CN1065266C - Efficient tower-less gas fractionation technology - Google Patents
Efficient tower-less gas fractionation technology Download PDFInfo
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- CN1065266C CN1065266C CN98110924A CN98110924A CN1065266C CN 1065266 C CN1065266 C CN 1065266C CN 98110924 A CN98110924 A CN 98110924A CN 98110924 A CN98110924 A CN 98110924A CN 1065266 C CN1065266 C CN 1065266C
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Abstract
The present invention discloses an efficient tower less energy saving gas fractionation technology which comprises the following steps: step 1, liquefied petroleum gas is absorbed from a stable part of a catalytic cracking device, and after being refined, the liquefied petroleum gas enters a depropanizing tower of a gas fractionation device; step 2, C@3 fractions are extracted from a lateral line of a rectifying section in the upper part of the depropanizing tower, and the C@3 fractions enter a propene tower, which leads propene and propane to be separated; step 3, a plurality of strands of extracted MTBE raw material or alkylation raw material is separated from a lateral line of an appropriate tower plate of a stripping section of the depropanizing tower, the quantity of each strand is controlled, and a certain propane-propylene ratio is obtained; step 4, propene is extracted from the lateral line of the rectifying section of the propene tower, and propane is extracted from the tower bottom. The technology can enhance the recovery rate of propene and can reduce investment for equipment, energy consumption and operating cost.
Description
The present invention relates to a kind of fractionation process of liquified petroleum gas.
The raw material of gas fractionation plant is to absorb the liquefied petroleum gas (LPG) that stabilizers is assigned in the catalytic cracking, its main products is fine propylene, MTBE raw material, raw material for alkylation or cis-1,4-polybutadiene rubber raw material, by-product civil liquefied gas, propane, a small amount of ethane gas (including 50% above propylene) and C5 fraction etc.This device generally by depropanizing tower, deethanizing column, propylene tower (being the series connection of two towers when producing fine propylene), deisobutanizer, depentanizer and supporting coldly change, equipment such as pump and return tank form.At present, the technical process of the most gas fractionation plants in the whole nation can be represented by Fig. 1, the advanced depropanizing tower of liquefied petroleum gas (LPG) after refining is told carbon three and C-4-fraction, and the cat head C3 fraction enters propylene tower again after deethanizing column is told ethane gas, tell propylene and propane by this tower; C-4-fraction at the bottom of the depropanizing tower enters depentanizer and removes C5 fraction as civil liquefied gas or cis-1,4-polybutadiene rubber raw material after deisobutanizer fractionates out light C-4-fraction (according to its purposes difference, can be used as MTBE raw material and raw material for alkylation).
The subject matter of above-mentioned gas fractionation process is: 1. when gently the carbon cut is as MTBE and raw material for alkylation, requirement has certain alkane alkene than (being the ratio of Trimethylmethane and all C 4 olefins), and the iso-butylene in the C-4-fraction and n-butene extremely difficult separation (is that volatility is very approaching, boiling point only differs from 0.6 ℃), owing to will satisfy the requirement of alkane alkene ratio, the designer generally will consider from isolating possibility between iso-butylene and the n-butene, so just make the diameter that takes off different alkane tower bigger, the tower tray number is more, that have even near propylene tower, this is very irrational, because purified propylene requires to be 95%-99.5%, but the former is the mixed fraction that only requires certain alkane alkene ratio; 2. the propylene amount in the ethane gas is too high, generally reach 50%-80%, and being these, propylene or fine propylene install topmost product, and the cat head discharging of deethanizing column than tower at the bottom of discharging much smaller, in order to tell a little ethane gas, need return stream to a large amount of propylene and propane, in view of the fractionation principle, be uneconomic not only, and a part of propylene is also lost in vain.
The objective of the invention is: the gas fractionation process of the energy-conservation high yield of a kind of province's tower is provided, and this technology can improve the propylene rate of recovery, reduces facility investment, energy consumption and process cost.
Technical scheme of the present invention is: the gas fractionation process of the energy-conservation high yield of a kind of province's tower comprises the following steps:
(1). absorb the liquefied petroleum gas (LPG) that stabilizers is assigned to from catalytic cracking unit, after making with extra care, enter the depropanizing tower of gas fractionation plant;
(2). extract C3 fraction out from depropanizing tower upper rectifying section side line, enter propylene tower and tell propylene and propane;
(3). divide multiply to extract MTBE raw material or raw material for alkylation out from the suitable trays side line of depropanizing tower stripping section, the control by each burst amount to it reaches certain alkane alkene ratio;
(4). extract propylene out from propylene tower rectifying section side line, go out propane at the bottom of the tower.
The further technical scheme of the present invention is: the gas fractionation process of the energy-conservation high yield of a kind of province's tower comprises the following steps:
(1). absorb the liquefied petroleum gas (LPG) that stabilizers is assigned to from catalytic cracking unit, after making with extra care, enter the depropanizing tower of gas fractionation plant;
(2). extract C3 fraction out from depropanizing tower upper rectifying section side line, enter propylene tower and tell propylene and propane;
(3). divide multiply to extract MTBE raw material or raw material for alkylation out from the suitable trays side line of depropanizing tower stripping section, the control by each burst amount to it reaches certain alkane alkene ratio;
(4). extract propylene out from propylene tower rectifying section side line, go out propane at the bottom of the tower;
(5). the C-4-fraction of depropanizing tower bottom enters depentanizer or enters deisobutanizer, also adopt side line to extract out after again the method for exchange obtain certain alkane alkene than the raw material for alkylation that requires.
The present invention's technical scheme in a step again is: the gas fractionation process of the energy-conservation high yield of a kind of province's tower comprises the following steps:
(1). absorb the liquefied petroleum gas (LPG) that stabilizers is assigned to from catalytic cracking unit, after making with extra care, enter the depropanizing tower of gas fractionation plant;
(2). extract C3 fraction out from depropanizing tower upper rectifying section side line, enter propylene tower and tell propylene and propane;
(3). divide multiply to extract MTBE raw material or raw material for alkylation out from the suitable trays side line of depropanizing tower stripping section, the control by each burst amount to it reaches certain alkane alkene ratio;
(4). extract propylene out from propylene tower rectifying section side line, go out propane at the bottom of the tower;
(5). the C-4-fraction of depropanizing tower bottom enters depentanizer or enters deisobutanizer, also adopt side line to extract out after again the method for exchange obtain certain alkane alkene than the raw material for alkylation that requires;
(6). depropanizing tower and propylene cat head contain the absorption steady component of a large amount of propylene gas Returning catalyticing cracking devices, enter the absorption tower with liquefied petroleum gas (LPG), slough C-2-fraction after, enter depropanizing tower with liquefied petroleum gas (LPG) again.
Advantage of the present invention is:
1. separation column is after setting up vapor-liquid equilibrium, because the relative volatility difference of its each component, on different column plates, all there is different components to distribute, and the raw material for alkylation requirement is certain alkane alkene ratio, rather than the purity of certain content, the present invention utilizes these characteristics, after extracting out, mixes side line on the different column plates of depropanizing tower stripping section (perhaps taking off light carbon four towers and depentanizer) method of converting again, reaching alkane alkene ratio requires, not only avoided the separation between the difficulty grouping divides, and can save deisobutanizer, if only when be the MTBE raw material, side line is extracted out with regard to easier meeting the demands.
2. because being absorption steady component rough segmentation by catalytic cracking unit, the liquefied petroleum gas (LPG) of this device goes out C-2-fraction and C5 fraction enters this device later on, the present invention extracts C3 fraction out from the rectifying section side line of depropanizing tower, propylene is extracted out from the rectifying section side line of propylene tower, and after this gas that cat head has a large amount of propylene on two mixes, the absorption steady component rough segmentation that turns back to catalytic cracking unit again goes out C-2-fraction recirculation and returns, not only avoid the waste of propylene, saved deethanizing column again.
3. the present invention has reduced propylene loss 40%--50%; Saved deethanizing column and deisobutanizer and supporting coldly change, backflow and pump etc., reduced energy consumption and process cost.
The present invention is further described below in conjunction with the drawings and Examples knot:
Fig. 1 is the process flow sheet of prior art;
Fig. 2 is a process flow sheet of the present invention.
Wherein: 1. depropanizing tower; 2. deethanizing column; 3. propylene tower; 4. deisobutanizer; 5. depentanizer.
Embodiment: the gas fractionation process of the energy-conservation high yield of a kind of province's tower comprises the following steps:
(1). absorb the liquefied petroleum gas (LPG) that stabilizers is assigned to from catalytic cracking unit, after making with extra care, enter the depropanizing tower [1] of gas fractionation plant;
(2). extract C3 fraction out from depropanizing tower [1] upper rectifying section side line, enter propylene tower [3] and tell propylene and propane;
(3). divide three strands to extract MTBE raw materials and raw material for alkylation out from the suitable trays side line of depropanizing tower [1] stripping section, the control by each burst amount to it reaches certain alkane alkene ratio;
(4). extract propylene out from propylene tower [3] rectifying section side line, go out propane at the bottom of the tower;
(5). the C-4-fraction of depropanizing tower bottom enters depentanizer or enters deisobutanizer, also adopt side line to extract out after again the method for exchange obtain certain alkane alkene than the raw material for alkylation that requires;
(6). depropanizing tower [1] and propylene [3] cat head contain the absorption steady component of a large amount of propylene gas Returning catalyticing cracking devices, enter the absorption tower with liquefied petroleum gas (LPG), slough C-2-fraction after, enter depropanizing tower [1] with liquefied petroleum gas (LPG) again.
Gas fractionation plant as certain refinery, design in November, 96, go into operation in April, 98, this matching requirements takes off Trimethylmethane alkane tower and tells the MEBT raw material that still can satisfy certain alkane alkene ratio after the MEBT device reaction falls the iso-butylene component, it is representing the harsh requirement of deisobutanizer, at that time, though find the problems of old technology, and deisobutanizer is optimized, its tower than traditional design has been dwindled more than 30%, but still do not solve root problem, existing is example with this device, and the material balance under original design technology and the technology of the present invention is contrasted as following table:
| Sequence number | Name of material | Quantity | Remarks | |
| Original design | The present invention | |||
| 1 | Charging: liquefied petroleum gas (LPG) | 22701．2 | 22701．2 | |
| 2 | Discharging: propylene | 7356．7 | 7578．9 | |
| Propane | 2590．3 | 2870．4 | ||
| The MTBE raw material | 9897．8 | 9897．8 | ||
| Carbon four C5 fractions | 2675．5 | 2270．5 | ||
| Ethane gas and loss | 180．0 | 83．6 | Descend 53.6% | |
| Add up to | 22701．2 | 22701．2 |
As can be seen from Table 1, the optimization technology that invention is recommended improves 3% than intrinsic propone output, ethane gas descends 53.6%, and this ethane is to put to dry gas by the absorption steady component of FCCU, wherein propylene content is than much smaller when the deethanizing cat head is emitted, because this part is to make carbon two isolating by absorbing with desorb, this just means the loss that has reduced propylene most possibly.
In addition, because the present invention there is no need the C-4-fraction in the C3 fraction is separated fully, this need expend the bigger energy, therefore, carbon four content are higher in the propane, so propane fraction is bigger than intrinsic amount, simultaneously, carbon four C5 fractions are lower than original design value again, usually factory with these two cuts altogether as civil liquefied gas.
Following table is the comparison (kw) of former design and process heat of the present invention load
As can be seen from the above table, when adopting technique of the present invention, the cat head thermic load descends 12.2% than former design, and thermic load descends 7.4% than former design at the bottom of the tower, on average descends 9.8%.
| Cat head thermic load (kw) | Thermic load at the bottom of the tower (kw) | |||
| The tower title | Former design | After the improvement | Former design | After the improvement |
| Depropanizing tower | 2579.0 | 3304.7 | 2729.1 | 3802.3 |
| Dethanizer | 747.4 | 0 | 931.9 | 0 |
| Propylene tower | 10830.2 | 11747.9 | 10674.1 | 11728.2 |
| Deisobutanizer | 3326.8 | 0 | 2763.7 | 0 |
| The FCCU absorption tower | 0 | 290.8 | 0 | 300 |
| Add up to | 17483.2 | 15343.4 | 17098.8 | 15830.5 |
In addition, adopt technique of the present invention can also save 6 pumps, 2 stream tanks, 4 condensers reach supporting with it valve, pipe fitting, instrument, automatic control, civil engineering occupation of land etc., amount to more than 1,000 ten thousand yuan.
Claims (3)
1. a gas fractionation process of economizing the energy-conservation high yield of tower is characterized in that comprising the following steps:
(1) absorbs the liquefied petroleum gas (LPG) that stabilizers is assigned to from catalytic cracking unit, after making with extra care, enter the depropanizing tower of gas fractionation plant;
(2) extract C3 fraction out from depropanizing tower upper rectifying section side line, enter propylene tower and tell propylene and propane;
(3) divide multiply to extract MTBE raw material or raw material for alkylation out from the suitable trays side line of depropanizing tower stripping section, the control by each burst amount to it reaches certain alkane alkene ratio;
(4) extract propylene out from propylene tower rectifying section side line, go out propane at the bottom of the tower.
2. the gas fractionation process of the energy-conservation high yield of province's tower according to claim 1 is characterized in that: also comprise the following steps:
(5) C-4-fraction of depropanizing tower bottom enters depentanizer or enters deisobutanizer, also adopt side line to extract out after again the method for exchange obtain certain alkane alkene than the raw material for alkylation that requires.
3. the gas fractionation process of the energy-conservation high yield of province's tower according to claim 2 is characterized in that: also comprise the following steps:
(6) depropanizing tower and propylene cat head contain the absorption steady component of a large amount of propylene gas Returning catalyticing cracking devices, enter the absorption tower with liquefied petroleum gas (LPG), slough C-2-fraction after, enter depropanizing tower with liquefied petroleum gas (LPG) again.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN98110924A CN1065266C (en) | 1998-06-26 | 1998-06-26 | Efficient tower-less gas fractionation technology |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN98110924A CN1065266C (en) | 1998-06-26 | 1998-06-26 | Efficient tower-less gas fractionation technology |
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| Publication Number | Publication Date |
|---|---|
| CN1199767A CN1199767A (en) | 1998-11-25 |
| CN1065266C true CN1065266C (en) | 2001-05-02 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN98110924A Expired - Fee Related CN1065266C (en) | 1998-06-26 | 1998-06-26 | Efficient tower-less gas fractionation technology |
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Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100348286C (en) * | 2005-02-08 | 2007-11-14 | 华南理工大学 | Double tower gas fractionator and fractional method |
| US8119848B2 (en) * | 2008-10-01 | 2012-02-21 | Catalytic Distillation Technologies | Preparation of alkylation feed |
| CN101844961A (en) * | 2010-07-05 | 2010-09-29 | 茂名实华东成化工有限公司 | Method and device for efficiently recovering propylene from ethane gas at the top of dethanizing tower |
| CN102603456B (en) * | 2011-01-24 | 2015-01-21 | 中国石油化工集团公司 | Gas fractionation method |
| CN103012033A (en) * | 2011-09-22 | 2013-04-03 | 西安石油大学 | Method for separating propylene and propane from liquid hydrocarbon |
| CN108211404B (en) * | 2016-12-21 | 2023-09-05 | 中国石油化工股份有限公司 | Alkylation reaction device and alkylation reaction separation method |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1123306A (en) * | 1995-08-10 | 1996-05-29 | 抚顺石油化工公司石油二厂 | On-line optimizing and controlling method of balanced microcomputer for producing processed materials by gas separation unit |
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1998
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Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1123306A (en) * | 1995-08-10 | 1996-05-29 | 抚顺石油化工公司石油二厂 | On-line optimizing and controlling method of balanced microcomputer for producing processed materials by gas separation unit |
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| CN1199767A (en) | 1998-11-25 |
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