CN104560115A - Absorption stabilizing system and working process and application thereof as well as method for preparing stabilized petrol - Google Patents
Absorption stabilizing system and working process and application thereof as well as method for preparing stabilized petrol Download PDFInfo
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- CN104560115A CN104560115A CN201310499508.6A CN201310499508A CN104560115A CN 104560115 A CN104560115 A CN 104560115A CN 201310499508 A CN201310499508 A CN 201310499508A CN 104560115 A CN104560115 A CN 104560115A
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- gas
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- stabilizer tower
- liquid separator
- absorbing
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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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- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
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- General Chemical & Material Sciences (AREA)
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention provides an absorption stabilizing system and a working process and application thereof as well as a method for preparing stabilized petrol. The working process comprises the following steps: arranging a gas-liquid separator between a stabilizing tower feed heat exchanger and a stabilizing tower; arranging a gas phase inlet above an original feeding opening of the stabilizing tower, wherein the gas phase inlet is connected with the gas-liquid separator; self-pressing gas phase oil of the gas-liquid separator into the stabilizing tower through the gas phase inlet, and further self-pressing liquid phase oil of the gas-liquid separator into the stabilizing tower along the existing working process through the original feeding opening. By the working process, cold reflux of the stabilizing tower can be reduced, reduction in the cooling load at the top of the stabilizing tower and the reboiling load at the bottom of the stabilizing tower can be facilitated, and through a buffering action of the gas-liquid separator, the operation of the stabilizing tower can be smoothened.
Description
Technical field
The invention belongs to refining of petroleum field, particularly a kind ofly realizing by changing stabilizer tower feeding manner the new technological process that absorbing-stabilizing system energy consumption reduces, and a kind of absorbing-stabilizing system and application thereof and a kind of method preparing stable gasoline.
Background technology
Absorbing-stabilizing system is the important component part of the crude oil secondary processing devices such as catalytic cracking, delayed coking, hydrocracking, form primarily of rich gas compressor, condensing oil tank, absorption tower, desorption tower, stabilizer tower, reabsorber and corresponding cold exchange device, its effect be utilize absorb and the method for rectifying independently the rich gas of fractionating column system and raw gasline (or raw naphtha) are separated into the qualified stable gasoline of dry gas, liquid hydrocarbon and vapour pressure (or petroleum naphtha) in the future.
Because the layout of absorption and desorption is different, Vapor recovery unit has single tower and double tower two kinds of flow processs usually.Single tower flow process collects absorption, desorb in a tower, and double-column process is then separated to be completed in two towers, thus than single tower flow process, has better absorption and desorption effect, applies more.
(see figure 1) in double-column process, is first compressed to specified pressure through compressor from main fractionating tower tower top catch pot, the rich gas that is rich in liquid hydrocarbon (LPG) and gasoline component, then through cooling into condensing oil tank, isolates gas phase and liquid phase.Subsequently, gas phase send absorption tower, and dependence raw gasline and stable gasoline (also known as supplementary absorption agent) remove C wherein
3 +component, obtains the lean gas of " more dry " relatively, and is rich in C from tower top
3 +the rich absorbent oil of component then delivers to condensing oil tank by extracting out at the bottom of tower.Absorption tower service temperature is lower, and assimilation effect is better, therefore usually arranges two or a water recirculator at middle part, to take solution heat away in time, maintains absorption tower lower temperature operation.Self-absorption tower top lean gas self-pressure is out gone at the bottom of reabsorber tower, and the product diesel oil downward by adverse current absorbs further, to obtain C
3 +component concentration is lower than 3%(mol) product dry gas, at the bottom of tower, rich diesel oil then returns main fractionating tower freshening.The effect of desorption tower T302 is then under the effect of boiling hot amount again at the bottom of tower, will be dissolved in the C in condensed oil
2component desorbs, and stripping gas is drawn through condensing oil tank by tower top and send absorption tower to enter next circulation; Deethanizing gasoline at the bottom of tower, then through being pumped to stabilizer tower, separating LPG product at tower top, obtaining stable gasoline at the bottom of tower.
In above-mentioned flow process, oil at the bottom of desorption tower and deethanizing gasoline are extracted out and laggard deethanizing gasoline ~ stable gasoline interchanger E305 that boosts through stabilizer tower fresh feed pump P304/1-2, send stabilizer tower T304 after heat temperature raising.There is following defect in this flow process: deethanizing gasoline is extracted out by the bottom of desorption tower with bubble point temperature, though through the suitable supercharging of pump, but still vaporize in a large number after heat exchange, namely be equivalent to complete once balance flash distillation or gas-liquid separation in interchanger, if gas-liquid two-phase also enters the same column plate of stabilizer tower jointly, be just equivalent to oneself and denied current separating-purifying; In other words, be just equivalent to the one piece of theoretical stage decreasing stabilizer tower, and have to strengthen cold reflux amount as making up, this will improve the load that to boil again at the bottom of the tower top cooling load of stabilizer tower and tower.
Summary of the invention
The object of the invention is to overcome in existing absorbing-stabilizing system flow process, oneself denies the gasification separation effect of deethanizing gasoline ~ stable gasoline interchanger, and increase the defect of stabilizer tower energy consumption, provide a kind of absorbing-stabilizing system new technological process realizing the reduction of stabilizer tower energy consumption by changing stabilizer tower feeding manner.
To achieve these goals, the invention provides a kind of workflow of absorbing-stabilizing system, wherein, this workflow comprises:
Between stabilizer tower feed exchanger and stabilizer tower, gas-liquid separator is set;
Above the former opening for feed of stabilizer tower, arrange gas phase import, this gas phase import is connected with gas-liquid separator;
The gas phase oil product of gas-liquid separator is by gas-phase feed mouth from compressing into stabilizer tower, and the liquid phase oil product of gas-liquid separator then continues certainly to compress into stabilizer tower along existing procedure by the former opening for feed of stabilizer tower.
The present invention also provides a kind of absorbing-stabilizing system, this absorbing-stabilizing system comprises: stabilizer tower and stabilizer tower feed exchanger, described stabilizer tower comprises fluid inlet, wherein, this absorbing-stabilizing system also comprises: gas-liquid separator, and described stabilizer tower also comprises: gas phase import, described gas phase import is positioned at the top of stabilizer tower, described gas-liquid separator is arranged between stabilizer tower feed exchanger and stabilizer tower, and the gas phase inlet communication of the gaseous phase outlet of gas-liquid separator and stabilizer tower, the liquid-phase outlet of gas-liquid separator is communicated with the fluid inlet of stabilizer tower.
The invention provides the application of absorbing-stabilizing system of the present invention in catalytic cracking unit, delayed coking unit and hydroeracking unit.
The present invention also provides a kind of method preparing stable gasoline, and the method is carried out in above-mentioned absorbing-stabilizing system, and the method comprises:
(1) deethanizing gasoline is heated in stabilizer tower feed exchanger, then enter in gas-liquid separator and carry out gas-liquid separation;
(2) gas gas-liquid separation obtained is fed to the gas phase import of stabilizer tower from the gaseous phase outlet of gas-liquid separator, liquid gas-liquid separation obtained is fed to the fluid inlet of stabilizer tower from the liquid-phase outlet of gas-liquid separator, at the bottom of the tower of stabilizer tower, obtain stable gasoline.
Workflow provided by the invention, by setting up feeding gas liquid/gas separator, and the different column plate positions gas of equilibrium flash vaporization in gas-liquid separator, liquid two phase materials being sent into respectively stabilizer tower realize.This master arranges one piece of theoretical stage owing to being equivalent to add stabilizer tower, thus decreases the cold reflux amount of stabilizer tower, then helps it to reduce to boil at the bottom of tower top cooling load and tower load again.Meanwhile, the shock absorption of gas-liquid separator also helps the operation of steady stabilizer tower.
Other features and advantages of the present invention are described in detail in embodiment part subsequently.
Accompanying drawing explanation
Fig. 1 is the workflow of the absorbing-stabilizing system of prior art;
Fig. 2 is the workflow according to a kind of absorbing-stabilizing system preferred embodiment of the present invention.
Embodiment
Below the specific embodiment of the present invention is described in detail.Should be understood that, embodiment described herein, only for instruction and explanation of the present invention, is not limited to the present invention.
The invention provides a kind of workflow of absorbing-stabilizing system, wherein, this workflow comprises:
Between stabilizer tower feed exchanger and stabilizer tower, gas-liquid separator is set;
Above the former opening for feed of stabilizer tower, arrange gas phase import, this gas phase import is connected with gas-liquid separator;
The gas phase oil product of gas-liquid separator is by gas phase import from compressing into stabilizer tower, and the liquid phase oil product of gas-liquid separator then continues certainly to compress into stabilizer tower along existing procedure by the former opening for feed of stabilizer tower.
Technical terms used in the present invention is in case of no particular description all according to the common version of this area.
In the present invention, by stabilizer tower feeding gas liquid/gas separator, gas, liquid two-phase are sent into the different column plate position of stabilizer tower, respectively to reduce stabilizer tower energy consumption.In addition, owing to being provided with gas-liquid separator and gas phase being sent into stabilizer tower comparatively upper position, make in feed exchanger, the flow pressure drop of deethanizing gasoline will obviously reduce, thus more be conducive to the energy consumption gasifying and reduce deethanizing gasoline extractor pump; Meanwhile, the pooling feature of gas-liquid separator will stablize charging, particularly gas-phase feed, and help stabilizer tower more stable operation.
In the present invention, owing to being provided with gas-liquid separator, and flashed vapour is sent into stabilizer tower comparatively upper position, more enhance the gasification of deethanizing gasoline in interchanger conversely, will the charging of stable stabilizer tower be conducive to simultaneously.
In the present invention, the working pressure of gas-liquid separator can adjust according to practical condition, and under preferable case, working pressure is set in 1-2MPa.
In the present invention, the column plate position arranging gas phase import in stabilizer tower can adjust according to practical condition, and under preferable case, the column plate position arranging gas phase import in stabilizer tower is positioned at 29-31 block plate above the former opening for feed of stabilizer tower.
In the present invention, above the former opening for feed of stabilizer tower, arrange gas phase import, can adjust the position of fluid inlet, usually, stabilizer tower is provided with three pieces of feed plates, has adjustment elasticity simultaneously.Under preferable case, the liquid phase oil product of gas-liquid separator then continues 18-20,22-24 and 26-28 block plate certainly being compressed into stabilizer tower along existing procedure by former opening for feed.
In the present invention, absorbing-stabilizing system can be the absorbing-stabilizing system of catalytic cracking unit, delayed coking unit, hydroeracking unit.
In the present invention, absorbing-stabilizing system can comprise: the rich gas compressor be connected, condensing oil tank, absorption tower, desorption tower, stabilizer tower and reabsorber.
The workflow of absorbing-stabilizing system provided by the invention is roughly based on following principle:
1, make use of the gasification function of feed exchanger.By setting up gas-liquid separator, and gas, liquid two-phase are sent into stabilizer tower respectively, thus be equivalent to add one piece of stabilizer tower theoretical stage.Make thus, maintaining under the constant condition of quality product, the cold reflux amount of stabilizer tower can be reduced, contribute to reducing its energy consumption;
2, reduce the flow pressure drop of deethanizing gasoline in feed exchanger, improve heat transfer effect, help the vaporization rate that improve deethanizing gasoline;
3, the charging of stabilizer tower, particularly gas-phase feed is stabilized, favourable to the operation of stable stabilizer tower.
The present invention also provides a kind of absorbing-stabilizing system, this absorbing-stabilizing system comprises: stabilizer tower and stabilizer tower feed exchanger, described stabilizer tower comprises fluid inlet, wherein, this absorbing-stabilizing system also comprises: gas-liquid separator, and described stabilizer tower also comprises: gas phase import, described gas phase import is positioned at the top of stabilizer tower, described gas-liquid separator is arranged between stabilizer tower feed exchanger and stabilizer tower, and the gas phase inlet communication of the gaseous phase outlet of gas-liquid separator and stabilizer tower, the liquid-phase outlet of gas-liquid separator is communicated with the fluid inlet of stabilizer tower.
In the present invention, the fluid inlet of stabilizer tower is generally the opening for feed of original stabilizer tower.Certainly, according to needing, its position also can adjust, and conveniently operates, and the fluid inlet of preferred described stabilizer tower is generally the opening for feed of original stabilizer tower.
In the present invention, the column plate position of described gas phase import can adjust according to practical condition, is preferably placed at the 29-31 block column plate above stabilizer tower fluid inlet.
Wherein the column plate position of fluid inlet is generally at 19-27 block column plate place.
In the present invention, absorbing-stabilizing system can also comprise: desorption tower, and the liquid-phase outlet of described desorption tower is communicated with stabilizer tower feed exchanger.Thus can be provided by desorption tower and be fed into stabilizer tower feed exchanger.This is well known to those skilled in the art, and is not described in detail at this.
In the present invention, absorbing-stabilizing system can also comprise: 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 conventionally be carried out, the present invention to this without particular requirement.
According to one of the present invention preferred embodiment, the outlet of preferred described rich gas compressor is communicated with the opening for feed of condensing oil tank, the described gaseous phase outlet of condensing oil tank is communicated with the opening for feed on absorption tower, the described liquid-phase outlet of condensing oil tank is communicated with the opening for feed of desorption tower, the gaseous phase outlet of described desorption tower and the inlet communication of rich gas compressor, the gaseous phase outlet on described absorption tower and the inlet communication of reabsorber.
The present invention also provides the above-mentioned application of absorbing-stabilizing system in catalytic cracking unit, delayed coking unit and hydroeracking unit.Absorbing-stabilizing system of the present invention is used for can be effectively energy-conservation in catalytic cracking unit, delayed coking unit and hydroeracking unit.
The present invention also provides a kind of method preparing stable gasoline, and the method is carried out in above-mentioned absorbing-stabilizing system, and the method comprises:
(1) deethanizing gasoline is heated in stabilizer tower feed exchanger, then enter in gas-liquid separator and carry out gas-liquid separation;
(2) gas gas-liquid separation obtained is fed to the gas phase import of stabilizer tower from the gaseous phase outlet of gas-liquid separator, liquid gas-liquid separation obtained is fed to the fluid inlet of stabilizer tower from the liquid-phase outlet of gas-liquid separator, at the bottom of the tower of stabilizer tower, obtain stable gasoline.
In the present invention, the working pressure of gas-liquid separator can adjust according to practical condition, is preferably set to 1-2MPa.
In the present invention, deethanizing gasoline stocks can obtain according to prior art, such as, can obtain as follows:
A rich gas compresses by () in rich gas compressor, obtain compressed oil;
B compressed oil carries out condensing by () in condensing oil tank, obtain condensed oil and gas;
C described condensed oil is sent into desorption tower and is carried out desorb by (), obtain deethanizing gasoline.
In the present invention, the method also comprises: absorbed through absorption tower successively by step (b) gained gas, then enter reabsorber and absorb, obtain dry gas from the tower top of reabsorber.
The present invention is mainly to add gas-liquid separator in the absorbing-stabilizing system of prior art, and on stabilizer tower, set up gas phase import, described gas phase import is positioned at the top of stabilizer tower, described gas-liquid separator is arranged between stabilizer tower feed exchanger and stabilizer tower, and the gas phase inlet communication of the gaseous phase outlet of gas-liquid separator and stabilizer tower, the liquid-phase outlet of gas-liquid separator is communicated with the fluid inlet of stabilizer tower.Other and prior art are all identical.
Based on preceding solution, hinge structure tool of the present invention has the following advantages and effect:
1, increase equipment is few, flow process simple, no matter is new project or transformation project, all easy to implement;
2, the feed operation of steady stabilizer tower is conducive to;
3, the pressure drop reducing deethanizing gasoline extractor pump is conducive to;
4, reduce the cold reflux amount of stabilizer tower, thus reduce the load that to boil again at the bottom of tower top cooling load and tower;
5, any impact is not formed on the product yield of stabilizer tower system and quality product.
Below in conjunction with embodiment, comparative example and accompanying drawing, the present invention is described in detail, but working of an invention mode is not limited thereto.
Comparative example
Comparative example is for illustration of the workflow of the absorbing-stabilizing system of prior art
As shown in Figure 1, deethanizing gasoline (121.8 DEG C, 1.26MPag, 96.50t/h) oil pump P304/1-2 pressure-raising at the bottom of desorption tower T302 enters the shell side of stabilizer tower T304 feed exchanger and deethanizing gasoline ~ stable gasoline interchanger E305 to 1.8MPag, by from the stable gasoline at the bottom of stabilizer tower tower once (176.4 DEG C, 80.40t/h) be heated to 130.3 DEG C (furnace capacity of corresponding pressure 1.15MPa, quality vaporization rate 11.11%, E305 be 118 × 10
4kcal/h) stabilizer tower the 27th, 23,19 blocks of column plates are entered.Now, stablize tower top working pressure 1.10MPa, temperature 61.3 DEG C, use recirculated water to do heat-eliminating medium, overhead oil gas is cooled to 47.7 DEG C and enters tower top and divide flow container V302, corresponding cold reflux amount 55.84t/h, tower top cooling load 565.9 × 10
4kcal/h; Column bottom temperature 176.4 DEG C, to use in main fractionating tower one once (241 DEG C, 1.4MPa, 200t/h) to do boiling hot source again, and the correspondence furnace capacity that boils again is 655.2 × 10
4kcal/h.Stable gasoline once to heat after deethanizing gasoline 154.3 DEG C from E305 out, then enters E304/1-2 tube side heating condensed oil.
Embodiment
Embodiment is for illustration of the workflow that the invention provides absorbing-stabilizing system
As shown in Figure 2, the following improvement of ratio flow implementation is compared:
1, between deethanizing gasoline ~ stable gasoline interchanger E305 and stabilizer tower T304, set up stabilizer tower charging knockout drum (numbering VN1), and the working pressure of VN1 has been set in 1.15MPa.
2, above the former opening for feed of stabilizer tower, the 30th piece of plate place has newly opened gas-phase feed mouth;
3, the gas-phase feed line connecting VN1 and stabilizer tower the 30th block of plate is provided with;
4, VN1 liquid phase is from compressing into stabilizer tower the 23rd block of plate.
Concrete operations are: deethanizing gasoline (121.8 DEG C, 1.26MPag, 96.50t/h) oil pump P304/1-2 pressure-raising at the bottom of desorption tower T302 enters the shell side of stabilizer tower T304 feed exchanger and deethanizing gasoline ~ stable gasoline interchanger E305 to 1.8MPag, by from the stable gasoline at the bottom of stabilizer tower tower once (176.4 DEG C, 80.40t/h) be heated to 130.3 DEG C (corresponding pressure be 1.15MPa, quality vaporization rate is 11.11%, the furnace capacity of E305 is 118 × 10
4kcal/h) newly-increased stabilizer tower charging knockout drum VN1 is entered.The working pressure of VN1 is set in 1.15MPa, by equilibrium flash vaporization, lightens gas phase 10.96t/h, certainly compresses into stabilizer tower the 30th block of column plate, and remaining liquid 85.53t/h is then from compressing into stabilizer tower the 23rd block of column plate.Now, stabilizer tower tower top pressure 1.10MPa, temperature 61.4 DEG C, use recirculated water to do heat-eliminating medium, overhead oil gas is cooled to 47.7 DEG C and enters tower top and divide flow container V302, corresponding cold reflux amount 47.37t/h(changes front 55.84t/h), tower top cooling load 499.4 × 10
4kcal/h(changes front 565.9 × 10
4kcal/h); At the bottom of tower 176.4 DEG C, to use in main fractionating tower one once (241 DEG C, 1.4MPa, 200t/h) to do boiling hot source, boiling hot load is 585.6 × 10 effectively more again
4kcal/h(changes front 655.2 × 10
4kcal/h).Stable gasoline once to heat after deethanizing gasoline 154.3 DEG C from E305 out, then inlet pipe journey heating condensed oil.
Adopt after the present embodiment, absorbing-stabilizing system operational circumstances and effect as follows:
1, effective boiling hot load 69.6 × 10 again at the bottom of stabilizer tower is saved
4kcal/h, is equivalent to decrease the equivalent energy consumption of about 1.2t/h middle pressure steam, therefore reduces whole catalytic unit energy consumption 105.6kg and marks oil/h, and folding 1.0kg marks oil/t raw material; Calculate by middle pressure steam 300 yuan/t, save running cost 360 yuan/hour, roll over 302.4 ten thousand yuan/year (go into operation in device year by within 8400 hours, calculating, lower together);
2, tower top cooling load 66.5 × 10 is stablized in minimizing
4kcal/h, corresponding minimizing device equivalent recirculated water consumes the 83.1t/h(recirculated water temperature difference and gets 8 DEG C), therefore reduce whole catalytic unit energy consumption 8.31kg and mark oil/h, folding 0.08kg marks oil/t raw material; By recirculated water unit price 0.3 yuan/ton calculating, cost-saving 24.9 yuan/time, roll over 20.94 ten thousand yuan/year;
3, new technological process is identical with comparative example flow process material balance, quality product is constant.
To sum up, the embodiment of the present invention is ensureing under absorbing-stabilizing system quality product and the constant prerequisite of yield, by changing stabilizer tower feeding manner, reduce stabilizer tower system energy consumption 113.9kg and mark oil/h, therefore reduce whole catalytic unit energy consumption 1.08kg and mark oil/t raw material, realize energy-saving benefit 384.9 yuan/time, roll over 323.34 ten thousand yuan/year.
Above-described embodiment is detailed embodiment of the present invention; but embodiments of the present invention are not restricted to the described embodiments; other are any do not deviate from spirit of the present invention and principle under do change, modification, substitute, combine, simplify; all should be the substitute mode of equivalence, be included within protection scope of the present invention.
Claims (15)
1. a workflow for absorbing-stabilizing system, is characterized in that, this workflow comprises:
Between stabilizer tower feed exchanger and stabilizer tower, gas-liquid separator is set;
Above the former opening for feed of stabilizer tower, arrange gas phase import, this gas phase import is connected with gas-liquid separator;
The gas phase oil product of gas-liquid separator is by gas phase import from compressing into stabilizer tower, and the liquid phase oil product of gas-liquid separator then continues certainly to compress into stabilizer tower along existing procedure by the former opening for feed of stabilizer tower.
2. workflow according to claim 1, wherein, the working pressure of gas-liquid separator is set in 1-2MPa.
3. workflow according to claim 1, wherein, 29-31 block plate above the former opening for feed that the column plate position of described gas phase import is positioned at stabilizer tower.
4. according to the workflow in claim 1-3 described in any one, wherein, the liquid phase oil product of gas-liquid separator then continues 18-20,22-24 and 26-28 block plate certainly being compressed into stabilizer tower along existing procedure by the former opening for feed of stabilizer tower.
5. according to the workflow in claim 1-3 described in any one, wherein, described absorbing-stabilizing system is the absorbing-stabilizing system of catalytic cracking unit, delayed coking unit or hydroeracking unit.
6. according to the workflow in claim 1-3 described in any one, wherein, described absorbing-stabilizing system comprises: the rich gas compressor be connected, condensing oil tank, absorption tower, desorption tower, stabilizer tower and reabsorber.
7. an absorbing-stabilizing system, this absorbing-stabilizing system comprises: stabilizer tower and stabilizer tower feed exchanger, described stabilizer tower comprises fluid inlet, it is characterized in that, this absorbing-stabilizing system also comprises: gas-liquid separator, and described stabilizer tower also comprises: gas phase import, described gas phase import is positioned at the top of stabilizer tower, described gas-liquid separator is arranged between stabilizer tower feed exchanger and stabilizer tower, and the gas phase inlet communication of the gaseous phase outlet of gas-liquid separator and stabilizer tower, the liquid-phase outlet of gas-liquid separator is communicated with the fluid inlet of stabilizer tower.
8. absorbing-stabilizing system according to claim 7, wherein, the column plate position of described gas phase import is positioned at the 29-31 block column plate above stabilizer tower fluid inlet.
9. absorbing-stabilizing system according to claim 7, wherein, this absorbing-stabilizing system also comprises: desorption tower, and the liquid-phase outlet of described desorption tower is communicated with stabilizer tower feed exchanger.
10. absorbing-stabilizing system according to claim 9, wherein, this absorbing-stabilizing system also comprises: rich gas compressor, condensing oil tank, absorption tower and reabsorber, the outlet of described rich gas compressor is communicated with the opening for feed of condensing oil tank, the described gaseous phase outlet of condensing oil tank is communicated with the opening for feed on absorption tower, the described liquid-phase outlet of condensing oil tank is communicated with the opening for feed of desorption tower, the gaseous phase outlet of described desorption tower and the inlet communication of rich gas compressor, the gaseous phase outlet on described absorption tower and the inlet communication of reabsorber.
The application of absorbing-stabilizing system in 11. claim 7-10 described in any one in catalytic cracking unit, delayed coking unit and hydroeracking unit.
12. 1 kinds of methods preparing stable gasoline, carry out in the absorbing-stabilizing system of the method in claim 7-10 described in any one, the method comprises:
(1) deethanizing gasoline is heated in stabilizer tower feed exchanger, then enter in gas-liquid separator and carry out gas-liquid separation;
(2) gas gas-liquid separation obtained is fed to the gas phase import of stabilizer tower from the gaseous phase outlet of gas-liquid separator, liquid gas-liquid separation obtained is fed to the fluid inlet of stabilizer tower from the liquid-phase outlet of gas-liquid separator, at the bottom of the tower of stabilizer tower, obtain stable gasoline.
13. methods according to claim 12, wherein, the working pressure of gas-liquid separator is set in 1-2MPa.
14. methods according to claim 12 or 13, wherein, described deethanizing gasoline obtains as follows:
A rich gas compresses by () in rich gas compressor, obtain compressed oil;
B compressed oil carries out condensing by () in condensing oil tank, obtain condensed oil and gas;
C described condensed oil is sent into desorption tower and is carried out desorb by (), obtain deethanizing gasoline.
15. methods according to claim 14, wherein, the method also comprises: absorbed through absorption tower successively by step (b) gained gas, then enter reabsorber and absorb, obtain dry gas from the tower top of reabsorber.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108795485A (en) * | 2018-07-19 | 2018-11-13 | 中国石化青岛炼油化工有限责任公司 | Naphtha modifies energy saver and modifying process |
| CN109929580A (en) * | 2017-12-15 | 2019-06-25 | 中海油惠州石化有限公司 | The method of delayed coking unit and processing catalytic slurry |
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| CN108795485A (en) * | 2018-07-19 | 2018-11-13 | 中国石化青岛炼油化工有限责任公司 | Naphtha modifies energy saver and modifying process |
| 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 |
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