CN220012508U - Industrial naphthalene production device - Google Patents
Industrial naphthalene production device Download PDFInfo
- Publication number
- CN220012508U CN220012508U CN202320921059.9U CN202320921059U CN220012508U CN 220012508 U CN220012508 U CN 220012508U CN 202320921059 U CN202320921059 U CN 202320921059U CN 220012508 U CN220012508 U CN 220012508U
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- CN
- China
- Prior art keywords
- rectifying tower
- heat
- industrial naphthalene
- heat exchanger
- reflux
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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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 112
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 25
- 238000010992 reflux Methods 0.000 claims abstract description 37
- 238000001704 evaporation Methods 0.000 claims abstract description 16
- 230000008020 evaporation Effects 0.000 claims abstract description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 15
- 239000002994 raw material Substances 0.000 claims description 9
- 239000012071 phase Substances 0.000 abstract description 12
- 239000007789 gas Substances 0.000 abstract description 7
- 238000009834 vaporization Methods 0.000 abstract description 6
- 230000008016 vaporization Effects 0.000 abstract description 6
- 238000000034 method Methods 0.000 abstract description 4
- 230000008569 process Effects 0.000 abstract description 4
- 239000007791 liquid phase Substances 0.000 abstract description 3
- 239000002918 waste heat Substances 0.000 abstract description 3
- 239000000047 product Substances 0.000 description 13
- 239000006200 vaporizer Substances 0.000 description 4
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- NESLWCLHZZISNB-UHFFFAOYSA-M sodium phenolate Chemical compound [Na+].[O-]C1=CC=CC=C1 NESLWCLHZZISNB-UHFFFAOYSA-M 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- 238000001816 cooling Methods 0.000 description 2
- 230000003712 anti-aging effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000002270 dispersing agent Substances 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000003631 expected effect Effects 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000002304 perfume Substances 0.000 description 1
- 239000004014 plasticizer Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000005060 rubber Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
- 239000012209 synthetic fiber Substances 0.000 description 1
- 229920002994 synthetic fiber Polymers 0.000 description 1
- 229920003002 synthetic resin Polymers 0.000 description 1
- 239000000057 synthetic resin Substances 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- 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
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses an industrial naphthalene production device, which comprises: a rectifying tower; the heat source inlet of the steam generator is connected with the top of the rectifying tower, an evaporation cavity is arranged in the steam generator, and water in the evaporation cavity is heated by a heat source to form steam; the heat medium inlet of the heat exchanger is connected with the heat source outlet of the steam generator; and the heat medium outlet of the heat exchanger is connected to the reflux groove, so that the heat medium subjected to heat exchange by the heat exchanger enters the reflux groove, and the reflux groove is respectively connected with the rectifying tower and the finished product tank. The utility model re-optimizes the process flow, the industrial naphthalene passing through the steam generator is still in gas phase, and then the temperature of the industrial naphthalene is reduced to about 120 ℃ to become liquid phase after passing through the heat exchanger, so that the quality of industrial naphthalene products is improved, the vaporization cooler can be stopped at the moment, the consumption of circulating water in the vaporization cooler is reduced, and the waste heat of the products is reasonably utilized in the whole production process.
Description
Technical Field
The utility model relates to the technical field of industrial naphthalene production, in particular to an industrial naphthalene production device.
Background
Industrial naphthalene is a basic chemical raw material, is mainly used for producing water reducing agent and dispersing agent, and is a raw material for producing synthetic resin, plasticizer, rubber anti-aging agent, surfactant, synthetic fiber, dye, medicine, perfume and the like. Naphthalene accounts for about 8-12% of the high temperature coal tar. And (3) cutting out a naphthalene oil fraction with the temperature range of 210-230 ℃ from the side line of the tar distillate tower, washing to dephenolate, rectifying and separating light components to obtain industrial naphthalene with the solidifying point of 78 ℃ and the purity of 96%.
The separation of the naphthalene oil fraction in the production adopts a rectification process, gas phase industrial naphthalene is cooled by an industrial naphthalene/raw material heat exchanger and an industrial naphthalene vaporizer after coming out from the top of an industrial naphthalene rectification tower, then flows into an industrial naphthalene reflux tank after being cooled by the vaporizer for the second time, one part of the gas phase industrial naphthalene is used as a rectification tower for reflux, and the other part of the gas phase industrial naphthalene is used as a final product and is sent into a finished product tank area.
In the actual production process, because a small amount of alkaline sodium phenolate is contained in the industrial naphthalene raw material, the moisture in the alkaline sodium phenolate is evaporated in the heat exchange process, and the alkaline sodium phenolate is attached to the wall of the heat exchange tube, so that the heat exchange effect of the heat exchanger is poor and the expected effect cannot be achieved. After being cooled by a vaporizer, the industrial naphthalene has high temperature (more than 150 ℃), serious oxidation and influences the quality of products. Moreover, after the heat exchange of the industrial naphthalene and the heat exchanger is finished, the industrial naphthalene still needs to be in a gas phase state, a large amount of cooling water still needs to be used for cooling, the energy is not effectively utilized, and the energy waste condition exists.
Disclosure of Invention
Aiming at the technical problems in the prior art, an embodiment of the utility model aims to provide an industrial naphthalene production device, which comprises:
a rectifying tower;
the heat source inlet of the steam generator is connected with the top of the rectifying tower, an evaporation cavity is arranged in the steam generator, and water in the evaporation cavity is heated by a heat source to form steam;
the heat medium inlet of the heat exchanger is connected with the heat source outlet of the steam generator;
and the heat medium outlet of the heat exchanger is connected to the reflux groove, so that the heat medium subjected to heat exchange by the heat exchanger enters the reflux groove, and the reflux groove is respectively connected with the rectifying tower and the finished product tank.
As an alternative embodiment, the inlet of the evaporation cavity is connected with a water source, and the outlet of the evaporation cavity is connected with a low-pressure steam pipe network.
As an alternative embodiment, a cold medium passage is arranged in the heat exchanger, and an inlet of the cold medium passage is connected with the raw material pipeline.
As an alternative embodiment, the industrial naphthalene production device further comprises a reflux pump, wherein the reflux pump is connected with the lower part of the reflux tank, and the reflux pump is connected with one side of the upper part of the rectifying tower through a reflux pipeline.
As an alternative embodiment, the return pump is also connected to the finished tank by means of a transport line.
As an alternative embodiment, one side of the middle part of the rectifying tower is respectively provided with a primary furnace feed inlet and a fine furnace feed inlet, and the primary furnace feed inlet is positioned above the fine furnace feed inlet.
As an optional embodiment, a rectifying tower hot oil pump is arranged at one side of the bottom of the rectifying tower, a discharge hole of the rectifying tower hot oil pump is connected with a feed inlet of the rectifying tower tubular furnace, and a discharge hole of the rectifying tower tubular furnace is connected with a feed inlet of the rectifying furnace.
As an optional embodiment, the discharge port of the refined tower hot oil pump is also connected with a wash oil heat exchanger, and the hot medium outlet of the wash oil heat exchanger is connected with a wash oil tank.
The embodiment of the utility model has the beneficial effects that:
the utility model re-optimizes the process flow, the industrial naphthalene passing through the steam generator is still in gas phase, and then the temperature of the industrial naphthalene is reduced to about 120 ℃ to become liquid phase after passing through the heat exchanger, so that the quality of industrial naphthalene products is improved, the vaporization cooler can be stopped at the moment, and the consumption of circulating water in the vaporization cooler is reduced. The whole production process reasonably utilizes the waste heat of the product, achieves the aim of completely recycling energy, and simultaneously stably controls the temperature of industrial naphthalene products and improves the quality of the products.
Drawings
Fig. 1 is a schematic structural diagram of an embodiment of the present utility model.
Reference numerals:
1. a rectifying tower; 2. a steam generator; 3. a heat exchanger; 4. a reflux groove; 5. a finished product tank; 6. a reflux pump; 7. a return line; 8. a transportation pipeline; 9. a primary furnace feed inlet; 10. a fine furnace feed inlet; 11. a refined tower hot oil pump; 12. rectifying tower tube furnace; 13. a wash oil heat exchanger; 14. and an oil washing tank.
Detailed Description
Various aspects and features of the present utility model are described herein with reference to the accompanying drawings.
It should be understood that various modifications may be made to the embodiments of the application herein. Therefore, the above description should not be taken as limiting, but merely as exemplification of the embodiments. Other modifications within the scope and spirit of the utility model will occur to persons of ordinary skill in the art.
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments of the utility model and, together with a general description of the utility model given above, and the detailed description of the embodiments given below, serve to explain the principles of the utility model.
These and other characteristics of the utility model will become apparent from the following description of a preferred form of embodiment, given as a non-limiting example, with reference to the accompanying drawings.
It is also to be understood that, although the utility model has been described with reference to some specific examples, those skilled in the art can certainly realize many other equivalent forms of the utility model.
The above and other aspects, features and advantages of the present utility model will become more apparent in light of the following detailed description when taken in conjunction with the accompanying drawings.
Specific embodiments of the present utility model will be described hereinafter with reference to the accompanying drawings; however, it is to be understood that the disclosed embodiments are merely exemplary of the utility model, which can be embodied in various forms. Well-known and/or repeated functions and constructions are not described in detail to avoid obscuring the utility model in unnecessary or unnecessary detail. Therefore, specific structural and functional details disclosed herein are not intended to be limiting, but merely as a basis for the claims and as a representative basis for teaching one skilled in the art to variously employ the present utility model in virtually any appropriately detailed structure.
The specification may use the word "in one embodiment," "in another embodiment," "in yet another embodiment," or "in other embodiments," which may each refer to one or more of the same or different embodiments in accordance with the utility model.
The embodiment of the utility model provides an industrial naphthalene production device, which is shown in figure 1 and comprises a rectifying tower 1, a steam generator 2, a heat exchanger 3 and a reflux tank 4. Valves are respectively arranged on connecting pipelines between the rectifying tower 1 and the steam generator 2, between the steam generator 2 and the heat exchanger 3 and between the heat exchanger 3 and the reflux tank 4.
The heat source inlet of the steam generator 2 is connected with the top of the rectifying tower 1, wherein gas-phase industrial naphthalene produced by the top of the rectifying tower 1 is used as a heat source. An evaporation cavity is arranged in the steam generator 2, and water in the evaporation cavity is heated by a heat source to form steam.
The heat medium inlet of the heat exchanger 3 is connected with the heat source outlet of the steam generator 2. The heat medium outlet of the heat exchanger 3 is connected to the reflux tank 4, so that the heat medium subjected to heat exchange by the heat exchanger 3 enters the reflux tank 4, and the reflux tank 4 is respectively connected with the rectifying tower 1 and the finished product tank 5.
As an alternative embodiment, the inlet of the evaporation cavity is connected with a water source, and the outlet of the evaporation cavity is connected with a low-pressure steam pipe network. Wherein, the water source can adopt softened water.
As an alternative embodiment, a cold medium passage is provided in the heat exchanger 3, and an inlet of the cold medium passage is connected to the raw material pipeline. The heat exchanger 3 can exchange heat with the heat source cooled by the steam generator 2, and can further heat the raw materials preliminarily, so that heat energy generated by the heat source is effectively utilized.
As an alternative embodiment, the industrial naphthalene production apparatus further comprises a reflux pump 6, wherein the reflux pump 6 is connected with the lower part of the reflux tank 4, and the reflux pump 6 is connected with one side of the upper part of the rectifying tower 1 through a reflux pipeline 7. As an alternative embodiment, the return pump 6 is also connected to the product tank 5 via a transport line 8. Valves are respectively arranged on the connecting pipe line between the reflux pump 6 and the reflux tank 4, the reflux pipe line 7 and the transportation pipe line 8.
As an alternative embodiment, a primary furnace feed inlet 9 and a fine furnace feed inlet 10 are respectively arranged on one side of the middle part of the rectifying tower 1, and the primary furnace feed inlet 9 is positioned above the fine furnace feed inlet 10. A valve is arranged between the rectifying tower 1 and the rectifying furnace feed inlet 10.
As an alternative embodiment, a rectifying tower hot oil pump 11 is arranged at one side of the bottom of the rectifying tower 1, a discharge port of the rectifying tower hot oil pump 11 is connected with a feed port of a rectifying tower tube furnace 12, and a discharge port of the rectifying tower tube furnace 12 is connected with the rectifying furnace feed port 10. And heating part of the bottom oil through the rectifying tower tube furnace 12, and re-entering the rectifying tower 1 from the heated bottom oil. Valves are respectively arranged on connecting pipelines between the rectifying tower 1 and the rectifying tower hot oil pump 11 and between the rectifying tower hot oil pump 11 and the rectifying tower tubular furnace 12.
As an alternative embodiment, the discharge port of the refined tower hot oil pump 11 is also connected with a wash oil heat exchanger 13, and the heat medium outlet of the wash oil heat exchanger 13 is connected with a wash oil tank 14. Valves are respectively arranged on connecting pipelines between the refined tower hot oil pump 11 and the wash oil heat exchanger 13 and between the wash oil heat exchanger 13 and the wash oil tank 14.
Part of naphthalene washing oil from the primary furnace is fed into the rectifying tower 1 through the discharging feed inlet, gas-phase industrial naphthalene is extracted from the top of the rectifying tower 1, and the temperature of the top of the rectifying tower 1 is controlled to be about 218 ℃. When passing through the steam generator 2, the gas-phase industrial naphthalene exchanges heat with the softened water in the evaporation cavity, and the exchanged heat is enough for a part of softened water to generate phase change to be changed into steam, and the part of low-pressure steam enters the low-pressure steam pipe network through the outlet of the evaporation cavity. At the same time, the temperature of the industrial naphthalene is reduced to about 170 ℃ and enters the heat exchanger 3 through the heat medium inlet, the heat exchanger 3 adopts the industrial naphthalene/raw material heat exchanger 3, the temperature of the industrial naphthalene after heat exchange with the raw material is reduced to about 120 ℃ and flows into the reflux tank 4, wherein one part of the industrial naphthalene flows back to the rectifying tower 1 through the reflux pipeline 7, and the other part of the industrial naphthalene is transported to the finished product tank 5 through the transportation pipeline 8 and is transported out as a finished product.
Compared with the prior domestic industrial naphthalene production which adopts a vaporizer cooling mode, the utility model ensures that the industrial naphthalene passing through the steam generator 2 is still in a gas phase in the production process, and then the temperature of the industrial naphthalene is reduced to about 120 ℃ to be changed into a liquid phase after passing through the heat exchanger 3, thereby improving the quality of industrial naphthalene products, stopping the vaporization cooler at the moment and reducing the consumption of circulating water in the vaporization cooler. The utility model optimizes the production process of industrial naphthalene, and the optimized production device can produce byproduct 0.5MPa low-pressure steam 2.5 tons/hour per hour, and the waste heat of the gas-phase industrial naphthalene is completely recycled after optimization.
The bottom oil of the rectifying tower 1 is sent to the rectifying tower tube furnace 12 by the rectifying tower hot oil pump 11 to be heated to about 280-300 ℃ and then sent back to the rectifying tower 1, and the heat of the rectifying tower 1 is also supplied in a hot oil circulation mode. In addition, a part of bottom oil is taken as low naphthalene wash oil from an outlet pipe of the refined tower hot oil pump 11, cooled by a wash oil heat exchanger 13 and then enters a wash oil tank 14, the part of bottom oil is used for maintaining the heat balance of the rectifying tower 1, and redundant bottom oil is taken after the materials are balanced.
The above embodiments are only exemplary embodiments of the present utility model and are not intended to limit the present utility model, the scope of which is defined by the claims. Various modifications and equivalent arrangements of this utility model will occur to those skilled in the art, and are intended to be within the spirit and scope of the utility model.
Claims (8)
1. An industrial naphthalene production apparatus, comprising:
a rectifying tower;
the heat source inlet of the steam generator is connected with the top of the rectifying tower, an evaporation cavity is arranged in the steam generator, and water in the evaporation cavity is heated by a heat source to form steam;
the heat medium inlet of the heat exchanger is connected with the heat source outlet of the steam generator;
and the heat medium outlet of the heat exchanger is connected to the reflux groove, so that the heat medium subjected to heat exchange by the heat exchanger enters the reflux groove, and the reflux groove is respectively connected with the rectifying tower and the finished product tank.
2. The industrial naphthalene production apparatus of claim 1 wherein the inlet of the evaporation chamber is connected to a water source and the outlet of the evaporation chamber is connected to a low pressure steam pipe network.
3. The industrial naphthalene production apparatus according to claim 1, wherein a cold medium passage is provided inside the heat exchanger, and an inlet of the cold medium passage is connected to a raw material line.
4. The industrial naphthalene production apparatus according to claim 1, further comprising a reflux pump connected to a lower portion of the reflux tank, the reflux pump being connected to an upper portion side of the rectifying column through a reflux line.
5. The industrial naphthalene production apparatus of claim 4 wherein the return pump is further connected to a finishing tank by a transportation line.
6. The industrial naphthalene production device according to claim 1, wherein a primary furnace feed port and a fine furnace feed port are respectively arranged on one side of the middle part of the rectifying tower, and the primary furnace feed port is positioned above the fine furnace feed port.
7. The industrial naphthalene production device according to claim 6, wherein a rectifying tower hot oil pump is arranged on one side of the bottom of the rectifying tower, a discharge port of the rectifying tower hot oil pump is connected with a feed port of a rectifying tower tube furnace, and a discharge port of the rectifying tower tube furnace is connected with the feed port of the rectifying furnace.
8. The industrial naphthalene production apparatus according to claim 7, wherein the outlet of the refined tower hot oil pump is further connected to a wash oil heat exchanger, and the hot medium outlet of the wash oil heat exchanger is connected to a wash oil tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320921059.9U CN220012508U (en) | 2023-04-21 | 2023-04-21 | Industrial naphthalene production device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320921059.9U CN220012508U (en) | 2023-04-21 | 2023-04-21 | Industrial naphthalene production device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220012508U true CN220012508U (en) | 2023-11-14 |
Family
ID=88675945
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202320921059.9U Active CN220012508U (en) | 2023-04-21 | 2023-04-21 | Industrial naphthalene production device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220012508U (en) |
-
2023
- 2023-04-21 CN CN202320921059.9U patent/CN220012508U/en active Active
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