CN114163289A - System and method for extracting crude anthracene by continuous cooling crystallization method - Google Patents
System and method for extracting crude anthracene by continuous cooling crystallization method Download PDFInfo
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- CN114163289A CN114163289A CN202111441835.7A CN202111441835A CN114163289A CN 114163289 A CN114163289 A CN 114163289A CN 202111441835 A CN202111441835 A CN 202111441835A CN 114163289 A CN114163289 A CN 114163289A
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- MWPLVEDNUUSJAV-UHFFFAOYSA-N anthracene Chemical compound C1=CC=CC2=CC3=CC=CC=C3C=C21 MWPLVEDNUUSJAV-UHFFFAOYSA-N 0.000 title claims abstract description 428
- 238000002425 crystallisation Methods 0.000 title claims abstract description 59
- 238000001816 cooling Methods 0.000 title claims abstract description 57
- 238000000034 method Methods 0.000 title claims abstract description 23
- 230000008025 crystallization Effects 0.000 claims abstract description 47
- 239000002994 raw material Substances 0.000 claims abstract description 7
- 239000013078 crystal Substances 0.000 claims description 26
- 239000000498 cooling water Substances 0.000 claims description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- 238000010992 reflux Methods 0.000 claims description 10
- 239000000463 material Substances 0.000 claims description 9
- 238000007599 discharging Methods 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims 1
- 238000000605 extraction Methods 0.000 abstract description 5
- 230000008569 process Effects 0.000 abstract description 5
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 230000006872 improvement Effects 0.000 abstract description 4
- 230000009467 reduction Effects 0.000 abstract description 3
- 238000004140 cleaning Methods 0.000 abstract description 2
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 230000000694 effects Effects 0.000 description 6
- 238000003756 stirring Methods 0.000 description 4
- 238000012986 modification Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000004806 packaging method and process Methods 0.000 description 3
- 238000012423 maintenance Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000012297 crystallization seed Substances 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000007790 scraping Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
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- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/14—Purification; Separation; Use of additives by crystallisation; Purification or separation of the crystals
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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Abstract
The invention relates to the technical field of crude anthracene extraction, in particular to a system and a method for extracting crude anthracene by a continuous cooling crystallization method, which comprises an anthracene oil tank, a crystallizer, a crystallized anthracene oil buffer tank, a centrifugal machine and a crystallized anthracene oil tank, wherein the crystallizer comprises a first crystallizer, a second crystallizer and a third crystallizer which are sequentially connected; the raw material anthracene oil enters three crystallizers connected in series for carrying out tertiary cooling crystallization, then automatically flows into an airtight vertical scraper automatic discharge centrifuge, the separated crystal-removed anthracene oil automatically flows into a crystal-removed anthracene oil groove, one part of the crystal-removed anthracene oil flows back to the primary crystallizer, and the crude anthracene is discharged to a crude anthracene intermediate tank at the bottom of the vertical scraper automatic discharge centrifuge, so that the purpose of continuous crude anthracene crystallization is achieved. The method for extracting crude anthracene by continuous cooling crystallization has the advantages of high automation degree, stable process index, improvement of product yield, reduction of labor intensity and energy consumption, few leakage points, frequent overhauling and cleaning, few and precise equipment, high practicability, environmental protection and the like.
Description
Technical Field
The invention relates to the technical field of crude anthracene extraction, and particularly relates to a system and a method for extracting crude anthracene by a continuous cooling crystallization method.
Background
At present, there are two methods for producing crude anthracene in China: firstly, a method of separating by a centrifuge after cooling crystallization in a stirring kettle way; and secondly, a crystallizer is adopted, the crude anthracene is crystallized, sweated, melted completely and the like in the crystallizer to produce liquid crude anthracene.
Patent CN103980085B discloses a crude anthracene extraction system and an extraction method, which realize continuous and rapid cooling, crystallization, crystal growing and centrifugal separation in the crude anthracene extraction process through twice crystallization; however, when the system is produced, the operation workload of workers is large, and the capacity release of equipment is influenced. The temperature reduction and crystallization process must be controlled in a segmented manner due to different temperatures and time, the automation degree of the crystallization process is low, the index control difficulty is high, and the crystallization effect and the product yield are greatly influenced by factors of manual control. During the crystallization period of a single crystallizer, pipelines and valves are easy to block. The equipment utilization rate is low, and the overhaul and maintenance cost is high. During the interval charging and discharging of the crystallizer, the consumption of cooling water is high, and the energy loss is large.
Disclosure of Invention
The invention aims to provide a system and a method for extracting crude anthracene by a continuous cooling crystallization method, which can reduce the influence of external environment on system operation.
The technical scheme for realizing the purpose is as follows:
a system for extracting crude anthracene by a continuous cooling crystallization method, which comprises,
the anthracene oil tank is used for storing and providing anthracene oil;
the crystallizer group comprises a first crystallizer, a second crystallizer and a third crystallizer which are connected in sequence; the inlet end of the first crystallizer is connected to an anthracene oil tank, and the outlet of the third crystallizer is connected to the anthracene oil crystallizing buffer tank;
the crystallized anthracene oil buffer tank is used for receiving the cooled crystals flowing out of the third crystallizer and allowing the crude anthracene crystals after cooling crystallization to stay for continuous growth;
the inlet end of the centrifuge is connected with the crystallized anthracene oil buffer tank; used for separating the anthracene oil after crystal growing into crude anthracene and decrystallized anthracene oil;
and the de-crystallized anthracene oil tank is used for storing de-crystallized anthracene oil and refluxing the de-crystallized anthracene oil to the first crystallizer.
Further, the first crystallizer, the second crystallizer and the third crystallizer are all horizontal stirred tank crystallizers.
Further, the first crystallizer, the second crystallizer and the third crystallizer are arranged from top to bottom, and materials in the crystallizers are discharged by self-flowing through height difference.
Furthermore, a circulating water cooling system is further arranged, and circulating water flows into the third crystallizer, the second crystallizer and the first crystallizer in sequence.
Still further, the crystallizer group sets up the multiunit, multiunit crystallizer group parallel connection in between an anthracene oil jar with crystallization anthracene oil buffer tank.
Further, an anthracene oil in the anthracene oil tank is lifted to the crystallizer through an anthracene oil charging pump.
Further, the decrystallized anthracene oil in the decrystallized anthracene oil tank is output to a system through a decrystallized anthracene oil delivery pump or flows back to the crystallizer to be used as a feeding material of the first crystallizer.
Further, the crude anthracene separated by the centrifugal machine enters a crude anthracene intermediate tank.
Further, the centrifugal machine adopts a vertical scraper automatic discharging centrifugal machine for separation.
A method for extracting crude anthracene by a continuous cooling crystallization method comprises the following steps:
and (3) extracting crude anthracene device: the device comprises an anthracene oil tank, a crystallizer group, a crystallized anthracene oil buffer tank, a centrifugal machine and a crystallized anthracene oil tank which are connected in sequence; the circulating water cooling system is further arranged, and the circulating water flows into the third crystallizer, the second crystallizer and the first crystallizer in sequence; the crystallizer groups are arranged into a plurality of groups, and the plurality of groups of crystallizer groups are connected in parallel between an anthracene oil tank and a crystallized anthracene oil buffer tank;
the method comprises the following steps:
s1, feeding anthracene oil into a first crystallizer through an anthracene oil tank, performing primary cooling crystallization by using circulating cooling water outlet of a second crystallizer and the cooling capacity of the decrystallized anthracene oil refluxed by the decrystallized anthracene oil tank, and then automatically flowing the cooled anthracene oil into the second crystallizer;
wherein the temperature of the anthracene oil is 75-80 ℃, and the temperature of the refluxing decrystallized anthracene oil is 45-50 ℃; the primary cooling crystallization temperature is 50-55 ℃;
s2, placing the anthracene oil after the first crystallization in a second crystallizer, performing secondary cooling crystallization by using the cold energy of the circulating cooling water of the first crystallizer, and automatically flowing the anthracene oil into a third crystallizer;
wherein the secondary cooling crystallization temperature is 40-45 ℃;
s3, cooling the anthracene oil subjected to the second crystallization in a second crystallizer by using the cold energy of circulating cooling water to finish the third cooling crystallization;
wherein the third cooling crystallization temperature is 30-38 ℃;
s4, naturally flowing the crude anthracene crystal after cooling and crystallization into a crystallized anthracene oil buffer tank for staying and continuously growing;
s5, separating the anthracene oil after crystal growing into crude anthracene and crystal removed anthracene oil by a centrifugal machine;
s6, enabling the decrystallized anthracene oil to automatically flow into a decrystallized anthracene oil tank, and enabling the decrystallized anthracene oil in the decrystallized anthracene oil tank to flow back to the first crystallizer; crude anthracene export system.
The invention has the beneficial effects that:
the invention provides a system and a method for extracting crude anthracene by a continuous cooling crystallization method. The raw material anthracene oil enters 3 crystallizers connected in series for carrying out tertiary cooling crystallization, then automatically flows into an airtight vertical scraper automatic discharge centrifuge, the separated crystal-removed anthracene oil automatically flows into a crystal-removed anthracene oil groove, one part of the crystal-removed anthracene oil flows back to the primary crystallizer, and the crude anthracene is discharged to a crude anthracene intermediate tank at the bottom of the vertical scraper automatic discharge centrifuge, so that the purpose of continuous crude anthracene crystallization is achieved. The method for extracting crude anthracene by continuous cooling crystallization has the advantages of high automation degree, stable process index, improvement of product yield, reduction of labor intensity and energy consumption, few leakage points, frequent overhauling and cleaning, few and precise equipment, high practicability, environmental protection and the like.
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 description of the embodiments or the prior art will be briefly described below. It should be apparent that the drawings in the following description are merely exemplary, and that other embodiments can be derived from the drawings provided by those of ordinary skill in the art without inventive effort.
The structures, ratios, sizes, and the like shown in the present specification are only used for matching with the contents disclosed in the specification, so as to be understood and read by those skilled in the art, and are not used to limit the conditions that the present invention can be implemented, so that the present invention has no technical significance, and any structural modifications, changes in the ratio relationship, or adjustments of the sizes, without affecting the effects and the achievable by the present invention, should still fall within the range that the technical contents disclosed in the present invention can cover.
FIG. 1 is a schematic diagram of a system for extracting crude anthracene by a continuous cooling crystallization method according to an embodiment of the invention.
In the figure, 1, an anthracene oil tank; 2. a group of crystallizers; 21. a first crystallizer; 22. a second crystallizer; 23. a third crystallizer; 3. a crystallized anthracene oil buffer tank; 4. a centrifuge; 5. a decrystallized anthracene oil tank; 6. a crude anthracene intermediate tank; 7. a packaging machine; 8. an anthracene oil charge pump.
Detailed Description
To make the objects, technical solutions and advantages of the embodiments of the present invention clearer and more complete, the technical solutions in the embodiments of the present invention will be described below, obviously, the described embodiments are only a part of the embodiments of the present application, but not all embodiments, and the description is only for further explaining the features and advantages of the present invention, and not for limiting the claims 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 application.
The following detailed description of embodiments of the present invention is provided in connection with the accompanying drawings and examples. The following examples are intended to illustrate the invention but are not intended to limit the scope of the invention.
In the description of the present application, it is to be understood that the terms "center", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience in describing the present application and simplifying the description, but do not indicate or imply that the referred device or element must have a particular orientation, be constructed in a particular orientation, and be operated, and thus should not be construed as limiting the present application.
The terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of the present application, "a plurality" means two or more unless otherwise specified.
In the description of the present application, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present application can be understood in a specific case by those of ordinary skill in the art.
Example 1
As shown in fig. 1, a single stirred tank cooling crystallization system comprises an anthracene oil tank 1, a crystallizer group 2, a crystallized anthracene oil buffer tank 3, a centrifuge 4 and a decrystallized anthracene oil tank 5 which are connected in sequence; the crystallizer group 2 comprises a first crystallizer 21, a second crystallizer 22 and a third crystallizer 23 which are connected in sequence; the inlet end of the first crystallizer 21 is connected to the anthracene oil tank 1, and the outlet end of the third crystallizer 23 is connected to the anthracene oil crystallizing buffer tank 3; a circulating water cooling system is further arranged, and the circulating water flows into the third crystallizer 23, the second crystallizer 22 and the first crystallizer 21 in sequence; the crystallizer groups 2 are arranged into a plurality of groups, and the plurality of groups of crystallizer groups 2 are connected in parallel between an anthracene oil tank 1 and a crystallized anthracene oil buffer tank 3; the centrifuge 4 is set into a plurality of groups, and the plurality of groups of centrifuges 4 correspond to the plurality of groups of crystallizer groups 2.
It is understood that an anthracene oil tank 1 for storing and supplying an anthracene oil; the crystallized anthracene oil buffer tank 3 is used for receiving the cooled crystals flowing out from the third crystallizer 23, and allowing the crude anthracene crystals after cooling crystallization to stay for continuous growth; a centrifuge 4 for separating the anthracene oil after crystal growth into crude anthracene and crystal removed anthracene oil; and the de-crystallized anthracene oil tank 5 is used for storing de-crystallized anthracene oil and refluxing the de-crystallized anthracene oil to the first crystallizer 21. The anthracene oil intermediate tank is also arranged and used for receiving the crude anthracene separated by the centrifuge 4 and outputting the crude anthracene to the crude anthracene intermediate tank 6, and the crude anthracene intermediate tank 6 outputs the crude anthracene to the automatic packaging machine 7 for packaging.
In some embodiments of the present application, the first crystallizer 21, the second crystallizer 22 and the third crystallizer 23 are all horizontal stirred tank crystallizers.
In some embodiments of the present application, the first crystallizer 21, the second crystallizer 22 and the third crystallizer 23 are arranged from top to bottom, and the materials in the crystallizer group 2 are discharged by self-flow by using height difference.
In some embodiments of the present application, an anthracene oil in the anthracene oil tank 1 is lifted to the crystallizer group 2 by an anthracene oil loading pump 8.
In some embodiments of the present application, the decrystallized anthracene oil in the decrystallized anthracene oil tank 5 is fed to the crystallizer group 2 through a decrystallized anthracene oil delivery pump output system or returned to the first crystallizer 21.
In some embodiments of the present application, the centrifuge 4 separation employs a vertical scraper autoloading centrifuge 4.
The method for extracting the crude anthracene by adopting the system continuous cooling crystallization method comprises the following steps:
s1, feeding anthracene oil into a first crystallizer through an anthracene oil tank, performing primary cooling crystallization by using circulating cooling water outlet of a second crystallizer and the cooling capacity of the decrystallized anthracene oil refluxed by the decrystallized anthracene oil tank, and then automatically flowing the cooled anthracene oil into the second crystallizer;
wherein the temperature of the anthracene oil is 75-80 ℃, and the temperature of the refluxing decrystallized anthracene oil is 45-50 ℃; the primary cooling crystallization temperature is 50-55 ℃;
s2, placing the anthracene oil after the first crystallization in a second crystallizer, performing secondary cooling crystallization by using the cold energy of the circulating cooling water of the first crystallizer, and automatically flowing the anthracene oil into a third crystallizer;
wherein the secondary cooling crystallization temperature is 40-45 ℃;
s3, cooling the anthracene oil subjected to the second crystallization in a second crystallizer by using the cold energy of circulating cooling water to finish the third cooling crystallization;
wherein the third cooling crystallization temperature is 30-38 ℃;
s4, naturally flowing the crude anthracene crystal after cooling and crystallization into a crystallized anthracene oil buffer tank 3 for staying and continuously growing;
s5, separating the anthracene oil after crystal growing into crude anthracene and crystal removed anthracene oil by a centrifuge 4;
s6, automatically allowing the decrystallized anthracene oil to flow into the decrystallized anthracene oil tank 5, and refluxing the decrystallized anthracene oil in the decrystallized anthracene oil tank 5 to the first crystallizer 21; crude anthracene export system.
The crude anthracene crystal prepared by the system provided by the embodiment accounts for 10-12% of anthracene oil. The crude anthracene crystal can be used as raw material for producing refined anthracene.
An anthracene oil fraction is fed into the crystallizer group 2 through an anthracene oil feeding pump 8 for crystallization; wherein the temperature of an anthracene oil fraction is maintained between 75 ℃ and 80 ℃. The outer wall of the crystallizer group 2 is provided with a cooling water jacket, a cooling jacket guide cylinder is arranged in the crystallizer group 2, and a stirrer with a material scraping function is arranged, so that heat transfer is enhanced, and crystallized crude anthracene can be scraped from a cooling wall. The stirring speed was 15 r/min.
In the embodiment of the application, the horizontal stirred tank type crystallizers are connected in series to form a group, the automatic control instrument is used for detecting and controlling, the feeding and discharging amount of anthracene oil and the amount of backflow materials are controlled, the continuous feeding and the continuous discharging are carried out, and in the production process, the feeding, discharging temperature, feeding and other indexes of each crystallizer are flexibly adjusted and controlled according to the crystallization effect and the yield, so that the process index is stable, the automation degree is high, and the labor intensity of workers is reduced.
The design of the 3 horizontal stirred tank type crystallizer groups adopts the high arrangement of the upper layer, the middle layer and the lower layer, so that the materials flow downwards in a self-flowing mode, the effect of cooling and crystallizing for many times is achieved, and the power energy consumption of the material passing delivery pump is reduced. At least 2 circulating pumps are reduced by the arrangement of the series downstream crystallizer groups.
A scraper type stirring device is designed in the horizontal stirring kettle type crystallizer, and through continuous charging and discharging, the blockage of equipment, pipelines and valves is reduced, the utilization rate of the equipment is improved, and the overhaul and maintenance cost is reduced.
By circulating and refluxing the decrystallized anthracene oil, the crystallization seed crystal of the anthracene oil serving as the raw material is provided, the crystallization effect is enhanced, and the yield of a crude anthracene product is improved.
Through 30-38 ℃ crystal removal anthracene oil circulation reflux, the cooling temperature of 75-80 ℃ raw material anthracene oil is reduced, and the cooling water consumption and energy consumption can be effectively saved.
After the horizontal stirred tank crystallizer equipment is connected in series, the cooling water quantity is fully utilized and saved through cross flow heat exchange of anthracene oil and circulating water, the consumption of primary cooling water is saved, and the energy-saving effect is achieved.
Although the invention has been described in detail above with reference to a general description and specific examples, it will be apparent to one skilled in the art that modifications or improvements may be made thereto based on the invention. Accordingly, such modifications and improvements are intended to be within the scope of the invention as claimed.
Claims (10)
1. The utility model provides a serialization cooling crystallization method draws crude anthracene system which characterized in that: comprises the steps of (a) preparing a mixture of a plurality of raw materials,
the anthracene oil tank is used for storing and providing anthracene oil;
the crystallizer group comprises a first crystallizer, a second crystallizer and a third crystallizer which are connected in sequence; the inlet end of the first crystallizer is connected to the anthracene oil tank, and the outlet end of the third crystallizer is connected to the anthracene oil crystallizing buffer tank;
the crystallized anthracene oil buffer tank is used for receiving the cooled crystals flowing out of the third crystallizer and allowing the crude anthracene crystals to stay for continuous growth;
the inlet end of the centrifuge is connected with the crystallized anthracene oil buffer tank; used for separating the anthracene oil after crystal growing into crude anthracene and decrystallized anthracene oil;
and the de-crystallized anthracene oil tank is used for storing de-crystallized anthracene oil and refluxing the de-crystallized anthracene oil to the first crystallizer.
2. The system for extracting crude anthracene according to claim 1, wherein the system comprises: the first crystallizer, the second crystallizer and the third crystallizer are all horizontal stirred tank crystallizers.
3. The system for extracting crude anthracene according to claim 1, wherein the system comprises: the first crystallizer, the second crystallizer and the third crystallizer are arranged from top to bottom, and materials in the crystallizers are discharged by self-flow through height difference.
4. The system for extracting crude anthracene according to claim 1, wherein the system comprises: and a circulating water cooling system is further arranged, and circulating water flows into the third crystallizer, the second crystallizer and the first crystallizer in sequence.
5. The system for extracting the crude anthracene according to any one of claims 1 to 4, wherein the system comprises: the crystallizer groups are arranged into a plurality of groups, and the plurality of groups of crystallizer groups are connected in parallel between the anthracene oil tank and the crystallized anthracene oil buffer tank.
6. The system for extracting crude anthracene according to claim 1, wherein the system comprises: an anthracene oil in the anthracene oil tank is lifted to the crystallizer through an anthracene oil charging pump.
7. The system for extracting crude anthracene according to claim 1, wherein the system comprises: and the decrystallized anthracene oil in the decrystallized anthracene oil tank is output to a crystallizer through a decrystallized anthracene oil delivery pump or flows back to the crystallizer to be used as a feeding material of the first crystallizer.
8. The system for extracting crude anthracene according to claim 1, wherein the system comprises: the centrifugal machine adopts a vertical scraper automatic discharging centrifugal machine for separation.
9. A method for extracting crude anthracene by a continuous cooling crystallization method is characterized by comprising the following steps:
and (3) extracting crude anthracene device: the device comprises an anthracene oil tank, a crystallizer group, a crystallized anthracene oil buffer tank, a centrifugal machine and a crystallized anthracene oil tank which are connected in sequence; the circulating water cooling system is further arranged, and the circulating water flows into the third crystallizer, the second crystallizer and the first crystallizer in sequence; the crystallizer groups are arranged into a plurality of groups, and the plurality of groups of crystallizer groups are connected in parallel between an anthracene oil tank and a crystallized anthracene oil buffer tank;
the method comprises the following steps:
s1, feeding anthracene oil into a first crystallizer through an anthracene oil tank, performing primary cooling crystallization by using circulating cooling water outlet of a second crystallizer and the cooling capacity of the decrystallized anthracene oil refluxed by the decrystallized anthracene oil tank, and then automatically flowing the cooled anthracene oil into the second crystallizer;
wherein the temperature of the anthracene oil is 75-80 ℃, and the temperature of the refluxing decrystallized anthracene oil is 45-50 ℃; the primary cooling crystallization temperature is 50-55 ℃;
s2, placing the anthracene oil after the first crystallization in a second crystallizer, performing secondary cooling crystallization by using the cold energy of the circulating cooling water of the first crystallizer, and automatically flowing the anthracene oil into a third crystallizer;
wherein the secondary cooling crystallization temperature is 40-45 ℃;
s3, cooling the anthracene oil subjected to the second crystallization in a second crystallizer by using the cold energy of circulating cooling water to finish the third cooling crystallization;
wherein the third cooling crystallization temperature is 30-38 ℃;
s4, naturally flowing the crude anthracene crystal after cooling and crystallization into a crystallized anthracene oil buffer tank for staying and continuously growing;
s5, separating the anthracene oil after crystal growing into crude anthracene and crystal removed anthracene oil by a centrifugal machine;
s6, enabling the decrystallized anthracene oil to automatically flow into a decrystallized anthracene oil tank, and enabling the decrystallized anthracene oil in the decrystallized anthracene oil tank to flow back to the first crystallizer; crude anthracene export system.
10. The method for extracting the crude anthracene according to claim 9, wherein the method comprises the following steps: the method provides the raw material anthracene oil crystal seed crystal through circulation reflux of the decrystallized anthracene oil, and improves the yield of the crude anthracene product.
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| CN114163289B (en) | 2022-08-30 |
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