CN1683042A - Double-tower gas fractionation device and fractionation method - Google Patents
Double-tower gas fractionation device and fractionation method Download PDFInfo
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- CN1683042A CN1683042A CN 200510033178 CN200510033178A CN1683042A CN 1683042 A CN1683042 A CN 1683042A CN 200510033178 CN200510033178 CN 200510033178 CN 200510033178 A CN200510033178 A CN 200510033178A CN 1683042 A CN1683042 A CN 1683042A
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- Prior art keywords
- tower
- propylene
- pipeline
- product
- depropanizer
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- 238000000034 method Methods 0.000 title claims description 26
- 238000005194 fractionation Methods 0.000 title claims description 25
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims abstract description 88
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims abstract description 86
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims abstract description 24
- 239000001294 propane Substances 0.000 claims abstract description 12
- 239000007788 liquid Substances 0.000 claims description 11
- 239000002994 raw material Substances 0.000 claims description 11
- 238000010992 reflux Methods 0.000 claims description 9
- 238000000605 extraction Methods 0.000 claims description 8
- 238000009833 condensation Methods 0.000 claims 3
- 230000005494 condensation Effects 0.000 claims 3
- 239000007789 gas Substances 0.000 abstract description 35
- 239000000463 material Substances 0.000 abstract description 7
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 abstract description 4
- 239000003915 liquefied petroleum gas Substances 0.000 abstract description 3
- 238000009835 boiling Methods 0.000 abstract 2
- 230000008569 process Effects 0.000 description 20
- 230000008901 benefit Effects 0.000 description 16
- 241000282326 Felis catus Species 0.000 description 9
- 238000011084 recovery Methods 0.000 description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 5
- 238000004364 calculation method Methods 0.000 description 5
- 229910052799 carbon Inorganic materials 0.000 description 5
- 238000002309 gasification Methods 0.000 description 4
- 238000012360 testing method Methods 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 241000196324 Embryophyta Species 0.000 description 3
- 238000004458 analytical method Methods 0.000 description 3
- 230000002950 deficient Effects 0.000 description 3
- 238000012423 maintenance Methods 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 238000007599 discharging Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- BKOOMYPCSUNDGP-UHFFFAOYSA-N 2-methylbut-2-ene Chemical group CC=C(C)C BKOOMYPCSUNDGP-UHFFFAOYSA-N 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 240000004859 Gamochaeta purpurea Species 0.000 description 1
- BZLVMXJERCGZMT-UHFFFAOYSA-N Methyl tert-butyl ether Chemical compound COC(C)(C)C BZLVMXJERCGZMT-UHFFFAOYSA-N 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- GOOHAUXETOMSMM-UHFFFAOYSA-N Propylene oxide Chemical compound CC1CO1 GOOHAUXETOMSMM-UHFFFAOYSA-N 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- -1 polypropylene Polymers 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 238000011027 product recovery Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 1
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- Separation By Low-Temperature Treatments (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The double tower gas fractionator consists of propane eliminating tower, propylene tower, heat exchanger, pump container and connecting pipeline. It features the propane eliminating tower with condensating circulation loop in the top and re-boiling circulation loop in the bottom; and the propylene tower with condensating circulation loop in the top and re-boiling circulation loop in the bottom. The present invention can raise the quality of liquefied petroleum gas material and control the C2 component concentration in the material within 0.001-0.2 mol%, so as to reach the aim of eliminating ethane eliminating tower while obtaining relatively high propylene recovering rate, up to 98 %.
Description
Technical field
The present invention relates to petrochemical equipment and technology, specifically be meant no light-component gas discharging, high propylene rate of recovery double tower gas fractionator.
The invention still further relates to described double tower gas fractionator and be used for the method for fractionation.
Background technology
Gas fractionation unit is one of important oil refining process units.It is that liquefied petroleum gas is separated into propylene, propane, carbon four components and pentane product.The product of gas fractionation unit can be used as polypropylene plant, MTBE device and alkyl plant raw material.
At present, domestic prevailing traditional gas fractionation unit is a three-column process flow, promptly
---liquefied petroleum gas is introduced into depropanizing tower, with C2, and C3 component and heavier C4, the C5 component is separated;
---from the C2 that the depropanization cat head distillates, the C3 component enters the dethanizer fractionation, and the dethanizer main purpose is to remove light component C2, so that can obtain highly purified fine propylene (95～99.8) %, but when removing C2, a large amount of C3 also overflow from cat head;
---the still liquid that removes C2 enters propylene tower, finally obtains fine propylene and C3 still liquid.
C4 at the bottom of the depropanizing tower, the C5 component can enter decarburization four towers and depentanizer successively as also separating., but the less application of this five tower flow processs.
Described C2 refers to carbon two components such as ethene, ethane etc.;
Described C3 refers to carbon three components such as propylene, propane etc.;
Described C4 refers to carbon four components such as butylene, butane etc.;
Described C5 refers to carbon five components such as amylene, pentane etc.
In above-mentioned three-column process flow,, must light components such as ethane be removed from the C3 component by dethanizer in order to obtain the higher fine propylene product of purity.And the C2 component because of the rule of gas-liquid phase equilibrium, can make a part of propylene follow the C2 component together to overflow from cat head when removing from deethanizer overhead.The molar concentration of C3 component is usually all more than 60% in the deethanization cat head gas phase distillate, and this part gas to be the gas that acts as a fuel mostly burn, therefore cause a large amount of propylene loss.It has been near the limit that the existing three-column process flow propylene rate of recovery reaches 95%, is difficult to further improve again.
In the existing three-column process flow, propylene loss has three places: the one, and the still liquid of depropanizing tower, the 2nd, the cat head gas phase distillate of dethanizer, the 3rd, propylene tower tower bottoms body.
With certain 120,000 tons of gas fractionation unit is example, and its propylene loss is as shown in table 1:
Certain 120,000 tons of gas fractionation unit propylene loss of table 1
| Tower | Depropanizing tower | Dethanizer | Propylene tower |
| Technic index | Cat head C4, tower still C3 are all≤0.1% | Tower still ethane≤0.1%. | Fine propylene 〉=99.6%, tower still propane 〉=97%. |
| Propylene loss (kg/hr) | 9 | 232 | 53 |
| Propylene loss percentage (%) | 3.06 | 78.91 | 18.03 |
| Propylene feed amount (kg/hr) | 5166 | ||
| The propylene rate of recovery (%) | 94.3 | ||
From table 1 data as can be seen, the propylene loss rate of dethanizer is 78.91%, has accounted for the major part of gas fractionation unit propylene loss.Thereby to increase substantially the propylene rate of recovery, unique effective way is the cancellation dethanizer.
Summary of the invention
The objective of the invention is to defective at the prior art existence, a kind of double tower gas fractionator is provided, improve the quality index of material liquid liquefied oil gas, make that the C2 concentration of component is controlled in 0.001～0.2% (mol) scope in the raw material, thereby reach the purpose of cancellation dethanizer, and obtain the higher propylene rate of recovery (can reach more than 98%), reduce cost of equipment and operating cost simultaneously.
The present invention also aims to provide the method that adopts described double tower gas fractionator to be used for gas fractionation.
Double tower gas fractionator of the present invention is made of depropanizing tower, propylene tower and heat exchanger, pump, container and the pipeline that is connected them; The top that is characterized in depropanizing tower is provided with condensing circuit; The bottom of depropanizing tower is provided with the tower still closed circuit that boils again; The propylene tower top is provided with condensing circuit; Propylene tower bottom is provided with the tower still closed circuit that boils again.
Fig. 1 is apparatus of the present invention structural representations, as shown in the figure, depropanizing tower 2 overhead products outlets be connected by pipeline 7, pump 10, pipeline 8 successively between propylene tower 14 enters the mouth.The overhead product of propane tower 2 enters propylene tower 14 by this pipe-line system.
Depropanizing tower 2 tops are provided with condensing circuit, and condensing circuit is made of the loop that depropanizing tower 2 tops connecting pipe 3 successively, condenser 4, pipeline 5, return tank 6, pipeline 7, pump 10, pipeline 9 form.
Depropanizing tower 2 bottoms are provided with the tower still closed circuit that boils again, and the tower still closed circuit that boils again is made of the loop that depropanizing tower 2 bottoms connecting pipe 11 successively, reboiler 12, pipeline 13 form.
Depropanizing tower 2 bottoms are provided with bottom product output channel 29.
Propylene tower is provided with cat head fine propylene product extraction pipeline 20, or the tower rectifying section is provided with fine propylene product side line extraction pipeline 30 near the cat head place.
For example, connect the output channel 20 of fine propylene product on the pipeline 22.Perhaps the propylene tower rectifying section is established fine propylene product side line extraction pipeline 30, when material liquid gasification C2 forms when defective, can pass through the qualified fine propylene of this pipeline extraction; Guarantee that the fine propylene product is qualified all the time.
Be provided with tower still products export at the bottom of propylene tower 14 towers, connect pipeline 26, pump 27, the pipeline 28 of output tower still product successively.
The method that apparatus of the present invention are used for gas fractionation comprises:
---the C2 concentration of component in the control raw material is in 0.001～0.2% (mol), and the material liquid gasification enters depropanizing tower 2 through piping 1;
---the pressure of control depropanizing tower 2 is 1.6～2.2Mpa, and the phegma temperature is 30～50 ℃;
By adjusting reflux ratio, can control the quality of overhead product effectively;
Be provided with reboiler at the bottom of depropanizing tower (2) tower, be used for product quality at the bottom of the control tower.
---the overhead product of depropanizing tower 2 directly enters propylene tower 14; No longer resemble traditional process earlier through dethanizer.
---the pressure of control propylene tower 14 is 1.2～2.0Mpa, and the phegma temperature is 30～50 ℃; The bottom product of propylene tower 14 is a propane.
By adjusting reflux ratio, can control the quality of overhead product effectively.
Be provided with reboiler at the bottom of depropanizing tower (2) tower, be used for product quality at the bottom of the control tower.The bottom product of propylene tower (14) is a propane, and overhead product is the fine propylene of purity 95～99.8% (mol).
---when C2 concentration was qualified in the raw material, the propylene tower product was by 20 extraction of cat head pipeline.In case C2 excessive concentration in the discovery raw material can be heated up in a steamer a small amount of C2 component of jar gas phase pipeline 31 dischargings from returning from side line pipeline 30 extraction fine propylenes simultaneously as interim measure.So just guaranteed that double tower gas fractionator also can produce qualified fine propylene product under the defective condition of raw material.In case it is normal that raw material recovers, and then still changes back by pipeline 20 extraction propylene product.
The present invention compared with prior art has following advantage:
1, flow process is simple, propylene rate of recovery height
The present invention proposes double tower gas fractionation new technological process, promptly cancels original dethanizer, only keeps depropanizing tower and propylene tower, makes flow process simpler.
The double tower new technological process is realized by C2 concentration of component to 0.001～0.2% (mol) in the reduction material liquid gasification.The loss that the present invention has avoided propylene to be taken out of by deethanization cat head gas has improved product recovery rate, has reduced operating cost, can increase by 873.2 ten thousand yuan/year of benefits to 120,000 tons of gas fractionation units.Gas fractionation unit can separate the propylene in the material liquid gasification and purify to 95～99.8% (mol) purity.
2, investment and operating cost have been saved
The present invention has cancelled parts and connecting pipes such as dethanizer and attached pump, heat exchanger, has reduced equipment investment significantly.In addition, also saved the operating maintenance expense of dethanizer and auxiliary device.
The specific embodiment
Certain 120,000 tons of gas fractionation unit, former employing three-column process flow, deethanizer overhead continuous blow-down deethanization gas.Density of propylene is controlled at below 0.1% in the depropanization tower bottoms, and the actual analysis value often is zero, also is that depropanization Tata still propylene loss is very little, and per hour propylene loss is only about 10kg.Propylene tower bottoms propane concentration is controlled at and is not less than 97%, and actual propane concentration is through being everlasting about 98%, and all the other are propylene, and this still liquid per hour propylene loss is controlled at below the 60kg.The device propylene rate of recovery remains on about 95% for a long time, so most of propylene loss system is overflowed by deethanizer overhead.
This is installed on and cuts place's dethanizer test in March, 2004.The test duration of test is as follows according to the relevant technological parameter summary of the record of production:
C2 concentration is controlled at below 0.03% (mol) in the raw material;
Depropanizing tower operating pressure 1.78Mpa, 35～36 ℃ of reflux temperatures, 45～47 ℃ of tower top temperatures, 108 ℃ of tower still temperature.
Propylene tower operating pressure 1.36Mpa, 30.7～31 ℃ of reflux temperatures, 32.1～32.4 ℃ of tower top temperatures, 44～44.8 ℃ of tower still temperature.Test was turned round 17 days continuously, and the fine propylene product design is 99.7～99.92% (vol%), and depropanization tower bottoms density of propylene is 0～0.03% (vol%), and propylene tower bottoms concentration is 97.3～98.3% (vol%).
Economic and Efficiency Analysis relatively
The quality of commercial plant is on the present economic benefit of final body.Be research object now, will compare by result of calculation and original flow process of new technological process among the present invention with certain 120,000 tons of gas fractionation unit.Investigate the product yield and the public work consumption of two kinds of flow processs, analyze economic benefit separately.Device benefit calculation and product price, public work price are contacted directly since these prices in time, the region fluctuation is bigger, therefore relatively must carry out detailed benefit calculation and just can obtain in conjunction with concrete condition at the benefit of certain gas fractionation unit.
Benefit Calculation
Benefit calculation adopts following formula: benefit=product sales revenue-operating cost
The Economic and Efficiency Analysis is here just made comparisons to the economic benefit of two kinds of flow processs, therefore can only consider product sales revenue and operating cost.
Product price relevant with gas fractionation unit and public work price are as follows:
5000 yuan/ton of fine propylenes, 1000 yuan/ton of fuel gas, 0.5 yuan/ton of recirculated water, 90 yuan/ton of steam.
The benefit benchmark
The present invention and three-column process flow compare under the same conditions, stipulate following benchmark:
(1) two kind of flow process raw material is just the same;
(2) quality requirement of each product is just the same, and requiring purified propylene in the fine propylene product is 99.6% (mol), and requiring purified propylene oxide in the propane product is 97% (mol).
(3) the tower still reboiler of new technological process saving is pressed the valuation of equivalent steam, and the condenser duty of saving is pressed the valuation of equivalent recirculated water.
(4) suppose former flow process deethanization gas discharge fuel tracheae net.
Economic benefit is calculated
The propylene rate of recovery increases the economic benefit that produces
Behind the cancellation dethanizer, tower overhead gas no longer discharges, and then the propylene volume increase is 232kg/hr, if year operation hour was equivalent to can increase every year 1856 tons of propone outputs by 8000 hours.Fine propylene and fuel gas price difference are 4000 yuan/ton, and then the propylene recovery section year economic benefit of Zeng Jiaing is 742.4 ten thousand yuan.
3.3.2 save operation, the maintenance cost of dethanizer
According to analog computation, the condenser of former dethanizer and the thermic load of reboiler are respectively-0.485Mkcal/h and 0.566Mkcal/h.If valuate by recirculated water and steam, then water rate and steam expense is respectively 24.4 ten thousand yuan/year and 86.4 ten thousand yuan/year.Add up to 110.8 ten thousand yuan/year.
The maintenance of equipment expense of dethanizer is by average 200,000 yuan/year.
Behind the cancellation dethanizer, can reduce 2 of pumps, its operating cost is saved and wouldn't be counted.
120,000 tons of above-mentioned three expenses savings of gas fractionation unit are increased by 873.2 ten thousand yuan/year of benefits altogether.
Claims (5)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100331787A CN100348286C (en) | 2005-02-08 | 2005-02-08 | Double tower gas fractionator and fractional method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100331787A CN100348286C (en) | 2005-02-08 | 2005-02-08 | Double tower gas fractionator and fractional method |
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| Publication Number | Publication Date |
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| CN1683042A true CN1683042A (en) | 2005-10-19 |
| CN100348286C CN100348286C (en) | 2007-11-14 |
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| CNB2005100331787A Expired - Fee Related CN100348286C (en) | 2005-02-08 | 2005-02-08 | Double tower gas fractionator and fractional method |
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| Country | Link |
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| CN (1) | CN100348286C (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102500119A (en) * | 2011-09-22 | 2012-06-20 | 天津大学 | Internal energy integration non-compression reflux device for ethylene separation and process flow thereof |
| CN102603456A (en) * | 2011-01-24 | 2012-07-25 | 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 |
| CN104140349A (en) * | 2014-07-16 | 2014-11-12 | 西安石油大学 | Novel light hydrocarbon separation system and method for LNG |
| US9234142B2 (en) | 2014-02-26 | 2016-01-12 | Uop Llc | Process and apparatus for hydroprocessing with two product fractionators |
| US10041008B2 (en) | 2014-02-26 | 2018-08-07 | Uop Llc | Process and apparatus for hydroprocessing with two product fractionators |
| WO2019019034A1 (en) * | 2017-07-26 | 2019-01-31 | 深圳市宏事达能源科技有限公司 | Gas fractionation device |
| CN113563917A (en) * | 2021-08-23 | 2021-10-29 | 中国石油化工股份有限公司 | Separation process and separation device for sulfuric acid alkylation reaction product |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1065266C (en) * | 1998-06-26 | 2001-05-02 | 诸雅志 | Efficient tower-less gas fractionation technology |
-
2005
- 2005-02-08 CN CNB2005100331787A patent/CN100348286C/en not_active Expired - Fee Related
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102603456A (en) * | 2011-01-24 | 2012-07-25 | 中国石油化工集团公司 | Gas fractionation method |
| CN102603456B (en) * | 2011-01-24 | 2015-01-21 | 中国石油化工集团公司 | Gas fractionation method |
| CN102500119A (en) * | 2011-09-22 | 2012-06-20 | 天津大学 | Internal energy integration non-compression reflux device for ethylene separation and process flow thereof |
| CN103012033A (en) * | 2011-09-22 | 2013-04-03 | 西安石油大学 | Method for separating propylene and propane from liquid hydrocarbon |
| US9234142B2 (en) | 2014-02-26 | 2016-01-12 | Uop Llc | Process and apparatus for hydroprocessing with two product fractionators |
| US10041008B2 (en) | 2014-02-26 | 2018-08-07 | Uop Llc | Process and apparatus for hydroprocessing with two product fractionators |
| CN104140349A (en) * | 2014-07-16 | 2014-11-12 | 西安石油大学 | Novel light hydrocarbon separation system and method for LNG |
| CN104140349B (en) * | 2014-07-16 | 2015-12-02 | 西安石油大学 | A kind of lighter hydrocarbons tripping device of natural gas liquids and method |
| WO2019019034A1 (en) * | 2017-07-26 | 2019-01-31 | 深圳市宏事达能源科技有限公司 | Gas fractionation device |
| CN113563917A (en) * | 2021-08-23 | 2021-10-29 | 中国石油化工股份有限公司 | Separation process and separation device for sulfuric acid alkylation reaction product |
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| Publication number | Publication date |
|---|---|
| CN100348286C (en) | 2007-11-14 |
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