CN210176751U - Industrial naphthalene production system - Google Patents
Industrial naphthalene production system Download PDFInfo
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- CN210176751U CN210176751U CN201920793624.1U CN201920793624U CN210176751U CN 210176751 U CN210176751 U CN 210176751U CN 201920793624 U CN201920793624 U CN 201920793624U CN 210176751 U CN210176751 U CN 210176751U
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- naphthalene
- heat exchange
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- inlet pipe
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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 336
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 32
- 238000010992 reflux Methods 0.000 claims abstract description 35
- 238000010438 heat treatment Methods 0.000 claims abstract description 30
- 238000003860 storage Methods 0.000 claims abstract description 25
- 239000007788 liquid Substances 0.000 claims abstract description 15
- 239000002826 coolant Substances 0.000 claims abstract description 9
- 238000004821 distillation Methods 0.000 claims description 49
- 238000011084 recovery Methods 0.000 claims description 31
- 239000000463 material Substances 0.000 claims description 16
- 239000002994 raw material Substances 0.000 claims description 14
- 238000007599 discharging Methods 0.000 claims description 8
- 239000000945 filler Substances 0.000 claims description 6
- 239000000126 substance Substances 0.000 claims description 4
- 239000003034 coal gas Substances 0.000 claims description 3
- 238000012856 packing Methods 0.000 claims description 3
- 238000005406 washing Methods 0.000 claims description 3
- 239000011280 coal tar Substances 0.000 abstract description 4
- 238000002425 crystallisation Methods 0.000 abstract description 4
- 230000008025 crystallization Effects 0.000 abstract description 4
- 238000012545 processing Methods 0.000 abstract description 4
- 238000000034 method Methods 0.000 description 4
- 239000013078 crystal Substances 0.000 description 3
- 230000005484 gravity Effects 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- 238000012423 maintenance Methods 0.000 description 2
- 238000000859 sublimation Methods 0.000 description 2
- 230000008022 sublimation Effects 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000012432 intermediate storage Methods 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 230000029058 respiratory gaseous exchange Effects 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model discloses an industry naphthalene production system belongs to coal tar deep-processing technical field. The industrial naphthalene storage tank is connected with the condensing device, the condensing device is connected with the top of the distilling device, the refluxing device is connected with the condensing device and the distilling device, and the industrial naphthalene storage tank is connected with the refluxing device. The condensing device comprises at least two naphthalene condensers connected in parallel, a naphthalene vapor inlet pipe, a liquid naphthalene outlet pipe, a heat exchange medium inlet pipe and a heat exchange medium outlet pipe are arranged on the naphthalene condensers, and the heat exchange medium inlet pipe comprises a cooling medium inlet pipe and a heating medium inlet pipe which are connected in parallel. Through setting up multistage condensing equipment, when production, regularly switch production to condensing equipment to let in heating medium in to the condenser, the crystallization that makes is retrieved in the naphthalene liquefaction on condenser surface, and then the smooth operation of guarantee production, has retrieved partial naphthalene simultaneously, realizes the resource recycle.
Description
Technical Field
The utility model belongs to the technical field of the coal tar deep-processing, concretely relates to industry naphthalene production system.
Background
The method for producing industrial naphthalene by using coal tar is a main source of industrial naphthalene, and the main processing flow is that coal tar is heated at high temperature to produce three-mixed oil, and then industrial naphthalene is separated from the three-mixed oil.
However, in the conventional processing technology, the naphthalene vapor at the top of the distillation tower is condensed by the condenser and liquefied into liquid naphthalene, but part of the liquid naphthalene is sublimated and crystallized and attached to the pipe wall of the condenser, so that the condensing efficiency is reduced, and the pipeline of the condenser is blocked after a long time, thereby affecting the normal production. The production stop maintenance not only needs to consume a large amount of manpower and material resources, but also causes the waste of the crystallized naphthalene in the maintenance process.
Disclosure of Invention
In view of this, the utility model provides an industrial naphthalene production system of the industrial naphthalene of guarantee production normal operating, recovery crystallization simultaneously.
The utility model provides a technical scheme that its technical problem adopted is:
an industrial naphthalene production system comprises a distillation device, a feeding preheating device, a condensing device, a reflux device and an industrial naphthalene storage tank, wherein the feeding preheating device is connected with the middle part of the distillation device and is used for preheating raw materials; the condensing device is connected with the top of the distillation device and is used for condensing the produced substances at the top of the distillation device; the reflux device is connected with the condensing device and the distillation device and is used for providing reflux for the distillation device; the industrial naphthalene storage tank is connected with the reflux device and is used for containing finished industrial naphthalene;
the condensing device comprises at least two naphthalene condensers connected in parallel, a naphthalene steam inlet pipe, a liquid naphthalene outlet pipe, a heat exchange medium inlet pipe and a heat exchange medium outlet pipe are arranged on the naphthalene condensers, an inlet valve is arranged on the naphthalene steam inlet pipe to switch the naphthalene condensers, the heat exchange medium inlet pipe comprises a cooling medium inlet pipe and a heating medium inlet pipe which are connected in parallel to switch cold and hot heat exchange media, the liquid naphthalene outlet pipe is communicated with the naphthalene steam inlet pipe, and the heat exchange medium outlet pipe is communicated with the heat exchange medium inlet pipe.
Preferably, the distillation device comprises a distillation tower, a circulating pump and a tubular heating furnace, wherein the feeding end of the circulating pump is connected to the bottom of the distillation tower, the feeding port of the tubular heating furnace is connected with the discharging end of the circulating pump, and the discharging port of the tubular heating furnace is connected with the distillation tower; the tubular heating furnace adopts coal gas as a heating medium, and the circulating pump provides power to circularly heat the raw materials in the distillation tower through the tubular heating furnace.
Preferably, the feeding preheating device comprises a first preheating heat exchanger and a second preheating heat exchanger which are sequentially connected, the hot material side of the first preheating heat exchanger is communicated with the top of the distillation tower, and the cold material side of the first preheating heat exchanger is communicated with the raw material feeding pipe; and the cold material side of the second preheating heat exchanger is communicated with the raw material feeding pipe, and the hot material side adopts high-temperature washing oil or steam.
Preferably, the reflux unit comprises a condensate intermediate tank and a reflux pump, wherein the feed end of the condensate intermediate tank is connected with the liquid naphthalene outlet pipe, the feed end of the reflux pump is connected with the bottom of the condensate intermediate tank, and the discharge end of the reflux pump is connected with the upper end of the distillation unit.
Preferably, the feed end of the industrial naphthalene storage tank is connected to the discharge port of the reflux pump so as to receive the industrial naphthalene product conveyed by the reflux pump.
Preferably, sublimation naphthalene recovery devices are arranged at the tops of the condensate intermediate tank and the industrial naphthalene storage tank and are used for capturing and recovering sublimation naphthalene dissipated from the tops of the condensate intermediate tank and the industrial naphthalene storage tank.
Preferably, the sublimated naphthalene recovery device comprises a naphthalene recovery tank, a heat exchange assembly and a naphthalene trapping filler, wherein the heat exchange assembly is connected to the naphthalene recovery tank, and the naphthalene trapping filler is filled in the naphthalene recovery tank;
the lower end of the naphthalene recovery tank is provided with a sublimated naphthalene inlet, and the upper end of the naphthalene recovery tank is provided with a tail gas discharge port; the heat exchange assembly comprises a heat exchange coil, a heat exchange medium feeding pipe and a heat exchange medium discharging pipe, the heat exchange coil is arranged in the naphthalene recovery tank, and the heat exchange medium feeding pipe and the heat exchange medium discharging pipe are connected to the heat exchange coil; the heat exchange medium feed pipe comprises a cooling medium feed pipe and a heating medium feed pipe which are connected in parallel.
Preferably, the bottom of the naphthalene recovery tank is inclined toward the sublimated naphthalene inlet.
Preferably, the naphthalene trapping packing is one of pall rings, wire mesh, raschig rings, intalox rings or ladder rings.
According to the above technical scheme, the utility model provides an industry naphthalene production system, its beneficial effect is: through setting up multistage condensing equipment, when production, regularly switch production to condensing equipment to let in heating medium in the condenser, the crystallization that makes is in the naphthalene liquefaction on condenser surface, and the lime set intermediate tank is retrieved in the backward flow under the action of gravity, and then the smooth operation of guarantee production, has retrieved the partial naphthalene of crystallization on condenser surface simultaneously, realizes the resource and recycles.
Drawings
FIG. 1 is a schematic view of piping connections of an industrial naphthalene production system.
Fig. 2 is a schematic diagram of the piping connections of the condensing unit.
FIG. 3 is a schematic view showing the structure of a sublimated naphthalene recovering apparatus.
In the figure: the industrial naphthalene production system 10, the distillation apparatus 100, the distillation tower 110, the circulation pump 120, the tube furnace 130, the feed preheater 200, the first preheater heat exchanger 210, the second preheater heat exchanger 220, the condenser 300, the naphthalene condenser 310, the naphthalene vapor inlet pipe 311, the inlet valve 3111, the liquid naphthalene outlet pipe 312, the heat exchange medium inlet pipe 313, the cooling medium inlet pipe 3131, the heating medium inlet pipe 3132, the heat exchange medium outlet pipe 314, the reflux apparatus 400, the condensate intermediate tank 410, the reflux pump 420, the industrial naphthalene storage tank 500, the sublimated naphthalene recovery apparatus 600, the naphthalene recovery tank 610, the sublimated naphthalene inlet port 611, the tail gas outlet port 612, the heat exchange assembly 620, the heat exchange coil 621, the heat exchange medium inlet pipe 622, the heat exchange medium outlet pipe 623, the cooling medium inlet pipe 6221, the heating medium inlet pipe 6222, and the naphthalene trapping.
Detailed Description
The following combines the utility model discloses an attached drawing is right the technical scheme and the technological effect of the embodiment of the utility model are further elaborated.
Referring to fig. 1 and 2, in one embodiment, an industrial naphthalene production system 10 includes a distillation apparatus 100, a feed preheating apparatus 200, a condensing apparatus 300, a reflux apparatus 400, and an industrial naphthalene storage tank 500. The feeding preheating device 200 is connected to the middle part of the distillation device 100 and used for preheating the raw materials. The condensing device 300 is connected to the top of the distillation device 100 and is used for condensing the produced substance at the top of the distillation device 100. The reflux unit 400 is connected to the condensing unit 300 and the distillation unit 100, and is used for providing reflux for the distillation unit 100. The industrial naphthalene storage tank 500 is connected with the reflux device 400 and is used for containing finished industrial naphthalene.
In production, the raw material three-mixed oil for producing industrial naphthalene is preheated by the feeding preheating device 200, after reaching the feeding temperature, the raw material three-mixed oil is fed from the middle part of the distillation tower 100, the material is heated and circulated in the tower kettle of the distillation tower 100, so that the material temperature reaches the technical value of industrial naphthalene extraction, the produced material at the top of the distillation tower 100 is cooled once by the feeding preheating device 200, and after heat recovery, the produced material at the top of the distillation tower enters the condensing device 300 for complete condensation and cooling, so that the produced material at the top of the distillation tower is liquefied and automatically flows into the middle storage tank under the action of gravity. The reflux unit 400 refluxes the liquid naphthalene in the intermediate storage tank to the top of the distillation column 100 to maintain the heat and mass transfer balance of the distillation column 100, and transfers the liquid naphthalene to the industrial naphthalene storage tank 500 as the finished industrial naphthalene.
Specifically, the condensing device 300 comprises at least two naphthalene condensers 310 connected in parallel, a naphthalene steam inlet pipe 311, a liquid naphthalene outlet pipe 312, a heat exchange medium inlet pipe 313 and a heat exchange medium outlet pipe 314 are arranged on the naphthalene condensers 310, an inlet valve 3111 is arranged on the naphthalene steam inlet pipe 311 to switch the naphthalene condensers, the heat exchange medium inlet pipe 313 comprises a cooling medium inlet pipe 3131 and a heating medium inlet pipe 3132 connected in parallel to switch cold and hot heat exchange media, the liquid naphthalene outlet pipe 312 is communicated with the naphthalene steam inlet pipe 311, and the heat exchange medium outlet pipe 314 is communicated with the heat exchange medium inlet pipe 313.
In the production operation process, after the condensing efficiency of the naphthalene condenser 310 is reduced and the pipeline is blocked, the naphthalene condenser 310 is switched to produce, so that the smooth production is ensured. After the switching is finished, the cold medium of the standby naphthalene condenser 310 is closed, the hot medium of the standby naphthalene condenser 310 is opened, the naphthalene condenser 310 is heated, crystals and naphthalene on the inner wall of the naphthalene condenser 310 are liquefied, and the crystals automatically flow into a condensate storage tank under the action of gravity.
In a specific embodiment, the upper portion of the standby naphthalene condenser 310 is communicated with the naphthalene vapor inlet pipe 311 of the in-use naphthalene condenser 310, so that the sublimated naphthalene generated in the process of heating and liquefying the standby naphthalene condenser 310 is further condensed and recovered by the in-use naphthalene condenser 310, and the recovery efficiency is improved.
In another embodiment, a pressure sensor is disposed on the naphthalene steam inlet pipe 311 to detect the inlet pressure of the naphthalene condenser 310 and assist in determining the blockage of the naphthalene condenser 310 and the heat exchange efficiency.
In another embodiment, the pressure sensor is electrically connected to the inlet valve 3111 for comparing the pressure detected by the pressure sensor with a preset pressure, so as to control the opening and closing of the inlet valve for automatically switching the naphthalene condenser 310.
In another embodiment, the distillation apparatus 100 comprises a distillation column 110, a circulation pump 120 and a tube heating furnace 130, wherein a feed end of the circulation pump 120 is connected to the bottom of the distillation column 110, a feed port of the tube heating furnace 130 is connected to a discharge end of the circulation pump 120, and a discharge port of the tube heating furnace 130 is connected to the distillation column 110; the tubular heating furnace 130 adopts coal gas as a heating medium, and the circulating pump 120 provides power to circularly heat the raw material in the distillation tower 110 through the tubular heating furnace 130.
Further, the feed preheating device 200 comprises a first preheating heat exchanger 210 and a second preheating heat exchanger 220 which are connected in sequence, wherein the hot material side of the first preheating heat exchanger 210 is communicated with the top of the distillation tower 100, and the cold material side is communicated with the raw material feeding pipe; the cold material side of the second preheating heat exchanger 220 is communicated with the raw material feeding pipe, and the hot material side adopts high-temperature washing oil or steam.
Further, the reflux device 400 comprises a condensate intermediate tank 410 and a reflux pump 420, wherein the feed end of the condensate intermediate tank 410 is connected with the liquid naphthalene outlet pipe 312, the feed end of the reflux pump 420 is connected with the bottom of the condensate intermediate tank 410, and the discharge end is connected with the upper end of the distillation device 100.
Further, the feeding end of the industrial naphthalene storage tank 500 is connected to the discharge port of the reflux pump 420 to receive the industrial naphthalene product conveyed by the reflux pump 420.
In the industrial naphthalene storage process, due to the breathing action of the tank top of the storage tank/storage tank, the sublimated naphthalene crystals are directly discharged out through the breather valve, a large amount of white atomized substances are dispersed in the air, so that the deterioration of the field operation environment is caused, and the atmospheric environment is polluted. And if the direct collection and disposal is through the VOC main, this in turn results in the waste of this portion of sublimated naphthalene. To solve this problem, referring to fig. 3, in another embodiment, a sublimated naphthalene recovery device 600 is disposed on the top of the condensate intermediate tank 420 and the industrial naphthalene storage tank 500 for capturing and recovering sublimated naphthalene escaping from the top of the condensate intermediate tank 420 and the industrial naphthalene storage tank 500.
Specifically, the sublimated naphthalene recovery apparatus 600 includes a naphthalene recovery tank 610, a heat exchange element 620, and a naphthalene trapping filler 630, wherein the heat exchange element 620 is connected to the naphthalene recovery tank 610, and the naphthalene trapping filler 630 is filled in the naphthalene recovery tank 610. The lower end of the naphthalene recovery tank 610 is provided with a sublimated naphthalene inlet 611, and the upper end is provided with a tail gas discharge port 612. The heat exchange assembly 620 comprises a heat exchange coil 621, a heat exchange medium feeding pipe 622 and a heat exchange medium discharging pipe 623, the heat exchange coil 621 is installed in the naphthalene recovery tank 610, and the heat exchange medium feeding pipe 622 and the heat exchange medium discharging pipe 623 are connected to the heat exchange coil 621. The heat transfer medium feeding pipe 622 includes a cooling medium feeding pipe 6221 and a heating medium feeding pipe 6222 connected in parallel to trap the sublimated naphthalene and periodically heat, liquefy and recover the sublimated naphthalene.
Further, the bottom of the naphthalene recovery tank 610 is inclined toward the sublimated naphthalene inlet 611, so that the liquefied naphthalene automatically flows into the condensate intermediate tank 420 and the industrial naphthalene storage tank 500.
Further, the naphthalene trapping packing 630 is one of a pall ring, a wire mesh, a raschig ring, an intalox ring, or a ladder ring.
While the invention has been described with reference to a preferred embodiment, it will be understood by those skilled in the art that various changes in form and details may be made therein without departing from the spirit and scope of the invention.
Claims (9)
1. The industrial naphthalene production system is characterized by comprising a distillation device, a feeding preheating device, a condensing device, a reflux device and an industrial naphthalene storage tank, wherein the feeding preheating device is connected with the middle part of the distillation device and is used for preheating raw materials; the condensing device is connected with the top of the distillation device and is used for condensing the produced substances at the top of the distillation device; the reflux device is connected with the condensing device and the distillation device and is used for providing reflux for the distillation device; the industrial naphthalene storage tank is connected with the reflux device and is used for containing finished industrial naphthalene;
the condensing device comprises at least two naphthalene condensers connected in parallel, a naphthalene steam inlet pipe, a liquid naphthalene outlet pipe, a heat exchange medium inlet pipe and a heat exchange medium outlet pipe are arranged on the naphthalene condensers, an inlet valve is arranged on the naphthalene steam inlet pipe to switch the naphthalene condensers, the heat exchange medium inlet pipe comprises a cooling medium inlet pipe and a heating medium inlet pipe which are connected in parallel to switch cold and hot heat exchange media, the liquid naphthalene outlet pipe is communicated with the naphthalene steam inlet pipe, and the heat exchange medium outlet pipe is communicated with the heat exchange medium inlet pipe.
2. The industrial naphthalene production system of claim 1, wherein the distillation apparatus comprises a distillation column, a circulation pump and a tubular heating furnace, a feed end of the circulation pump is connected to the bottom of the distillation column, a feed inlet of the tubular heating furnace is connected to a discharge end of the circulation pump, and a discharge outlet of the tubular heating furnace is connected to the distillation column;
the tubular heating furnace adopts coal gas as a heating medium, and the circulating pump provides power to circularly heat the raw materials in the distillation tower through the tubular heating furnace.
3. The industrial naphthalene production system of claim 2, wherein the feed preheating device comprises a first preheating heat exchanger and a second preheating heat exchanger which are connected in sequence, the hot feed side of the first preheating heat exchanger is communicated with the top of the distillation tower, and the cold feed side of the first preheating heat exchanger is communicated with the raw material feed pipe; and the cold material side of the second preheating heat exchanger is communicated with the raw material feeding pipe, and the hot material side adopts high-temperature washing oil or steam.
4. The industrial naphthalene production system of claim 1, wherein the reflux device comprises a condensate tundish and a reflux pump, a feed end of the condensate tundish is connected with the liquid naphthalene outlet pipe, a feed end of the reflux pump is connected with the bottom of the condensate tundish, and a discharge end of the reflux pump is connected with the upper end of the distillation device.
5. The industrial naphthalene production system of claim 4, wherein a feed end of the industrial naphthalene storage tank is connected to a discharge port of the reflux pump to receive the product industrial naphthalene delivered by the reflux pump.
6. The industrial naphthalene production system of claim 4 or 5, wherein the condensate intermediate tank and the top of the industrial naphthalene storage tank are provided with a sublimated naphthalene recovery device for capturing and recovering sublimated naphthalene escaping from the top of the condensate intermediate tank and the top of the industrial naphthalene storage tank.
7. The industrial naphthalene production system of claim 6, wherein the sublimated naphthalene recovery device comprises a naphthalene recovery tank, a heat exchange assembly and a naphthalene trapping filler, wherein the heat exchange assembly is connected to the naphthalene recovery tank, and the naphthalene trapping filler is filled in the naphthalene recovery tank;
the lower end of the naphthalene recovery tank is provided with a sublimated naphthalene inlet, and the upper end of the naphthalene recovery tank is provided with a tail gas discharge port; the heat exchange assembly comprises a heat exchange coil, a heat exchange medium feeding pipe and a heat exchange medium discharging pipe, the heat exchange coil is arranged in the naphthalene recovery tank, and the heat exchange medium feeding pipe and the heat exchange medium discharging pipe are connected to the heat exchange coil; the heat exchange medium feed pipe comprises a cooling medium feed pipe and a heating medium feed pipe which are connected in parallel.
8. The industrial naphthalene production system of claim 7 wherein the bottom of the naphthalene recovery tank is sloped toward the sublimated naphthalene inlet.
9. The industrial naphthalene production system of claim 7, wherein the naphthalene capture packing is one of a pall ring, a wire mesh, a raschig ring, an intalox ring, or a ladder ring.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920793624.1U CN210176751U (en) | 2019-05-29 | 2019-05-29 | Industrial naphthalene production system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920793624.1U CN210176751U (en) | 2019-05-29 | 2019-05-29 | Industrial naphthalene production system |
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| Publication Number | Publication Date |
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| CN210176751U true CN210176751U (en) | 2020-03-24 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201920793624.1U Expired - Fee Related CN210176751U (en) | 2019-05-29 | 2019-05-29 | Industrial naphthalene production system |
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| Country | Link |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111334325A (en) * | 2020-03-26 | 2020-06-26 | 中国平煤神马能源化工集团有限责任公司 | Method for transforming industrial naphthalene system into wash oil purification system |
-
2019
- 2019-05-29 CN CN201920793624.1U patent/CN210176751U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111334325A (en) * | 2020-03-26 | 2020-06-26 | 中国平煤神马能源化工集团有限责任公司 | Method for transforming industrial naphthalene system into wash oil purification system |
| CN111334325B (en) * | 2020-03-26 | 2021-12-28 | 中国平煤神马能源化工集团有限责任公司 | Method for transforming industrial naphthalene system into wash oil purification system |
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Granted publication date: 20200324 |