CN106147826B - A kind of bifilar feed process of tower of pyrolysis gasoline hydrogenation device decarburization five - Google Patents
A kind of bifilar feed process of tower of pyrolysis gasoline hydrogenation device decarburization five Download PDFInfo
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- CN106147826B CN106147826B CN201510176617.3A CN201510176617A CN106147826B CN 106147826 B CN106147826 B CN 106147826B CN 201510176617 A CN201510176617 A CN 201510176617A CN 106147826 B CN106147826 B CN 106147826B
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- pyrolysis gasoline
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Abstract
The invention discloses a kind of bifilar feed process of tower of pyrolysis gasoline hydrogenation device decarburization five.In the middle part of the tower of decarburization five and bottom sets charging aperture respectively；Quenching water column oil enters after cooling and standings are dehydrated from the tower bottom charging aperture of decarburization five；Debutanizing tower base oil enters from charging aperture in the middle part of the tower of decarburization five.The present invention reduces the tower bottom reboiler load of pyrolysis gasoline hydrogenation device decarburization five, energy-saving effect is notable, be advantageous to device capacity expansion revamping, the more debutanizing tower base oil of lighter hydrocarbons containing light dydrocarbon is not required to enter tank field standing in addition, decreases the air environmental pollution caused by tank field lighter hydrocarbons volatilize.
Description
Technical field
The present invention relates to drippolene light dydrocarbon separation field, further say, be to be related to a kind of pyrolysis gasoline hydrogenation device
The bifilar feed process of the tower of decarburization five.
Background technology
Drippolene is the accessory substance of preparing ethylene by steam cracking, consisting of light dydrocarbon does 205 DEG C to the cut of carbon more than nine
Left and right, the gasoline are rich in aromatic hydrocarbons, can be as high-knock rating gasoline or the raw material of aromatic device after hydrogenated.
Quenching water column and debutanizing tower of the drippolene in ethylene unit, the wherein gasoline fraction at debutanizing tower bottom with
It is not aqueous based on C5, C6, and the gasoline fraction that quenching water column is separated, based on C6+ components, C5 contents are considerably less, and contain
Water.Above-mentioned two strands of gasoline mixing, it is cooled to after normal temperature and sends out cracker battery limit (BL) as drippolene product, it is quiet first delivers to tank field
Dehydration is put, pyrolysis gasoline hydrogenation device is then sent into by tank field again.
In said process, cooling procedure is to reduce the speed of diene polymerization in drippolene, avoiding in equipment pipe
Middle coking, therefore the tower feeding temperature of decarburization five in pyrolysis gasoline hydrogenation device is generally not more than 60 DEG C of (most domestic cracking
The tower feeding temperature of gasoline hydrogenation device decarburization five is normal temperature, and this causes the tower reboiler of decarburization five higher)；Dehydration is to keep away
Exempt from water and enter hydrogenation reactor, cause catalyst inactivation.
However, debutanizing tower base oil is not aqueous, it may not be necessary to is dehydrated in tank field；Diene content in quenching water column oil is very
It is few, even if temperature, more than 100 DEG C, polymerization speed is also relatively slow, will not the coking in equipment pipe in the case that the residence time is short.But
After debutanizing tower base oil mixes with quenching water column oil, the debutanizing tower oil for causing to be dehydrated will also enter tank field standing, and de-
Volatile quantity is larger during lighter hydrocarbons in butane bottom of towe oil are stood in tank field, causes light hydrocarbon product loss and environmental pollution；Chilling
Water tower oil normal temperature enters the tower of decarburization five, adds the reboiler of the tower of decarburization five, and the Low Temperature Thermal in pyrolysis gasoline hydrogenation device
Lacking low temperature hot trap can not fully be recycled, and part Low Temperature Thermal can only be cooled down and dumped.
The content of the invention
To solve in the prior art the problem of Low Temperature Thermal can not make full use of, and device load is big, the invention provides one kind
The bifilar feed process of tower of pyrolysis gasoline hydrogenation device decarburization five.I.e. debutanizing tower base oil does not mix with quenching water column oil, Qian Zheyou
Ethylene unit cracking battery limit (BL) is fed directly to gasoline hydrogenation device, and tank field is delivered to after only the latter need to be cooled down and stands dehydration, so as to keep away
The volatilization loss during debutanizing tower base oil is stood in tank field is exempted from；Quenching water column oil utilizes gasoline hydrogenation before entering the tower of decarburization five
Low Temperature Thermal more than needed in device is preheated to higher temperature (such as 70~100 DEG C), avoids quenching water column oil cooling from being taken off caused by feeding
Light dydrocarbon tower reboiler is higher.
It is an object of the invention to provide a kind of bifilar feed process of tower of pyrolysis gasoline hydrogenation device decarburization five.
In the middle part of the tower of decarburization five and bottom sets charging aperture respectively；
Quenching water column oil enters after cooling and standings are dehydrated from the tower bottom charging aperture of decarburization five；
Debutanizing tower base oil enters from charging aperture in the middle part of the tower of decarburization five.
Wherein, preferably：
The bottom charging aperture is arranged in the middle part of the tower stripping section of decarburization five.
Quenching water column oil exchanges heat after cooling and standings are dehydrated with hydrogasoline to 70~100 DEG C of laggard towers of decarburization five.
Debutanizing tower base oil enters the tower of decarburization five at normal temperature or 60~110 DEG C.
The tower top pressure of decarburization five is 50kPag~100kPag, and column bottom temperature is 100~130 DEG C.
The present invention is achieved through the following technical solutions：
A kind of bifilar feeding process of tower of pyrolysis gasoline hydrogenation device decarburization five, wherein：(a) taken off in pyrolysis gasoline hydrogenation device
Two charging apertures are set on light dydrocarbon tower；(b) the tower feedstock oil of decarburization five in the feeding process is bifilar charging respectively from two
Individual charging aperture enters tower；(c) the bifilar charging in the tower feeding process of decarburization five, is to incorporate upstream ethylene unit and downstream cleavage vapour
The production of the oily covering device of hydrogenation plant two needs, i.e., upstream ethylene unit has at two (debutanizing tower and chilling water scrubber) output to split
Gasoline is solved, former flow send downstream cleavage gasoline hydrogenation device to be combined into one；(d) the bifilar feeding process optimizes upstream ethene
The drippolene product extraction scheme of device, reduces the drippolene reactor product cooler of upstream ethylene unit, and according to this two
The property of stock raw material, two bursts of chargings are set in the tower of decarburization five of pyrolysis gasoline hydrogenation device, while reduce upstream ethylene unit
The consumption of cooling water and the steam consumption of the tower of pyrolysis gasoline hydrogenation device decarburization five, meet ethylene industry device energy-conservation drop instantly
The target of consumption, this innovation to processing technology routine between ethylene unit and the covering device of pyrolysis gasoline hydrogenation device upstream and downstream two,
Linking between equipment and pipeline arrangement, all creative change.
Wherein two strands of feedstock oils are respectively debutanizing tower base oil (main component is light dydrocarbon, the cut of carbon six) and quenching water column oil
(main component is carbon six to the cut of carbon more than nine).After quenching water column oil is cooled to normal temperature, stands and be dehydrated into storage tank, stand
Quenching water column oil after dehydration is delivered to hydrogasoline preheater again, and the tower of decarburization five is delivered to after being preheated to 70~100 DEG C；And de- fourth
Alkane bottom of towe oil is then not required to stand into storage tank, can be fed directly to the tower of decarburization five.
Debutanizing tower base oil can directly or moderately cool down the laggard tower of decarburization five, and quenching water column oil exchanges heat to 70 with hydrogasoline
~100 DEG C of laggard towers of decarburization five.
Debutanizing tower base oil enters tower by being arranged on the charging aperture in the middle part of the tower of decarburization five, and quenching water column oil is by being arranged on decarburization five
The charging aperture of tower bottom enters tower.
Specifically：
The quenching water column oil of cracker is cooled to normal temperature, and wherein debutanizing tower base oil is fed directly to pyrolysis gasoline hydrogenation
Device, quenching water column oil enters after storage tank stands dehydration is delivered to pyrolysis gasoline hydrogenation device again.Pyrolysis gasoline hydrogenation device takes off
Light dydrocarbon tower sets two charging apertures, and one of charging aperture carries in the middle part of the tower of decarburization five, another charging aperture in the tower of decarburization five
Evaporate the middle part of section.Wherein charging aperture of the debutanizing tower base oil in the middle part of tower enters tower, and quenching water column oil is by entering in the middle part of tower stripping section
Material mouth enters tower.
The inventive method is suitable for the light dydrocarbon separating technology of pyrolysis gasoline hydrogenation device, such as separates work for following light dydrocarbons
Skill, the wherein tower top pressure of decarburization five are 50kPag~100kPag, and column bottom temperature is 100~130 DEG C.The present invention utilizes decarburization five
The bifilar feeding process of tower, the charging of the tower of decarburization five, which is divided into, need to stand dehydration, heatable quenching water column oil, and is not required to stand and takes off
This two bursts water, not heatable debutanizing tower base oil chargings, it is different from the mixed feeding technique of existing process.
Current pyrolysis gasoline hydrogenation device raw gasoline raw material is one compound, itself can not realize weight component point
Cut, therefore can not also realize that weight component sets two charging apertures on the tower of decarburization five.The present invention is bifilar using the tower of decarburization five
Feeding process, by the tower of decarburization five charging be divided into need to stand dehydration, heatable quenching water column oil, and be not required to stand be dehydrated, can not
This two bursts chargings of the debutanizing tower base oil of heating, it is different from the mixed feeding technique of existing process.
The present invention effect be：One side debutanizing tower base oil need not stand in tank field and be dehydrated, and reduce light dydrocarbon lighter hydrocarbons
Volatile emission, advantageously reduce the discharge of dusty gas；On the other hand heatable quenching water column oil is through exchanging heat to 70~100 DEG C
Enter tower again afterwards, the normal temperature charging of more former flow, greatly save the load of the tower bottom reboiler of decarburization five, reduce reboiler steam and disappear
Consumption；In addition, bifilar charging can reduce the gas-liquid phase load of the tower of decarburization five, in inlet amount under the same conditions, bifilar charging
Low the 11% of rectifying section liquid phase duty ratio sub-thread charging, be advantageous to the capacity expansion revamping of device.
Brief description of the drawings
Fig. 1 is the debutanizing tower base oil of prior art and the process chart of quenching water column oil mixed feeding；
Fig. 2 is the process chart of debutanizing tower base oil provided by the invention and the bifilar charging of quenching water column oil；
Reference is as follows：
1st, quenching water column；2nd, quenching water column oil cooler；3rd, basin；4th, debutanizing tower；5th, debutanizing tower base oil cooler；
6th, the tower feed exchanger of decarburization five；7th, the tower of decarburization five；8th, quenching water column oil；9th, drippolene after standing；10th, debutanizing tower bottom
Oil；11st, hydrogasoline；12nd, C5 fraction；13rd, the bottom of towe of decarburization five oil；A ethylene units battery limit (BL)；B pyrolysis gasoline hydrogenation devices circle
Area.
Embodiment
With reference to embodiment, the present invention is further illustrated.
Embodiment
As shown in Fig. 2 the debutanizing tower base oil 10 of ethylene unit battery limit (BL) is fed directly to taking off in pyrolysis gasoline hydrogenation device
Butane bottom of towe oil cooler 5 before light dydrocarbon tower, control temperature enter tower after 100 DEG C into the middle part charging aperture of five tower of decarburization 7；Chilling
Water tower oil 8 carries out standing dehydration, the quenching water column oil 9 after dehydration delivers to cracking again after the cooling of subcooler 2 into tank field 3
Gasoline hydrogenation device, and the hydrogasoline 11 first with high temperature before the tower 7 of decarburization five is entered carries out heat exchange 6, finally in the tower 7 of decarburization five
Charging aperture in the middle part of stripping section enters tower.
The tower top pressure of decarburization five is 90kpag, and column bottom temperature is 126 DEG C of quenching water column oil after cooling and standings are dehydrated and added
Hydrogen gasoline exchanges heat to 80 DEG C of laggard towers of decarburization five.
By taking the pyrolysis gasoline hydrogenation device of 700,000 tons/year of chemical plant as an example, illustrate the bifilar feeding process flow of the present invention.The dress
Put be 1,000,000 tons/year of ethylene crackers corollary apparatus, drippolene caused by preparing ethylene by steam cracking device is added
Hydrogen processing, the source of feedstock oil is oily for the debutanizing tower base oil and quenching water column of ethylene unit, the mass flow of this two strands of materials
Close, Main Ingredients and Appearance is that light dydrocarbon to C 9 fraction, feedstock oil composition is shown in Table 1.The device is midbarrel (C6~C8) hydrogenation stream
Journey, i.e. feedstock oil first pass through the tower of decarburization five and the tower of decarburization nine by more than light dydrocarbon and component of the carbon below nine is cut out, and only retain carbon six
Two-stage hydrogenation reaction is carried out to the component of carbon eight.
The pyrolysis gasoline hydrogenation device feedstock oil of table 1 forms, mol%
Comparative example
As shown in figure 1, debutanizing tower base oil and quenching water column oil through cooler are cooled to normal temperature after mixing, it is quiet to deliver to tank field
Dehydration is put, then delivers to pyrolysis gasoline hydrogenation device again, the tower of decarburization five is entered by charging aperture in the middle part of tower.
Following two problems be present in comparative example：1st, due to existing in debutanizing tower base oil containing more cyclopentadiene, the material
The condition of high temperature easily generates dicyclopentadiene or even coking, therefore feedstock oil feeding temperature can not too high (design feeding temperature be
60 DEG C), existing procedure is that normal temperature feeds (32 DEG C), and feeding temperature is relatively low to cause the tower bottom reboiler load of decarburization five higher, disappears more
Consume steam (under conditions of full production, reboiler 7.37MW)；2nd, due to debutanizing tower base oil lighter hydrocarbons containing light dydrocarbon compared with
It is more and not aqueous, during being mixed into tank field standing with quenching water column oil, on the one hand there are part light dydrocarbon lighter hydrocarbons to pass through storage tank breathing
Hole is evaporate into air, causes environmental pollution, is on the other hand also resulted in tank and is held unnecessary waste.
Embodiment is bifilar charging flow, and charging aperture is set up in the middle part of the tower stripping section of decarburization five.Debutanizing tower base oil appropriateness
The tower of decarburization five of the present apparatus is delivered to after cooling, tower is entered by charging aperture in the middle part of tower；Quenching water column oil still walks former stream in cracking battery limit (BL)
Journey, the present apparatus is delivered to after standing dehydration in tank field, higher temperatures (such as 113 DEG C) are warming up to hydrogasoline heat exchange, then by taking off
Charging aperture enters tower in the middle part of light dydrocarbon tower stripping section.
Application flow simulation softward Aspen Plus carry out flowsheeting to flow of the present invention, and result of calculation shows, use
The bifilar charging flow of the present invention, debutanizing tower base oil keeps (60 DEG C) chargings, and quenching water column oil can be preheated to 113 DEG C and enter
Material, and under conditions of the mass flow of two bursts of chargings keeps constant, the tower bottom reboiler load of decarburization five is down to 5.38MW, carries
Evaporate section liquid phase load also while have dropped 13.7%.And the flow after optimizing still keeps the separation accuracy of former flow, embodiment he
The overhead stream component of decarburization five of comparative example is shown in Table 2.
The embodiment of table 2 and the contrast of comparative example decarburization tower top stream components, mol%
Analyzed more than, after the bifilar charging flow using the present invention, the tower bottom reboiler of decarburization five can be reduced and born
Lotus 1.99MW, energy-conservation 27.0%.Stripping section liquid phase load declines 13.7%, and also implying that the tower of decarburization five can expand can compare accordingly
Example.In addition the more debutanizing tower base oil of lighter hydrocarbons containing light dydrocarbon is not required to enter tank field standing, decreases big caused by lighter hydrocarbons volatilize
Gas environmental pollution.
Claims (4)
- A kind of 1. bifilar feed process of tower of pyrolysis gasoline hydrogenation device decarburization five, it is characterised in that：In the middle part of the tower of decarburization five and bottom sets charging aperture respectively；Quenching water column oil enters after cooling and standings are dehydrated from the tower bottom charging aperture of decarburization five；Debutanizing tower base oil enters from charging aperture in the middle part of the tower of decarburization five；Wherein, quenching water column oil exchanges heat after cooling and standings are dehydrated with hydrogasoline to 70~100 DEG C of laggard towers of decarburization five.
- 2. the bifilar feed process of tower of pyrolysis gasoline hydrogenation device decarburization five as claimed in claim 1, it is characterised in that：The bottom charging aperture is arranged in the middle part of the tower stripping section of decarburization five.
- 3. the bifilar feed process of tower of pyrolysis gasoline hydrogenation device decarburization five as claimed in claim 1, it is characterised in that：Debutanizing tower base oil enters the tower of decarburization five at normal temperature or 60~110 DEG C.
- 4. the bifilar feed process of tower of pyrolysis gasoline hydrogenation device decarburization five as described in one of claims 1 to 3, its feature exist In：The tower top pressure of decarburization five is 50kPag~100kPag, and column bottom temperature is 100~130 DEG C.
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| CN101172923A (en) * | 2006-10-31 | 2008-05-07 | 中国石油化工股份有限公司 | Combination technique for producing olefin hydrocarbon with mixed C_4 |
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| WO2012004809A1 (en) * | 2010-07-08 | 2012-01-12 | Indian Oil Corporation Ltd. | Two stage fluid catalytic cracking process and apparatus |
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| CN101172923A (en) * | 2006-10-31 | 2008-05-07 | 中国石油化工股份有限公司 | Combination technique for producing olefin hydrocarbon with mixed C_4 |
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