CN105567286B - A kind of oil refining Vapor recovery unit method - Google Patents
A kind of oil refining Vapor recovery unit method Download PDFInfo
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- CN105567286B CN105567286B CN201410526737.7A CN201410526737A CN105567286B CN 105567286 B CN105567286 B CN 105567286B CN 201410526737 A CN201410526737 A CN 201410526737A CN 105567286 B CN105567286 B CN 105567286B
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Abstract
The invention discloses a kind of oil refining Vapor recovery unit methods.Including：1) enter absorption tower after the compressed cooling of refinery's rich gas, the tower reactor logistics on absorption tower is sent to desorber, and top gaseous phase is sent to reabsorber；2) it compresses and is sent to stripper after intersegmental gained lime set is collected, stripper overhead gas phase returns to suction port of compressor, and tower reactor liquid phase either produces or be sent to stabilizer as product；3) desorption column overhead obtains concentrate gas tower reactor liquid phase and is sent to stabilizer；4) reabsorber tower top obtains fuel gas, and tower reactor is rich re-absorption agent；5) stabilizer overhead extraction liquefied gas, tower reactor obtain stable gasoline, and a part returns to absorption tower as supplement absorbent, and a part is produced as product.The method of the present invention flow is simple, easy to operate, is built again without individually standby, you can obtains the concentrate gas rich in three component of carbon two and carbon.
Description
Technical field
The present invention relates to rich gas body recycling fields, further say, are to be related to a kind of oil refining Vapor recovery unit method.
Background technology
The rich gas body recycling that the fractionating columns such as country's oil plant catalytic cracking at present, delayed coking generate is mainly steady using absorbing
Determine system, flow is compressed raw material rich gas (0.6~1.6MPa) after cooling and separation, and gas and condensed oil respectively enter
Absorption tower.Absorption and desorption process is domestic at present, and there are two kinds of flows：A kind of flow is to carry out absorbing and another in a tower
Desorption is carried out in one tower, this flow domestic contrast is common.Another flow is that absorption and desorption are carried out in a tower
The top of flow, tower is absorber portion, and lower part is desorption section.Design at present more rare in this flow country.Two kinds of flows are all
Make absorbent with raw gasoline.Due to being unable to reach assimilation effect as absorbent by raw gasoline merely, stablize so must use
Gasoline is as supplement absorbent.Generally use adjusts the dosage of supplement absorbent to reach different assimilation effects.And it supplements
The dosage of absorbent also directly affects the vapour on absorption tower, liquid phase load.It absorbs tower top dry gas (or lean gas) and enters reabsorber
It is reabsorbed with light diesel fuel fraction, further to recycle heavy constituent therein, rich absorbent oil returns again to main fractionating tower.Dry gas from
Reabsorber liftout attachment.The gas absorbed by gasoline passes through desorption, enters stabilizer together with gasoline after abjection Cl, C2
To isolate C3, C4 liquid hydrocarbon fraction, a part for bottom of tower stable gasoline returns again to absorption tower and is used as absorbent.Another part goes out
Device.
It is dry gas that absorbing-stabilizing system, which recycles one of rich gas technique products obtained therefrom, is also contained in these dry gas more considerable
Three component of carbon two and carbon generally requires to recycle this part resource and builds dry-gas recovery device again, and investment is big.
Invention content
To solve the problems such as loss of two component of carbon is larger in absorbing-stabilizing system rich gas in the prior art, the present invention provides
A kind of oil refining Vapor recovery unit method.During recycling rich gas, to the carbon two and three component of carbon progress concentrate in rich gas.This hair
Bright method flow is simple, easy to operate, is built again without individually standby, you can obtains the concentrate gas rich in three component of carbon two and carbon.
An object of the present invention is to provide a kind of oil refining Vapor recovery unit method.
Including：
1) enter absorption tower after the compressed cooling of refinery's rich gas, absorbent enters at the top of absorption tower, absorbs in rich gas
C2 fractions and more heavy component；The tower reactor logistics on absorption tower is sent to desorber, and top gaseous phase is sent to reabsorber；The absorbent is
Raw gasoline；
2) it compresses and is sent to stripper after intersegmental gained lime set is collected, stripper overhead gas phase returns to suction port of compressor, tower reactor
Liquid phase either produces or is sent to stabilizer as product；
3) desorption column overhead obtains concentrate gas, is produced as product, and tower reactor liquid phase is sent to stabilizer；Re-absorption agent is light bavin
Oil or naphtha；
4) reabsorber tower top obtains fuel gas, and tower reactor is rich re-absorption agent；
5) stabilizer overhead extraction liquefied gas, tower reactor obtain stable gasoline, and a part returns to absorption tower and absorbed as supplement
Agent, a part are produced as product.
Wherein, preferably：
In step (1), rich gas compressed pressure in refinery's is stepped up to 3.0~4.5MPa；It is subsequently cooled to 25~50 DEG C
Enter absorption tower afterwards.
The compression is using two sections or three sections compressions.
In step (1), using cooling water cooling.
The number of theoretical plate of stripper is 5-40, operating pressure 1.0-3.0MPa；
Absorption tower Optimization Theory plate number is 15~60, and operating pressure is 2.0~4.5MPa, and tower top temperature is 30~50 DEG C；
The number of theoretical plate of the reabsorber is 10-50, operating pressure 1.0-4.0MPa；
The number of theoretical plate of desorber is 20-60, operating pressure 1.0-4.0MPa.
The present invention specifically includes following steps：
1) rich gas compressed pressure in refinery's is stepped up to 3.0~4.5MPa；It is subsequently cooled to 25~50 DEG C；
2) it compresses and is sent to stripper after intersegmental gained lime set is collected, stripper overhead gas phase returns to suction port of compressor, tower reactor
Liquid phase can be used as product to produce, can also be sent to stabilizer according to composition.
3) into absorption tower, absorbent enters rich gas after cooling at the top of absorption tower, absorbs C2 fractions in rich gas and more
Heavy component；The tower reactor logistics on absorption tower is sent to desorber, and top gaseous phase is sent to reabsorber；
4) logistics of desorber top gaseous phase is mainly the concentrate gas of carbon containing two and three component of carbon, is produced as product, tower reactor
Liquid phase is sent to stabilizer；
5) reabsorber top gaseous phase is the fuel gas containing components such as methane, hydrogen, can directly be discharged into fuel gas pipe network,
Tower reactor is rich re-absorption agent.
6) stablize column overhead and mainly produce liquefied gas, be one of the product of the present apparatus, tower reactor is stable gasoline, and a part is returned
Absorption tower is gone back to as absorbent, a part is produced as product.
Specific technical solution is as follows：
(1) it compresses：Refinery's rich gas pressure is increased to 3.0~4.5MPa；
(2) cooling：The compressed rich gas that the step 1) obtains is cooled to 25~50 DEG C；Rich gas warp after cooling
Gas-liquid separation, gas phase are sent to subsequent absorption tower, compress after intersegmental lime set is collected and introduce stripper.
(3) it strips：After gas-liquid separation, gas phase is sent to absorption tower to rich gas in cooling procedure after continuing cooling, and liquid phase is drawn
Enter stripper and carries out stripping processing.
(4) it absorbs：Absorbent enters at the top of absorption tower, absorbs C-2-fraction and more heavy component in rich gas；Absorption tower
Tower reactor logistics send to desorber processing；Gaseous overhead stream is sent to reabsorber；
(5) it desorbs：Tower reactor logistics from absorption tower enters desorber, and the lean solvent that tower reactor obtains is by cooling
Afterwards, stabilizer is sent to be handled；It is the concentrate gas rich in three component of carbon two and carbon that tower top, which obtains gas phase, is produced as product.
(6) it reabsorbs：Enter in reabsorber from the gaseous stream for absorbing tower top, the molten of entrainment is recycled with agent is reabsorbed
Agent, reabsorber tower top are fuel gas, are directly discharged into fuel gas pipe network, and tower reactor is rich re-absorption agent, is produced as product.
(7) stablize：Enter stabilizer, the production of overhead extraction liquefied gas from the logistics of desorber tower reactor and stripper tower reactor liquid phase
Product, tower reactor produce stable gasoline, and a portion returns to absorption tower and used as supplement absorbent, and another part is adopted as product
Go out.
In compression step, refinery's rich gas generally requires and improves pressure step by step, and preferably pressure is increased to 3.0~4.5MPa,
To the hop count of compression, there is no particular limitation, it is preferred to use two sections or three sections compressions；
In cooling step, refinery's rich gas is preferably cooled to 25~50 DEG C.Patent of the present invention absorbs for room temperature, energy consumption
It is low, to equipment also without particular/special requirement.It is preferred that being cooled down using cooling water.
In stripping step, method of the invention does not specially require stripping mode, can be according to producer's concrete condition
It determines.Gaseous stream after stripping returns to suction port of compressor, in the liquid phase after stripping, if the above group component of light dydrocarbon is less, and the liquid
The extraction of liquefied gas product is mutually can be used as, if the above component of light dydrocarbon is more, stabilizer is sent to and is further processed.
It is preferred that the number of theoretical plate of the stripper is 5-40, operating pressure 1.0-3.0MPa.
In absorption step, the absorbent uses raw gasoline.Since absorbent damages mistake from absorption tower tower top, so needing
It is supplemented, on the one hand supplement absorbent takes full advantage of resource using one of present apparatus products obtained therefrom stable gasoline, another
Aspect increases independence and the flexibility of device, saves investment.
In the method for the invention, absorbent dosage is not required particularly, those skilled in the art can be according to existing
There is the common sense of technology to determine.
The absorption tower Optimization Theory plate number is 15~60, and operating pressure is 2.0~4.5MPa, and tower top temperature is 40 DEG C of left sides
It is right.
The gaseous stream of the absorption tower tower top is sent to reabsorber.It reabsorbs agent from tower top to enter, absorbs and be carried over
Absorbent, reabsorber top gaseous phase are directly discharged into fuel gas pipe network, and tower reactor liquid phase is produced as product；The re-absorption agent is excellent
Select light diesel fuel, naphtha.
It is preferred that the number of theoretical plate of the reabsorber is 10-50, operating pressure 1.0-4.0MPa.
In desorption procedure, since there are pressure differences for pressure and the desorber of the tower reactor logistics from absorption tower, rely on
Pressure difference can enter desorber.Liquid phase after the desorption that desorber tower reactor obtains is sent to stabilizer and is handled after heat exchange, solution
It is concentrate gas to inhale column overhead extraction gas phase.
It is preferred that the number of theoretical plate of the desorber is 20-60, operating pressure 1.0-4.0MPa.
In stabilizing step, material enters in the middle part of tower, and by separation, tower top obtains liquefied gas product, and tower reactor is to stablize vapour
Oil product, part return to absorption tower and are used as absorbent, and part extraction is used as product.
It is preferred that the number of theoretical plate of the stabilizer is 20-60, operating pressure 0.5-4.0MPa.
If desired, the method for the present invention further includes dry and purifying step, dry and purifying step can be intersegmental in compression
It carries out, can also carry out after desorption, there is no particular limitation to the concrete technology condition of the step, those skilled in the art
Its concrete operations condition and method can be suitably determined according to other methods.
The oil refining Vapor recovery unit new process of the present invention has the characteristics that：
1) absorption stabilizing process for refining oil products obtained therefrom of the invention has fuel gas, concentrate gas, liquefied gas and stable gasoline, rich
Useful constituent in gas is fully recycled, and compare conventional suction systems stabilisation, is no longer needed to build device and be returned to dry gas
It receives, saves investment.
2) it is 40 DEG C or so that method of the invention, which absorbs temperature, belongs to room temperature absorption, low energy consumption, is wanted without special to equipment
It asks.
3) method using the present invention boosts to 3.0~4.5MPa to refinery's rich gas, larger due to boosting, compressed
Cheng Zhong, recombination therein segregates out, thus reduces the treating capacity on absorption tower, saves energy consumption.
4) it is one of present apparatus product to use present invention process, absorbent, not only takes full advantage of device product resource, also
Independence and the flexibility for increasing device, save investment.
Description of the drawings
Fig. 1 is the oil refining Vapor recovery unit method schematic diagram of the present invention.
Reference sign：
1 compression suction tank；2 compressors；3 heat exchangers；4 condensate strippers；5 absorption towers；6 desorbers；7 inhale again
Receive tower；8 stabilizers；9 refinery's rich gases；10 reabsorb agent；11 absorbents；12 fuel gas；13 rich re-absorption agent；14 concentrates
Gas；15 liquefied gas；16 stable gasolines.
Specific implementation mode
With reference to embodiment, further illustrate the present invention.
Embodiment：
As shown in Figure 1, including：Compressor 2, condensate stripper 4；Absorption tower 5, Analytic Tower 6, reabsorber 7；Stabilizer 8.
Rich gas compressed suction tank 1 in refinery's enters compressor, step by step adherence pressure.Suction tank tank bottom lime set is sent to lime set vapour
Stripper 4, tower top light component return to one section of compressor, and tower reactor liquid phase is sent to stabilizer and is further processed.Through compressor adherence pressure
Refinery's rich gas afterwards enters absorption tower 5, and 5 top gas of absorption tower passes through the absorbent of the recycling entrainment of reabsorber 7, absorption tower 5
Bottoms material enters desorber 6, and stabilizer 8, desorption are entered after collecting with stripping tower bottoms after the heat exchange of 6 tower reactor lean solvent of desorber
6 overhead extraction of tower is concentrate gas product, 8 overhead extraction liquefied gas product of stabilizer, tower reactor extraction stable gasoline product.
Refinery's rich gas composition is as shown in table 1,
Table 1
Refinery's rich gas composition is shown in Table 1, supplied materials 12000kg/h, and the raw gasoline absorbent used is 5500kg/h.
Include the following steps：
(1) it compresses：Refinery's rich gas is sent to compressibility, is compressed by two sections, and pressure rise to 3.8MPa is cooled to 40
DEG C enter absorption tower；
(2) lime set strips：Stripper number of theoretical plate is 10, operating pressure 1.5MPa.Lime set enters from tower top in tower,
Two or more light component of carbon, which is stripped out, returns to one section of compressor, and tower reactor lighter hydrocarbons main component is three or less heavy constituent of carbon, is sent to
Stabilizer is further processed.
(3) it absorbs：The number of theoretical plate on absorption tower is 39, operating pressure 3.6MPa, 42 DEG C of tower top temperature.Absorbent used
Enter in tower from absorbing tower jacking with the stable gasoline mixture from stabilizer tower reactor, absorbent for raw gasoline, rich gas is from
18 blocks of column plates enter.Carbon two and its heavy constituent in dry gas are got off by solvent absorption, are produced from tower reactor, send to desorber, absorb
Tower top is the light components such as methane, hydrogen, and is entrained with a small amount of absorbent, is sent into reabsorber.
(4) it desorbs：The number of theoretical plate of desorber is 30, operating pressure 2.85MPa, and feedboard is the 20th block of column plate.Solution
It is carbon two and carbon three to inhale column overhead gaseous products key component, is produced as concentrate gas product, and tower reactor liquid phase is sent to after heat exchange
Stabilizer.
(5) it reabsorbs：The number of theoretical plate of reabsorber is 12, operating pressure 1.0MPa.It reabsorbs agent and uses light diesel fuel,
Reabsorber tower top is fuel gas, is directly discharged into fuel gas pipe network, and tower reactor liquid phase is rich diesel oil, is produced as product.
(6) stablize：The number of theoretical plate of stabilizer is 38, operating pressure 1.0MPa, and feedboard is the 25th block of column plate.Stablize
Column overhead produces liquefied gas product, and tower reactor liquid phase is stable gasoline product, and part returns to absorption tower and used as absorbent, part
It is produced as product.
Obtained concentrate gas product is 1195kg/h, and composition is shown in Table 2.
Table 2
| Composition | Mol% |
| Carbon dioxide | 4.38 |
| Methane | 4.64 |
| Ethane | 18.14 |
| Ethylene | 31.55 |
| Propane | 5.30 |
| Propylene | 30.00 |
| Iso-butane | 3.21 |
| Normal butane | 0.22 |
| Butylene 1 | 1.59 |
| Anti- butylene 2 | 0.42 |
| Maleic 2 | 0.34 |
Obtained liquefied gas product is 6500kg/h, and composition is shown in Table 3.
Table 3
| Composition | Mol% |
| Ethane | 4.06 |
| Ethylene | 4.91 |
| Propane | 6.91 |
| Propylene | 31.90 |
| Iso-butane | 20.73 |
| Normal butane | 3.73 |
| Butylene 1 | 14.48 |
| Anti- butylene 2 | 7.13 |
| Maleic 2 | 5.21 |
Gained stable gasoline product is 7982kg/h, and composition is shown in Table 4.
Table 4
| Composition | Mol% |
| Normal butane | 0.11 |
| Butylene 1 | 0.04 |
| Anti- butylene 2 | 0.23 |
| Maleic 2 | 0.88 |
| Isopentane | 21.27 |
| Amylene | 20.80 |
| Gasoline | 56.65 |
Claims (4)
1. a kind of oil refining Vapor recovery unit method, it is characterised in that the method includes:
1) enter absorption tower after the compressed cooling of refinery's rich gas, absorbent enters at the top of absorption tower, and the C2 absorbed in rich gas evaporates
Point and more heavy component；The tower reactor logistics on absorption tower is sent to desorber, and top gaseous phase is sent to reabsorber；The absorbent is thick vapour
Oil；Rich gas compressed pressure in refinery's is stepped up to 3.0~4.5MPa；Enter absorption tower after being subsequently cooled to 25~50 DEG C；It inhales
Receipts tower operating pressure is 2.0~4.5MPa；
2) it compresses and is sent to stripper after intersegmental gained lime set is collected, stripper overhead gas phase returns to suction port of compressor, tower reactor liquid phase
Stabilizer is either produced or is sent to as product；
3) there are pressure differences with desorber for the pressure of the tower reactor logistics from absorption tower, enter desorber by pressure difference；Desorber tower
Top obtains concentrate gas, is produced as product, and tower reactor liquid phase is sent to stabilizer；
4) reabsorber tower top obtains fuel gas, and tower reactor is rich re-absorption agent；It is light diesel fuel or naphtha to reabsorb agent；
5) stabilizer overhead extraction liquefied gas, tower reactor obtain stable gasoline, and a part returns to absorption tower as supplement absorbent, and one
Part is produced as product.
2. oil refining Vapor recovery unit method as described in claim 1, it is characterised in that：
The compression is using two sections or three sections compressions.
3. oil refining Vapor recovery unit method as described in claim 1, it is characterised in that：
In step (1), using cooling water cooling.
4. the oil refining Vapor recovery unit method as described in one of claims 1 to 3, it is characterised in that：
The number of theoretical plate of stripper is 5-40, operating pressure 1.0-3.0MPa；
The number of theoretical plate on absorption tower is 15~60, and tower top temperature is 30~50 DEG C；
The number of theoretical plate of the reabsorber is 10-50, operating pressure 1.0-4.0MPa；
The number of theoretical plate of desorber is 20-60, operating pressure 1.0-4.0MPa；
The number of theoretical plate of the stabilizer is 20-60, operating pressure 0.5-4.0MPa.
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101063048A (en) * | 2006-04-27 | 2007-10-31 | 中国石油化工股份有限公司 | Method for separating plant catalytic dry gas by employing middle-cool-oil absorption process |
| CN101987983A (en) * | 2009-08-03 | 2011-03-23 | 中国石油化工股份有限公司 | Coking rich gas light dydrocarbon recovery method and device thereof |
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2014
- 2014-10-09 CN CN201410526737.7A patent/CN105567286B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101063048A (en) * | 2006-04-27 | 2007-10-31 | 中国石油化工股份有限公司 | Method for separating plant catalytic dry gas by employing middle-cool-oil absorption process |
| CN101987983A (en) * | 2009-08-03 | 2011-03-23 | 中国石油化工股份有限公司 | Coking rich gas light dydrocarbon recovery method and device thereof |
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