CN112337261A - Tail gas treatment system and process in refined naphthalene production process by fractional crystallization method - Google Patents
Tail gas treatment system and process in refined naphthalene production process by fractional crystallization method Download PDFInfo
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- CN112337261A CN112337261A CN202011348551.9A CN202011348551A CN112337261A CN 112337261 A CN112337261 A CN 112337261A CN 202011348551 A CN202011348551 A CN 202011348551A CN 112337261 A CN112337261 A CN 112337261A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/14—Purification; Separation; Use of additives by crystallisation; Purification or separation of the crystals
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28B—STEAM OR VAPOUR CONDENSERS
- F28B1/00—Condensers in which the steam or vapour is separate from the cooling medium by walls, e.g. surface condenser
- F28B1/06—Condensers in which the steam or vapour is separate from the cooling medium by walls, e.g. surface condenser using air or other gas as the cooling medium
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28B—STEAM OR VAPOUR CONDENSERS
- F28B9/00—Auxiliary systems, arrangements, or devices
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F1/00—Tubular elements; Assemblies of tubular elements
- F28F1/10—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses
- F28F1/12—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses the means being only outside the tubular element
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Abstract
The invention relates to a tail gas treatment system and a process in the process of producing refined naphthalene by a fractional crystallization method, wherein the system comprises an industrial naphthalene raw material tank, a plurality of fractionation tanks, a residue tank, a plurality of crystallization boxes, a refined naphthalene tank and a sublimated naphthalene catcher; the sublimed naphthalene catcher consists of a box body and a plurality of groups of air-cooled heat exchange finned tubes arranged in the box body; according to the invention, the sublimed naphthalene catcher is additionally arranged to catch the naphthalene-containing tail gas of each naphthalene-containing device, the pressure fluctuation of the system is reduced through the nitrogen seal, the caught sublimed naphthalene is melted by the industrial naphthalene raw material periodically and is recycled into the industrial naphthalene raw material tank, the naphthalene loss is reduced, the tail gas discharge amount is also reduced, and the influence of the high naphthalene-containing tail gas on a subsequent exhaust and cleaning system is avoided.
Description
Technical Field
The invention relates to the technical field of naphthalene-containing tail gas treatment, in particular to a tail gas treatment system and a tail gas treatment process in a refined naphthalene production process by a fractional crystallization method.
Background
When refined naphthalene is produced by fractional crystallization, industrial naphthalene is used as raw material, and naphthalene residual oil and refined naphthalene are used as products. Due to the volume limitation of the crystallization box, the crystallization box usually consists of a plurality of sets of crystallization systems, and each set of crystallization system takes the crystallization box as a core device. The crystallization box is a square box type crystallizer, fin heat exchange tubes which are horizontally, transversely and longitudinally arranged layer by layer are arranged in the crystallization box, a circulating heat carrier flows in the fin heat exchange tubes, and materials are filled in the crystallization box outside the fin heat exchange tubes. The temperature of the circulating heat carrier is reduced, and the materials can be cooled and crystallized; the material can be sweated (slowly heated for partial melting) and melted by increasing the temperature of the circulating heat carrier. Therefore, 3 strands of materials with gradually increased naphthalene content can be obtained by feeding the raw materials with different naphthalene contents into the crystallization box, wherein the materials are respectively discharge liquid, perspiration liquid and melting liquid, and the materials are respectively fed into different naphthalene oil tanks according to the naphthalene content, wherein the material with the lowest naphthalene content enters the residual oil tank, the material with the highest naphthalene content enters the refined naphthalene tank (namely the refined naphthalene product tank), and the rest naphthalene fractions at all stages enter the corresponding fraction tanks.
The most equipment in the process of producing refined naphthalene by a fractional crystallization method is a naphthalene oil tank (comprising a naphthalene residual oil tank, various levels of naphthalene fraction tanks and a refined naphthalene tank) and a crystallization box, wherein the naphthalene oil tank and the crystallization box are all naphthalene-containing equipment, and tail gas of the naphthalene-containing equipment is basically naphthalene vapor; at present, the treatment mode of the tail gas is basically an exhaust gas cleaning system which is integrated into other production processes. Because the crystallization point of pure naphthalene is 79.6 ℃, the heat preservation of the naphthalene-containing tail gas pipeline is very important, otherwise, the blockage of throttling equipment and pipe fittings of the tail gas pipeline is easily caused, so that the heat preservation burden of the subsequent tail gas pipeline is aggravated, and the oil washing of an exhaust cleaning system is easily failed quickly.
The tail gas treatment in the refined naphthalene production process needs to be analyzed and distinguished according to the characteristics of the tail gas, so that the pollution to the environment is prevented, the quantity of the tail gas is reduced to the maximum extent, the running cost of environment-friendly equipment is reduced, and in addition, available resources are utilized, so that the tail gas treatment process is scientific, feasible, optimized, safe and economic.
Disclosure of Invention
The invention provides a tail gas treatment system and a tail gas treatment process in a refined naphthalene production process by a fractional crystallization method.
In order to achieve the purpose, the invention adopts the following technical scheme:
a tail gas treatment system in the process of producing refined naphthalene by a fractional crystallization method comprises an industrial naphthalene raw material tank, a plurality of fractionation tanks, a raffinate tank, a plurality of crystallization boxes, a refined naphthalene tank and a sublimed naphthalene catcher; the sublimed naphthalene catcher consists of a box body and a plurality of groups of air-cooled heat exchange finned tubes arranged in the box body; a tail gas inlet is formed in one side of the lower part of the box body, an industrial naphthalene outlet is formed in the other side of the lower part of the box body, an industrial naphthalene inlet and a tail gas outlet are formed in the top of the box body, and an industrial naphthalene full-flow port is formed in one side of the upper part of the box body; the top of the industrial naphthalene raw material tank, the top of each distillation tank, the top of the raffinate tank, the top of each crystallization box and the top of the refined naphthalene tank are respectively provided with a diffused gas outlet which is connected with a tail gas inlet at the bottom of the sublimated naphthalene catcher through a diffused gas main pipe; the industrial naphthalene full-flow port and the industrial naphthalene outlet are connected with a recovered industrial naphthalene inlet at the top of the industrial naphthalene raw material tank through an industrial naphthalene recovery pipeline; the industrial naphthalene inlet is connected with an industrial naphthalene conveying pipeline, and the industrial naphthalene conveying pipeline is additionally connected with an industrial naphthalene feeding hole at the top of the industrial naphthalene raw material groove.
The end, close to the sublimed naphthalene catcher, of the main diffused gas pipe is provided with a nitrogen inlet and a residual tail gas outlet respectively, the nitrogen inlet is connected with a nitrogen pipeline, and a nitrogen self-supporting regulating valve is arranged on the nitrogen pipeline; the residual tail gas outlet is connected with an external exhaust cleaning system through a residual tail gas pipeline, a pressure regulating valve and a pressure recording regulating instrument are arranged on the residual tail gas pipeline, and the pressure regulating valve and the pressure recording regulating instrument are controlled in an interlocking mode.
The box of the sublimed naphthalene trap is a rectangular box, a plurality of groups of air cooling heat exchange finned tubes are horizontally arranged in the box along the height direction, and 2 adjacent groups of air cooling heat exchange finned tubes are arranged in a criss-cross mode.
The lower part of the box body is provided with a clapboard, and the box body below the clapboard is internally provided with an auxiliary heater.
The auxiliary heater is a spiral steam heating pipeline, a steam inlet is formed in one end of the steam heating pipeline and connected with the steam pipeline, and a condensate outlet is formed in the other end of the steam heating pipeline and connected with a condensate recovery pipeline.
The baffle is obliquely arranged, and one end close to the tail gas inlet is higher than one end close to the industrial naphthalene outlet.
And a first valve is arranged on the industrial naphthalene conveying pipeline connected with the sublimed naphthalene catcher.
The industrial naphthalene outlet is connected with an industrial naphthalene recovery pipeline through a traffic pipe, and a second valve is arranged on the traffic pipe.
A tail gas treatment process in the refined naphthalene production process by a fractional crystallization method comprises the following steps:
1) the diffused gases of the residue tank, the distillation tanks, the industrial naphthalene raw material tank and the refined naphthalene tank and the diffused gases of the crystallization tanks are all collected into a diffused gas main pipe and are intensively sent to a sublimed naphthalene catcher; the sublimed naphthalene trap exchanges heat with diffused gas in an air cooling mode to trap sublimed naphthalene vapor; the air passes through the tube pass, and the sublimated naphthalene vapor passes through the shell pass; the sublimated naphthalene vapor is condensed and then attached to the air-cooled heat exchange finned tube to achieve the trapping effect;
2) the operation pressure of each distillation tank and the crystallization box is controlled to be-0.2-0.4 kPa, and the operation pressure is automatically adjusted by a nitrogen self-supporting adjusting valve; when the pressure of the system is lower than-0.2 kPa, nitrogen is supplemented, and when the pressure recording and adjusting instrument displays that the pressure of the system is higher than 0.4kPa, redundant tail gas is automatically discharged through a pressure adjusting valve, so that the pressure of the system is kept stable;
3) after the running time of the sublimed naphthalene catcher reaches the set time, carrying out melting operation on the sublimed naphthalene; opening a second valve on the traffic pipe and a first valve on the industrial naphthalene conveying pipeline to enable the industrial naphthalene to enter the sublimed naphthalene catcher; after the industrial naphthalene is fully filled with the sublimed naphthalene catcher, the sublimed naphthalene attached to the air-cooled heat exchange finned tube is washed off and automatically flows into an industrial naphthalene raw material tank together with the industrial naphthalene through an industrial naphthalene full flow port; and after the operation of melting the sublimed naphthalene is finished, closing the first valve, emptying the industrial naphthalene in the sublimed naphthalene catcher to the industrial naphthalene raw material tank, closing the second valve, and restarting the sublimed naphthalene catching operation.
And in the step 3), when the sublimed naphthalene is melted, the auxiliary heater at the bottom of the sublimed naphthalene catcher is started, so that the sublimed naphthalene in the sublimed naphthalene catcher is melted and emptied more cleanly and thoroughly.
Compared with the prior art, the invention has the beneficial effects that:
1) the sublimed naphthalene catcher is adopted to catch the naphthalene-containing tail gas of each naphthalene-containing device, so that the loss of naphthalene vapor volatilization can be reduced, the tail gas emission can be reduced, and the heat-preservation burden of a subsequent exhaust system pipeline is eliminated;
2) the sublimed naphthalene catcher is characterized by large heat exchange area and small heat exchange amount, and adopts an air cooling mode, thereby saving a large amount of circulating water resources and reducing the operation cost;
3) a plurality of groups of air cooling fin heat exchange tubes are arranged in the sublimed naphthalene catcher, so that the space occupied by naphthalene vapor is small, the sublimed naphthalene is conveniently melted by adopting industrial naphthalene as a raw material, and the energy is saved;
4) the sublimed naphthalene trap has simple structure and convenient operation.
Drawings
FIG. 1 is a schematic structural diagram of a tail gas treatment system in a process of producing refined naphthalene by a fractional crystallization method according to the present invention.
FIG. 2 is a schematic diagram of the sublimating naphthalene trap according to the present invention.
In the figure: 1. residue tank 2.2# fractionation tank 3, industrial naphthalene raw material tank 4.4# fractionation tank 5.5# fractionation tank 6, refined naphthalene tank 7.1# crystallization tank 8.2# crystallization tank 9, sublimed naphthalene catcher 91, tail gas inlet 92, tail gas outlet 93, industrial naphthalene inlet 94, industrial naphthalene outlet 95, industrial naphthalene full flow port 96, partition 97, auxiliary heater 98, air-cooled heat exchange fin tube 10, nitrogen self-supporting regulating valve 11, pressure regulating valve 12, valve I13, valve II PRC01, pressure recording regulating instrument
Detailed Description
The following further describes embodiments of the present invention with reference to the accompanying drawings:
as shown in figure 1, the tail gas treatment system in the process of producing refined naphthalene by the fractional crystallization method comprises an industrial naphthalene raw material tank 3, a plurality of fractional tanks, a raffinate tank 1, a plurality of crystallization boxes, a refined naphthalene tank 6 and a sublimated naphthalene catcher 9; as shown in fig. 2, the sublimed naphthalene catcher 9 consists of a box body and a plurality of groups of air-cooled heat exchange finned tubes 98 arranged in the box body; a tail gas inlet 91 is formed in one side of the lower part of the box body, an industrial naphthalene outlet 94 is formed in the other side of the lower part of the box body, an industrial naphthalene inlet 93 and a tail gas outlet 92 are formed in the top of the box body, and an industrial naphthalene full-flow port 95 is formed in one side of the upper part of the box body; the top of the industrial naphthalene raw material tank 3, the top of each distillation tank, the top of the raffinate tank 1, the top of each crystallization box and the top of the refined naphthalene tank 6 are respectively provided with a diffused gas outlet which is connected with a tail gas inlet 91 at the bottom of the sublimated naphthalene trap 9 through a diffused gas main pipe; the industrial naphthalene full flow port 95 and the industrial naphthalene outlet 94 are connected with a recovered industrial naphthalene inlet at the top of the industrial naphthalene raw material tank 3 through an industrial naphthalene recovery pipeline; the industrial naphthalene inlet 93 is connected with an industrial naphthalene conveying pipeline, and the industrial naphthalene conveying pipeline is additionally connected with an industrial naphthalene feeding hole at the top of the industrial naphthalene raw material groove 3.
A nitrogen inlet and a residual tail gas outlet are respectively arranged at one end of the main diffusing gas pipe close to the sublimed naphthalene catcher 9, the nitrogen inlet is connected with a nitrogen pipeline, and a nitrogen self-supporting regulating valve 10 is arranged on the nitrogen pipeline; the residual tail gas outlet is connected with an external exhaust cleaning system through a residual tail gas pipeline, a pressure regulating valve 11 and a pressure recording regulating instrument PRC01 are arranged on the residual tail gas pipeline, and the pressure regulating valve 11 and the pressure recording regulating instrument PRC01 are controlled in an interlocking mode.
The box body of the sublimed naphthalene catcher 9 is a rectangular box body, a plurality of groups of air cooling heat exchange finned tubes 98 are horizontally arranged in the box body along the height direction, and 2 adjacent groups of air cooling heat exchange finned tubes 98 are arranged in a criss-cross mode.
A partition plate 96 is arranged at the lower part of the box body, and an auxiliary heater 97 is arranged in the box body below the partition plate 96.
The auxiliary heater 97 is a spiral steam heating pipeline, a steam inlet is arranged at one end of the steam heating pipeline and is connected with the steam pipeline, and a condensate outlet is arranged at the other end of the steam heating pipeline and is connected with a condensate recovery pipeline.
The partition plate 96 is obliquely arranged, and one end close to the tail gas inlet is higher than one end close to the industrial naphthalene outlet.
And a first valve 12 is arranged on the industrial naphthalene conveying pipeline connected with the sublimed naphthalene catcher 9.
The industrial naphthalene outlet 94 is connected with an industrial naphthalene recovery pipeline through a traffic pipe, and a second valve 13 is arranged on the traffic pipe.
A tail gas treatment process in the refined naphthalene production process by a fractional crystallization method comprises the following steps:
1) the diffused gases of the residue liquid tank 1, each fraction tank, the industrial naphthalene raw material tank 3 and the refined naphthalene tank 6 and the diffused gases of each crystallization tank are all collected into a diffused gas main pipe and are intensively sent to a sublimed naphthalene catcher 9; the sublimed naphthalene catcher 9 adopts an air cooling mode to exchange heat with the diffused gas to catch the sublimed naphthalene vapor; the air passes through the tube pass, and the sublimated naphthalene vapor passes through the shell pass; the sublimated naphthalene vapor is condensed and then attached to the air-cooled heat exchange finned tube 98, so that the trapping effect is achieved;
2) the operation pressure of each fractionating groove and the crystallization box is controlled to be-0.2-0.4 kPa, and the operation pressure is automatically adjusted through a nitrogen self-supporting adjusting valve 10; when the pressure of the system is lower than-0.2 kPa, nitrogen is supplemented, and when a pressure recording and adjusting instrument PRC01 shows that the pressure of the system is higher than 0.4kPa, redundant tail gas is automatically discharged through a pressure adjusting valve 11, so that the pressure of the system is kept stable;
3) after the running time of the sublimed naphthalene catcher 9 reaches the set time, carrying out melting operation on the sublimed naphthalene; opening a second valve 13 on the traffic pipe and a first valve 12 on the industrial naphthalene conveying pipeline to enable the industrial naphthalene to enter the sublimed naphthalene catcher 9; after the sublimed naphthalene catcher 9 is filled with the industrial naphthalene, the sublimed naphthalene attached to the air-cooled heat exchange finned tube 98 is washed down and automatically flows into the industrial naphthalene raw material tank 3 together with the industrial naphthalene through the industrial naphthalene full flow port 95; and after the operation of melting the sublimated naphthalene is finished, closing the first valve 12, emptying the industrial naphthalene in the sublimated naphthalene catcher 9 to the industrial naphthalene raw material tank 3, closing the second valve 13, and restarting the operation of trapping the sublimated naphthalene.
In the step 3), when the sublimed naphthalene is melted, the auxiliary heater at the bottom of the sublimed naphthalene catcher 9 is started, so that the sublimed naphthalene in the sublimed naphthalene catcher 9 is melted and emptied more cleanly and thoroughly.
The following examples are carried out on the premise of the technical scheme of the invention, and detailed embodiments and specific operation processes are given, but the scope of the invention is not limited to the following examples. The methods used in the following examples are conventional methods unless otherwise specified.
[ examples ] A method for producing a compound
In this embodiment, a tail gas processing system in refined naphthalene production process by fractional crystallization method, including industrial naphthalene raw materials groove 3, 2# fractionation groove 2, 4# fraction groove 4, 5# fractionation groove 5, raffinate groove 1, 1# crystallization case 7, 2# crystallization case 8, refined naphthalene groove 6 and sublimed naphthalene catcher 9.
The diffused gas at the top of the industrial naphthalene raw material tank 3, the residual liquid tank 1, the fractional tanks (2, 4 and 5), the refined naphthalene tank 6 and the crystallization boxes (7 and 8) is collected into a diffused gas main pipe and is intensively sent to a sublimed naphthalene catcher 9.
The sublimed naphthalene catcher 9 is a square box type catcher, wherein a plurality of layers of air-cooled heat exchange finned tubes 98 are densely arranged, and each layer consists of a plurality of horizontally arranged heat exchange finned tubes; the method has the characteristics of large heat exchange area and small heat exchange amount, and adopts an air cooling mode to collect the sublimated naphthalene. The adjacent 2 layers of air-cooled heat exchange finned tubes 98 are arranged alternately along the transverse direction and the longitudinal direction, and two ends of each heat exchange finned tube are communicated with the outside atmosphere, namely air flows in the heat exchange finned tubes; in the sublimed naphthalene catcher 9, the naphthalene vapor volatilized by each naphthalene containing device is basically caught, thereby reducing the emission amount of the tail gas.
In order to keep the pressure of the system stable, nitrogen is supplied through the nitrogen self-standing type regulating valve 10 when the pressure of the system is reduced, and a part of exhaust gas is discharged through the pressure regulating valve 11 when the pressure of the system is raised, so that the pressure of the system is kept stable.
When the amount of the tail gas in the sublimed naphthalene catcher 9 is obviously increased after the sublimed naphthalene catcher 9 is operated for a period of time, the sublimed naphthalene needs to be melted. Opening a second valve 13 on the traffic pipe and a first valve 12 on the industrial naphthalene conveying pipeline to enable the industrial naphthalene to enter the sublimed naphthalene catcher 9; after the sublimed naphthalene catcher 9 is filled with the industrial naphthalene, the sublimed naphthalene attached to the air-cooled heat exchange finned tube 98 is washed down and automatically flows into the industrial naphthalene raw material tank 3 together with the industrial naphthalene through the industrial naphthalene full flow port 95; and after the operation of melting the sublimated naphthalene is finished, closing a first valve 12 on the industrial naphthalene conveying pipeline, emptying the industrial naphthalene in the sublimated naphthalene catcher 9 to the industrial naphthalene raw material tank 3, then closing a second valve 13 on the cross pipe, and restarting the operation of trapping the sublimated naphthalene.
Be equipped with auxiliary heater 97 in subliming naphthalene trap 9's the bottom intermediate layer, when subliming naphthalene trap 9 melts the operation, can start auxiliary heater 97, make the subliming naphthalene among the subliming naphthalene trap 9 melt, the unloading is cleaner, more thorough. The partition plate 96 adopts an inclined design, so that the industrial naphthalene can be conveniently emptied.
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 (10)
1. A tail gas treatment system in the refined naphthalene production process by a fractional crystallization method is characterized by comprising an industrial naphthalene raw material tank, a plurality of fractionation tanks, a residue tank, a plurality of crystallization boxes, a refined naphthalene tank and a sublimed naphthalene catcher; the sublimed naphthalene catcher consists of a box body and a plurality of groups of air-cooled heat exchange finned tubes arranged in the box body; a tail gas inlet is formed in one side of the lower part of the box body, an industrial naphthalene outlet is formed in the other side of the lower part of the box body, an industrial naphthalene inlet and a tail gas outlet are formed in the top of the box body, and an industrial naphthalene full-flow port is formed in one side of the upper part of the box body; the top of the industrial naphthalene raw material tank, the top of each distillation tank, the top of the raffinate tank, the top of each crystallization box and the top of the refined naphthalene tank are respectively provided with a diffused gas outlet which is connected with a tail gas inlet at the bottom of the sublimated naphthalene catcher through a diffused gas main pipe; the industrial naphthalene full-flow port and the industrial naphthalene outlet are connected with a recovered industrial naphthalene inlet at the top of the industrial naphthalene raw material tank through an industrial naphthalene recovery pipeline; the industrial naphthalene inlet is connected with an industrial naphthalene conveying pipeline, and the industrial naphthalene conveying pipeline is additionally connected with an industrial naphthalene feeding hole at the top of the industrial naphthalene raw material groove.
2. The tail gas treatment system in the process of producing refined naphthalene by the fractional crystallization method according to claim 1, wherein the end of the main diffusing gas pipe close to the sublimed naphthalene catcher is respectively provided with a nitrogen inlet and a residual tail gas outlet, the nitrogen inlet is connected with a nitrogen pipeline, and the nitrogen pipeline is provided with a self-supporting nitrogen regulating valve; the residual tail gas outlet is connected with an external exhaust cleaning system through a residual tail gas pipeline, a pressure regulating valve and a pressure recording regulating instrument are arranged on the residual tail gas pipeline, and the pressure regulating valve and the pressure recording regulating instrument are controlled in an interlocking mode.
3. The tail gas treatment system in the process of producing refined naphthalene by the fractional crystallization method according to claim 1, wherein the box body of the sublimation naphthalene catcher is a rectangular box body, a plurality of groups of air-cooling heat exchange finned tubes are horizontally arranged in the box body along the height direction, and 2 adjacent groups of air-cooling heat exchange finned tubes are arranged in a criss-cross mode.
4. The tail gas treatment system in the refined naphthalene production process by the fractional crystallization method according to claim 1 or 3, wherein a partition plate is arranged at the lower part of the box body, and an auxiliary heater is arranged in the box body below the partition plate.
5. The tail gas treatment system in the process of producing refined naphthalene by the fractional crystallization method according to claim 4, wherein the auxiliary heater is a spiral steam heating pipeline, a steam inlet is formed at one end of the steam heating pipeline and connected with the steam pipeline, and a condensate outlet is formed at the other end of the steam heating pipeline and connected with a condensate recovery pipeline.
6. The system for treating tail gas generated in the process of producing refined naphthalene by the fractional crystallization method according to claim 4, wherein the partition is disposed in an inclined manner, and one end of the partition close to the tail gas inlet is higher than one end close to the industrial naphthalene outlet.
7. The system for treating the tail gas generated in the process of producing refined naphthalene by the fractional crystallization method according to claim 1, wherein a first valve is arranged on an industrial naphthalene conveying pipeline connected with the sublimed naphthalene catcher.
8. The tail gas treatment system in the process of producing refined naphthalene by the fractional crystallization method according to claim 1, wherein the industrial naphthalene outlet is connected with an industrial naphthalene recovery pipeline through a traffic pipe, and a second valve is arranged on the traffic pipe.
9. The tail gas treatment process in the refined naphthalene production process by the fractional crystallization method based on any one of the systems of claims 1 to 8 is characterized by comprising the following steps:
1) the diffused gases of the residue tank, the distillation tanks, the industrial naphthalene raw material tank and the refined naphthalene tank and the diffused gases of the crystallization tanks are all collected into a diffused gas main pipe and are intensively sent to a sublimed naphthalene catcher; the sublimed naphthalene trap exchanges heat with diffused gas in an air cooling mode to trap sublimed naphthalene vapor; the air passes through the tube pass, and the sublimated naphthalene vapor passes through the shell pass; the sublimated naphthalene vapor is condensed and then attached to the air-cooled heat exchange finned tube to achieve the trapping effect;
2) the operation pressure of each distillation tank and the crystallization box is controlled to be-0.2-0.4 kPa, and the operation pressure is automatically adjusted by a nitrogen self-supporting adjusting valve; when the pressure of the system is lower than-0.2 kPa, nitrogen is supplemented, and when the pressure recording and adjusting instrument displays that the pressure of the system is higher than 0.4kPa, redundant tail gas is automatically discharged through a pressure adjusting valve, so that the pressure of the system is kept stable;
3) after the running time of the sublimed naphthalene catcher reaches the set time, carrying out melting operation on the sublimed naphthalene; opening a second valve on the traffic pipe and a first valve on the industrial naphthalene conveying pipeline to enable the industrial naphthalene to enter the sublimed naphthalene catcher; after the industrial naphthalene is fully filled with the sublimed naphthalene catcher, the sublimed naphthalene attached to the air-cooled heat exchange finned tube is washed off and automatically flows into an industrial naphthalene raw material tank together with the industrial naphthalene through an industrial naphthalene full flow port; and after the operation of melting the sublimed naphthalene is finished, closing the first valve, emptying the industrial naphthalene in the sublimed naphthalene catcher to the industrial naphthalene raw material tank, closing the second valve, and restarting the sublimed naphthalene catching operation.
10. The tail gas treatment process in the process of producing refined naphthalene by the fractional crystallization method according to claim 9, wherein in the step 3), when the sublimed naphthalene is melted, an auxiliary heater at the bottom of the sublimed naphthalene catcher is turned on, so that the sublimed naphthalene in the sublimed naphthalene catcher is melted and emptied more cleanly and thoroughly.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202011348551.9A CN112337261A (en) | 2020-11-26 | 2020-11-26 | Tail gas treatment system and process in refined naphthalene production process by fractional crystallization method |
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| CN202011348551.9A CN112337261A (en) | 2020-11-26 | 2020-11-26 | Tail gas treatment system and process in refined naphthalene production process by fractional crystallization method |
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| CN112337261A true CN112337261A (en) | 2021-02-09 |
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| CN202011348551.9A Pending CN112337261A (en) | 2020-11-26 | 2020-11-26 | Tail gas treatment system and process in refined naphthalene production process by fractional crystallization method |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112999767A (en) * | 2021-03-09 | 2021-06-22 | 中冶焦耐(大连)工程技术有限公司 | Tail gas recovery system and process in naphthalene sheeting and packaging processes |
| CN115417743A (en) * | 2022-08-25 | 2022-12-02 | 中建安装集团有限公司 | Fractional melting crystallization process for preparing refined naphthalene from industrial naphthalene |
| CN116688703A (en) * | 2023-08-09 | 2023-09-05 | 河北斐然环保工程有限公司 | Petroleum naphthalene extraction device with shallow cooling condensing system |
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2020
- 2020-11-26 CN CN202011348551.9A patent/CN112337261A/en active Pending
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112999767A (en) * | 2021-03-09 | 2021-06-22 | 中冶焦耐(大连)工程技术有限公司 | Tail gas recovery system and process in naphthalene sheeting and packaging processes |
| CN115417743A (en) * | 2022-08-25 | 2022-12-02 | 中建安装集团有限公司 | Fractional melting crystallization process for preparing refined naphthalene from industrial naphthalene |
| CN115417743B (en) * | 2022-08-25 | 2024-01-30 | 中建安装集团有限公司 | Fractional melting crystallization process for industrial naphthalene refined naphthalene |
| CN116688703A (en) * | 2023-08-09 | 2023-09-05 | 河北斐然环保工程有限公司 | Petroleum naphthalene extraction device with shallow cooling condensing system |
| CN116688703B (en) * | 2023-08-09 | 2023-10-17 | 河北斐然环保工程有限公司 | Petroleum naphthalene extraction device with shallow cooling condensing system |
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