CN113384912A - Negative pressure single-furnace single-tower industrial naphthalene rectification system and process - Google Patents
Negative pressure single-furnace single-tower industrial naphthalene rectification system and process Download PDFInfo
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- CN113384912A CN113384912A CN202110579736.9A CN202110579736A CN113384912A CN 113384912 A CN113384912 A CN 113384912A CN 202110579736 A CN202110579736 A CN 202110579736A CN 113384912 A CN113384912 A CN 113384912A
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- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 title claims abstract description 148
- 238000000034 method Methods 0.000 title claims abstract description 26
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims abstract description 138
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 66
- 238000005406 washing Methods 0.000 claims abstract description 63
- 238000000926 separation method Methods 0.000 claims abstract description 31
- 238000009833 condensation Methods 0.000 claims abstract description 22
- 230000005494 condensation Effects 0.000 claims abstract description 22
- 238000004821 distillation Methods 0.000 claims abstract description 21
- 238000010438 heat treatment Methods 0.000 claims description 24
- 239000011229 interlayer Substances 0.000 claims description 14
- 238000009834 vaporization Methods 0.000 claims description 11
- 230000008016 vaporization Effects 0.000 claims description 11
- 239000002994 raw material Substances 0.000 claims description 9
- 238000005192 partition Methods 0.000 claims description 7
- 238000004519 manufacturing process Methods 0.000 claims description 6
- 239000000498 cooling water Substances 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 3
- 238000005086 pumping Methods 0.000 claims description 2
- 239000007789 gas Substances 0.000 abstract description 21
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 238000004939 coking Methods 0.000 abstract description 3
- 230000000694 effects Effects 0.000 abstract description 3
- 239000002918 waste heat Substances 0.000 abstract description 3
- 238000012423 maintenance Methods 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 128
- 101000793686 Homo sapiens Azurocidin Proteins 0.000 description 6
- 239000010724 circulating oil Substances 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000003670 easy-to-clean Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/10—Vacuum distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- 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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- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to the technical field of metallurgical coking industrial naphthalene rectification, in particular to a negative pressure single-furnace single-tower industrial naphthalene rectification system and a process. The industrial naphthalene rectifying tower is divided into an upper section, a middle section and a lower section, wherein the lower section is a distillation section, the middle section is a phenol oil-water separation section, and the upper section is a phenol oil condensation section; the top of the phenol oil condensation section is connected with an outfeed vacuum tail gas pipeline, and a vacuum cooler and a vacuum pump are sequentially arranged on the outfeed vacuum tail gas pipeline. The industrial naphthalene rectifying tower is changed into negative pressure operation, so that the temperature of the whole process flow is reduced, and a good energy-saving effect is achieved; the invention fundamentally solves the problems that the washed mixed components are not easy to adjust and block when being heated in the tubular furnace section; the heat exchange between the washed mixed part and the product washing oil is carried out, so that the waste heat of the product washing oil is reasonably utilized, and the energy consumption is reduced; collect phenol oil condensation, phenol oil water separator in an organic whole, reduce equipment quantity, save investment and take up an area of, be convenient for operation and maintenance.
Description
Technical Field
The invention relates to the technical field of metallurgical coking industrial naphthalene rectification, in particular to a negative pressure single-furnace single-tower industrial naphthalene rectification system and a process.
Background
At present, a large-scale industrial naphthalene production system in the coking industry mostly adopts a tubular furnace continuous rectification method to prepare industrial naphthalene, and mainly comprises three processes of double-furnace double-tower, single-furnace double-tower and single-furnace single-tower, wherein the double-furnace double-tower process refers to a normal-pressure double-furnace double-tower, the single-furnace double-tower is divided into a pressure-reducing single-furnace double-tower and a pressure-increasing single-furnace double-tower, and the single-furnace single-tower refers to a normal-pressure single-furnace single-tower.
The process adopts a tubular furnace and a rectifying tower, phenol oil is extracted from the top of the tower, industrial naphthalene is cut from the side line, and wash oil is adopted from a pressure outlet pipe of a hot oil circulating pump. The washed mixed raw materials are sent to a convection section of a tubular furnace by a pump to be preheated to 250-260 ℃ and then enter an industrial naphthalene rectifying tower. And (3) condensing and cooling the phenol oil vapor with the temperature of 194-198 ℃ escaping from the tower top to 82 ℃, separating oil from water, and feeding the phenol oil into a reflux tank. Thus, a part of the phenol oil is refluxed, and the rest of the phenol oil is sent out. And (3) feeding the washing oil at the bottom of the tower at the temperature of 270-280 ℃ into a tubular furnace by using a hot oil circulating pump, heating to 310-315 ℃, and returning to the evaporation section at the bottom of the tower to circularly supply heat to the rectifying tower. Industrial naphthalene with the temperature of 219 ℃ is extracted from the side line of the rectifying tower, is cooled to 110 ℃ through vaporization and condensation, enters an industrial naphthalene high-temperature tank, and is sent out.
The normal pressure single furnace single tower process has advantages in investment, land occupation and the like compared with the double tower process, but because the washed mixed part enters the industrial naphthalene rectifying tower after being preheated in the convection section of the pipe type furnace, the washed mixed part in the convection section of the pipe type furnace is easy to coke and block in the section, and the development of the process is always troubled by the problem. The method has the advantages that the treatment capacity of the washed mixed components is certain for analysis reasons, the heat of the radiation section of the tubular furnace is also certain in order to ensure the temperature of the circulating wash oil entering the industrial naphthalene rectifying tower, the temperature of the convection section of the tubular furnace is not effectively regulated, all the raw materials of the washed mixed components at the section are high in temperature, the washed mixed components are easy to coke and block in the convection section of the tubular furnace, the washed mixed components are not easy to clean, the overhauling difficulty is high, and the technical production operation is not facilitated. And the normal pressure single furnace single tower process has relatively high energy consumption and no energy saving because of the high temperature of the whole process.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention provides a negative-pressure single-furnace single-tower industrial naphthalene rectification system and a process, which reduce the temperature of the whole process flow and fundamentally solve the problems that the heating of the washed mixed components in the convection section of a tubular furnace is not easy to adjust and is easy to block; meanwhile, energy consumption is reduced through reasonable heat exchange.
In order to achieve the purpose, the invention adopts the following technical scheme:
a negative pressure single furnace single tower industrial naphthalene rectification system comprises an industrial naphthalene rectification tower, wherein the industrial naphthalene rectification tower is divided into an upper section, a middle section and a lower section, the lower section is a distillation section, the middle section is a phenol oil-water separation section, and the upper section is a phenol oil condensation section; the top of the phenol oil condensation section is connected with an outfeed vacuum tail gas pipeline, and a vacuum cooler and a vacuum pump are sequentially arranged on the outfeed vacuum tail gas pipeline.
And the phenol oil condensing section is provided with a phenol oil condenser.
The oil-water separation section of the phenol oil is characterized in that a cylindrical gas cap is arranged in the tower wall, the tower wall and the gas cap form an annular interlayer, and a partition plate is arranged between the tower wall and the gas cap and divides the annular interlayer into a left part and a right part.
And a phenol oil-water outlet, a phenol oil-water inlet, an outflowing phenol oil outlet, a backflow phenol oil outlet and a separated water outlet are arranged on the wall of the phenol oil-water separation section tower.
The phenol oil-water separation section is connected with an outgoing phenol oil pipeline, and a phenol oil cooler is arranged on the outgoing phenol oil pipeline.
The system also comprises a washing oil circulating pump, a tubular heating furnace, an industrial naphthalene vaporization cooler, a washed mixed part heater, a washed mixed part and washing oil heat exchanger and a pipeline mixer; the distillation section is connected with the tubular heating furnace through a pipeline, and a washing oil circulating pump and a pipeline mixer are arranged on the connected pipeline; the industrial naphthalene vaporization cooler is connected with the distillation section through a pipeline; the distillation section is connected with a washed mixed part input pipeline, and a washed mixed part heater, a washed mixed part and a washing oil heat exchanger are arranged on the washed mixed part input pipeline.
A negative pressure single furnace single tower industrial naphthalene rectification process specifically comprises the following steps:
1) tail gas at the top of the phenol oil condensation section is sent into a vacuum pump after passing through a vacuum cooler, the operation of the industrial naphthalene rectifying tower under negative pressure is ensured under the action of the vacuum pump, and noncondensable vacuum tail gas is sent out through a vacuum tail gas delivery pipeline;
2) phenol oil steam from the gas of the phenol oil-water separation section is completely condensed in the phenol oil condenser under the action of cooling water and automatically flows to the phenol oil-water separation section;
3) the phenol oil-water separation section receives phenol oil and water from the phenol oil condensation section, the phenol oil and water are stored in an upper part in an annular interlayer formed by a gas cap and a tower wall, then the phenol oil and water are separated from the annular interlayer through a phenol oil-water outlet and a phenol oil-water inlet, the water density is heavy, the phenol oil and the water are discharged from the bottom and sent out according to the density difference of the oil and the water, the density of the phenol oil is light, the phenol oil overflows to the other side of the partition plate, then the phenol oil flows back from the bottom through a backflow phenol oil outlet and flows to the top of a distillation section of the industrial naphthalene rectification tower, the middle phenol oil flows into a phenol oil cooler through a phenol oil outlet for further cooling, and the cooled phenol oil is sent out;
4) industrial naphthalene is collected from the side line of the distillation section of the industrial naphthalene rectifying tower and is sent out after being cooled by an industrial naphthalene vaporization cooler;
5) pumping out the washing oil at the bottom of the tower by using a washing oil circulating pump, sending out the washing oil in three strands, sending out one strand of product washing oil to enter a washed mixed part and a washing oil heat exchanger to exchange heat with the washed mixed part of the coming raw materials; one part of circulating washing oil is sent to a washed mixed part heater to continuously heat the washed mixed part, the washed mixed part is sent to the middle lower part of an industrial naphthalene rectifying tower after being heated to a specified temperature, and the product washing oil is sent out after heat exchange; one strand of washing oil heated by the washed mixed part is mixed with the third strand of main circulating washing oil of the washing oil circulating pump through a pipeline mixer, then the mixture is sent into a tubular heating furnace for heating, and the heated circulating washing oil returns to the bottom of the industrial naphthalene rectifying tower to provide heat required by the production of the industrial naphthalene rectifying tower.
Compared with the prior art, the invention has the beneficial effects that:
1) the industrial naphthalene rectifying tower is changed into negative pressure operation, so that the temperature of the whole process flow is reduced, and a good energy-saving effect is achieved;
2) the invention changes the washed mixed parts and the circulating oil washing process route, and fundamentally solves the problems that the washed mixed parts are not easy to adjust and block when being heated in the tubular furnace section;
3) according to the invention, the heat exchange between the washed mixed part and the product washing oil is carried out, so that the waste heat of the product washing oil is reasonably utilized, and the energy consumption is reduced;
4) the washed mixed part is heated by part of the washing oil, and the heated washing oil is mixed with the main circulation washing oil by the pipeline mixer and then is sent into the tubular heating furnace, so that the temperature control of the tubular heating furnace is more facilitated;
5) the industrial naphthalene rectifying tower integrates phenol oil condensation and phenol oil-water separation, reduces the number of equipment, saves investment and land occupation, and is convenient to operate and overhaul.
Drawings
FIG. 1 is a schematic diagram of the structure and process of the present invention;
FIG. 2 is a schematic front view of the structure of the oil-water separation section of the phenol oil of the present invention and a schematic process diagram;
FIG. 3 is a schematic top view of the structure of the oil-water separation section of the phenol oil of the present invention.
In the figure: 1-an industrial naphthalene rectifying tower, 2-a distillation section, 3-a phenol oil-water separation section, 4-a phenol oil condensation section, 5-a vacuum cooler, 6-a vacuum pump, 7-a wash oil circulating pump, 8-a tubular heating furnace, 9-an industrial naphthalene vaporization cooler, 10-a washed mixed part heater, 11-a washed mixed part and wash oil heat exchanger, 12-a pipeline mixer, 13-a phenol oil cooler, 31-a phenol oil-water outlet, 32-a phenol oil-water inlet, 33-a partition board, 34-an external phenol oil outlet, 35-a backflow phenol oil outlet, 36-a separation water outlet and 37-a gas cap.
Detailed Description
The following further describes embodiments of the present invention with reference to the accompanying drawings:
as shown in fig. 1 to 3, a negative pressure single-furnace single-tower industrial naphthalene rectification system comprises an industrial naphthalene rectification tower 1, a wash oil circulating pump 7, a tubular heating furnace 8, an industrial naphthalene vaporization cooler 9, a washed mixed part heater 10, a washed mixed part and wash oil heat exchanger 11 and a pipeline mixer 12.
The industrial naphthalene rectifying tower 1 is divided into an upper section, a middle section and a lower section, wherein the lower section is a distillation section 2, the middle section is a phenol oil-water separation section 3, and the upper section is a phenol oil condensation section 4. The top of the phenol oil condensation section is connected with an outfeed vacuum tail gas pipeline, and a vacuum cooler 5 and a vacuum pump 6 are sequentially arranged on the outfeed vacuum tail gas pipeline. The top of the rectifying tower is provided with a vacuum pump 6, tail gas at the top of the phenol oil condensing section passes through a vacuum cooler 5 and then is sent into the vacuum pump, and the industrial naphthalene rectifying tower 1 is changed into negative pressure operation, so that the temperature of the whole process flow is reduced.
The phenol oil condensation section 4 is provided with a phenol oil condenser, and phenol oil steam emitted from the phenol oil-water separation section 3 is completely condensed under the action of cooling water in the phenol oil condenser and automatically flows to the phenol oil-water separation section 3.
As shown in fig. 2 and 3, a cylindrical air cap 37 is arranged in the tower wall of the phenol oil-water separation section 3, so that the tower wall and the air cap 37 form an annular interlayer, and a partition plate 33 is arranged between the tower wall and the air cap 37 to divide the annular interlayer into a left part and a right part.
The wall of the left annular interlayer tower of the phenol oil-water separation section 3 is provided with a phenol oil-water outlet 31, a phenol oil-water inlet 32 and a separated water outlet 36. An outgoing phenol oil outlet 34 and a backflow phenol oil outlet 35 are arranged on the wall of the right annular interlayer tower of the phenol oil-water separation section 3.
As shown in figure 1, the phenol oil-water separation section 3 is connected with a phenol oil delivery pipeline, and a phenol oil cooler 13 is arranged on the phenol oil delivery pipeline.
The bottom of the distillation section 2 is connected with the bottom of the tubular heating furnace 8 through a pipeline, and a washing oil circulating pump 7 and a pipeline mixer 12 are arranged on the connected pipeline. The industrial naphthalene vaporization cooler 9 is connected to the distillation section 2 via a pipe. The distillation section 2 is connected with a washed mixed part input pipeline, and a washed mixed part heater 10 and a washed mixed part and washing oil heat exchanger 11 are arranged on the pipeline. The upper part of the tubular heating furnace 8 is connected with the tower wall of the distillation section 2 through a pipeline.
A negative pressure single furnace single tower industrial naphthalene rectification process specifically comprises the following steps:
1) and the tail gas at the top of the phenol oil condensation section 4 passes through a vacuum cooler 5 and then is sent into a vacuum pump 6, so that the industrial naphthalene rectification tower 1 is ensured to operate under negative pressure under the action of the vacuum pump 6, and the noncondensable vacuum tail gas is sent out.
2) The phenol oil condensation section 4 is provided with a phenol oil condenser, and phenol oil steam from the gas cap 37 of the phenol oil-water separation section 3 is completely condensed under the action of cooling water in the phenol oil condenser and automatically flows to the phenol oil-water separation section 3.
3) The phenol oil-water separation section 3 receives the phenol oil and water from the phenol oil condensation section 4, the phenol oil and water are stored in an annular interlayer upper part of the gas cap 37 and the tower wall, then the phenol oil and water are separated from the interlayer middle part between the gas cap 37 and the tower wall through a phenol oil-water outlet 31, the water density is heavy and the phenol oil is discharged from the bottom and sent out according to the density difference of the oil and the water, the density of the phenol oil is light and the phenol oil overflows to the other side from a partition plate 33, then the phenol oil flows back from the bottom through a backflow phenol oil outlet 35 and flows to the top of the distillation section 2 of the industrial naphthalene rectification tower, the middle phenol oil automatically flows into the phenol oil cooler 13 through a phenol oil outlet 34 to be further cooled, and the cooled phenol oil is sent out.
4) Industrial naphthalene is collected from the side of the distillation section 2 of the industrial naphthalene rectifying tower 1 and is sent out after being cooled by an industrial naphthalene vaporization cooler 9. The washing oil at the bottom of the tower is pumped out by a washing oil circulating pump 7 and is sent out in three strands, one strand of product washing oil is sent out and enters a washed mixed part and washing oil heat exchanger 11 to exchange heat with the washed mixed part of the coming raw materials, because the yield of the product washing oil is low, the calorific value is limited, and the washed mixed part can not be heated to the temperature of entering the tower, one strand of part of circulating washing oil is also needed to be sent to a washed mixed part heater 10 to continue heating the washed mixed part, the washed mixed part is heated to the proper temperature and then sent to the middle lower part of the industrial naphthalene rectifying tower 1, and the product washing oil is sent out after heat exchange. One strand of washing oil heated by the washed mixed part is mixed with the third strand of main circulating washing oil of the washing oil circulating pump 7 through the pipeline mixer 12, then the mixture is sent into the tubular heating furnace 8 for heating, and the heated circulating washing oil returns to the bottom of the industrial naphthalene rectifying tower 1 to provide heat required by the production of the industrial naphthalene rectifying tower 1.
Examples are: taking the process of treating 30 ten thousand/a of anhydrous tar by mixing parts per year as an example, according to the conventional composition, the product washing oil amount is 2.25t/h, the treatment amount of the washed mixed part of the raw material is 6.56t/h, the temperature of washing oil at the bottom of an industrial naphthalene rectification tower is 240 ℃, the temperature of the finished product washing oil after being cooled is 80 ℃, the incoming temperature of the washed mixed part of the raw material is 60 ℃, the washed mixed part of the raw material after being heated by the product washing oil reaches about 114 ℃, if the temperature of the washed mixed part entering the tower is 185 ℃, all the washed mixed part of the raw material needs to be heated to 185 ℃ by one part of circulating washing oil, the washing oil is supposed to be from 240 ℃ to 220 ℃, the part of the circulating washing oil is about 24t/h, because the tower needs more heat, therefore, the third main circulation wash oil and the part of circulation wash oil for heating the washed mixed part are mixed in the pipeline mixer and then are sent to the tubular heating furnace for heating, and the heat required by the production of the industrial naphthalene rectifying tower is provided.
The industrial naphthalene rectifying tower is changed into negative pressure operation, so that the temperature of the whole process flow is reduced, and a good energy-saving effect is achieved; the invention changes the washed mixed parts and the circulating oil washing process route, and fundamentally solves the problems that the washed mixed parts are not easy to adjust and block when being heated in the tubular furnace section; according to the invention, the heat exchange between the washed mixed part and the product washing oil is carried out, so that the waste heat of the product washing oil is reasonably utilized, and the energy consumption is reduced; the washed mixed part is heated by part of the washing oil, and the heated washing oil is mixed with the main circulation washing oil by the pipeline mixer and then is sent into the tubular heating furnace, so that the temperature control of the tubular heating furnace is more facilitated; the industrial naphthalene rectifying tower integrates phenol oil condensation and phenol oil-water separation, reduces the number of equipment, saves investment and land occupation, and is convenient to operate and overhaul.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and the technical solutions and the inventive concepts thereof according to the present invention should be equivalent or changed within the scope of the present invention.
Claims (7)
1. The negative-pressure single-furnace single-tower industrial naphthalene rectification system is characterized by comprising an industrial naphthalene rectification tower, wherein the industrial naphthalene rectification tower is divided into an upper section, a middle section and a lower section, the lower section is a distillation section, the middle section is a phenol oil-water separation section, and the upper section is a phenol oil condensation section; the top of the phenol oil condensation section is connected with an outfeed vacuum tail gas pipeline, and a vacuum cooler and a vacuum pump are sequentially arranged on the outfeed vacuum tail gas pipeline.
2. The negative pressure single furnace single tower industrial naphthalene rectification system of claim 1 wherein said phenol oil condensation section is provided with a phenol oil condenser.
3. The negative pressure single-furnace single-tower industrial naphthalene rectification system as claimed in claim 1, wherein a cylindrical gas cap is arranged in the tower wall of the phenol oil-water separation section, the tower wall and the gas cap form an annular interlayer, and a partition plate is arranged between the tower wall and the gas cap to divide the annular interlayer into a left part and a right part.
4. The negative pressure single-furnace single-tower industrial naphthalene rectification system of claim 1, wherein a phenol oil water outlet, a phenol oil water inlet, an outgoing phenol oil outlet, a return phenol oil outlet and a separated water outlet are formed in the wall of the phenol oil water separation section.
5. The negative pressure single-furnace single-tower industrial naphthalene rectification system of claim 1, wherein the phenol oil water separation section is connected with a phenol oil delivery pipeline, and a phenol oil cooler is arranged on the phenol oil delivery pipeline.
6. The negative pressure single-furnace single-tower industrial naphthalene rectification system of claim 1, further comprising a wash oil circulating pump, a tubular heating furnace, an industrial naphthalene vaporization cooler, a washed mixed fraction heater, a washed mixed fraction and wash oil heat exchanger and a pipeline mixer; the distillation section is connected with the tubular heating furnace through a pipeline, and a washing oil circulating pump and a pipeline mixer are arranged on the connected pipeline; the industrial naphthalene vaporization cooler is connected with the distillation section through a pipeline; the distillation section is connected with a washed mixed part input pipeline, and a washed mixed part heater, a washed mixed part and a washing oil heat exchanger are arranged on the washed mixed part input pipeline.
7. A negative pressure single-furnace single-tower industrial naphthalene rectification process based on the negative pressure single-furnace single-tower industrial naphthalene rectification system of any one of claims 1 to 6 is characterized by comprising the following steps:
1) tail gas at the top of the phenol oil condensation section is sent into a vacuum pump after passing through a vacuum cooler, the operation of the industrial naphthalene rectifying tower under negative pressure is ensured under the action of the vacuum pump, and noncondensable vacuum tail gas is sent out through a vacuum tail gas delivery pipeline;
2) phenol oil steam from the gas of the phenol oil-water separation section is completely condensed in the phenol oil condenser under the action of cooling water and automatically flows to the phenol oil-water separation section;
3) the phenol oil-water separation section receives phenol oil and water from the phenol oil condensation section, the phenol oil and water are stored in an upper part in an annular interlayer formed by a gas cap and a tower wall, then the phenol oil and water are separated from the annular interlayer through a phenol oil-water outlet and a phenol oil-water inlet, the water density is heavy, the phenol oil and the water are discharged from the bottom and sent out according to the density difference of the oil and the water, the density of the phenol oil is light, the phenol oil overflows to the other side of the partition plate, then the phenol oil flows back from the bottom through a backflow phenol oil outlet and flows to the top of a distillation section of the industrial naphthalene rectification tower, the middle phenol oil flows into a phenol oil cooler through a phenol oil outlet for further cooling, and the cooled phenol oil is sent out;
4) industrial naphthalene is collected from the side line of the distillation section of the industrial naphthalene rectifying tower and is sent out after being cooled by an industrial naphthalene vaporization cooler;
5) pumping out the washing oil at the bottom of the tower by using a washing oil circulating pump, sending out the washing oil in three strands, sending out one strand of product washing oil to enter a washed mixed part and a washing oil heat exchanger to exchange heat with the washed mixed part of the coming raw materials; one part of circulating washing oil is sent to a washed mixed part heater to continuously heat the washed mixed part, the washed mixed part is sent to the middle lower part of an industrial naphthalene rectifying tower after being heated to a specified temperature, and the product washing oil is sent out after heat exchange; one strand of washing oil heated by the washed mixed part is mixed with the third strand of main circulating washing oil of the washing oil circulating pump through a pipeline mixer, then the mixture is sent into a tubular heating furnace for heating, and the heated circulating washing oil returns to the bottom of the industrial naphthalene rectifying tower to provide heat required by the production of the industrial naphthalene rectifying tower.
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