly reduced; the low-boiling point methanol or ethanol replaces the traditional high-boiling point extractant, and the energy consumption for distilling and recovering the solvent or the extractant is greatly reduced.
(2) The ammonia water containing organic matters is adsorbed and decontaminated by polystyrene skeleton resin, the COD of the effluent is less than 100mg/L, and the resin is regenerated by methanol or ethanol, so that the difficult problem that the phenol-containing ammonia water is difficult to purify is solved;
(3) Realizes the recovery of ammonia and phenol in the wastewater, and the COD of the final effluent is less than 50mg/L.
Drawings
FIG. 1 is a schematic diagram of the technological process structure of the utility model.
The codes in the drawings are respectively: 1 is a deamination tower, 2 is a first feed preheater, 3 is a first overhead condenser, 4 is an ammonia water impurity removal adsorption column, 5 is a low Wen Yanxi device, 6 is a phase separator, 7 is an adsorption dephenolization column, 8 is a rectifying tower, 9 is a second feed preheater, 10 is a second overhead condenser, 11 is a catalytic oxidation reactor, 12 is a phenol ammonia wastewater first feed line, 13 is a phenol ammonia wastewater second feed line, 14 is a first hot gas exhaust line, 15 is a hot fluid exhaust line, 16 is a hot ammonia water exhaust line, 17 is a first regenerated liquid recovery line, 18 is a pure ammonia water exhaust line, 19 is a second hot gas exhaust line, 20 is a third hot gas exhaust line, 21 is a second overhead reflux line, 22 is a first crude phenol exhaust line, 23 is a hot fluid inlet line, 24 is a low temperature exhaust line, 25 is a post-phase liquid exhaust line, 26 is a post-dephenolization liquid exhaust line, 27 is an exhaust line, 28 is a second phenol exhaust line, 29 is a first regenerated liquid exhaust line, 30 is a chilled water exhaust line, and 37 is a refrigerant inlet line, and a refrigerant inlet line is a refrigerant inlet line.
Detailed Description
The present utility model is not limited by the following examples, and specific embodiments can be determined according to the technical scheme and practical situations of the present utility model.
In the present utility model, for convenience of description, the description of the relative positional relationship of each component is described according to the layout manner of fig. 1 of the specification, for example: the positional relationship of front, rear, upper, lower, left, right, etc. is determined in accordance with the layout direction of fig. 1 of the specification.
The utility model is further described below with reference to examples and figures:
example 1: the device for recycling phenol and ammonia from the phenol-ammonia wastewater produced by the semi-coke comprises a deamination unit, an ammonia water impurity removal unit, a low-temperature salting-out unit, an adsorption dephenolization unit, a regenerant rectification recovery unit and a catalytic oxidation unit, wherein the deamination unit is fixedly communicated with the ammonia water impurity removal unit and the low-temperature salting-out unit through pipelines respectively, the ammonia water impurity removal unit and the adsorption dephenolization unit are fixedly communicated with the regenerant rectification recovery unit through pipelines respectively, the low-temperature salting-out unit is fixedly communicated with the adsorption dephenolization unit through pipelines, and the adsorption dephenolization unit is fixedly communicated with the catalytic oxidation unit through pipelines.
The working flow of the utility model is as follows: the method comprises the steps of enabling waste water from phenol and ammonia production by semi-coke to enter a deamination unit for deamination to obtain phenol-containing ammonia water and deamination liquid, enabling the phenol-containing ammonia water to enter an ammonia water impurity removal unit for adsorption impurity removal to obtain pure ammonia water, enabling the deamination liquid to enter a low-temperature salting-out unit for phenol precipitation separation through salting-out to obtain crude phenol and residual solution, enabling the residual solution to enter an adsorption dephenolization unit for further dephenolization, enabling effluent of the adsorption dephenolization unit to enter a catalytic oxidation unit for COD removal to reach emission standard, enabling an adsorbent of the ammonia water impurity removal unit and an adsorbent of the adsorption dephenolization unit to be saturated and penetrated, regenerating by a regenerant, enabling the regenerated solution to enter a regenerant rectification recovery unit for rectification recovery of the regenerant for recycling.
The device for recycling phenol and ammonia from the waste water of phenol and ammonia production from semi-coke can be further optimized or/and improved according to actual needs:
example 2, which differs from example 1 in that: as shown in figure 1, the deamination unit comprises a deamination tower 1, a first feed preheater 2 and a first tower top condenser 3, the ammonia water impurity removal unit comprises an ammonia water impurity removal adsorption column 4, the low-temperature salting-out unit comprises a low Wen Yanxi device 5 and a phase separator 6, the adsorption dephenolization unit comprises an adsorption dephenolization column 7, the regenerant rectification recovery unit comprises a rectification tower 8, a second feed preheater 9 and a second tower top condenser 10, the catalytic oxidation unit comprises a catalytic oxidation reactor 11, a cold fluid inlet of the first feed preheater 2 is fixedly communicated with a first feed pipeline 12 of phenolic ammonia wastewater, a second feed pipeline 13 of phenolic ammonia wastewater is fixedly communicated between a cold fluid outlet of the first feed preheater 2 and a second inlet at the upper part of the deamination tower 1, a first hot gas discharge pipeline 14 is fixedly communicated between a top outlet of the deamination tower 1 and a hot fluid inlet of the first tower top condenser 3, a hot fluid discharge pipeline 15 is fixedly communicated between the bottom outlet of the deamination tower 1 and the hot fluid inlet of the first feed preheater 2, a hot ammonia water discharge pipeline 16 is fixedly communicated between the hot fluid outlet of the first tower top condenser 3 and the upper inlet of the ammonia water impurity removal adsorption column 4, a first regenerated liquid recovery pipeline 17 is fixedly communicated between the bottom outlet of the ammonia water impurity removal adsorption column 4 and the cold fluid inlet of the second feed preheater 9, a pure ammonia water discharge pipeline 18 is fixedly communicated with the lower outlet of the ammonia water impurity removal adsorption column 4, a cooled ammonia water discharge pipeline 37 is fixedly communicated between the cold fluid outlet of the second feed preheater 9 and the upper second inlet of the rectifying tower 8, a second hot gas discharge pipeline 19 is fixedly communicated between the top outlet of the rectifying tower 8 and the hot fluid inlet of the second feed preheater 9, a third hot gas discharge pipeline 20 is fixedly communicated between the hot fluid outlet of the second feed preheater 9 and the hot fluid inlet of the second overhead condenser 10, a second overhead reflux pipeline 21 is fixedly communicated between the hot fluid outlet of the second overhead condenser 10 and the first inlet at the upper part of the rectifying tower 8, a first crude phenol discharge pipeline 22 is fixedly communicated with the outlet at the bottom of the rectifying tower 8, a hot fluid inlet pipeline 23 is fixedly communicated between the hot fluid outlet of the first feed preheater 2 and the middle inlet of the low Wen Yanxi device 5, a low-temperature discharge pipeline 24 is fixedly communicated between the middle outlet of the low Wen Yanxi device 5 and the middle inlet of the phase separator 6, a post-separation liquid discharge pipeline 25 is fixedly communicated between the upper outlet of the phase separator 6 and the upper inlet of the adsorption dephenolizing column 7, a post-dephenolizing liquid discharge pipeline 26 is fixedly communicated between the lower outlet of the adsorption dephenolizing column 7 and the top inlet of the catalytic oxidation reactor 11, a second crude phenol discharge pipeline 28 is fixedly communicated with the outlet pipeline 27 is fixedly communicated with the outlet at the bottom outlet of the rectifying tower 11, a second crude phenol discharge pipeline 39 is fixedly communicated with the outlet of the bottom of the phase separator 6, and a second recycling liquid recovery pipeline 39 is fixedly communicated between the top outlet of the adsorption dephenolizing column 7 and the first recycling liquid 17.
The catalytic oxidation reactor 11 in the present utility model may be an ozone catalytic oxidation reactor or an ultraviolet catalytic oxidation reactor, as required.
Example 3, which is different from examples 1 to 2 in that: as shown in fig. 1, an adsorption dephenolization regenerant inlet line 29 is fixedly connected between the second overhead reflux line 21 and the bottom inlet of the adsorption dephenolization column 7.
Example 4, which is different from examples 1 to 3, is that: as shown in fig. 1, a impurity-removing and adsorbing regenerant inlet pipeline 30 is fixedly communicated between the adsorption and dephenolizing regenerant inlet pipeline 29 and the top inlet of the ammonia water impurity-removing adsorption column 4.
In the utility model, the resin filled in the ammonia water impurity removal adsorption column 4 and the resin filled in the adsorption dephenolization column 7 can be regenerated by using a regenerant, so that the investment cost and the energy consumption can be greatly reduced, and the impurity removal adsorption regenerant and the adsorption dephenolization regenerant can be methanol or ethanol.
According to the requirement, polystyrene skeleton resin can be filled in the ammonia water impurity removal adsorption column 4, phenolic ammonia water (low boiling point component) obtained by the ammonia water impurity removal unit enters the ammonia water impurity removal adsorption column 4 and is adsorbed and removed by the polystyrene skeleton resin, so that pure ammonia water with COD less than 100mg/L can be obtained; the polyacrylate skeleton resin can be filled in the adsorption dephenolization column 7, the liquid discharged from the phase separator 6 enters an adsorption dephenolization process to carry out adsorption dephenolization, the total phenol of the adsorbed water is less than 1mg/L, and the COD is less than 200mg/L. Simultaneously, the tops of the ammonia water impurity removal adsorption column 4 and the adsorption dephenolization column 7 are respectively provided with a regenerant inlet, after the regenerant is added for the first time, the ammonia water impurity removal adsorption column 4 and the adsorption dephenolization column 7 are regenerated by the regenerant, the obtained regenerated liquid is respectively conveyed into the rectifying tower 8 to be recycled through a first regenerated liquid recycling pipeline 17 and a second regenerated liquid recycling pipeline 39, crude phenol obtained at the bottom of the rectifying tower 8 is discharged and then collected, and the regenerant methanol or ethanol is respectively conveyed into the ammonia water impurity removal adsorption column 4 and the adsorption dephenolization column 7 to be recycled through an adsorption dephenolization regenerant inlet pipeline 29 and an impurity removal adsorption regenerant inlet pipeline 30 after being recycled.
Example 5, which is different from examples 1 to 4, is that: as shown in fig. 1, a first reagent adding pipeline 31 is fixedly communicated with a second feeding pipeline 13 of the phenol-ammonia wastewater, and a second reagent adding pipeline 40 is fixedly communicated with the top inlet of the low Wen Yanxi device 5.
And according to the requirement, the chemical agent added into the phenol-ammonia wastewater is sodium hydroxide, and the pH value of the phenol-ammonia wastewater is regulated to be higher than 12. Then the phenol ammonia wastewater enters a deamination tower 1 for deamination, wherein the temperature of the tower top of the deamination tower 1 is 95-100 ℃, the temperature of the tower bottom is 105-110 ℃, and the ammonia nitrogen in the water discharged from the tower bottom is less than 10mg/L.
Example 6, which is different from examples 1 to 5, is that: as shown in fig. 1, the inlet at the lower part of the deamination tower 1 is fixedly communicated with a first low-pressure steam pipeline 32, and the inlet at the lower part of the rectifying tower 8 is fixedly communicated with a second low-pressure steam pipeline 33.
Example 7, which is different from examples 1 to 6, is that: as shown in fig. 1, a stirrer 34 and a freezing jacket are arranged in the low Wen Yanxi device 5, a freezing jacket liquid inlet is fixedly communicated with a freezing water inlet pipeline 35, and a freezing jacket liquid outlet is fixedly communicated with a freezing water outlet pipeline 36.
According to the requirement, in practical application, the low Wen Yanxi device 5 can be provided with a dosing port, and the solid sodium sulfate and sulfuric acid serving as medicaments are added into the low Wen Yanxi device 5 through the second medicament adding pipeline 40 through the dosing port, so that the salt concentration and the pH value of the solution are controlled. And a refrigerating jacket arranged on the low Wen Yanxi device 5 takes low-temperature refrigerating water as a cold source. After solid sodium sulfate is added into the low Wen Yanxi device 5, the salt concentration is regulated to be 150g/L to 200g/L, the pH value of the solution is controlled to be 6 to 7, the temperature of the solution is controlled to be 2 ℃ to 10 ℃, under the salting-out effect, phenol in the solution is separated out to precipitate, the solution enters the phase separator 6 to be separated to obtain crude phenol, the total phenol in the residual solution is less than 80mg/L, and the COD is less than 1000mg/L.
Example 8, which is different from examples 1 to 7, is that: as shown in FIG. 1, a first overhead reflux line 38 is fixedly connected between the hot aqueous ammonia discharge line 16 and the upper first inlet of the deamination column 1.
The utility model further removes COD after the absorption dephenolized effluent enters a catalytic oxidation unit, and the COD of the oxidized effluent is less than 50mg/L, which accords with the emission standard.
The technical characteristics form the embodiment of the utility model, have stronger adaptability and implementation effect, and can increase or decrease unnecessary technical characteristics according to actual needs so as to meet the requirements of different situations.
Claims (10)
1. The device for recycling phenol and ammonia from the phenol-ammonia wastewater in the semi-coke production is characterized by comprising an ammonia removal unit, an ammonia water impurity removal unit, a low-temperature salting-out unit, an adsorption dephenolization unit, a regenerant rectification recovery unit and a catalytic oxidation unit, wherein the ammonia removal unit is fixedly communicated with the ammonia water impurity removal unit and the low-temperature salting-out unit through pipelines respectively, the ammonia water impurity removal unit and the adsorption dephenolization unit are fixedly communicated with the regenerant rectification recovery unit through pipelines respectively, the low-temperature salting-out unit is fixedly communicated with the adsorption dephenolization unit through pipelines, and the adsorption dephenolization unit is fixedly communicated with the catalytic oxidation unit through pipelines.
2. The apparatus for recovering phenol and ammonia from semi-coke produced phenol-ammonia wastewater according to claim 1, wherein the deamination unit comprises a deamination tower, a first feed preheater and a first overhead condenser, the ammonia removal unit comprises an ammonia removal adsorption column, the low temperature salting-out unit comprises a low Wen Yanxi device and a phase separator, the adsorption dephenolization unit comprises an adsorption dephenolization column, the regenerant rectification recovery unit comprises a rectification tower, a second feed preheater and a second overhead condenser, the catalytic oxidation unit comprises a catalytic oxidation reactor, the cold fluid inlet of the first feed preheater is fixedly connected with a first feed line of phenol-ammonia wastewater, the cold fluid outlet of the first feed preheater is fixedly connected with a second feed line of phenol-ammonia wastewater between the cold fluid outlet of the deamination tower and the second inlet of the deamination tower, a first hot fluid exhaust line is fixedly connected between the outlet of the deamination tower top and the hot fluid inlet of the first feed preheater, a hot fluid exhaust line is fixedly connected between the hot fluid outlet of the deamination tower bottom and the first feed preheater, a hot fluid exhaust line is fixedly connected with the hot fluid inlet of the first feed preheater, the cold fluid exhaust line is fixedly connected with the cold fluid inlet of the first feed preheater, a second feed line is fixedly connected with the hot fluid exhaust inlet of the cold fluid inlet of the first feed preheater, a second feed line is fixedly connected with the hot fluid exhaust line is connected with the hot fluid exhaust inlet of the top of the first feed preheater, a third feed preheater is fixedly connected with the hot fluid exhaust inlet of the ammonia preheater, a second tower top reflux pipeline is fixedly communicated between a second tower top condenser hot fluid outlet and a first inlet at the upper part of the rectifying tower, a first crude phenol discharge pipeline is fixedly communicated with a rectifying tower bottom outlet, a hot fluid inlet pipeline is fixedly communicated between a first feeding preheater hot fluid outlet and a middle inlet of a low Wen Yanxi device, a low-temperature discharge pipeline is fixedly communicated between a middle outlet of the low Wen Yanxi device and a middle inlet of a phase separator, a phase-separated liquid discharge pipeline is fixedly communicated between a phase separator upper outlet and an adsorption dephenolization column upper inlet, a dephenolization liquid discharge pipeline is fixedly communicated between an adsorption dephenolization column lower outlet and a catalytic oxidation reactor top inlet, a water outlet pipeline is fixedly communicated with a catalytic oxidation reactor bottom outlet, a second crude phenol discharge pipeline is fixedly communicated with a phase separator bottom outlet, and a second regeneration liquid recovery pipeline is fixedly communicated between the adsorption dephenolization column top outlet and the first regeneration liquid recovery pipeline.
3. The apparatus for recovering phenol and ammonia from waste water from phenol and ammonia production from semi-coke as claimed in claim 2, wherein an adsorption dephenolizing regenerant inlet line is fixedly connected between the second top reflux line and the bottom inlet of the adsorption dephenolizing column.
4. The apparatus for recovering phenol and ammonia from waste water from phenol and ammonia production from semi-coke as claimed in claim 3, wherein a dephenolization adsorbent inlet line is fixedly connected with a dephenolization adsorbent inlet line between the adsorption dephenolization regenerant inlet line and the ammonia water dephenolization adsorbent column top inlet.
5. The apparatus for recovering phenol and ammonia from waste water from semi-coke production of phenol and ammonia as claimed in claim 2 or 4, wherein the second feed line of the waste water is fixedly connected with a first chemical adding pipeline, and the top inlet of the low Wen Yanxi device is fixedly connected with a second chemical adding pipeline.
6. The apparatus for recovering phenol and ammonia from waste water from phenol and ammonia production from semi-coke as claimed in claim 3, wherein the second feed line of the waste water is fixedly connected with a first chemical adding pipeline, and the top inlet of the low Wen Yanxi device is fixedly connected with a second chemical adding pipeline.
7. The apparatus for recovering phenol and ammonia from waste water from phenol and ammonia production from semi-coke according to claim 2, 4 or 6, wherein the inlet at the lower part of the deamination tower is fixedly connected with a first low pressure steam line, and the inlet at the lower part of the rectification tower is fixedly connected with a second low pressure steam line.
8. The apparatus for recovering phenol and ammonia from waste water from phenol and ammonia production from semi-coke according to claim 2, 4 or 6, wherein a stirrer and a freezing jacket are arranged in the low Wen Yanxi device, a freezing jacket liquid inlet is fixedly communicated with a freezing water inlet pipeline, and a freezing jacket liquid outlet is fixedly communicated with a freezing water outlet pipeline.
9. The apparatus for recovering phenol and ammonia from waste water from phenol and ammonia production from semi-coke according to claim 2, 4 or 6, wherein a first overhead reflux line is fixedly connected between the hot aqueous ammonia discharge line and the first inlet at the upper part of the deamination tower.
10. The apparatus for recovering phenol and ammonia from waste water from phenol and ammonia production from semi-coke as defined in claim 8, wherein a first overhead reflux line is fixedly connected between the hot aqueous ammonia discharge line and the first inlet at the upper portion of the deamination tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222922861.8U CN219259758U (en) | 2022-11-03 | 2022-11-03 | Device for recycling phenol and ammonia from waste water of phenol-ammonia production from semi-coke |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222922861.8U CN219259758U (en) | 2022-11-03 | 2022-11-03 | Device for recycling phenol and ammonia from waste water of phenol-ammonia production from semi-coke |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN219259758U true CN219259758U (en) | 2023-06-27 |
Family
ID=86872981
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202222922861.8U Active CN219259758U (en) | 2022-11-03 | 2022-11-03 | Device for recycling phenol and ammonia from waste water of phenol-ammonia production from semi-coke |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN219259758U (en) |
-
2022
- 2022-11-03 CN CN202222922861.8U patent/CN219259758U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107434335B (en) | Comprehensive treatment method for recycling semi-coke wastewater phenol ammonia | |
| CN102259943B (en) | Energy-saving method for recycling wastewater containing phenol and ammonia | |
| WO2016155101A1 (en) | System and treatment process for combined removal of phenol oil from phenol-ammonia wastewater | |
| CN101235014A (en) | Method for treating and reclaiming waste water of 2-aminopyridine production | |
| CN110002629B (en) | Oil and phenol removal combined treatment method and system for high-concentration phenol-ammonia wastewater | |
| CN108623067B (en) | Process for treating coal chemical wastewater | |
| CN106698785B (en) | Coal gasification wastewater phenol-ammonia recovery process | |
| CN111646620B (en) | Semi-coke wastewater treatment method and device | |
| CN210084997U (en) | Device for recycling cyclohexanone ammoximation device wastewater | |
| CN107473311A (en) | A kind of recycling processing method of coal gasification waste water | |
| CN112142618B (en) | Low-concentration dimethylformamide wastewater recovery system and method | |
| CN112624477A (en) | Treatment device and treatment method for phenolic sodium salt decomposition wastewater | |
| CN102417264B (en) | Method for treating nitrochlorobenzene production wastewater | |
| CN214936766U (en) | Phenol ammonia sewage single tower processing system | |
| CN219259758U (en) | Device for recycling phenol and ammonia from waste water of phenol-ammonia production from semi-coke | |
| CN110655259B (en) | Coal chemical wastewater extraction dephenolization recycling treatment process | |
| CN113754171A (en) | Semi-coke wastewater treatment method combining rectification and membrane separation | |
| CN215250211U (en) | Waste water treatment device | |
| CN106927596A (en) | The processing method of octanol waste lye | |
| CN213977317U (en) | Crude phenol refining waste water treatment equipment | |
| CN216005580U (en) | Petroleum sludge cleaning and organic solvent recovery device | |
| CN211170278U (en) | Coal chemical wastewater extraction dephenolization resourceful treatment system | |
| CN215439953U (en) | High concentration phenol-containing waste water precipitation method phenol desorption and recovery unit | |
| CN115445242B (en) | Device and method for treating dapagliflozin intermediate mother liquor | |
| CN216837522U (en) | System for retrieve oil-free aqueous ammonia in follow oily ammoniacal waste water |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |