CN104560115B - Absorbing-stabilizing system and its workflow and application and a kind of method for preparing stable gasoline - Google Patents
Absorbing-stabilizing system and its workflow and application and a kind of method for preparing stable gasoline Download PDFInfo
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- CN104560115B CN104560115B CN201310499508.6A CN201310499508A CN104560115B CN 104560115 B CN104560115 B CN 104560115B CN 201310499508 A CN201310499508 A CN 201310499508A CN 104560115 B CN104560115 B CN 104560115B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
- C10G7/02—Stabilising gasoline by removing gases by fractioning
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
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Abstract
The invention provides absorbing-stabilizing system and its workflow and application and a kind of method for preparing stable gasoline, the workflow includes：Gas-liquid separator is set between stabilizer feed exchanger and stabilizer；Gas phase import is set above stabilizer original charging aperture, the gas phase import is connected with gas-liquid separator；The gas phase oil product of gas-liquid separator then continues to be pressed into stabilizer certainly by former charging aperture along existing procedure by gas phase import from stabilizer, the liquid phase oil product of gas-liquid separator is pressed into.The workflow can reduce the cold reflux amount of stabilizer, and tower top cools down load and bottom of towe boils load again to help it to reduce, meanwhile, the cushioning effect of gas-liquid separator also helps the operation of steady stabilizer.
Description
Technical field
The invention belongs to PETROLEUM PROCESSING field, more particularly to one kind realizes Vapor recovery unit by changing stabilizer feeding manner
The new technological process of system energy consumption reduction, and a kind of absorbing-stabilizing system and its application and a kind of method for preparing stable gasoline.
Background technology
The important composition of the crude oil secondary operation device such as absorbing-stabilizing system is catalytic cracking, delayed coking, be hydrocracked
Part, mainly by rich gas compressor, condensing oil tank, absorption tower, desorber, stabilizer, reabsorber and corresponding cold exchange device
Composition, its effect is using the rich gas and raw gasoline absorbed with the method autonomous fractionating column system in future of rectifying（Or crude naphtha）
It is separated into dry gas, liquid hydrocarbon and the qualified stable gasoline of vapour pressure（Or naphtha）.
Because the arrangement of absorption and desorption is different, Vapor recovery unit generally has two kinds of flows of single column and double tower.Single column flow collection
Absorb, desorb in a tower, and double-column process is then divided among being completed in two towers, thus than single column flow, with more preferable
Absorption and desorption effect, using more.
In double-column process（See Fig. 1）, from main fractionating tower tower top catch pot, rich in liquid hydrocarbon（LPG）With gasoline group
The rich gas for dividing first is compressed to authorized pressure through compressor, then through cooling down into condensing oil tank, isolates gas phase and liquid phase.Then, gas
Absorption tower is mutually sent, by raw gasoline and stable gasoline（Also known as supplement absorbent）Remove C therein3 +Component, phase is obtained from tower top
To the lean gas of " more dry ", and it is rich in C3 +The rich absorbent oil of component is then extracted out by bottom of towe and delivers to condensing oil tank.Absorption tower operation temperature
Lower, assimilation effect is better, therefore generally sets two or a water recirculator at middle part, to take heat of solution away in time, dimension
Hold absorption tower lower temperature operation.Self-absorption tower top lean gas out goes reabsorber bottom of towe from pressure, by the product that adverse current is downward
Diesel oil further absorbs, to obtain C3 +Constituent content is less than 3%（mol）Product dry gas, and bottom of towe richness diesel oil then return to main fractionation
Tower freshening.The effect of desorber T302 is then that in the presence of bottom of towe again boiling hot amount, will be dissolved in the C in condensed oil2Component solution
Sucking out, and stripping gas is drawn through into condensing oil tank by tower top send absorption tower to enter next circulation；Bottom of towe deethanization gasoline
Then it is pumped up to stabilizer, LPG products is separated in tower top, bottom of towe obtains stable gasoline.
In above-mentioned flow, desorber base oil is that deethanization gasoline is extracted out through stabilizer feed pump P304/1-2 and boosts laggard
Deethanization gasoline~heat exchanger the E305 of stable gasoline No. a time, send stabilizer T304 after heated intensification.This flow exists following
Defect：Deethanization gasoline is extracted out with bubble point temperature by desorber bottom, though be suitably pressurized through pump, still a large amount of vaporizations after heat exchange, i.e.,
Equivalent to once balance flash distillation or gas-liquid separation is completed in heat exchanger, if gas-liquid two-phase is also jointly into the same of stabilizer
One block of column plate, is equivalent to self deny current separating-purifying；In other words, it is equivalent to reduce one piece of reason of stabilizer
By plate, and have to increase cold reflux amount as making up, this tower top cooling load and bottom of towe that will improve stabilizer boil negative again
Lotus.
The content of the invention
It is an object of the invention in overcoming existing absorbing-stabilizing system flow, self deny deethanization gasoline~stabilization vapour
An oily gasification separation effect for heat exchanger, and increase the defect of stabilizer energy consumption, there is provided one kind is entered by changing stabilizer
Material mode realizes the absorbing-stabilizing system new technological process of stabilizer energy consumption reduction.
To achieve these goals, the present invention provides a kind of workflow of absorbing-stabilizing system, wherein, the workflow
Including：
Gas-liquid separator is set between stabilizer feed exchanger and stabilizer；
Gas phase import is set above stabilizer original charging aperture, the gas phase import is connected with gas-liquid separator；
, by gas-phase feed mouthful from stabilizer is pressed into, the liquid phase oil product of gas-liquid separator is then for the gas phase oil product of gas-liquid separator
Continue to be pressed into stabilizer certainly by the former charging aperture of stabilizer along existing procedure.
The present invention also provides a kind of absorbing-stabilizing system, and the absorbing-stabilizing system includes：Stabilizer and stabilizer charging are changed
Hot device, the stabilizer includes fluid inlet, wherein, the absorbing-stabilizing system also includes：Gas-liquid separator, and the stabilizer
Also include：Gas phase import, the gas phase import is located at the top of stabilizer, and the gas-liquid separator is arranged on stabilizer charging and changes
Between hot device and stabilizer, and gaseous phase outlet and the stabilizer of gas-liquid separator gas phase inlet communication, the liquid of gas-liquid separator
Mutually outlet is connected with the fluid inlet of stabilizer.
The present invention provides absorbing-stabilizing system of the present invention and is split in catalytic cracking unit, delayed coking unit and hydrogenation
Disguise the application in putting.
The present invention also provides a kind of method for preparing stable gasoline, and the method is carried out in above-mentioned absorbing-stabilizing system,
The method includes：
（1）Deethanization gasoline is heated in stabilizer feed exchanger, subsequently into carrying out gas-liquid in gas-liquid separator
Separate；
（2）The gas that gas-liquid separation is obtained feeds to the gas phase import of stabilizer from the gaseous phase outlet of gas-liquid separator,
The liquid that gas-liquid separation is obtained feeds to the fluid inlet of stabilizer from the liquid-phase outlet of gas-liquid separator, from the tower of stabilizer
Bottom obtains stable gasoline.
The workflow that the present invention is provided, by setting up charging gas-liquid separator, and by equilibrium flash in gas-liquid separator
The phase materials of air-liquid two be respectively fed to the different tray locations of stabilizer and realize.The master arranges due to steady equivalent to increased
Determine one piece of theoretical plate of tower, so as to reduce the cold reflux amount of stabilizer, then help it to reduce tower top cooling load and bottom of towe
Load is boiled again.Meanwhile, the cushioning effect of gas-liquid separator also helps the operation of steady stabilizer.
Other features and advantages of the present invention will be described in detail in subsequent specific embodiment part.
Brief description of the drawings
Fig. 1 is the workflow of the absorbing-stabilizing system of prior art；
Fig. 2 is a kind of workflow of absorbing-stabilizing system preferred embodiment of the invention.
Specific embodiment
Specific embodiment of the invention is described in detail below.It should be appreciated that described herein specific
Implementation method is merely to illustrate and explain the present invention, and is not intended to limit the invention.
The present invention provides a kind of workflow of absorbing-stabilizing system, wherein, the workflow includes：
Gas-liquid separator is set between stabilizer feed exchanger and stabilizer；
Gas phase import is set above stabilizer original charging aperture, the gas phase import is connected with gas-liquid separator；
The gas phase oil product of gas-liquid separator by gas phase import from being pressed into stabilizer, the liquid phase oil product of gas-liquid separator then after
It is continuous that stabilizer is pressed into by the former charging aperture of stabilizer certainly along existing procedure.
Technical terms used is in case of no particular description according to the common version of this area in the present invention.
In the present invention, gas-liquid separator is fed by stabilizer air-liquid two-phase is respectively fed to stabilizer difference column plate position
Put, to reduce stabilizer energy consumption.Further, since there is provided gas-liquid separator and by gas phase send into stabilizer compared with upper position, make
Obtain in feed exchanger, the flow pressure drop of deethanization gasoline will be reduced substantially, so as to be more beneficial for the deethanization vapour that gasifies and reduce
The energy consumption of oily drawing pump；Meanwhile, the pooling feature of gas-liquid separator feeds stabilization, particularly gas-phase feed, and helps stabilization
The more stable operation of tower.
In the present invention, due to being provided with gas-liquid separator, and by flashed vapour feeding stabilizer compared with upper position, in turn
Gasification of the deethanization gasoline in heat exchanger is more enhanced, while being beneficial to stablize the charging of stabilizer.
In the present invention, the operating pressure of gas-liquid separator can be adjusted according to practical condition, under preferable case,
Operating pressure is set in 1-2MPa.
In the present invention, the tray location that gas phase import is set in stabilizer can be adjusted according to practical condition
Whole, under preferable case, the tray location that gas phase import is set in stabilizer is located at stabilizer original charging aperture top 29-31 blocks
Plate.
In the present invention, gas phase import is set above stabilizer original charging aperture, while the position of fluid inlet can be adjusted,
Generally, stabilizer is provided with three pieces of feedboards, with adjustment elasticity.Under preferable case, the liquid phase oil product of gas-liquid separator then continues
Pass through former charging aperture from 18-20,22-24 and 26-28 the block plate for being pressed into stabilizer along existing procedure.
In the present invention, absorbing-stabilizing system can be catalytic cracking unit, delayed coking unit, hydrocracking unit
Absorbing-stabilizing system.
In the present invention, absorbing-stabilizing system can include：Rich gas compressor, condensing oil tank, absorption tower, the solution being connected
Inhale tower, stabilizer and reabsorber.
The workflow of the absorbing-stabilizing system that the present invention is provided is generally based on following principle：
1st, make use of the gasification function of feed exchanger.By setting up gas-liquid separator, and air-liquid two-phase is respectively fed to
Stabilizer, so as to equivalent to increased one piece of stabilizer theoretical plate.So that, under conditions of maintaining product quality constant,
The cold reflux amount of stabilizer can be reduced, helps to reduce its energy consumption；
2nd, flow pressure drop of the deethanization gasoline in feed exchanger is reduced, heat transfer effect is improved, helps improve
The rate of gasification of deethanization gasoline；
3rd, the charging of stabilizer, particularly gas-phase feed are stabilized, the operation to stablizing stabilizer is favourable.
The present invention also provides a kind of absorbing-stabilizing system, and the absorbing-stabilizing system includes：Stabilizer and stabilizer charging are changed
Hot device, the stabilizer includes fluid inlet, wherein, the absorbing-stabilizing system also includes：Gas-liquid separator, and the stabilizer
Also include：Gas phase import, the gas phase import is located at the top of stabilizer, and the gas-liquid separator is arranged on stabilizer charging and changes
Between hot device and stabilizer, and gaseous phase outlet and the stabilizer of gas-liquid separator gas phase inlet communication, the liquid of gas-liquid separator
Mutually outlet is connected with the fluid inlet of stabilizer.
In the present invention, the fluid inlet of stabilizer is generally the charging aperture of original stabilizer.Certainly, according to needs, its position
Putting to adjust, and operates for convenience, and the fluid inlet of preferably described stabilizer is generally the charging aperture of original stabilizer.
In the present invention, the tray location of the gas phase import can be adjusted according to practical condition, be preferably placed at
29-31 block column plates above stabilizer fluid inlet.
The tray location of wherein fluid inlet is general at 19-27 block column plates.
In the present invention, absorbing-stabilizing system can also include：Desorber, liquid-phase outlet and the stabilizer of the desorber enter
Material heat exchanger connection.Stabilizer feed exchanger is fed into such that it is able to be provided by desorber.This is those skilled in the art
It is known, it is not described here in detail.
In the present invention, absorbing-stabilizing system can also include：Rich gas compressor, condensing oil tank, absorption tower and reabsorber,
Wherein, the annexation of rich gas compressor, condensing oil tank, absorption tower and reabsorber can be carried out according to prior art, this hair
It is bright to this without particular/special requirement.
It is of the invention it is a kind of preferred embodiment, the outlet of preferably described rich gas compressor and entering for condensing oil tank
Material mouth is connected, and the gaseous phase outlet of the condensing oil tank connects with the charging aperture on absorption tower, the liquid-phase outlet of the condensing oil tank and
The charging aperture connection of desorber, the gaseous phase outlet of the desorber and the inlet communication of rich gas compressor, the gas on the absorption tower
Mutually export the inlet communication with reabsorber.
The present invention also provides above-mentioned absorbing-stabilizing system in catalytic cracking unit, delayed coking unit and is hydrocracked dress
Application in putting.Absorbing-stabilizing system of the invention is used in catalytic cracking unit, delayed coking unit and hydrocracking unit
Being capable of effective energy-conservation.
The present invention also provides a kind of method for preparing stable gasoline, and the method is carried out in above-mentioned absorbing-stabilizing system, should
Method includes：
（1）Deethanization gasoline is heated in stabilizer feed exchanger, subsequently into carrying out gas-liquid in gas-liquid separator
Separate；
（2）The gas that gas-liquid separation is obtained feeds to the gas phase import of stabilizer from the gaseous phase outlet of gas-liquid separator,
The liquid that gas-liquid separation is obtained feeds to the fluid inlet of stabilizer from the liquid-phase outlet of gas-liquid separator, from the tower of stabilizer
Bottom obtains stable gasoline.
In the present invention, the operating pressure of gas-liquid separator can be adjusted according to practical condition, be preferably set to
1-2MPa。
In the present invention, deethanization gasoline stocks can be obtained according to prior art, for example, can obtain as follows：
（a）Rich gas is compressed in rich gas compressor, compressed oil is obtained；
（b）Compressed oil is carried out in condensing oil tank condensing, obtain condensed oil and gas；
（c）Condensed oil feeding desorber is desorbed, deethanization gasoline is obtained.
In the present invention, the method also includes：By step（b）Gained gas sequentially passes through absorption tower and is absorbed, Ran Houjin
Enter reabsorber to be reabsorbed, dry gas is obtained from the tower top of reabsorber.
The present invention essentially consists in and gas-liquid separator is increased in the absorbing-stabilizing system of prior art, and on stabilizer
Gas phase import is additionally arranged, the gas phase import is located at the top of stabilizer, and the gas-liquid separator is arranged on stabilizer charging and changes
Between hot device and stabilizer, and gaseous phase outlet and the stabilizer of gas-liquid separator gas phase inlet communication, the liquid of gas-liquid separator
Mutually outlet is connected with the fluid inlet of stabilizer.Other and prior art all same.
Based on preceding solution, the present invention has the following advantages that and effect compared with the prior art：
1st, increase that equipment is few, flow simple, either grassroot project or transformation project, are easy to implement；
2nd, the feed operation of steady stabilizer is conducive to；
3rd, the pressure drop of deethanization gasoline drawing pump is advantageously reduced；
4th, the cold reflux amount of stabilizer is reduced, load is boiled again so as to reduce tower top cooling load and bottom of towe；
5th, any influence is not constituted on the product yield and product quality of stablizing Tower System.
With reference to embodiment, comparative example and accompanying drawing, the present invention is described in detail, but the implementation method of invention is not limited to
This.
Comparative example
Comparative example is used for the workflow of the absorbing-stabilizing system for illustrating prior art
As shown in figure 1, deethanization gasoline（121.8℃、1.26MPag、96.50t/h）Through desorber T302 base oil pumps
P304/1-2 pressure-raisings enter stabilizer T304 feed exchangers i.e. deethanization gasoline~heat exchanger of stable gasoline No. a time to 1.8MPag
The shell side of E305, by the stable gasoline from stabilizer bottom of towe once（176.4℃、80.40t/h）It is heated to 130.3 DEG C（Correspondence
Pressure 1.15MPa, the effective heat duty of quality rate of gasification 11.11%, E305 are 118 × 104kcal/h）Enter stabilizer the 27th,
23rd, 19 blocks of column plates.Now, stabilization tower top operating pressure 1.10MPa, 61.3 DEG C of temperature, do cooling medium, by tower using recirculated water
Top oil gas is cooled to 47.7 DEG C and enters tower top point flow container V302, and correspondence cold reflux amount 55.84t/h, tower top cooling load 565.9 ×
104kcal/h；176.4 DEG C of column bottom temperature, using in main fractionating tower one once（241℃、1.4MPa、200t/h）Do again boiling hot
Source, it is 655.2 × 10 that correspondence boils effective heat duty again4kcal/h.Stable gasoline once heat after deethanization gasoline 154.3 DEG C from
E305 out, then enters E304/1-2 tube sides heating condensed oil.
Embodiment
Embodiment is used to illustrate the workflow that the present invention provides absorbing-stabilizing system
As shown in Fig. 2 comparing the following improvement of comparative example flow implementation：
1st, enter in deethanization gasoline~be additionally arranged stabilizer between stable gasoline No. a time heat exchanger E305 and stabilizer T304
Material knockout drum（Numbering VN1）, and the operating pressure of VN1 is set in 1.15MPa.
2nd, it is new at the 30th block of plate above stabilizer original charging aperture to have opened gas-phase feed mouthful；
3rd, it is provided with connection the 30th piece of gas-phase feed line of plate of VN1 and stabilizer；
4th, VN1 liquid phases are pressed into the 23rd block of plate of stabilizer certainly.
Concrete operations are：Deethanization gasoline（121.8℃、1.26MPag、96.50t/h）Through desorber T302 base oil pumps
P304/1-2 pressure-raisings enter stabilizer T304 feed exchangers i.e. deethanization gasoline~heat exchanger of stable gasoline No. a time to 1.8MPag
The shell side of E305, by the stable gasoline from stabilizer bottom of towe once（176.4℃、80.40t/h）It is heated to 130.3 DEG C（Correspondence
The effective heat duty that pressure is 1.15MPa, quality rate of gasification is 11.11%, E305 is 118 × 104kcal/h）Enter newly-increased steady
Determine tower charging knockout drum VN1.The operating pressure of VN1 is set in 1.15MPa, by equilibrium flash, lightens gas phase 10.96t/
H, is pressed into the 30th block of column plate of stabilizer certainly, and extraction raffinate 85.53t/h is then pressed into the 23rd block of column plate of stabilizer certainly.Now, stabilization column overhead
61.4 DEG C of pressure 1.10MPa, temperature, cooling medium is done using recirculated water, overhead oil air cooling is entered into tower top to 47.7 DEG C and divides liquid
Tank V302, correspondence cold reflux amount 47.37t/h（Change preceding 55.84t/h）, tower top cooling load 499.4 × 104kcal/h（Before changing
565.9×104kcal/h）；176.4 DEG C of bottom of towe, using in main fractionating tower one once（241 DEG C, 1.4MPa, 200t/h）Do and boil again
Thermal source, effectively boiling hot load is 585.6 × 10 again4kcal/h（Change preceding 655.2 × 104kcal/h）.Stable gasoline once heats de-
154.3 DEG C out, are then entered tube side heating condensed oil from E305 after ethane gasoline.
After the present embodiment, absorbing-stabilizing system operational circumstances and effect are as follows：
1st, the effective boiling hot load 69.6 × 10 again in stabilizer bottom is saved4Kcal/h, presses equivalent to reducing in about 1.2t/h
The equivalent energy consumption of steam, therefore whole catalytic unit energy consumption 105.6kg marks oil/h is reduced, folding 1.0kg mark oil/t raw materials；By middle pressure
300 yuan/t of steam is calculated, and saves yuan/hour of operating cost 360, rolls over 302.4 ten thousand yuan/year（Device year went into operation based on 8400 hours
Calculate, similarly hereinafter）；
2nd, stabilization tower top cooling load 66.5 × 10 is reduced4Kcal/h, it is corresponding to reduce the circulation water consumption of device equivalent
83.1t/h（The recirculated water temperature difference takes 8 DEG C）, therefore whole catalytic unit energy consumption 8.31kg marks oil/h is reduced, folding 0.08kg marks oil/t
Raw material；By recirculated water unit price, 0.3 yuan/ton calculates, cost-effective 24.9 yuan/when, roll over 20.94 ten thousand yuan/year；
3rd, new technological process is identical with comparative example flow material balance, product quality is constant.
To sum up, the embodiment of the present invention ensure absorbing-stabilizing system product quality and yield it is constant on the premise of, by changing
Tower feeding manner is stabilized, stabilizer system energy consumption 113.9kg mark oil/h is reduced, therefore reduce whole catalytic unit energy consumption
1.08kg mark oil/t raw materials, realize 384.9 yuan of energy-saving benefit/when, roll over 323.34 ten thousand yuan/year.
Above-described embodiment is detailed embodiment of the invention, but embodiments of the present invention are not by above-described embodiment
Limitation, other it is any without departing from Spirit Essence of the invention and the change, modification, replacement made under principle, combine, simplification,
Equivalent substitute mode is should be, is included within protection scope of the present invention.
Claims (15)
1. a kind of workflow of absorbing-stabilizing system, it is characterised in that the workflow includes：
Gas-liquid separator is set between stabilizer feed exchanger and stabilizer；
Gas phase import is set above stabilizer original charging aperture, the gas phase import is connected with gas-liquid separator；
By gas phase import from stabilizer is pressed into, the liquid phase oil product of gas-liquid separator then continues edge to the gas phase oil product of gas-liquid separator
Existing procedure is pressed into stabilizer certainly by the former charging aperture of stabilizer.
2. workflow according to claim 1, wherein, the operating pressure of gas-liquid separator is set in 1-2MPa.
3. workflow according to claim 1, wherein, the tray location of the gas phase import is located at the of stabilizer
29-31 block plates.
4. the workflow according to any one in claim 1-3, wherein, the liquid phase oil product of gas-liquid separator then continues
It is pressed into 18-20,22-24 and 26-28 block plate of stabilizer certainly by the former charging aperture of stabilizer along existing procedure.
5. the workflow according to any one in claim 1-3, wherein, the absorbing-stabilizing system is catalytic cracking
The absorbing-stabilizing system of device, delayed coking unit or hydrocracking unit.
6. the workflow according to any one in claim 1-3, wherein, the absorbing-stabilizing system includes：It is connected
Logical rich gas compressor, condensing oil tank, absorption tower, desorber, stabilizer and reabsorber.
7. a kind of absorbing-stabilizing system, the absorbing-stabilizing system includes：Stabilizer and stabilizer feed exchanger, the stabilizer
Including fluid inlet, it is characterised in that the absorbing-stabilizing system also includes：Gas-liquid separator, and the stabilizer also includes：Gas
Phase import, the gas phase import be located at stabilizer top, the gas-liquid separator be arranged on stabilizer feed exchanger with it is steady
Determine between tower, and gaseous phase outlet and the stabilizer of gas-liquid separator gas phase inlet communication, the liquid-phase outlet of gas-liquid separator with
The fluid inlet connection of stabilizer.
8. absorbing-stabilizing system according to claim 7, wherein, the tray location of the gas phase import is located at stabilizer
29-31 block column plates.
9. absorbing-stabilizing system according to claim 7, wherein, the absorbing-stabilizing system also includes：Desorber, the solution
The liquid-phase outlet for inhaling tower is connected with stabilizer feed exchanger.
10. absorbing-stabilizing system according to claim 9, wherein, the absorbing-stabilizing system also includes：Rich gas compressor,
Condensing oil tank, absorption tower and reabsorber, the outlet of the rich gas compressor are connected with the charging aperture of condensing oil tank, described condensing
The gaseous phase outlet of oil tank is connected with the charging aperture on absorption tower, and the liquid-phase outlet of the condensing oil tank connects with the charging aperture of desorber
It is logical, the gaseous phase outlet of the desorber and the inlet communication of rich gas compressor, the gaseous phase outlet and reabsorber on the absorption tower
Inlet communication.
Absorbing-stabilizing system in 11. claim 7-10 described in any one catalytic cracking unit, delayed coking unit and
Application in hydrocracking unit.
A kind of 12. methods for preparing stable gasoline, Vapor recovery unit system of the method in the claim 7-10 described in any one
Carried out in system, the method includes：
(1) deethanization gasoline is heated in stabilizer feed exchanger, subsequently into carrying out gas-liquid separation in gas-liquid separator；
(2) gas for obtaining gas-liquid separation feeds to the gas phase import of stabilizer, by gas from the gaseous phase outlet of gas-liquid separator
The isolated liquid of liquid feeds to the fluid inlet of stabilizer from the liquid-phase outlet of gas-liquid separator, is obtained from the bottom of towe of stabilizer
To stable gasoline.
13. methods according to claim 12, wherein, the operating pressure of gas-liquid separator is set in 1-2MPa.
14. method according to claim 12 or 13, wherein, the deethanization gasoline is obtained as follows：
A () compresses rich gas in rich gas compressor, obtain compressed oil；
B compressed oil is carried out in condensing oil tank condensing, obtains condensed oil and gas by ()；
C () is desorbed condensed oil feeding desorber, obtain deethanization gasoline.
15. methods according to claim 14, wherein, the method also includes：Step (b) gained gas is sequentially passed through into suction
Receive tower to be absorbed, reabsorbed subsequently into reabsorber, dry gas is obtained from the tower top of reabsorber.
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| CN109929580B (en) * | 2017-12-15 | 2021-03-23 | 中海油惠州石化有限公司 | Delayed coking unit and method for processing catalytic slurry oil |
| CN108795485B (en) * | 2018-07-19 | 2024-05-07 | 中国石油化工股份有限公司 | Naphtha upgrading energy-saving device and upgrading process |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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