CN111334325A - Method for transforming industrial naphthalene system into wash oil purification system - Google Patents
Method for transforming industrial naphthalene system into wash oil purification system Download PDFInfo
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- CN111334325A CN111334325A CN202010224194.9A CN202010224194A CN111334325A CN 111334325 A CN111334325 A CN 111334325A CN 202010224194 A CN202010224194 A CN 202010224194A CN 111334325 A CN111334325 A CN 111334325A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1003—Waste materials
- C10G2300/1007—Used oils
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Abstract
The invention relates to a method for transforming an industrial naphthalene system into a wash oil purification system. The method is characterized in that a mixed oil groove is added on the basis of an industrial naphthalene system, and the mixed oil groove is connected with an oil washing outlet; connecting the mixed oil groove with the washed three-mixed oil groove through a pipeline, feeding the mixed oil in the mixed oil groove into the washed three-mixed oil groove through the pipeline after primary distillation separation, then carrying out secondary distillation separation in a rectifying tower without flowing through a primary distillation tower; the industrial naphthalene system is used for emptying a storage tank or adding a high-quality wash oil storage tank to be connected with an industrial naphthalene outflow port so as to receive high-quality wash oil separated by secondary distillation. The reforming method provided by the invention realizes the first and the last two distillation processes in one distillation tower, basically does not change the pipeline connection relation of the original system, can obviously reduce the reforming workload of the distillation system and reduce the reforming cost.
Description
Technical Field
The invention belongs to the field of distillation devices, and particularly relates to a method for transforming an industrial naphthalene system into an oil washing purification system.
Background
Distillation separation is an important means for oil separation. Taking coal tar as an example, high-temperature coal tar is a complex mixture composed of aromatic hydrocarbons, and when the coal tar is continuously distilled, fractions such as light oil, phenol oil, naphthalene oil, wash oil, anthracene oil, asphalt and the like can be cut, and the fractions can be further processed to separate and prepare various products. In further processing, secondary distillation (primary distillation and rectification) is often needed to obtain industrial products with higher purity, such as industrial naphthalene produced by three-component oil, industrial naphthalene produced by heavy benzene, distillation separation of wash oil and the like.
Taking the tar distillation product three-mixed oil as a raw material to produce industrial naphthalene as an example, the three-mixed oil needs to be subjected to a secondary distillation process of primary distillation and rectification to obtain the industrial naphthalene, and the process comprises the following steps: and primarily distilling the tertiary mixed oil in a primary distillation tower to obtain a product phenol oil at the top of the primary distillation tower, obtaining the secondary mixed oil of naphthalene washing at the bottom of the primary distillation tower, sending the secondary mixed oil of naphthalene washing to a rectification tower for rectification, obtaining industrial naphthalene at the top of the rectification tower, and obtaining washing oil at the bottom of the rectification tower.
Distillation separation belongs to high energy consumption operation, and the collection of components and the multi-stage utilization of heat energy need to be reasonably set according to the physical properties of components at the top and the bottom of a tower. For example, in the industrial naphthalene distillation process disclosed in the chinese patent application with application publication No. CN103242131A, after phenol oil vapor obtained from the top of the primary tower is evaporated from the top of the primary tower, the phenol oil vapor is subjected to gas-liquid separation by a condenser-cooler and then subjected to oil-water separation by an oil-water separator, so as to obtain a phenol oil product meeting the requirements. And condensing and cooling industrial naphthalene vapor extracted from the top of the rectifying tower to obtain an industrial naphthalene product. Meanwhile, the tower top component and the tower bottom component are fluids carrying different heat energy, and the distillation system needs to consider the heat exchange of the fluids carrying different heat energy to fully utilize the heat energy.
The characteristics determine that the physical properties of original oil products and separated components are always required to be considered in the construction of a secondary distillation system, and corresponding fraction collecting systems are respectively matched in the primary distillation process and the rectification process to finish the collection of different separated components. With the development of enterprises, new oil products and new separation requirements are continuously increased, and besides constructing a new secondary distillation system, the modification of the existing secondary distillation system is also one of the ways for the enterprises to complete optimization and upgrade and improve the product competitiveness.
If the existing secondary distillation system is modified according to different collection requirements of the primary distillation component and the rectification component, the engineering quantity is large, the modification cost is high, the production line debugging period is long, and the requirement of rapid development of enterprises cannot be met.
Disclosure of Invention
The invention aims to provide a method for transforming an industrial naphthalene system into an oil washing purification system, which has the characteristics of small transformation engineering amount and low transformation cost.
In order to realize the purpose, the technical scheme adopted by the method for transforming the industrial naphthalene system into the wash oil purification system is as follows:
the method comprises the steps of transforming an industrial naphthalene system into an oil washing and purifying system, wherein the industrial naphthalene system comprises a washed three-mixed oil groove, a primary distillation tower, a rectifying tower top component collecting device and a rectifying tower bottom component collecting device, and the rectifying tower top component collecting device comprises an industrial naphthalene cooling system with an industrial naphthalene outflow port and an industrial naphthalene storage tank for collecting industrial naphthalene; the rectifying tower bottom component collecting device comprises a tower bottom component cooling system with an oil washing outlet and an oil washing storage tank for collecting oil washing;
the method is characterized in that a mixed oil groove is added on the basis of an industrial naphthalene system, and the mixed oil groove is connected with an oil washing outlet; the washing oil to be purified does not flow through the primary distillation tower in a distillation mode, primary distillation separation is carried out in the rectification tower, and the mixed oil groove is used for receiving mixed oil separated by the primary distillation separation;
connecting the mixed oil groove with the washed three-mixed oil groove through a pipeline, feeding the mixed oil in the mixed oil groove into the washed three-mixed oil groove through the pipeline after primary distillation separation, then carrying out secondary distillation separation in a rectifying tower without flowing through a primary distillation tower; using an empty storage tank of an industrial naphthalene system or adding a high-quality wash oil storage tank to be connected with an outlet of the industrial naphthalene to receive high-quality wash oil separated by secondary distillation;
or on the basis of an industrial naphthalene system, an oil washing storage tank is connected with a washed three-oil-mixing tank through a pipeline, the oil to be purified does not flow through a primary distillation tower, primary distillation separation is carried out in a rectification tower, and the oil washing storage tank is used for receiving the mixed oil separated by the primary distillation; after the primary distillation separation, feeding the mixed oil in the oil washing storage tank to a washed three-mixed oil tank through a pipeline, then carrying out secondary distillation separation in a rectifying tower without flowing through a primary distillation tower; and (3) connecting an empty storage tank of the industrial naphthalene system or adding a high-quality wash oil storage tank with an outlet of the industrial naphthalene to receive high-quality wash oil separated by secondary distillation.
The modification method provided by the invention modifies the industrial naphthalene system into the wash oil purification system, and realizes the first and second distillation processes in one distillation tower, and the pipeline connection relation of the original system is basically not changed, so that the modification workload of the distillation system can be obviously reduced, and the modification cost is reduced.
In order to further reduce the workload of system transformation and facilitate product circulation, preferably, when a mixed oil tank is added, the vacant storage tank of the industrial naphthalene system is an oil washing storage tank, the oil washing storage tank is connected with the outlet of the industrial naphthalene flow, a high-quality oil washing storage tank is added and connected at the downstream of the oil washing storage tank, and high-quality oil washing separated by secondary distillation flows to the high-quality oil washing storage tank after being circulated in the oil washing storage tank.
In order to facilitate feeding and further improve the production continuity of the distillation system, preferably, when a mixed oil tank is added, the vacant storage tank of the industrial naphthalene system is an oil washing storage tank, the oil washing storage tank is connected with the outlet of the industrial naphthalene, and the oil washing storage tank is connected with the washed three-mixed oil tank; before the primary distillation separation, the wash oil storage tank is used for storing the wash oil to be purified.
In order to further improve the utilization effect of the tower bottom components after the secondary distillation separation, preferably, an anthracene oil vat is added, the anthracene oil vat is used for storing the anthracene oil components separated from the coal tar, the wash oil outlet is also connected with the anthracene oil vat, and the tower bottom components separated by the secondary distillation separation are mixed with the anthracene oil, so that the quality of the anthracene oil is improved. The tower bottom component after the secondary distillation separation is heavy oil, the components of the heavy oil are close to the main components of anthracene oil, and the anthracene oil quality can be improved after the heavy oil is mixed with the anthracene oil.
In order to optimize the cooling effect on the industrial naphthalene, the industrial naphthalene cooling system preferably comprises an industrial naphthalene condenser, an industrial naphthalene cooler and an industrial naphthalene vaporization condensation cooler which are sequentially connected in series along the outflow direction of the industrial naphthalene. In order to optimize the cooling effect on the bottom fraction, it is preferred that the bottom fraction cooling system comprises at least two stages of wash oil coolers.
In order to further improve the heat utilization efficiency of the distillation system and improve the distillation efficiency, preferably, the industrial naphthalene system comprises a reflux circulation pipeline which is arranged outside the rectifying tower; the reflux circulation pipeline is provided with a heating device for heating the tower bottom components flowing through, and the heated tower bottom components circularly flow into the tower bottom of the rectifying tower to supply heat for distillation;
a heat exchanger is also arranged on the reflux circulation pipeline; the heat exchanger is provided with a hot fluid channel and a cold fluid channel, the hot fluid channel is used for tower bottom components of the rectifying tower to flow through, the cold fluid channel is used for materials flowing out of the primary rectifying tower to flow through, and the materials flowing out of the primary rectifying tower enter the rectifying tower for distillation and separation after being heated by the heat exchanger.
To further optimize the heat utilization of the distillation system, it is preferred that the heat exchanger is arranged upstream of the heating device in the direction of the return circulation.
Preferably, the heating device is a tube furnace in terms of energy consumption and heating efficiency of the heating device.
Drawings
FIG. 1 is a schematic diagram of the structure of an industrial naphthalene system prior to modification in an embodiment of the present invention;
FIG. 2 is a schematic diagram of a modified industrial naphthalene system (wash oil purification system) according to an embodiment of the present invention;
FIG. 3 is a schematic view showing the connection relationship between the washed three oil mixing tank, the wash oil intermediate tank and the oil mixing tank in FIG. 2;
in the figure, 1-a preliminary distillation tower, 2-a preliminary distillation tower feeding pipeline, 3-a preliminary distillation tower reflux circulation pipeline, 4-a rectification tower, 5-a rectification tower feeding pipeline, 6-a rectification tower reflux circulation pipeline, 7-a washed three oil mixing tank, 8-a vacuum buffer tank, 9-a phenol oil water separator, 10-a phenol oil reflux tank, 11-a tube furnace, 12-an industrial naphthalene reflux tank, 13-a washing oil intermediate tank, 14-a mixed oil tank, 15-a vacuum unit pipeline, 16-a phenol water tank pipeline, 17-an industrial naphthalene finished product tank pipeline, 18-a secondary distillation tower top component pipeline, 19-a secondary distillation tower bottom component storage tank pipeline and 20-a mixed oil tank pipeline;
e1-phenol oil condensation cooler, E2-noncondensable gas condenser, E3-oil washing heat exchanger, E4-industrial naphthalene condenser, E5-first oil washing cooler, E6-industrial naphthalene cooler, E7-second oil washing cooler, E8-industrial naphthalene vaporization condensation cooler;
p1-industrial naphthalene raw material pump, P2-phenol oil reflux pump, P3-two-mixing extraction pump, P4-two-mixing circulating pump, P5-oil washing circulating pump, P6-industrial naphthalene reflux pump and P7-industrial naphthalene conveying pump.
Detailed Description
The following further describes embodiments of the present invention with reference to the drawings.
And washing the three-mixed oil of the tar distillation product by using distillate to obtain the washed three-mixed oil. The distillate wash is mainly dephenolized (phenol, cresol, xylenol, etc.). Dephenolization is a process of extracting phenol from three-mixed oil fraction cut from coal tar distillation by using NaOH solution. The schematic diagram of the original secondary distillation system (before modification) for producing industrial naphthalene by using washed three-component mixed oil through primary distillation and rectification is shown in figure 1.
The industrial naphthalene system before modification comprises a primary distillation system and a rectification system, wherein the primary distillation system comprises a primary distillation tower 1, a primary distillation tower feeding pipeline 2, a primary distillation tower reflux circulation pipeline 3 and a primary distillation tower top component collecting device. The rectification system comprises a rectification tower 4, a rectification tower feeding pipeline 5, a rectification tower reflux circulation pipeline 6, a rectification tower top component collecting device and a rectification tower bottom component collecting device.
(1) Primary distillation system
The washed three-oil mixing tank 7 and the connecting pipeline of the feed inlet of the preliminary distillation tower 1 form a feed pipeline 2 of the preliminary distillation tower, and a cold fluid channel of an industrial naphthalene cooler E6 and a cold fluid channel of a first oil washing cooler E5 are sequentially connected on the feed pipeline of the preliminary distillation tower in series along the feed direction of the preliminary distillation tower. The washed three-oil mixture in the washed three-oil mixture tank 7 is pumped out by an industrial naphthalene raw material pump P1, and enters the preliminary distillation tower 1 after being heated by an industrial naphthalene cooler E6 and a first oil washing cooler E5.
The primary distillation tower reflux circulation pipeline 2 is arranged on the outer side of the bottom of the primary distillation tower 1, along the reflux circulation direction, a cold fluid channel of an industrial naphthalene condenser E4 and a cold fluid channel of a wash oil heat exchanger E3 are sequentially connected in series on the primary distillation tower reflux circulation pipeline, the wash oil heat exchanger E3 is a secondary heat exchanger, and comprises a first heat exchanger and a second heat exchanger arranged on the downstream of the first heat exchanger along the flow direction of the wash oil, the wash oil at the bottom of the rectifying tower flows through the hot fluid channel of the first heat exchanger and the hot fluid channel of the second heat exchanger, and the cold fluid channel of the second heat exchanger is connected in series on the primary distillation tower reflux circulation pipeline 2. The naphthalene washing mixed oil (two mixed oil) in the primary tower 1 is pumped out by the two mixing and circulating pumps P4, heated by the industrial naphthalene condenser E4 and the washing oil heat exchanger E3 (specifically, the second heat exchanger), and then returned to the tower bottom of the primary tower to supply heat to the primary tower.
The top component collecting device of the primary tower comprises a phenol oil condensing cooler E1, a non-condensable gas condenser E2, a vacuum buffer tank 8, a phenol oil-water separator 9 and a phenol oil reflux tank 10. The phenol oil steam at the top of the primary tower is subjected to gas-liquid separation in a phenol oil condensation cooler E1, the gas phase enters a non-condensable gas condenser E2 for further condensation, namely further gas-liquid separation, the gas phase separated by the non-condensable gas condenser E2 further enters a vacuum buffer tank 8 for gas-liquid separation, and the separated gas phase enters a vacuum unit through a vacuum unit pipeline 15 and is washed and then enters a tail gas system. The liquid phase separated by the phenol oil condensation cooler E1, the non-condensable gas condenser E2 and the vacuum buffer tank 8 is merged into the phenol oil-water separator 9. After the materials entering the phenol oil-water separator 9 are subjected to standing separation, the waste water at the bottom enters a waste water tank (phenol water tank) through a phenol water tank pipeline 16, and the phenol oil extracted at the top enters a phenol oil reflux tank 10. A part of the phenol oil in the phenol oil reflux tank 10 is sent to the top of the primary distillation tower 1 through a phenol oil reflux pump P2 to be used as reflux liquid, and the temperature of the top of the tower is controlled; the other part of the phenol oil enters the phenol oil product tank through a full flow pipeline at the top of the phenol oil reflux tank 10.
(2) Rectification system
The pipeline connecting the bottom discharge port of the primary distillation tower and the feed port of the rectification tower forms a feed pipeline 5 of the rectification tower, and a cold fluid channel of a first heat exchanger of an oil washing heat exchanger E3 is connected in series on the feed pipeline 5 of the rectification tower. The two mixed oil at the bottom of the primary distillation tower is pumped out by a two-mixed pump P3, heated by a first heat exchanger and then enters the middle part of the rectifying tower 4.
The rectifying tower reflux circulation pipeline 6 is arranged at the outer side of the bottom of the rectifying tower 4, and a hot fluid channel of the oil washing heat exchanger E3 and the tubular furnace 11 are sequentially connected in series on the rectifying tower reflux circulation pipeline 6 along the reflux circulation direction. The wash oil at the bottom of the rectifying tower passes through a wash oil circulating pump P5 and sequentially passes through a first heat exchanger of a wash oil heat exchanger E3 and a hot fluid channel of a second heat exchanger, and then is heated by the tubular furnace 11 and returns to the rectifying tower 4 to be used as a tower kettle heat source of the rectifying tower.
The top component collecting device of the rectifying tower comprises an industrial naphthalene condenser E4, an industrial naphthalene cooler E6, an industrial naphthalene vaporization and condensation cooler E8, an industrial naphthalene reflux tank 12 and an industrial naphthalene product tank. Naphthalene oil gas extracted from the top of the rectifying tower sequentially flows through hot fluid channels of an industrial naphthalene condenser E4 and an industrial naphthalene cooler E6, is cooled by an industrial naphthalene vaporization condensation cooler E8 and then enters an industrial naphthalene reflux tank 12. The reflux liquid in the industrial naphthalene reflux tank is sent to the top of the rectifying tower for reflux through an industrial naphthalene reflux pump P6, and the other part of the reflux liquid is sent to an industrial naphthalene finished product tank through an industrial naphthalene delivery pump P7 along an industrial naphthalene finished product tank pipeline 17.
The device for collecting the components at the bottom of the rectifying tower comprises a first wash oil cooler E5, a second wash oil cooler E7 and a wash oil intermediate tank 13, wherein the wash oil at the bottom of the rectifying tower enters the wash oil intermediate tank 13 after being cooled by the first wash oil cooler E5 and the second wash oil cooler E7.
The wash oil produced by the original secondary distillation system can not meet the application requirement of the high-performance benzene washing oil at the present stage, and the wash oil product needs to be optimized and upgraded, namely the wash oil needs to be subjected to secondary distillation separation, so that the components playing the main role are enriched, and the high-quality wash oil is obtained. During secondary distillation, naphthalene-rich components (tower top) and mixed naphthalene-removed oil (tower bottom) are obtained in the primary distillation section of the secondary distillation, the mixed naphthalene-removed oil is further rectified and separated, and high-quality wash oil (tower top) and heavy oil (tower bottom) are obtained in the rectification section.
The technical indexes of the high-quality wash oil obtained after the optimization and upgrade of the original wash oil and the wash oil products are shown in the following table 1.
TABLE 1 comparison of technical indices of crude wash oil and high quality wash oil
The method for modifying the original industrial naphthalene system is described below by specific examples.
Example 1
In the method for transforming the industrial naphthalene system into the wash oil purification system, the raw materials are subjected to primary distillation (primary distillation) and secondary distillation (rectification) in the rectification tower 4 firstly and secondly, and the primary distillation tower has no distillation separation process, only supplies materials to flow through and plays a role in buffering; correspondingly, the reflux circulation pipeline of the primary distillation tower is closed, and no extraction is produced at the top of the primary distillation tower. The modified secondary distillation system (wash oil purification system) is shown in fig. 2 and 3.
The intermediate washing oil tank 13 (i.e. raw material storage tank) for storing washing oil is not connected with the tower bottom extraction of the rectifying tower, but is connected with the washed three-oil mixing tank 7 (i.e. feed tank) through a pipeline, for example, the volume of the intermediate washing oil tank 13 and the washed three-oil mixing tank 7 is 300m3The tank body of (1) is usually provided with a tank bottom pipeline and a tank top pipeline, and the tank bottom pipeline of the wash oil intermediate tank 13 is connected with the tank bottom pipeline of the washed three-mixed oil tank 7. The connection between the wash oil intermediate tank 13 and the washed three-oil-mixing tank 7 is for conveying the distillation raw material to the washed three-oil-mixing tank 7, and in other implementation cases, if the wash oil is stored in another container, the container may be connected to the washed three-oil-mixing tank, and the above adjustment may not be performed.
The washing oil to be purified enters the primary distillation tower from a primary distillation tower feeding pipeline 2, no distillation flow passes through the primary distillation tower, the primary distillation tower plays roles of homogenization and buffering, the physical properties of the material such as the flowing state, the temperature and the like are stable and consistent, and then the washing oil enters the rectification tower 4 through a rectification tower feeding pipeline 5 and is subjected to primary distillation in the rectification tower 4.
The primary distillation separates a primary distillation overhead component and a primary distillation bottoms component, which can be collected by the original collection device along the industrial naphthalene finished product tank pipeline 17 (forming a primary distillation overhead component collection).
In the original system, the middle washing oil tank 13 for collecting the primary distillation tower bottom components is connected with the tank bottom pipeline of the washed three-oil-mixing tank 7 through the tank bottom pipeline after being modified, in this embodiment, a mixed oil tank 14 can be added to collect the primary distillation tower bottom components (through a mixed oil tank pipeline 20), and after the primary distillation is finished, the mixed oil tank 14 is connected with the feeding pipeline of the primary distillation tower to feed materials through the original feeding mode of the system and carry out secondary distillation (namely rectification). Particularly, when the device is connected with a feeding pipeline of the preliminary distillation tower, a connecting port can be arranged on the feeding pipeline of the preliminary distillation tower or other connecting modes known in the field can be adopted.Here, in order to further reduce the amount of technical modification, the oil mixing tank 14 may be connected to the washed three-oil mixing tank 7, for example, the tank bottom pipelines of the two tanks may be connected, and when the oil mixing tank 14 feeds the washed three-oil mixing tank 7 for the secondary distillation, the initial distillation raw material (the wash oil to be purified) in the washed three-oil mixing tank 7 is controlled to be completely fed. For example, the actual volume of the oil-mixing tank and the washed three-oil-mixing tank is 300m3Each time feeding is 200m3And calculating that the full load feeding amount of the distillation system is 4t/h, the feeding time is 48h each time, and then controlling the mixed oil groove 14 to feed the washed three-mixed oil groove 7, wherein continuous production can be realized by circulating in sequence.
And (3) separating a secondary distillation tower top component and a secondary distillation tower bottom component by secondary distillation, and connecting an outflow port of the industrial naphthalene reflux tank 12 with a secondary distillation tower top component storage tank (for storing high-quality wash oil) through a secondary distillation tower top component pipeline 18 when the secondary distillation tower top component is collected. In this embodiment, the top component of the secondary distillation tower is high-quality wash oil, the outflow port of the industrial naphthalene reflux tank 12 can be connected to the wash oil intermediate tank 13, the wash oil intermediate tank is completely fed (empty tank), and the high-quality wash oil separated by the secondary distillation flows to the high-quality wash oil large tank after flowing in the wash oil intermediate tank 13. In other embodiments, the high-quality wash oil separated by the secondary distillation can also directly flow to the high-quality wash oil large tank without flowing through the wash oil middle tank 13. When the secondary distillation tower bottom component is collected, the outflow port of the second wash oil cooler E7 is connected with a secondary distillation tower bottom component storage tank through a secondary distillation tower bottom component storage tank pipeline 19. In other embodiments, an anthracene oil vat can be added for storing anthracene oil components separated from coal tar, the wash oil outlet of the wash oil intermediate vat 13 is further connected with the anthracene oil vat, and the tower bottom components separated by secondary distillation are mixed with anthracene oil to improve the quality of the anthracene oil.
The method for reforming the industrial naphthalene system into the wash oil purification system of the embodiment is utilized to carry out secondary distillation production on the wash oil, the naphthalene-rich component and the mixed oil with naphthalene removed are obtained in the primary distillation process, the mixed oil with naphthalene removed is further rectified, and the high-quality wash oil and heavy oil are obtained through separation in the rectification process. The naphthalene-rich component can be utilized in a grading manner according to the change of the naphthalene content, for example, the naphthalene content in the naphthalene-rich component at the initial stage of primary distillation is about 85%, the naphthalene-rich component at the stage can be mixed into the three-component oil, the industrial naphthalene production is carried out again in an industrial naphthalene production system, and the naphthalene content in the naphthalene-rich component at the middle stage of primary distillation is more than 95%, so that the naphthalene-rich component can be collected as an industrial naphthalene product. The application quality of the high-quality wash oil is improved through optimization and upgrading, and the heavy oil can be mixed into anthracene oil for producing the high-quality anthracene oil.
By utilizing the method for transforming the industrial naphthalene system into the washing oil purification system, the technical modification engineering amount is reduced to the greatest extent, the transformation cost is saved, the original industrial naphthalene production system meets the production requirement of high-quality washing oil, and the optimized upgrading of products is realized.
Example 2
The method for modifying an industrial naphthalene system into a wash oil purification system in this embodiment is substantially the same as the modification method in embodiment 1, except that a wash oil intermediate tank is used for receiving a primary distillation tower bottom component, the wash oil intermediate tank is connected with a washed tertiary mixing tank through a pipeline, a valve is arranged on a connecting pipeline between the wash oil intermediate tank and the washed tertiary mixing tank, the valve is opened after the feeding of the washed tertiary mixing tank is completed, the primary distillation tower bottom component in the wash oil intermediate tank enters a distillation system from the washed tertiary mixing tank for secondary distillation, the secondary distillation tower bottom component and the secondary distillation tower top component separated by the secondary distillation are collected by adding a secondary distillation tower bottom component storage tank and a secondary distillation tower top component storage tank respectively.
Claims (9)
1. A method for transforming an industrial naphthalene system into an oil washing purification system is characterized in that,
the industrial naphthalene system comprises a washed three-mixed oil groove, a primary distillation tower, a rectification tower top component collecting device and a rectification tower bottom component collecting device, wherein the rectification tower top component collecting device comprises an industrial naphthalene cooling system with an industrial naphthalene outflow port and an industrial naphthalene storage tank for collecting industrial naphthalene; the rectifying tower bottom component collecting device comprises a tower bottom component cooling system with an oil washing outlet and an oil washing storage tank for collecting oil washing;
the method is characterized in that a mixed oil groove is added on the basis of an industrial naphthalene system, and the mixed oil groove is connected with an oil washing outlet; the washing oil to be purified does not flow through the primary distillation tower in a distillation mode, primary distillation separation is carried out in the rectification tower, and the mixed oil groove is used for receiving mixed oil separated by the primary distillation separation;
connecting the mixed oil groove with the washed three-mixed oil groove through a pipeline, feeding the mixed oil in the mixed oil groove into the washed three-mixed oil groove through the pipeline after primary distillation separation, then carrying out secondary distillation separation in a rectifying tower without flowing through a primary distillation tower; using an empty storage tank of an industrial naphthalene system or adding a high-quality wash oil storage tank to be connected with an outlet of the industrial naphthalene to receive high-quality wash oil separated by secondary distillation;
or on the basis of an industrial naphthalene system, an oil washing storage tank is connected with a washed three-oil-mixing tank through a pipeline, the oil to be purified does not flow through a primary distillation tower, primary distillation separation is carried out in a rectification tower, and the oil washing storage tank is used for receiving the mixed oil separated by the primary distillation; after the primary distillation separation, feeding the mixed oil in the oil washing storage tank to a washed three-mixed oil tank through a pipeline, then carrying out secondary distillation separation in a rectifying tower without flowing through a primary distillation tower; and (3) connecting an empty storage tank of the industrial naphthalene system or adding a high-quality wash oil storage tank with an outlet of the industrial naphthalene to receive high-quality wash oil separated by secondary distillation.
2. The method of claim 1, wherein when the mixing tank is added, the empty storage tank of the industrial naphthalene system is a wash oil storage tank, the wash oil storage tank is connected with the outlet of the industrial naphthalene, a high-quality wash oil storage tank is added and connected with the downstream of the wash oil storage tank, and the high-quality wash oil separated by the secondary distillation flows to the high-quality wash oil storage tank after flowing in the wash oil storage tank.
3. The method of retrofitting an industrial naphthalene system to a wash oil purification system as claimed in claim 1 wherein when adding a mix tank, the industrial naphthalene system empty reservoir is a wash oil reservoir, the wash oil reservoir is connected to said industrial naphthalene flow outlet using a wash oil reservoir, the wash oil reservoir is connected to a washed three mix tank; before the primary distillation separation, the wash oil storage tank is used for storing the wash oil to be purified.
4. The method of claim 1, further comprising adding an anthracene oil vat for storing the anthracene oil component separated from the coal tar, wherein the wash oil outlet is further connected to the anthracene oil vat, and wherein the anthracene oil is blended with the bottoms separated by the secondary distillation to improve the quality of the anthracene oil.
5. The method of retrofitting an industrial naphthalene system to an oil wash purification system according to any of claims 1-4 wherein said industrial naphthalene cooling system comprises an industrial naphthalene condenser, an industrial naphthalene cooler, and an industrial naphthalene evaporative condensation cooler connected in series in the direction of industrial naphthalene outflow.
6. The method of retrofitting an industrial naphthalene system to a wash oil purification system according to any of claims 1-4 wherein said bottoms cooling system comprises at least a two-stage wash oil cooler.
7. The method for revamping an industrial naphthalene system to a wash oil purification system as claimed in any one of claims 1 to 4, wherein the industrial naphthalene system comprises a reflux recycle line, disposed outside the rectification column; the reflux circulation pipeline is provided with a heating device for heating the tower bottom components flowing through, and the heated tower bottom components circularly flow into the tower bottom of the rectifying tower to supply heat for distillation;
a heat exchanger is also arranged on the reflux circulation pipeline; the heat exchanger is provided with a hot fluid channel and a cold fluid channel, the hot fluid channel is used for tower bottom components of the rectifying tower to flow through, the cold fluid channel is used for materials flowing out of the primary rectifying tower to flow through, and the materials flowing out of the primary rectifying tower enter the rectifying tower for distillation and separation after being heated by the heat exchanger.
8. The method of retrofitting an industrial naphthalene system to an oil wash purification system of claim 7 wherein a heat exchanger is placed upstream of the heating device in the direction of the return circulation.
9. The method of retrofitting an industrial naphthalene system to an oil wash purification system of claim 7 wherein said heating device is a tube furnace.
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