CN104910951A - Catalytic cracking unit of rich gas and crude gasoline - Google Patents
Catalytic cracking unit of rich gas and crude gasoline Download PDFInfo
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- CN104910951A CN104910951A CN201510273547.3A CN201510273547A CN104910951A CN 104910951 A CN104910951 A CN 104910951A CN 201510273547 A CN201510273547 A CN 201510273547A CN 104910951 A CN104910951 A CN 104910951A
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- gasoline
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Abstract
The invention discloses a catalytic cracking unit of rich gas and crude gasoline. The catalytic cracking unit comprises a balance tank, an absorbing tower, and a re-absorbing tower which are connected successively; compressed rich gas is delivered into the balance tank; rich oil obtained from the bottom of the absorbing tower is delivered back to the balance tank; tower bottom diesel oil is obtained from the bottom of the re-absorbing tower; dry gas is obtained from the top of the re-absorbing tower; the balance tank is connected with the top of a desorption column; the desorption column is provided with a heat exchanger; ethane-free gasoline obtained from the bottom of the desorption column is delivered into a stabilizer column; dry gas and liquefied gas are separated from the stabilizer column; the stabilizer column is connected with a reboiler; a supplement absorbent is delivered into the stabilizer column through the reboiler; the supplement absorbent and crude gasoline are directly delivered into the absorbing tower; and stabilized gasoline obtained from the stabilizer column is delivered into the absorbing tower. Based on the principles above, separation absorption and cracking of different gas can be realized, stable fractionation cracking of rich gas and crude gasoline is realized, and stable dry gas, liquefied gas, and steam-qualified stabilized gasoline are obtained.
Description
Technical field
The present invention relates to refining of petroleum field, be specifically related to the catalytic cracking unit of rich gas and raw gasline.
Background technology
Catalytic cracking technology is studied successfully by French E.J. Hu Deli, realizes industrialization in 1936, adopts fixed-bed reactor (reaction and catalyst regeneration carry out in turn off and in same reactor) at that time.Coming years, catalytic cracking is to moving-bed (TCC, reaction and catalyst regeneration carry out respectively in reactor and revivifier, and stock oil and catalyzer or air move from top to bottom in reactor and revivifier) and fluidized-bed (FCC, reaction and catalyst regeneration are also carry out in reactor and revivifier respectively, be catalyzer and oil gas or air are fluidized state) both direction develops.Moving bed catalytic cracking is eliminated gradually because of equipment complexity, fluid catalystic cracking because of equipment compared with simple, processing power greatly, more easy to operate and obtain large development.20 century 70s, riser tube is combined with zeolite catalyst and makes fluid catalytic cracking technology there occurs qualitative leap, and raw material range is wider, and product is more versatile and flexible, and device operation is more stable.Due in rich gas with gasoline component, and in raw gasline, be dissolved with C3, C4 component, utilize existing fractionating method well the magazins' layout in rich gas can not be obtained stable gas.
Summary of the invention
Instant invention overcomes the deficiencies in the prior art, the catalytic cracking unit of rich gas and raw gasline is provided, separate absorbent, cracking can be carried out to different gas, realize realizing stable fractionation cracking to rich gas and raw gasline, obtain the stable gasoline that stable dry gas, liquefied gas and steam are qualified.
For solving above-mentioned technical problem, the present invention is by the following technical solutions: the catalytic cracking unit of rich gas and raw gasline, comprise connect successively surge tank, absorption tower and reabsorber, and pass into compression rich gas to surge tank, the rich absorbent oil obtained bottom absorption tower flows back to surge tank, obtain diesel oil at the bottom of tower in the bottom of reabsorber, obtain dry gas at the top of reabsorber; Described surge tank also connects desorption tower top, mounting heat exchanger gone back by desorption tower, stabilizer tower sent into by the deethanizing gasoline obtained bottom desorption tower, stabilizer tower isolates dry gas and liquefied gas, stabilizer tower also connects reboiler, and the supplementary absorption agent entering stabilizer tower first enters stabilizer tower again after reboiler; Also directly pass into supplementary absorption agent and raw gasline in described absorption tower, the stable gasoline that stabilizer tower obtains passes into absorption tower.Raw gasline in absorption tower absorbs most of carbon more than three component in gas and part carbon two component as absorption agent, also allow simultaneously the stable gasoline of stabilizer tower as a supplement absorption agent assist raw gasline to carry out absorption carbon more than three component; And containing carbon two component in the rich oil suction obtained bottom absorption tower, if directly send into stabilizer tower, be unfavorable for the stable operation of stabilizer tower, therefore desorption tower is set between absorption tower and stabilizer tower, by carbon two component in rich oil suction after tower top distillation, remaining deethanizing gasoline is sent in stabilizer tower again, stabilizer tower is again by the liquefied gas isolating carbon three in the gasoline of carbon more than five, carbon four is master, condensing cooling, a part makes trim the top of column, and another part goes out device after sending to desulfurization.Be the stable gasoline that vapour pressure is qualified at the bottom of tower, successively with deethanizing gasoline, the heat exchange of desorption tower feed oil, be cooled to 40 DEG C, part pump is squeezed into and is absorbed the supplementary absorption agent of tower top work, rest part carrying device.The stable gasoline obtained in existing material rich absorbent oil and stabilizer tower is utilized to carry out assist absorption in this fractionation cracking operation, also utilize the carbon binary in desorption tower removal rich absorbent oil simultaneously, avoid it on the impact of stabilizer tower essence separation column, make fractionation process more stable, thus compression rich gas and raw gasline fractionation are obtained the qualified stable gasoline of required dry gas, liquefied gas and steam.
The stable gasoline that raw gasline and stabilizer tower are separated is all from the input of absorption tower tower top, and rich absorbent oil enters at the bottom of absorbing tower.
Reabsorber also passes into solar oil cut.
The lean gas that top, described absorption tower is separated enters reabsorber.
Interchanger is arranged on the side-lower of desorption tower, and reboiler is arranged on the side-lower of stabilizer tower.
Compared with prior art, the invention has the beneficial effects as follows: in this fractionation cracking operation, utilize the stable gasoline obtained in existing material rich absorbent oil and stabilizer tower to carry out assist absorption, also utilize the carbon binary in desorption tower removal rich absorbent oil simultaneously, avoid it on the impact of stabilizer tower essence separation column, make fractionation process more stable, thus compression rich gas and raw gasline fractionation are obtained the qualified stable gasoline of required dry gas, liquefied gas and steam.
Accompanying drawing explanation
Fig. 1 is functional block diagram of the present invention.
Embodiment
Below in conjunction with accompanying drawing, the present invention is further elaborated, and embodiments of the invention are not limited thereto.
Embodiment:
As shown in Figure 1, the present invention includes connect successively surge tank, absorption tower and reabsorber, and pass into compression rich gas to surge tank, the rich absorbent oil obtained bottom absorption tower flows back to surge tank, obtain diesel oil at the bottom of tower in the bottom of reabsorber, obtain dry gas at the top of reabsorber; Described surge tank also connects desorption tower top, mounting heat exchanger gone back by desorption tower, stabilizer tower sent into by the deethanizing gasoline obtained bottom desorption tower, stabilizer tower isolates dry gas and liquefied gas, stabilizer tower also connects reboiler, and the supplementary absorption agent entering stabilizer tower first enters stabilizer tower again after reboiler; Also directly pass into supplementary absorption agent and raw gasline in described absorption tower, the stable gasoline that stabilizer tower obtains passes into absorption tower.
The stable gasoline that raw gasline and stabilizer tower are separated is all from the input of absorption tower tower top, and rich absorbent oil enters at the bottom of absorbing tower.
Reabsorber also passes into solar oil cut.
The lean gas that top, described absorption tower is separated enters reabsorber.
Interchanger is arranged on the side-lower of desorption tower, and reboiler is arranged on the side-lower of stabilizer tower.
Compression rich gas mixes with the stripping gas from the rich absorbent oil bottom absorption tower and desorption tower top after pressurization, condensing cooling, be further cooled to 40 DEG C, enter surge tank and carry out equilibrium evaporation, non-condensable gas wherein enters bottom absorption tower, the condensed oil extracted out at the bottom of tank and stable gasoline heat exchange at the bottom of stabilizer tower, to after 80 DEG C, enter desorption tower top.
In absorption tower, by raw gasline as absorption agent, the stable gasoline absorption agent as a supplement that stabilizer tower comes, is squeezed into by tower top respectively, contacts with the non-condensable gas entered at the bottom of tower is reverse.In gas, most more than C3 component (part C2 component) is absorbed.Absorbing tower ejects the gas come and carries a small amount of absorption agent (gasoline component), is called lean gas, removes reabsorber.In reabsorber, make absorption agent with solar oil cut and again reclaim gasoline component wherein, tower top gained dry gas delivers to gas pipe network, and at the bottom of tower, diesel oil returns separation column.
Containing C2 component in rich absorbent oil at the bottom of absorption tower, be unfavorable for the operation of stabilizer tower, the effect of desorption tower is exactly desorbed by the C2 in rich absorbent oil.Have interchanger heat supply at the bottom of tower, tower top stripping gas out, except containing except C2 component, also has a considerable amount of C3, C4 component, mixes, enter surge tank through cooling with compression rich gas.Be deethanizing gasoline at the bottom of tower, enter stabilizer tower.
Stabilizer tower is in fact a rectifying tower isolating C3, C4 from the gasoline of more than C5.Deethanizing gasoline and stable gasoline heat exchange, to 165 DEG C, reach in the middle part of stabilizer tower.Have reboiler heat supply at the bottom of stabilizer tower, below the C4 component in deethanizing gasoline steamed from tower top, obtain the liquefied gas based on C3, C4, through condensing cooling, a part makes trim the top of column, and another part goes out device after sending to desulfurization.Be the stable gasoline that vapour pressure is qualified at the bottom of tower, successively with deethanizing gasoline, the heat exchange of desorption tower feed oil, be cooled to 40 DEG C, part pump is squeezed into and is absorbed the supplementary absorption agent of tower top work, rest part carrying device.
The stable gasoline obtained in existing material rich absorbent oil and stabilizer tower is utilized to carry out assist absorption in this fractionation cracking operation, also utilize the carbon binary in desorption tower removal rich absorbent oil simultaneously, avoid it on the impact of stabilizer tower essence separation column, make fractionation process more stable, thus compression rich gas and raw gasline fractionation are obtained the qualified stable gasoline of required dry gas, liquefied gas and steam.
Just this invention can be realized as mentioned above.
Claims (5)
1. the catalytic cracking unit of rich gas and raw gasline, it is characterized in that: comprise connect successively surge tank, absorption tower and reabsorber, and pass into compression rich gas to surge tank, the rich absorbent oil obtained bottom absorption tower flows back to surge tank, obtain diesel oil at the bottom of tower in the bottom of reabsorber, obtain dry gas at the top of reabsorber; Described surge tank also connects desorption tower top, mounting heat exchanger gone back by desorption tower, stabilizer tower sent into by the deethanizing gasoline obtained bottom desorption tower, stabilizer tower isolates dry gas and liquefied gas, stabilizer tower also connects reboiler, and the supplementary absorption agent entering stabilizer tower first enters stabilizer tower again after reboiler; Also directly pass into supplementary absorption agent and raw gasline in described absorption tower, the stable gasoline that stabilizer tower obtains passes into absorption tower.
2. the catalytic cracking unit of rich gas according to claim 1 and raw gasline, is characterized in that: the stable gasoline that raw gasline and stabilizer tower are separated is all from the input of absorption tower tower top, and rich absorbent oil enters at the bottom of absorbing tower.
3. the catalytic cracking unit of rich gas according to claim 1 and raw gasline, is characterized in that: on reabsorber, also pass into solar oil cut.
4. the catalytic cracking unit of rich gas according to claim 1 and raw gasline, is characterized in that: the lean gas that top, described absorption tower is separated enters reabsorber.
5. the catalytic cracking unit of rich gas according to claim 1 and raw gasline, is characterized in that: interchanger is arranged on the side-lower of desorption tower, and reboiler is arranged on the side-lower of stabilizer tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN201510273547.3A CN104910951A (en) | 2015-05-26 | 2015-05-26 | Catalytic cracking unit of rich gas and crude gasoline |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201510273547.3A CN104910951A (en) | 2015-05-26 | 2015-05-26 | Catalytic cracking unit of rich gas and crude gasoline |
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| CN104910951A true CN104910951A (en) | 2015-09-16 |
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| CN201510273547.3A Pending CN104910951A (en) | 2015-05-26 | 2015-05-26 | Catalytic cracking unit of rich gas and crude gasoline |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107298989A (en) * | 2016-04-14 | 2017-10-27 | 中国石油化工股份有限公司 | A kind of absorption stabilizing process and system |
| CN110240933A (en) * | 2019-06-20 | 2019-09-17 | 山东京博石油化工有限公司 | A kind of processing method of catalytic cracking diesel oil |
| CN112745935A (en) * | 2019-10-31 | 2021-05-04 | 中国石油化工股份有限公司 | Method and device for desulfurizing and separating catalytic cracking light product |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6416656B1 (en) * | 1999-06-23 | 2002-07-09 | China Petrochemical Corporation | Catalytic cracking process for increasing simultaneously the yields of diesel oil and liquefied gas |
| CN101250426A (en) * | 2008-03-13 | 2008-08-27 | 华南理工大学 | Method for reducing propylene concentration of dry gas in catalytic cracking device absorption stabilizing system |
-
2015
- 2015-05-26 CN CN201510273547.3A patent/CN104910951A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6416656B1 (en) * | 1999-06-23 | 2002-07-09 | China Petrochemical Corporation | Catalytic cracking process for increasing simultaneously the yields of diesel oil and liquefied gas |
| CN101250426A (en) * | 2008-03-13 | 2008-08-27 | 华南理工大学 | Method for reducing propylene concentration of dry gas in catalytic cracking device absorption stabilizing system |
Non-Patent Citations (1)
| Title |
|---|
| 詹雪兰: "催化裂化主分馏塔和吸收稳定系统的全流程模拟与优化", 《华东理工大学硕士学位论文 工程科技Ⅰ辑》 * |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107298989A (en) * | 2016-04-14 | 2017-10-27 | 中国石油化工股份有限公司 | A kind of absorption stabilizing process and system |
| CN107298989B (en) * | 2016-04-14 | 2019-03-19 | 中国石油化工股份有限公司 | A kind of absorption stabilizing process and system |
| CN110240933A (en) * | 2019-06-20 | 2019-09-17 | 山东京博石油化工有限公司 | A kind of processing method of catalytic cracking diesel oil |
| CN110240933B (en) * | 2019-06-20 | 2021-11-09 | 山东京博石油化工有限公司 | Method for treating catalytic cracking diesel oil |
| CN112745935A (en) * | 2019-10-31 | 2021-05-04 | 中国石油化工股份有限公司 | Method and device for desulfurizing and separating catalytic cracking light product |
| CN112745935B (en) * | 2019-10-31 | 2022-09-27 | 中国石油化工股份有限公司 | Method and device for desulfurizing and separating catalytic cracking light product |
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