CN114890623A - Resource-recoverable acylation wastewater treatment process and system - Google Patents
Resource-recoverable acylation wastewater treatment process and system Download PDFInfo
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Abstract
The invention discloses a process and a system for treating acylation wastewater capable of recycling resources, wherein the process comprises the steps of (1) adjusting the pH value of the acylation wastewater to be alkaline to obtain a suspension containing aluminum hydroxide precipitate, and filtering the suspension to obtain an aluminum hydroxide filter cake and a filtrate; (2) adjusting the pH value of the filtrate to acidity, then transferring the filtrate into an extracting agent, stirring and standing to obtain a layered raffinate phase and an extract phase; (3) performing biochemical treatment on the raffinate phase to reach the standard and discharging; (4) and rectifying and separating the extract phase to obtain nitrobenzene and the extractant, recycling the nitrobenzene as an organic solvent, and reusing the extractant for extracting the filtrate. The resource-recoverable acylation wastewater treatment process provided by the invention takes the extraction process as a core, realizes the recycling of organic matters in the acylation wastewater, extracts aluminum ions to produce the water treatment medicament polyaluminium chloride, and realizes the purpose of changing waste into valuable.
Description
Technical Field
The invention belongs to the technical field of water treatment, and particularly relates to a process and a system for treating acylation wastewater capable of recycling resources.
Background
Friedel-Crafts acylation is an organic reaction of great importance in the industrial production of fine chemicals, specialty chemicals and pharmaceutical intermediates (proceedings of the university of Changzhou (Nature science edition), 2010,22(02): 28-30.). Mainly means that acyl halide reacts with aromatic compound under the catalysis of Lewis acid (such as aluminum trichloride), so as to introduce acyl on aromatic ring.
Although Friedel-Crafts acylation reaction is an important organic reaction, the industrial application of Friedel-Crafts acylation reaction still has great limitation, mainly because the acylation reaction can generate a large amount of industrial wastewater with high salt content and high toxicity. Mainly because the solvent used in the acylation reaction (1) is mainly nitrobenzene, the waste water of the acylation reaction contains a large amount of nitrobenzene, and the nitrobenzene has strong toxicity and is an important carcinogenic substance; (2) aluminum trichloride is the most commonly used catalyst for catalytic acylation reaction, has the advantages of high catalytic activity and mild reaction conditions, but most of the aluminum trichloride enters wastewater after the reaction, and the concentration of the aluminum trichloride in the wastewater is higher; (3) small amounts of acylating agents, benzene series and acylated products may also be present in the wastewater. Therefore, the waste water after the acylation reaction is mainly high-toxicity and high-salt-content organic waste water which is difficult to biodegrade (Table 1), and is extremely difficult to treat. Under the current increasingly strict environmental regulations, the difficultly biodegradable organic wastewater generated by the acylation reaction is the main symptom limiting the industrialization of the Friedel-Crafts acylation reaction.
TABLE 1 quality of acylated wastewater
Therefore, it is necessary to develop a treatment technology for the non-biodegradable organic wastewater generated by the acylation reaction.
Disclosure of Invention
The first purpose of the invention is to provide a resource-recoverable acylation wastewater treatment process, which takes an extraction process as a core, realizes the recycling of organic matters in the acylation wastewater, extracts aluminum ions to produce a water treatment medicament polyaluminium chloride, realizes the purpose of changing waste into valuable and has important application value.
The second purpose of the invention is to provide an acylation waste water treatment system capable of resource recovery.
To this end, an embodiment of the first aspect of the present invention provides a resource-recoverable acylated wastewater treatment process, comprising the steps of:
(1) adjusting the pH value of the acylation wastewater to be alkaline to obtain a suspension containing aluminum hydroxide precipitate, and filtering the suspension to obtain an aluminum hydroxide filter cake and a filtrate;
(2) adjusting the pH value of the filtrate to acidity, then transferring the filtrate into an extracting agent, stirring and standing to obtain a layered raffinate phase and an extract phase;
(3) performing biochemical treatment on the raffinate phase to reach the standard and discharging;
(4) rectifying and separating the extract phase to obtain nitrobenzene and the extractant, recycling the nitrobenzene as an organic solvent, and reusing the extractant for extracting the filtrate;
(5) and adding concentrated hydrochloric acid into the filter cake, heating and dissolving, adding an auxiliary agent, and polymerizing to obtain the polyaluminum chloride.
The resource-recoverable acylation wastewater treatment process provided by the embodiment of the invention takes the extraction process as a core, realizes the recycling of organic matters in the acylation wastewater, extracts aluminum ions to produce the water treatment medicament polyaluminium chloride, realizes the purpose of changing waste into valuable, and has important application value.
In some embodiments of the present invention, in the step (1), the adjusting the pH of the acylated wastewater to alkaline comprises: adjusting the pH value of the acylation wastewater to 8-10 by adopting an alkali raw material, wherein the alkali raw material is one or more than two of sodium hydroxide, potassium hydroxide or liquid ammonia. The pH of the acylation waste water is preferably adjusted to about 9 by using an alkali raw material in the embodiment of the present invention, as long as the alkali raw material can completely precipitate aluminum ions.
In some embodiments of the invention, the adjusting the pH of the filtrate to acidity in step (2) comprises: and adjusting the pH of the filtrate to 2-3 by using acid, wherein the acid is one or more than two of hydrochloric acid, nitric acid or sulfuric acid.
In some embodiments of the invention, in step (2), the extractant is a non-polar organic solvent, and the volume ratio of the extractant to the filtrate is 0.5-5: 1.
In some embodiments of the invention, the extractant is one or more of n-heptane, n-octane, n-hexane, benzene, toluene, xylene, carbon tetrachloride.
In some embodiments of the present invention, in the step (3), the biochemical treatment is performed by an activated sludge method; in the step (5), the heating and dissolving temperature is 40-50 ℃, and the weight ratio of the filter cake to the concentrated hydrochloric acid is 0.5-2.5: 1.
In some embodiments of the invention, in step (5), the additive is added in an amount of 2-10 wt% based on the dry weight of the filter cake, and the additive is calcium aluminate or/and magnesium aluminate.
The main component of the raffinate phase of the invention is water plus a small amount of nitrobenzene.
In a second aspect, the present invention provides a resource-recoverable acylated wastewater treatment system, comprising:
the sedimentation tank is used for generating aluminum hydroxide sediment;
the inlet of the filtering unit is communicated with the outlet of the sedimentation tank;
the inlet of the extraction unit is communicated with the filtrate outlet of the filtering unit, and the extraction unit is provided with an extractant inlet;
the inlet of the rectifying tower is communicated with the extraction phase outlet of the extraction unit, the extractant outlet of the rectifying tower is communicated with the extractant inlet, and the nitrobenzene outlet of the rectifying tower is communicated with the organic solvent pipeline for production;
the inlet of the biochemical treatment unit is communicated with the raffinate phase outlet of the extraction unit, and the outlet of the biochemical treatment unit is communicated with a wastewater standard discharge pipeline;
the outlet of the dissolving tank is communicated with the filter cake outlet of the filtering unit, and the dissolving tank is provided with a concentrated hydrochloric acid inlet;
and the inlet of the reaction kettle is communicated with the outlet of the dissolving tank.
The beneficial effects of the resource-recoverable acylation wastewater treatment system and the resource-recoverable acylation wastewater treatment process in the embodiments of the present invention are substantially the same, and are not described herein again,
In some embodiments of the invention, the extraction unit is a centrifugal extraction device; the filtering unit is a plate-and-frame filter press.
In some embodiments of the invention, the biochemical treatment unit is an activated sludge treatment system.
Additional aspects and advantages of the invention will be set forth in part in the description which follows and, in part, will be obvious from the description, or may be learned by practice of the invention.
Drawings
The foregoing and/or additional aspects and advantages of the present invention will become apparent and readily appreciated from the following description of the embodiments, taken in conjunction with the accompanying drawings of which:
FIG. 1 is a flow diagram of a process for treating resource-recoverable, acylated wastewater (i.e., a diagram of a resource-recoverable, acylated wastewater treatment system) in accordance with one embodiment of the present invention.
Fig. 2 is a diagram of a conventional activated sludge treatment system (i.e., an activated sludge process flow diagram).
FIG. 3 is a graph showing the change in COD during the treatment of the acylated wastewater by the resource-recoverable acylated wastewater treatment process of example 1 of the present invention.
FIG. 4 is a graph showing the change in COD during the treatment of the acylated wastewater by the resource-recoverable acylated wastewater treatment process of example 2 of the present invention.
FIG. 5 is a graph showing the change in COD during the treatment of the acylated wastewater by the resource-recoverable acylated wastewater treatment process of example 3 of the present invention.
Reference numerals:
1-a regulating reservoir; 2-a sedimentation tank; 3-a filtration unit; 4-an extraction unit; 5-a rectifying tower; 6-biochemical treatment unit; 601-an aeration tank; 602-a secondary sedimentation tank; 7-a dissolving tank; 8-a reaction kettle.
Detailed Description
Reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings. The embodiments described below with reference to the drawings are illustrative and intended to be illustrative of the invention and are not to be construed as limiting the invention.
A resource-recoverable acylated wastewater treatment process, a resource-recoverable acylated wastewater treatment system, according to embodiments of the present invention, will now be described with reference to the accompanying drawings.
FIG. 1 is a flow diagram of a process for treating resource-recoverable, acylated wastewater (i.e., a system diagram of a resource-recoverable, acylated wastewater treatment process) according to one embodiment of the present invention.
As shown in fig. 1, the resource-recoverable acylated wastewater treatment system of the embodiment of the present invention comprises: the device comprises a sedimentation tank 2, a filtering unit 3, an extraction unit 4, a rectifying tower 5, a biochemical treatment unit 6, a dissolving tank 7 and a reaction kettle 8; the sedimentation tank 2 is used for generating aluminum hydroxide sediment; the inlet of the filtering unit 3 is communicated with the outlet of the sedimentation tank 2; the inlet of the extraction unit 4 is communicated with the filtrate outlet of the filtering unit 3, and the extraction unit 4 is provided with an extractant inlet; an inlet of the rectifying tower 5 is communicated with an extract phase outlet of the extraction unit 4, an extractant outlet of the rectifying tower 5 is communicated with an extractant inlet, and a nitrobenzene outlet of the rectifying tower 5 is communicated with a production organic solvent pipeline; an inlet of the biochemical treatment unit 6 is communicated with a raffinate phase outlet of the extraction unit 4, and an outlet of the biochemical treatment unit 6 is communicated with a wastewater discharge pipeline reaching the standard; an outlet of the dissolving tank 7 is communicated with a filter cake outlet of the filtering unit 3, and the dissolving tank 7 is provided with a concentrated hydrochloric acid inlet; the inlet of the reaction kettle 8 is communicated with the outlet of the dissolving tank 7.
Optionally, the extraction unit is a centrifugal extraction device, such as a commercially available centrifugal extractor or the like.
Alternatively, the biochemical treatment unit may employ an activated sludge treatment system. The activated sludge system is not the key point of the invention, and a conventional activated sludge treatment system is adopted. As shown in fig. 2, the conventional activated sludge treatment system includes an aeration tank 601, a secondary sedimentation tank 602, a reflux system, a surplus sludge discharge system, an oxygen supply system, and the like, in some embodiments of the present invention, the raffinate phase outlet of the extraction unit 4 is communicated with the water inlet of the aeration tank 601, i.e., the raffinate phase can be introduced into the activated sludge treatment system, and treated according to the conventional activated sludge method, so as to achieve the standard discharge.
It should be noted that, in the resource-recoverable acylation wastewater treatment system of the embodiment of the present invention, the communication mode between the components can be realized by pipeline communication or transportation by a transport vehicle or the like according to the properties of the materials, and if the pipeline communication is adopted, valves and pumps can be installed on the corresponding pipelines according to the needs, which belong to the conventional technologies and are not the key points of the present invention.
Optionally, in order to adjust the water amount, balance the water quality, and pre-treat the acylated wastewater, the acylated wastewater treatment system capable of recovering resources of the embodiment of the invention further comprises an adjusting tank arranged in front of the sedimentation tank. The method comprises the steps of firstly adjusting the water quality and the water quantity of the acylation wastewater in an adjusting tank, pretreating the acylation wastewater, and then feeding the acylation wastewater into a sedimentation tank.
Alternatively, the reaction kettle may be a stainless steel reaction kettle or the like. The sedimentation tank can adopt a horizontal flow sedimentation tank or a vertical flow sedimentation tank and the like, and the filtering unit can adopt a plate-and-frame filter press. The dissolving tank can be a common dissolving tank, and the rectifying tower can be a packed tower or a plate tower and the like.
The work principle of the resource-recoverable acylation wastewater treatment system provided by the embodiment of the invention is as follows:
when in use, the acylation wastewater firstly enters the regulating tank 1 to regulate the water quantity, balance the water quality and carry out pretreatment, and then enters the sedimentation tank 2; adjusting the pH of the acylation wastewater entering the sedimentation tank 2 to be alkaline (the pH is about 9) by an alkali source, precipitating aluminum ions in the acylation wastewater into aluminum hydroxide, filtering suspension containing the aluminum hydroxide precipitate in a filtering unit 3, wherein the filtrate enters an extraction unit 4, extracting and layering the filtrate by an extractant in the extraction unit 4 under the stirring condition to form an extraction phase and a raffinate phase, then enabling the extraction phase to enter a rectifying tower 5 to realize efficient separation of nitrobenzene and the extractant to obtain raw materials of nitrobenzene and the extractant, enabling the extractant coming out of the rectifying tower 5 to reenter the extraction unit 4 to participate in extraction of the filtrate, and enabling the nitrobenzene coming out of the rectifying tower 5 to enter an organic solvent pipeline for production of related chemicals; the raffinate phase from the extraction unit 4 enters a biochemical treatment unit 6, and is discharged after reaching the standard after biochemical treatment. And the aluminum hydroxide filter cake discharged from the filtering unit 3 enters a dissolving tank 7, is heated and dissolved under the action of concentrated hydrochloric acid in the dissolving tank 7, then enters a reaction kettle, and is polymerized with an auxiliary agent added into the reaction kettle 8 to obtain a water treatment agent polyaluminum chloride, wherein the quality of the obtained polyaluminum chloride meets the national standard GB/T22627-2014 water treatment agent polyaluminum chloride.
In the resource-recoverable acylation wastewater treatment process according to the embodiment of the present invention, the treatment of the acylation wastewater and the recovery of the resource can be performed by the resource-recoverable acylation wastewater treatment system according to the embodiment of the present invention, but the system apparatus by which the treatment is performed is not limited to the resource-recoverable acylation wastewater treatment system according to the embodiment of the present invention.
The resource-recoverable acylation wastewater treatment process of the embodiments of the present invention will be described with reference to specific examples.
Raw material reagents and equipment involved in the examples of the present invention are commercially available reagents and equipment unless otherwise specified; the detection methods and the like involved in the embodiments of the present invention are all conventional methods unless otherwise specified.
The following examples of the present invention were conducted under laboratory conditions, and the suction filtration was performed using a laboratory suction filtration apparatus composed of a buchner funnel, a suction flask, a hose, a suction pump, and filter paper.
Example 1
500mL of acylation wastewater (COD: 6530mg/L, nitrobenzene: 3200mg/L, chloride ion: 3000mg/L, and aluminum ion: 3000mg/L) is taken to be put into a beaker, 8g of sodium hydroxide is added, the pH is adjusted to 9.0, and the reaction is carried out for 0.5h, so as to obtain suspension containing aluminum hydroxide precipitate; and then, carrying out suction filtration on the suspension to obtain a filter cake and filtrate, and naturally airing the filter cake. The pH of the filtrate was adjusted to 2 with 18 wt% hydrochloric acid, and the filtrate was transferred to a separatory funnel containing 500mL of n-heptane, shaken well and then allowed to stand for 30min for separation. And (3) transferring the supernatant (extract phase) into a packed tower for rectification recovery (the number of tower plates is 15, the reflux ratio is 0.06, the temperature at the top of the tower is 98 ℃, and the temperature at the bottom of the tower is 176 ℃) to obtain a nitrobenzene raw material with the purity of 99 percent and an extracting agent n-heptane with the purity of 98 percent, wherein the recovery rate of nitrobenzene is 90 percent, and the loss amount of the extracting agent n-heptane is only 3 percent. Transferring the lower layer solution (raffinate phase) of the separating funnel into an activated sludge treatment system for further treatment for 10 hours. 10000mg of dried filter cake is added into a beaker filled with 5000mL of concentrated hydrochloric acid to be dissolved at 40 ℃, and then the filter cake reacts with 500mg of calcium aluminate at 70 ℃ and 0.5MPa to obtain the polyaluminium chloride product.
Through detection, after the activated sludge treatment system is used for treatment, the COD (chemical oxygen demand) in effluent is 55mg/L (shown in figure 3), and the nitrobenzene concentration is 0.5mg/L, which meet the requirements of the discharge standard GB8978-1996 integrated wastewater discharge standard (COD <100mg/L, nitrobenzene <1.0 mg/L); the main indexes of the obtained product polyaluminium chloride are as follows: the mass fraction of the aluminum chloride is 29 percent, the basicity is 55 percent, the mass fraction of the water-insoluble substance is 0.2, the pH value is 4.5, the mass fraction of the iron is 1.0 percent, arsenic, lead, chromium, mercury and cadmium are not detected, and all indexes of the product polyaluminum chloride meet the requirements of the national standard GB/T22627-2014 water treatment agent-polyaluminum chloride.
Example 2
500mL of acylation wastewater (COD: 6900mg/L, nitrobenzene: 2700mg/L, chloride ion: 3000mg/L, and aluminum ion: 3000mg/L) is taken to be put into a beaker, 7.5g of potassium hydroxide is added, the pH is adjusted to 9.2, and the reaction is carried out for 0.5h, so as to obtain suspension containing aluminum hydroxide precipitate; and then, carrying out suction filtration on the suspension to obtain a filter cake and filtrate, and naturally airing the filter cake. The pH of the filtrate was adjusted to 2.5 with 50 wt% sulfuric acid, and the filtrate was transferred to a separatory funnel containing 600mL of n-heptane, shaken well and allowed to stand for 30min for separation. And (3) transferring the supernatant (extract phase) into a rectifying tower for rectification and recovery (the number of tower plates is 15, the reflux ratio is 0.06, the temperature at the top of the tower is 98 ℃, and the temperature at the bottom of the tower is 176 ℃) to obtain a nitrobenzene raw material with the purity of 99 percent and an extracting agent n-heptane with the purity of 98 percent, wherein the recovery rate of nitrobenzene reaches 92 percent, and the loss amount of the extracting agent n-heptane is only 4 percent. Transferring the lower layer solution (raffinate phase) of the separating funnel into an activated sludge treatment system for further treatment for 12 hours. 10000mg of dried filter cake is added into a dissolving tank containing 6000mL of concentrated hydrochloric acid to be dissolved at 45 ℃, and then the filter cake reacts with 400mg of magnesium aluminate at 80 ℃ and 0.7MPa to obtain the polyaluminium chloride product.
Through detection, after the activated sludge treatment system is used for treatment, the COD (chemical oxygen demand) in effluent is 50mg/L (shown in figure 4), and the nitrobenzene concentration is 0.5mg/L, which meet the requirements of the discharge standard GB8978-1996 integrated wastewater discharge standard (COD <100mg/L, nitrobenzene <1.0 mg/L); the main indexes of the obtained product polyaluminium chloride are as follows: 30 percent of aluminum chloride, 56 percent of basicity, 0.3 percent of water-insoluble substances, 5.0 percent of pH value and 1.0 percent of iron, wherein arsenic, lead, chromium, mercury and cadmium are not detected, and all indexes of the product polyaluminium chloride meet the requirements of national standard GB/T22627-2014 water treatment agent-polyaluminium chloride.
Example 3
500mL of acylation waste water (COD: 7200mg/L, nitrobenzene: 4200mg/L, chloride ion: 3000mg/L, aluminum ion: 2500mg/L) is taken out of a beaker, 8.2g of potassium hydroxide is added, the pH is adjusted to 9.0, and the reaction is carried out for 0.5h, so as to obtain a suspension containing aluminum hydroxide precipitate; and then, carrying out suction filtration on the suspension to obtain a filter cake and filtrate, and naturally airing the filter cake. The pH of the filtrate is adjusted to 3 by 15 wt% hydrochloric acid, and the filtrate is transferred into a separating funnel filled with 600mL of n-heptane, shaken up and then kept stand for 30min for layering. And (3) transferring the supernatant (extract phase) into a rectifying tower for rectification and recovery (the number of tower plates is 15, the reflux ratio is 0.06, the temperature at the top of the tower is 98 ℃, and the temperature at the bottom of the tower is 176 ℃) to obtain a nitrobenzene raw material with the purity of 99% and an extracting agent n-heptane with the purity of 99%, wherein the recovery rate of nitrobenzene is 88%, and the loss of the extracting agent n-heptane is only 6%. Transferring the lower layer solution (raffinate phase) of the separating funnel into an activated sludge treatment system for further treatment for 12 hours. 8000mg of the dried filter cake is added into a dissolving tank containing 5000mL of concentrated hydrochloric acid to be dissolved at 50 ℃, and then the obtained product reacts with 450mg of magnesium aluminate at 80 ℃ and 0.7MPa to obtain the polyaluminium chloride product.
Through detection, after the activated sludge treatment system is used for treatment, the COD (chemical oxygen demand) in effluent is 55mg/L (shown in figure 5), and the nitrobenzene concentration is 0.5mg/L, which meet the requirements of the discharge standard GB8978-1996 integrated wastewater discharge standard (COD <100mg/L, nitrobenzene <1.0 mg/L); the main indexes of the obtained product polyaluminium chloride are as follows: the aluminum chloride has the mass fraction of 31 percent, the basicity of 62 percent, the mass fraction of water-insoluble substances of 0.4, the pH value of 6.5 and the mass fraction of iron of 2.0 percent, arsenic, lead, chromium, mercury and cadmium are not detected, and all indexes of the product polyaluminium chloride meet the requirements of the national standard GB/T22627-2014 water treatment agent-polyaluminium chloride.
Example 4
This example is essentially the same as example 1 except that the extractant is carbon tetrachloride.
Example 5
This example is substantially the same as example 1 except that the extractant is a mixture of n-octane and xylene in a volume ratio of 1: 1.
In the present disclosure, the terms "one embodiment," "some embodiments," "an example," "a specific example," or "some examples" and the like mean that a specific feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present disclosure. In this specification, the schematic representations of the terms used above are not necessarily intended to refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, various embodiments or examples and features of different embodiments or examples described in this specification can be combined and combined by one skilled in the art without contradiction.
In the present invention, unless otherwise explicitly stated or limited, the terms "mounted," "connected," "fixed," and the like are to be construed broadly, e.g., as being permanently connected, detachably connected, or integral; may be mechanically coupled, may be electrically coupled or may be in communication with each other; they may be directly connected or indirectly connected through intervening media, or they may be connected internally or in any other suitable relationship, unless expressly stated otherwise. The specific meanings of the above terms in the present invention can be understood according to specific situations by those of ordinary skill in the art.
Although embodiments of the present invention have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention, and that variations, modifications, substitutions and alterations can be made to the above embodiments by those of ordinary skill in the art within the scope of the present invention.
Claims (10)
1. A resource-recoverable acylation wastewater treatment process is characterized by comprising the following steps:
(1) adjusting the pH value of the acylation wastewater to be alkaline to obtain a suspension containing aluminum hydroxide precipitate, and filtering the suspension to obtain an aluminum hydroxide filter cake and a filtrate;
(2) adjusting the pH value of the filtrate to acidity, then transferring the filtrate into an extracting agent, stirring and standing to obtain a layered raffinate phase and an extract phase;
(3) performing biochemical treatment on the raffinate phase to reach the standard and discharging;
(4) rectifying and separating the extract phase to obtain nitrobenzene and the extractant, recycling the nitrobenzene as an organic solvent, and reusing the extractant for extracting the filtrate;
(5) and adding concentrated hydrochloric acid into the filter cake, heating and dissolving, adding an auxiliary agent, and polymerizing to obtain the polyaluminum chloride.
2. The process for treating resource-recoverable acylated wastewater according to claim 1, wherein in step (1), the adjusting the pH of the acylated wastewater to alkaline comprises: adjusting the pH value of the acylation wastewater to 8-10 by adopting an alkali raw material, wherein the alkali raw material is one or more than two of sodium hydroxide, potassium hydroxide or liquid ammonia.
3. The resource-recoverable, acylated wastewater treatment process according to claim 1, wherein in step (2), said adjusting the filtrate to acidic pH comprises: and adjusting the pH of the filtrate to 2-3 by using acid, wherein the acid is one or more than two of hydrochloric acid, nitric acid or sulfuric acid.
4. The process for treating acylation waste water capable of resource recovery according to claim 1, wherein in the step (2), the extractant is a non-polar organic solvent, and the volume ratio of the extractant to the filtrate is 0.5-5: 1.
5. The process for treating acylation waste water capable of resource recovery according to claim 4, wherein the extraction agent is one or more than two of n-heptane, n-octane, n-hexane, benzene, toluene, xylene and carbon tetrachloride.
6. The process for treating acylation waste water recyclable according to claim 1, wherein in the step (3), the biochemical treatment is an activated sludge method; in the step (5), the heating and dissolving temperature is 40-50 ℃, and the weight ratio of the filter cake to the concentrated hydrochloric acid is 0.5-2.5: 1.
7. The process for treating acylation waste water capable of recycling resources according to claim 1, wherein in the step (5), the addition amount of the auxiliary agent is 2-10 wt% of the dry weight of the filter cake, and the auxiliary agent is calcium aluminate or/and magnesium aluminate.
8. A resource-recoverable, acylated wastewater treatment system, comprising:
the sedimentation tank is used for generating aluminum hydroxide sediment;
the inlet of the filtering unit is communicated with the outlet of the sedimentation tank;
an inlet of the extraction unit is communicated with a filtrate outlet of the filtering unit, and the extraction unit is provided with an extractant inlet;
the inlet of the rectifying tower is communicated with the extraction phase outlet of the extraction unit, the extractant outlet of the rectifying tower is communicated with the extractant inlet, and the nitrobenzene outlet of the rectifying tower is communicated with the organic solvent pipeline for production;
the inlet of the biochemical treatment unit is communicated with the raffinate phase outlet of the extraction unit, and the outlet of the biochemical treatment unit is communicated with a wastewater standard discharge pipeline;
the outlet of the dissolving tank is communicated with the filter cake outlet of the filtering unit, and the dissolving tank is provided with a concentrated hydrochloric acid inlet;
and the inlet of the reaction kettle is communicated with the outlet of the dissolving tank.
9. The resource-recoverable, acylated wastewater treatment system according to claim 8, wherein said extraction unit is a centrifugal extraction device; the filtering unit is a plate-and-frame filter press.
10. The resource-recoverable, acylated wastewater treatment system according to claim 8, characterized in that the biochemical treatment unit is an activated sludge treatment system.
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| CN202210530956.7A CN114890623B (en) | 2022-05-16 | 2022-05-16 | Acylation wastewater treatment process and system capable of recycling resources |
| PCT/CN2022/115478 WO2023040641A1 (en) | 2021-09-14 | 2022-08-29 | Acylation solution and process method for continuously synthesizing acyl naphthalene using acylation solution |
| JP2022573236A JP2023546762A (en) | 2021-09-14 | 2022-08-29 | Acylation liquid and process method for continuous synthesis of acylnaphthalene using acylation liquid |
| US18/057,394 US20230095165A1 (en) | 2021-09-14 | 2022-11-21 | Method for continuous synthesis of acylnaphthalene with acylation liquid |
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| WO2023040641A1 (en) * | 2021-09-14 | 2023-03-23 | 煤炭科学技术研究院有限公司 | Acylation solution and process method for continuously synthesizing acyl naphthalene using acylation solution |
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