CN102703113A - Light gasoline and heavy gasoline separating method - Google Patents
Light gasoline and heavy gasoline separating method Download PDFInfo
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- CN102703113A CN102703113A CN2012101670891A CN201210167089A CN102703113A CN 102703113 A CN102703113 A CN 102703113A CN 2012101670891 A CN2012101670891 A CN 2012101670891A CN 201210167089 A CN201210167089 A CN 201210167089A CN 102703113 A CN102703113 A CN 102703113A
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Abstract
A light gasoline and heavy gasoline separating method belongs to the technical field of petrochemicals and is used for reducing energy consumption in a light gasoline and heavy gasoline separating process and solving a problem of salt coagulation in the separating process. The light gasoline and heavy gasoline separating method is realized in a main fractionating tower; a light gasoline and heavy gasoline separating component is designed into an upper section and a lower section; a dewatering facility is arranged between the two sections; a heavy gasoline stripping tower is arranged; the dewatering facility arranged between the two sections leads water-containing oil at the bottom of the upper light gasoline and heavy gasoline separating section out of the main fractionating tower; and the water-containing oil is dewatered by a dewatering tank, pressurized by a pump and heated by a heater and returns to the upper part of the lower light gasoline and heavy gasoline separating section of the fractionating tower. The light gasoline and heavy gasoline separating method is low in energy consumption in the light gasoline and heavy gasoline separating process, can completely solve the problem of salt coagulation on the upper part of the fractionating tower and is applied to a petroleum processing device with a light gasoline and heavy gasoline separating requirement.
Description
Technical field
The invention belongs to the petrochemical technology field, particularly a kind of weight gasoline separation method.
Background technology
In petroleum refining process, often using weight gasoline separates.Full distillation gasoline boiling range is over point～205 ℃, and the petroleum naphtha boiling range is over point～100 ℃, and the heavy petrol boiling range is 100 ℃～205 ℃.The petroleum naphtha olefin(e) centent is high, octane value is high, sulphur content is low, is fit to do the raw material of ether-based device.The heavy petrol olefin(e) centent is relatively low, octane value is relatively low, sulphur content is high, is fit to do gasoline hydrodesulfurizationmethod device raw material.Therefore petroleum chemical enterprise need separate light, heavy petrol to process respectively.Petroleum chemical enterprise adjusts the product mix, and increases petroleum naphtha etherificate, heavy petrol hydrogenation unit, adopts the original production device motionless at present usually, sets up the weight gasoline separation tower separately.This method is with full distillation gasoline heating, gets into then in the weight gasoline separation tower, reboiler is set at the bottom of the tower to rectifying heat is provided, and cat head petroleum naphtha oil gas obtains the petroleum naphtha product after cooling, and part is returned the knockout tower top as backflow.This method need be imported a large amount of heats for keeping distillation operation at the bottom of tower, so this method energy consumption is high.
Summary of the invention
The purpose of this invention is to provide a kind of weight gasoline separation method, reduce weight gasoline sepn process energy consumption significantly, and thoroughly solve sepn process salt crust problem.
The technical solution adopted for the present invention to solve the technical problems is: weight gasoline is separated in the main fractionating tower and carries out; Weight gasoline separative element is set on separation column top; The heavy petrol stripping tower is set, and weight gasoline separative element is designed to 2 sections up and down, the intersegmental dehydration facility that is provided with.
Described weight gasoline separative element is a column plate, or filler, or column plate, filler mix.
The dehydration facility is weight gasoline to be separated the moisture oil product in epimere bottom draw outside the tower between described weight gasoline segregation section, returns separation column weight gasoline separation hypomere top through water knockout dehydration, pump supercharging and heater heats or after not heating.
Described weight gasoline separates the epimere bottom oil header is set, and oil header is provided with liquidometer, controls out tower oil product flow; Or oil header is not provided with liquidometer, and oil product is drawn from the oil header riser and returned weight gasoline through water knockout dehydration back gravity flow and separate above the hypomere.
Described fractionation cat head adopts cold reflux, or thermal backflow, or pump around circuit.
Described heavy petrol stripping tower separative element is a column plate, or filler, or column plate, filler mix; Or the heavy petrol stripping tower is not set.
Catalytic cracking, coking process process petroleum naphtha, heavy petrol get into separation column with gas phase state, and weight gasoline is separated in does not then need extra input heat in the main fractionating tower, and weight gasoline sepn process energy consumption is reduced significantly.
RFCC, coking process process reaction oil gas contain a large amount of water vapors; Along with oil gas upwards flows, temperature and water vapor saturation ratio reduce, and carry out when weight gasoline is separated in the main fractionating tower in separation column; Tower top temperature further reduces, and makes water vapor condensation.RFCC and coking raw material oil contain impurity such as nitride, sulfide and inorganic salt; Nitrogen compound and inorganic salt resolve into NH3 and HCl under hot conditions; Under the hot environment of separation column bottom, exist,, then water of condensation can occur when following when temperature drops to the water vapor dew-point temperature along with oil gas upwards flows with NH3 and HCl gas phase form; NH3 combines with HCl to generate the NH4Cl and the formation NH4Cl aqueous solution soluble in water, and the NH4CL aqueous solution is with internal reflux to lower floor tower tray.Separate the epimere bottom at weight gasoline and be provided with oil header, the brackish water oil product is collected and all drawn tower carry out processed outward.Dehydration back oil product returns separation column weight gasoline and separates the hypomere top after pump supercharging, heater heats.
Innovative point of the present invention and positively effect:
Innovative point of the present invention is: weight gasoline is separated in the main fractionating tower and carries out, and weight gasoline separative element is designed to 2 sections up and down, the intersegmental dehydration facility that is provided with; Return separation column weight gasoline after the oil product heater via heating after the dehydration and separate the hypomere top.
Positively effect of the present invention is: the sepn process of weight gasoline does not need a large amount of heats of extra input, and weight gasoline sepn process energy consumption is reduced significantly, and separation column top salt crust not.
Description of drawings
Fig. 1 is a kind of synoptic diagram of weight gasoline separation method.
1-epimere separative element, the intersegmental oil header of 2-, 3-hypomere separative element, 4-bottom oil header, 5-separation column, 6-high-temperature oil gas; 7-refluxes, 8-liquidometer, the intersegmental oil product of 9-, 10-water knockout, 11-brackish water, the intersegmental oil pump of 12-, 13-variable valve; The 14-interchanger, 15-heavy petrol stripping column plate, 16-heavy petrol stripping tower, 17-stripped vapor, 18-heavy petrol pump; 19-heavy petrol water cooler, the big and heavy gasoline of 20-, 21-stripping oil gas, 22-heavy petrol product, 23-fractionation cat head oil gas.
Fig. 2 is the synoptic diagram of another kind of weight gasoline separation method.
1-epimere separative element, the intersegmental oil header of 2-, 3-hypomere separative element, 4-bottom oil header, 5-separation column, 6-high-temperature oil gas; 7-fractionation cat head oil gas, 8-liquidometer, the intersegmental oil product of 9-, 10-water knockout, 11-brackish water, the intersegmental oil pump of 12-, 13-variable valve; The 14-interchanger, 15-heavy petrol stripping column plate, 16-heavy petrol stripping tower, 17-stripped vapor, 18-heavy petrol pump, 19-heavy petrol water cooler; The big and heavy gasoline of 20-, 21-stripping oil gas, 22-heavy petrol product, 23-is dutiful from element on the top, and 24-follows oil header in the top, and 25-follows oil in the top; 26-follows oily water knockout in the top, and 27-follows oily brackish water in the top, and 28-follows oil pump in the top, and 29-follows oil heat exchanger in the top, and 30-follows oil cooler in the top.
Embodiment
Fig. 1 provides a kind of synoptic diagram of weight gasoline separation method, and this scheme fractionation cat head adopts cold reflux.Separation column 5 tops are provided with 2 sections weight gasoline separative elements, epimere separative element 1 and hypomere separative element 3; Also have 2 oil headers, intersegmental oil header 2 and bottom oil header 4.Intersegmental dehydration facility comprises 10-water knockout, the intersegmental oil pump of 12-, 13-variable valve 14-interchanger.Heavy petrol stripping tower system comprises heavy petrol stripping tower 16, heavy petrol stripping column plate 15, heavy petrol pump 18, heavy petrol water cooler 19.
High-temperature oil gas 6 gets into from separation column 5 bottoms, in tower on flow into weight gasoline separated region.Big and heavy gasoline 20 heavy petrol segregation section bottom oil header 4 is on the lenient side drawn; To heavy petrol stripping tower 16; Be provided with 4-6 piece column plate 15 in it; Feed stripped vapor 17 in its underpart, discharge stripping oil gas 21 at its top, the heavy petrol behind the stripping obtains heavy petrol product 22 and carrying device behind heavy petrol pump 18, heavy petrol water cooler 19.Oil gas continues upwards to flow into weight gasoline segregation section middle part in the tower; Intersegmental oil product 9 leads to water knockout 10 from intersegmental oil header 2; Deviate from brackish water 11; Between the intersegmental oil product approach section after the dehydration in the oil pump 12, supercharging is after variable valve 13 (by oil product flow between liquidometer 8 control sections), interchanger 14 controlled temperature return separation column hypomere separative element 3 upper positions.Oil gas continues upwards to flow through epimere separative element 1 in the tower, and fractionation cat head oil gas 23 flows out from cat head, refluxes 7 to get into from epimere separative element 1 top.
Fig. 2 provides the synoptic diagram of another kind of weight gasoline separation method, and this scheme fractionation cat head adopts pump around circuit.Separation column 5 tops are provided with 3 sections separative elements, are dutiful from element 23, epimere separative element 1 and hypomere separative element 3 in the top; Also have 3 oil headers, oil header 24, intersegmental oil header 2 and bottom oil header 4 follow on the top.Intersegmental dehydration facility comprises water knockout 10, intersegmental oil pump 12, variable valve 13, interchanger 14.The top is followed the dehydration facility and is comprised that oily water knockout 26 is followed on the top, oil pump 28 is followed on the top, and oil heat exchanger 29 is followed on the top, and oil cooler 30 follows on the top.Heavy petrol stripping tower system comprises heavy petrol stripping tower 16, heavy petrol stripping column plate 15, heavy petrol pump 18, heavy petrol water cooler 19.
High-temperature oil gas 6 gets into from separation column 5 bottoms, in tower on flow into weight gasoline separated region.Big and heavy gasoline 20 heavy petrol segregation section bottom oil header 4 is on the lenient side drawn; To heavy petrol stripping tower 16; Be provided with 4-6 piece column plate 15 in it; Feed stripped vapor 17 in its underpart, discharge stripping oil gas 21 at its top, the heavy petrol behind the stripping obtains heavy petrol product 22 and carrying device behind heavy petrol pump 18, heavy petrol water cooler 19.Oil gas continues upwards to flow into weight gasoline segregation section middle part in the tower; Intersegmental oil product 9 leads to water knockout 10 from intersegmental oil header 2; Deviate from brackish water 11; Between the intersegmental oil product approach section after the dehydration in the oil pump 12, supercharging is after variable valve 13 (by oil product flow between liquidometer 8 control sections), interchanger 14 controlled temperature return separation column hypomere separative element 3 top positions.Oil gas continues upwards to flow through epimere separative element 1 entering top pump around circuit section in the tower; The top is followed oil 25 and is followed oil header 24 from the top and lead to the top and follow oily water knockout 26; Deviate from the top and follow oily brackish water 27; Top after the dehydration is followed oil entering top and is followed in the oil pump 28, and supercharging is after oil heat exchanger 29 is followed on the top, the top is followed oil cooler 30 and returned fractionation top pumparound section top position.Last fractionation cat head oil gas 7 flows out from separation column 5 tops.
Claims (6)
1. weight gasoline separation method; Weight gasoline is separated in the main fractionating tower and carries out, and weight gasoline separative element is set on separation column top, and the heavy petrol stripping tower is set; It is characterized in that weight gasoline separative element being designed to 2 sections up and down, the intersegmental dehydration facility that is provided with.
2. weight gasoline separation method according to claim 1 is characterized in that: weight gasoline separative element is a column plate, or filler, or column plate, filler mix.
3. weight gasoline separation method according to claim 1; It is characterized in that: the dehydration facility is weight gasoline to be separated the moisture oil product in epimere bottom draw outside the tower between weight gasoline segregation section, returns separation column weight gasoline separation hypomere top through water knockout dehydration, pump supercharging and heater heats or after not heating.
4. weight gasoline separation method according to claim 1 is characterized in that: weight gasoline separates the epimere bottom oil header is set, and oil header is provided with liquidometer, controls out tower oil product flow; Or oil header is not provided with liquidometer, and oil product is drawn from the oil header riser and returned weight gasoline through water knockout dehydration back gravity flow and separate above the hypomere.
5. weight gasoline separation method according to claim 1 is characterized in that: the fractionation cat head adopts cold reflux, or thermal backflow, or pump around circuit.
6. weight gasoline separation method according to claim 1 is characterized in that: heavy petrol stripping tower separative element is a column plate, or filler, or column plate, filler mix; Or the heavy petrol stripping tower is not set.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012101670891A CN102703113A (en) | 2012-05-28 | 2012-05-28 | Light gasoline and heavy gasoline separating method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012101670891A CN102703113A (en) | 2012-05-28 | 2012-05-28 | Light gasoline and heavy gasoline separating method |
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| CN102703113A true CN102703113A (en) | 2012-10-03 |
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| CN2012101670891A Pending CN102703113A (en) | 2012-05-28 | 2012-05-28 | Light gasoline and heavy gasoline separating method |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106433771A (en) * | 2016-10-26 | 2017-02-22 | 华南理工大学 | Low-energy-consumption catalytic cracking and catalytic gasoline selective hydrogenation combined process |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201272777Y (en) * | 2008-05-15 | 2009-07-15 | 中国石油天然气股份有限公司 | Circulating dewatering device of gasoline/diesel fractionating column top |
| CN101580731A (en) * | 2008-05-15 | 2009-11-18 | 中国石油天然气股份有限公司 | Method for raising diesel yield through gasoline-diesel fractionating towers |
| CN102250635A (en) * | 2010-05-21 | 2011-11-23 | 中国石油化工集团公司 | Method and device for removing salt for fractionate tower |
-
2012
- 2012-05-28 CN CN2012101670891A patent/CN102703113A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201272777Y (en) * | 2008-05-15 | 2009-07-15 | 中国石油天然气股份有限公司 | Circulating dewatering device of gasoline/diesel fractionating column top |
| CN101580731A (en) * | 2008-05-15 | 2009-11-18 | 中国石油天然气股份有限公司 | Method for raising diesel yield through gasoline-diesel fractionating towers |
| CN102250635A (en) * | 2010-05-21 | 2011-11-23 | 中国石油化工集团公司 | Method and device for removing salt for fractionate tower |
Non-Patent Citations (2)
| Title |
|---|
| 刘建新等: "分馏塔顶循环脱水技术在催化裂化装置中的应用研究", 《石油炼制与化工》 * |
| 张华东等: "重油催化裂化装置分馏塔顶循环回流脱水新技术", 《炼油技术与工程》 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106433771A (en) * | 2016-10-26 | 2017-02-22 | 华南理工大学 | Low-energy-consumption catalytic cracking and catalytic gasoline selective hydrogenation combined process |
| CN106433771B (en) * | 2016-10-26 | 2018-04-13 | 华南理工大学 | A kind of catalytic cracking of low energy consumption and catalytic gasoline selective hydrogenation process integration |
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Address after: 100011, Beijing, Dongcheng District, 136 Wai Wai Street, imperial international A block 4, A0406-025 Applicant after: Li Xiaoyan Address before: 100013 Beijing, Dongcheng District Anwai garden 9 Building 5 No. 303 Applicant before: Li Xiaoyan |
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Application publication date: 20121003 |