CN203558986U - Device for refining and machining aromatic hydrocarbons by using liquefied gas - Google Patents
Device for refining and machining aromatic hydrocarbons by using liquefied gas Download PDFInfo
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- CN203558986U CN203558986U CN201320502518.6U CN201320502518U CN203558986U CN 203558986 U CN203558986 U CN 203558986U CN 201320502518 U CN201320502518 U CN 201320502518U CN 203558986 U CN203558986 U CN 203558986U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
The utility model discloses a device for refining and machining aromatic hydrocarbons by using liquefied gas. The device comprises a raw material washing system, an aromatization reaction system, a stabilization system and a heavy component removal device. A discharge opening of the raw material washing system is communicated with a feeding hole of a raw material feeding pump; a discharge opening of the raw material feeding pump is communicated with a shell pass inlet of a heat exchanger; a shell-pass outlet of the heat exchanger is communicated with a feeding hole of a heating furnace; a discharge opening of the heating furnace is communicated with a feeding hole of a reactor; a discharge opening of the reactor is communicated with a shell-pass inlet of a reboiler at the bottom of a stabilizer; a shell-pass outlet of the reboiler at the bottom of the stabilizer is communicated with the shell-pass inlet of the heat exchanger; the shell-pass outlet of the heat exchanger is communicated with a feeding hole of a water cooler; a discharge opening of the water cooler is communicated with a feeding hole of a reaction product gas-liquid separator. Because the reaction product air cooler and other equipment in the conventional devices are removed or stopped operating, the coal amount of steam boilers is directly reduced, the energy is saved, and the production cost is reduced.
Description
Technical field
The utility model relates to liquefied gas processing unit (plant), particularly a kind of device with liquefied gas processing refining aromatic hydrocarbons.
Background technology
In Chemical Manufacture, the technique of liquefied gas processing used hydrocarbon processed has multiple.Mainly containing of generally adopting in industry is at present a kind of, first carry out raw materials pretreatment, methyl alcohol in raw material liquefied gas is removed from raw material water wash column, raw material washing overhead extraction cleaning raw material liquefied gas, incoming stock liquefied gas surge tank, through former material conveying pump, enter process furnace heating and enter reactor reaction, reaction product out enters knockout drum from reactor bottom, gas phase directly enters absorption Analytic Tower, reaction product liquid phase enters absorption Analytic Tower by reaction product liquid phase fresh feed pump, in absorbing Analytic Tower, remove after the dry gas in reaction product, enter again the separated poor alkene liquefied gas of stabilizer tower and BTX aromatics, BTX aromatics is isolated light aromatic hydrocarbons and heavy aromatics through de-heavy system again.As shown in Figure 1, the technique device used of above-mentioned liquefied gas processing hydrocarbon processed includes raw material water wash system, aromatization system, absorption resolution system, stable system and de-heavy system, raw material water wash column 2 bottoms are communicated with raw material washing tower bottom pump 1, raw material water wash column 2 discharge ports are communicated with raw material surge tank 3 opening for feeds, raw material surge tank 3 discharge ports are communicated with raw material fresh feed pump 4 opening for feeds, raw material fresh feed pump 4 discharge ports are communicated with interchanger 5 shell side entrances, heat exchanger shell pass 5 outlets are communicated with process furnace 6 opening for feeds, process furnace 6 discharge ports are communicated with reactor 7 opening for feeds, reactor 7 discharge ports are communicated with stable tower bottom reboiler 8 tube side entrances, stablizing tower bottom reboiler 8 tube side outlets is communicated with interchanger 5 tube side entrances, interchanger 5 tube side outlets are communicated with reaction product air cooler 9 opening for feeds, reaction product air cooler 9 discharge ports are communicated with water cooler 10 opening for feeds, water cooler 10 discharge ports are communicated with reaction product vapor-liquid separation tank 11 opening for feeds, the gaseous phase outlet of reaction product vapor-liquid separation tank 11 is communicated with absorption Analytic Tower 13 gas phase entrances, reaction product liquid phase fresh feed pump 12 opening for feeds, discharge port respectively with the liquid-phase outlet of reaction product vapor-liquid separation tank 11, absorbing Analytic Tower 13 liquid phase entrances is communicated with, absorbing Analytic Tower 13 gaseous phase outlets is communicated with variable valve 14 one end, variable valve 14 the other ends are communicated with fuel system, absorb and resolve column bottoms pump 18 opening for feeds, discharge port respectively with absorb Analytic Tower 13 outlet at bottoms, stabilizer tower charging the first preheater 19 shell side entrances are communicated with, stabilizer tower charging the first preheater 19 shell side outlets are communicated with stabilizer tower charging the second preheater 20 shell side entrances, stabilizer tower charging the second preheater 20 shell side outlets are communicated with stabilizer tower 21 opening for feeds, stabilizer tower 21 gaseous phase outlets are communicated with stable return tank of top of the tower 25 by air cooler 23, water cooler 24 successively, stablizing return tank of top of the tower 25 is communicated with variable valve 26 one end, variable valve 26 the other ends are communicated with fuel system, stablize tower top reflux pump 27 two ends and are communicated with stable return tank of top of the tower 26, stabilizer tower 21 respectively, stabilizer tower 21 outlet at bottoms are communicated with stabilizer tower charging the first preheater 19 tube side entrances, stablizing column bottoms pump 22 opening for feeds is communicated with stabilizer tower charging the first preheater 19 tube side outlets, absorb Analytic Tower 13 top charging product and be communicated with the discharge port of stable column bottoms pump 22, stabilizer tower charging the first preheater 19 tube side outlets and de-heavy system connectivity, absorb Analytic Tower 13 stage casings and absorb stage casing water cooler 15, a cooling loop of absorption stage casing pump 16 compositions, absorb Analytic Tower 13 bottoms and absorb a heating circuit of Analytic Tower tower bottom reboiler 17 compositions.The shortcoming that the processing process being formed by this device exists is that equipment and heat energy are had relatively high expectations, very high from reactor reaction product temperature out, need first to after reaction product cooling, enter again and absorb the separated dry gas of Analytic Tower, progressively heat up again and enter stable system, de-heavy system, thereby the method is harsh for heat condition, energy consumption is higher, device operation is inharmonious, absorbs resolution system equipment maintenance cost high.
Summary of the invention
It is few that the technical problem that the utility model solves is to provide a kind of equipment, save energy, easy handling, the device with liquefied gas processing refining aromatic hydrocarbons operating steadily.
Technical solutions of the utility model are done in such a way that a kind of device with liquefied gas processing refining aromatic hydrocarbons, include raw material water wash system, aromatization system, stable system, de-heavy system.
Described aromatization system includes raw material fresh feed pump, interchanger, process furnace, reactor, stablize tower bottom reboiler, water cooler, reaction product knockout drum, raw material water wash system discharge port is communicated with raw material fresh feed pump opening for feed, raw material fresh feed pump discharge port is communicated with heat exchanger shell pass entrance, heat exchanger shell pass outlet is communicated with furnace charge mouth, process furnace discharge port is communicated with reactor feed mouth, reactor discharge port is communicated with stable tower bottom reboiler tube side entrance, stablizing the outlet of tower bottom reboiler tube side is communicated with heat exchanger tube pass entrance, heat exchanger tube pass outlet is communicated with water cooler opening for feed, water cooler discharge port is communicated with reaction product knockout drum opening for feed.
Described raw material water wash system comprises raw material water wash column, raw material surge tank, and raw material surge tank opening for feed is communicated with raw material water wash column discharge port; Described raw material water wash system discharge port is raw material surge tank discharge port.
Described stable system includes stabilizer tower, stabilizer tower feed preheater, stablizes tower bottom reboiler, air cooler, water cooler, stablize return tank of top of the tower, variable valve; The gaseous phase outlet of reaction product vapor-liquid separation tank, liquid-phase outlet are communicated with stabilizer tower feed preheater shell side entrance, and the outlet of stabilizer tower feed preheater shell side is communicated with stabilizer tower opening for feed; Stabilizer tower gaseous phase outlet is communicated with stable return tank of top of the tower inlet mouth by air cooler, water cooler successively, stablizes return tank of top of the tower air outlet and is communicated with variable valve one end, and stabilizer tower outlet at bottom is communicated with stabilizer tower feed preheater tube side entrance; The variable valve the other end is communicated with fuel system, stablizes tower top reflux pump two ends and is communicated with stable return tank of top of the tower, stabilizer tower respectively.
Described stabilizer tower feed preheater is provided with two, and one is stabilizer tower charging the first preheater, and another is stabilizer tower charging the second preheater; The gaseous phase outlet of reaction product vapor-liquid separation tank, liquid-phase outlet are communicated with stabilizer tower charging the first preheater shell side entrance, stabilizer tower charging the first preheater shell side outlet is communicated with stabilizer tower charging the second preheater shell side entrance, stabilizer tower charging the second preheater shell side outlet is communicated with stabilizer tower opening for feed, and stabilizer tower outlet at bottom is communicated with stabilizer tower charging the first preheater tube side entrance.
Described stabilizer tower charging the first preheater tube side outlet and de-heavy system connectivity.
Described stabilizer tower feed preheater tube side outlet and de-heavy system connectivity.
Between described reactor discharge port and heat exchanger tube pass entrance, be provided with variable valve, variable valve two ends are communicated with reactor discharge port, heat exchanger tube pass entrance respectively.
Described stabilizer tower reflux pump opening for feed, discharge port are communicated with stable return tank of top of the tower, stabilizer tower inlet mouth respectively.
Technique effect of the present utility model is: due to the utility model by the reaction product air cooler in existing apparatus, reaction product liquid phase fresh feed pump, absorb Analytic Tower, absorb stage casing pump, stage casing water cooler, absorb and resolve column bottoms pump, stablize column bottoms pump, absorb that the equipment such as parsing tower bottom reboiler remove or out of service, directly reduced the coal consumption of steam boiler, when reducing, equipment also saved the energy, when bringing convenience to operation, also guaranteed operating steadily of device, produce qualified aromatic hydrocarbon product, reduced production cost.
Accompanying drawing explanation
Fig. 1 is the structural representation of prior art.
Fig. 2 is structural representation of the present utility model.
Embodiment
By reference to the accompanying drawings the utility model is described in further detail, as shown in Figure 2, a kind of device with liquefied gas processing refining aromatic hydrocarbons, includes raw material water wash system, aromatization system, stable system, de-heavy system.
Described raw material water wash system comprises raw material water wash column 2, raw material surge tank 3, and raw material surge tank 3 opening for feeds are communicated with raw material water wash column 2 discharge ports.
Described aromatization system includes raw material fresh feed pump 4, interchanger 5, process furnace 6, reactor 7, stablize tower bottom reboiler 8, water cooler 10, reaction product knockout drum 11, raw material surge tank 3 discharge ports are communicated with raw material fresh feed pump 4 opening for feeds, raw material fresh feed pump 4 discharge ports are communicated with interchanger 5 shell side entrances, interchanger 5 shell side outlets are communicated with process furnace 6 opening for feeds, process furnace 6 discharge ports are communicated with reactor 7 opening for feeds, reactor 7 discharge ports are communicated with stable tower bottom reboiler 8 tube side entrances, stablizing tower bottom reboiler 8 tube side outlets is communicated with interchanger 5 tube side entrances, interchanger 5 tube side outlets are communicated with water cooler 10 opening for feeds, water cooler 10 discharge ports are communicated with reaction product knockout drum 11 opening for feeds.
Described stable system includes stabilizer tower 21, stabilizer tower feed preheater, stablizes tower bottom reboiler 8, air cooler 23, water cooler 24, stablize return tank of top of the tower 25, variable valve 26; The gaseous phase outlet of reaction product vapor-liquid separation tank 11, liquid-phase outlet are communicated with stabilizer tower feed preheater shell side entrance, and the outlet of stabilizer tower feed preheater shell side is communicated with stabilizer tower 21 opening for feeds; Stabilizer tower 21 gaseous phase outlets are communicated with stable return tank of top of the tower 25 inlet mouths by air cooler 23, water cooler 24 successively, stablize return tank of top of the tower 25 air outlets and be communicated with variable valve 26 one end, stabilizer tower 21 outlet at bottoms are communicated with stabilizer tower feed preheater tube side entrance; Variable valve 26 the other ends are communicated with fuel system, stablize tower top reflux pump 27 two ends and are communicated with stable return tank of top of the tower 26, stabilizer tower 21 respectively.
Described stabilizer tower feed preheater is provided with two, and one is stabilizer tower charging the first preheater 19, and another is stabilizer tower charging the second preheater 20; The gaseous phase outlet of reaction product vapor-liquid separation tank 11, liquid-phase outlet are communicated with stabilizer tower charging the first preheater shell side 19 entrances, stabilizer tower charging the first preheater 19 shell side outlets are communicated with stabilizer tower charging the second preheater 20 shell side entrances, stabilizer tower charging the second preheater 20 shell side outlets are communicated with stabilizer tower 21 opening for feeds, and stabilizer tower 21 outlet at bottoms are communicated with stabilizer tower charging the first preheater 19 tube side entrances.
Described stabilizer tower charging the first preheater 19 tube side outlets and de-heavy system connectivity.
Described stabilizer tower feed preheater tube side outlet and de-heavy system connectivity.
Between described reactor 7 discharge ports and interchanger 5 tube side entrances, be provided with variable valve 28, variable valve 28 two ends are communicated with reactor 7 discharge ports, interchanger 5 tube side entrances respectively.
Described stabilizer tower reflux pump 27 opening for feeds, discharge port are communicated with stable return tank of top of the tower 25, stabilizer tower 21 inlet mouths respectively.
Incoming stock surge tank 3 after incoming stock water wash column 2 methanol removals of raw material liquefied gas, enters process furnace 6 through raw material fresh feed pump 4, interchanger 5; After process furnace 6 heating, enter in reactor 7 and react, under the effect of polymerization catalyst, in liquefied gas, C 4 olefin generation building-up reactions generates macromole hydrocarbon, because exothermic heat of reaction makes oil gas temperature, raise, reactor 7 discharge ports mixed oil and gas temperature is out at 300-395 ℃ simultaneously; High-temperature oil gas from reactor 7 discharge ports out, first give and stablize tower bottom reboiler 8 heating, then in interchanger 5 and the heat exchange of raw material liquefied gas, after water cooler 10 is cooling, enter reaction product vapor-liquid separation tank 11; From reaction product vapor-liquid separation tank 11 gas phase, liquid phase out, by self-pressure, through stabilizer tower charging the first preheater 19, stabilizer tower charging the second preheater 20, give stabilizer tower 21 feed; The poor alkene liquefied gas at stabilizer tower 21 tops with micro-dry gas from stabilizer tower 21 gaseous phase outlets out, through air cooler 23, water cooler 24, enter and stablize return tank of top of the tower 25, dry gas accumulates to while stablizing return tank of top of the tower 25 pressure high limit and opens variable valve 26 directly toward fuel system pressure release, the pressure that guarantees stable system is normal, and poor alkene liquefied gas quality is qualified; The BTX aromatics of separating from stabilizer tower 21 is through stabilizer tower charging the first preheater 19 self-pressures to weight-removing column charging, and BTX aromatics is isolated light aromatic hydrocarbons and heavy aromatics through de-heavy system again.
It should be noted that: the various device adopting in the utility model, be the conventional equipment using in the production technique of this area, and the operation of each equipment, parameter is all carried out according to routine operation.
Claims (8)
1. with liquefied gas, process the device of refining aromatic hydrocarbons for one kind, it is characterized in that: include raw material water wash system, aromatization system, stable system, de-heavy system, raw material water wash system discharge port is communicated with the raw material fresh feed pump opening for feed of aromatization system, the gaseous phase outlet of the reaction product vapor-liquid separation tank of aromatization system, liquid-phase outlet are communicated with the stabilizer tower feed preheater shell side entrance of stable system, the stabilizer tower feed preheater tube side outlet of stable system and de-heavy system connectivity.
2. a kind of device with liquefied gas processing refining aromatic hydrocarbons according to claim 1, it is characterized in that: described aromatization system includes raw material fresh feed pump, interchanger, process furnace, reactor, stablize tower bottom reboiler, water cooler, reaction product knockout drum, raw material water wash system discharge port is communicated with raw material fresh feed pump opening for feed, raw material fresh feed pump discharge port is communicated with heat exchanger shell pass entrance, heat exchanger shell pass outlet is communicated with furnace charge mouth, process furnace discharge port is communicated with reactor feed mouth, reactor discharge port is communicated with stable tower bottom reboiler tube side entrance, stablizing the outlet of tower bottom reboiler tube side is communicated with heat exchanger tube pass entrance, heat exchanger tube pass outlet is communicated with water cooler opening for feed, water cooler discharge port is communicated with reaction product knockout drum opening for feed.
3. a kind of device with liquefied gas processing refining aromatic hydrocarbons according to claim 2, it is characterized in that: described raw material water wash system comprises raw material water wash column, raw material surge tank, raw material surge tank opening for feed is communicated with raw material water wash column discharge port, and described raw material water wash system discharge port is raw material surge tank discharge port.
4. a kind of device with liquefied gas processing refining aromatic hydrocarbons according to claim 3, is characterized in that: described stable system includes stabilizer tower, stabilizer tower feed preheater, stablizes tower bottom reboiler, air cooler, water cooler, stablize return tank of top of the tower, variable valve; The gaseous phase outlet of reaction product vapor-liquid separation tank, liquid-phase outlet are communicated with stabilizer tower feed preheater shell side entrance, and the outlet of stabilizer tower feed preheater shell side is communicated with stabilizer tower opening for feed; Stabilizer tower gaseous phase outlet is communicated with stable return tank of top of the tower inlet mouth by air cooler, water cooler successively, stablizes return tank of top of the tower air outlet and is communicated with variable valve one end, and stabilizer tower outlet at bottom is communicated with stabilizer tower feed preheater tube side entrance; The variable valve the other end is communicated with fuel system, stablizes tower top reflux pump two ends and is communicated with stable return tank of top of the tower, stabilizer tower respectively.
5. a kind of device with liquefied gas processing refining aromatic hydrocarbons according to claim 4, is characterized in that: described stabilizer tower feed preheater is provided with two, and one is stabilizer tower charging the first preheater, and another is stabilizer tower charging the second preheater; The gaseous phase outlet of reaction product vapor-liquid separation tank, liquid-phase outlet are communicated with stabilizer tower charging the first preheater shell side entrance, stabilizer tower charging the first preheater shell side outlet is communicated with stabilizer tower charging the second preheater shell side entrance, stabilizer tower charging the second preheater shell side outlet is communicated with stabilizer tower opening for feed, and stabilizer tower outlet at bottom is communicated with stabilizer tower charging the first preheater tube side entrance.
6. a kind of device with liquefied gas processing refining aromatic hydrocarbons according to claim 5, is characterized in that: described stabilizer tower charging the first preheater tube side outlet and de-heavy system connectivity.
7. a kind of device with liquefied gas processing refining aromatic hydrocarbons according to claim 4, it is characterized in that: between described reactor discharge port and heat exchanger tube pass entrance, be provided with variable valve, variable valve two ends are communicated with reactor discharge port, heat exchanger tube pass entrance respectively.
8. according to a kind of device with liquefied gas processing refining aromatic hydrocarbons described in claim 4 or 5 or 6 or 7, it is characterized in that: described stabilizer tower reflux pump opening for feed, discharge port are communicated with stable return tank of top of the tower, stabilizer tower inlet mouth respectively.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320502518.6U CN203558986U (en) | 2013-08-18 | 2013-08-18 | Device for refining and machining aromatic hydrocarbons by using liquefied gas |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201320502518.6U CN203558986U (en) | 2013-08-18 | 2013-08-18 | Device for refining and machining aromatic hydrocarbons by using liquefied gas |
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| CN203558986U true CN203558986U (en) | 2014-04-23 |
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| CN201320502518.6U Expired - Fee Related CN203558986U (en) | 2013-08-18 | 2013-08-18 | Device for refining and machining aromatic hydrocarbons by using liquefied gas |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104152177A (en) * | 2014-08-19 | 2014-11-19 | 山东利丰达生物科技有限公司 | Aromatization method for liquefied gas |
| CN107523327A (en) * | 2017-09-15 | 2017-12-29 | 武汉凯顺石化科技有限公司 | The reuse means and method of C4 accessory substances obtained by a kind of gasoline production |
-
2013
- 2013-08-18 CN CN201320502518.6U patent/CN203558986U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104152177A (en) * | 2014-08-19 | 2014-11-19 | 山东利丰达生物科技有限公司 | Aromatization method for liquefied gas |
| CN104152177B (en) * | 2014-08-19 | 2016-03-16 | 山东利丰达生物科技有限公司 | A kind of method of liquefied gas through aromatization |
| CN107523327A (en) * | 2017-09-15 | 2017-12-29 | 武汉凯顺石化科技有限公司 | The reuse means and method of C4 accessory substances obtained by a kind of gasoline production |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20140423 Termination date: 20140818 |
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| EXPY | Termination of patent right or utility model |