CN101906318A - Method and device for upgraded recycle of energy of raffinate tower and extract tower - Google Patents
Method and device for upgraded recycle of energy of raffinate tower and extract tower Download PDFInfo
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- CN101906318A CN101906318A CN2010102426797A CN201010242679A CN101906318A CN 101906318 A CN101906318 A CN 101906318A CN 2010102426797 A CN2010102426797 A CN 2010102426797A CN 201010242679 A CN201010242679 A CN 201010242679A CN 101906318 A CN101906318 A CN 101906318A
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Abstract
The invention discloses a method and a device for upgraded recycle of energy of a raffinate tower and an extract tower in a molecular sieve dewaxing device. The method comprises the steps of: respectively performing heat transfer and temperature reduction to the column plate liquid extracted from the raffinate tower and the extract tower and the heating medium with temperature lower than that the column plate liquid, and raising the temperature of the heating medium; returning the temperature-reduced column plate liquid to the raffinate tower and the extract tower respectively; and recycling the energy in the raffinate tower and the extract tower by using the temperature-raised heating medium as a heat source of a heat sink . The device realizing the method comprises the raffinate tower and the extract tower, wherein a middle reflux device I and a middle reflux device II are respectively arranged above the feed ports of the raffinate tower and the extract tower. The invention can equally reduce the cooling load at the tops of the towers after removing heat by reflux in the middle reflux devices and is beneficial to overcoming the shortcoming that the operation is instable because of the high environment temperature and difficult cooling in summer.
Description
Technical field
The invention belongs to the refining of petroleum field, particularly a kind of method and device with raffinate tower in the molecular sieve dewaxing unit and the upgrade recycling of Extract tower energy.
Background technology
Dewaxing by molecular sieve is under isothermal, equipressure, liquid-phase condition, the process of utilizing the selection characterization of adsorption of molecular sieve to isolate normal paraffin from virgin kerosene, produce paraffin.The basic procedure of dewaxing by molecular sieve is with the prefractionation of raw material virgin kerosene elder generation, cuts the boiling range that satisfies product requirement, and hydrofining then removes sulphur, nitrogen, arsenic etc. to the deleterious impurity of molecular sieve, isolates H by stripping tower again
2S, NH
3Deng, obtain kerosene raffinate; Kerosene raffinate is being equipped with solid adsorbent (by positive structure C
5With isomery C
8Form) fixed bed in simulation moving-bed mode and sorbent material counter current contact, the positive structure C of sorbent material
5Part removes normal paraffin in the kerosene, and the Extract of formation (mixed solution of normal paraffin and desorbing agent) enters in the Extract tower, isolates normal paraffin by fractionated method from Extract, and reclaims desorbing agent, recycles; Sorbent material isomery C
8Part removes isoparaffin in the kerosene, and the raffinate of formation (mixed solution of isoparaffin and desorbing agent) enters in the raffinate tower, isolates isoparaffin by fractionated method from raffinate, and reclaims desorbing agent, recycles;
The flow process of raffinate tower is: the raffinate from dewaxing by molecular sieve unit tempering tank comes, enter the raffinate tower, and the cat head gas phase is told cold reflux and desorbing agent through air cooling and laggard minute flow container of water-cooled cooling.Be rich in isomery C
8Side stream extract out from the tower intercepting basin, after pressurization, part is returned tower as backflow, part is merged into the desorbing agent stripping tower with Extract tower side line; Obtain non-n-alkane at the bottom of the tower, after heat exchange, cooling, send the tank field; Full tower provides heat by the tower reboiler.
The flow process of Extract tower is: the Extract that comes from dewaxing by molecular sieve unit tempering tank after converging with washing fluid, enters the Extract tower; The cat head gas phase is cooled off into minute flow container through air cooling and water-cooled, tells cold reflux and desorbing agent.Extracting side line out converges through pump pressurization back and raffinate tower side line and send the stripping tower top; At the bottom of the tower C
10～C
14Normal paraffin is delivered to the aftercut unit and is further separated; Full tower provides heat by tower bottom reboiler.
No matter be raffinate tower or Extract tower, their chargings heats going along with and a large amount of higher potential temperatures that tower bottom reboiler provides except that small part is taken away by tower base stream, have all degraded into the cat head cooling load; Tower top temperature is all not high simultaneously, reclaims very difficult under the existing engineering condition.This just means also that in molecular sieve dewaxing unit Extract tower and raffinate tower the energy of a large amount of higher quality is seriously degraded.Therefore, be necessary under the prerequisite that does not influence product yield and quality, change into callable heat and be used the upgrading of cat head low temperature exhaust heat.
Summary of the invention
Primary and foremost purpose of the present invention is to overcome raffinate tower and Extract tower energy degradation is serious, the cat head cooling load is big shortcoming, and the method for a kind of raffinate tower and the upgrade recycling of Extract tower energy is provided.
Another object of the present invention is to provide the device of realizing aforesaid method.
Purpose of the present invention is achieved through the following technical solutions: the method for a kind of raffinate tower and the upgrade recycling of Extract tower energy comprises following steps:
(1) carries out the heat exchange cooling, the rising of heating medium temperature from raffinate tower column plate liquid phase of extracting out and the heating medium that temperature is lower than the column plate liquid phase; Column plate liquid phase after the cooling turns back on the column plate of raffinate tower again, and promptly the column plate liquid phase turns back to and returns on the column plate; The extraction amount of column plate liquid phase is according to returning column plate and near the column plate of cat head dry plate not for guaranteeing to be next to;
(2) carry out the heat exchange cooling, the rising of heating medium temperature from Extract tower column plate liquid phase of extracting out and the heating medium that temperature is lower than the column plate liquid phase; Column plate liquid phase after the cooling is returned on the column plate of Extract tower again, and promptly the column plate liquid phase turns back to and returns on the column plate; The extraction amount of column plate liquid phase is according to returning column plate and near the column plate of cat head dry plate not for guaranteeing to be next to;
(3) heating medium of the rising of the temperature in step (1) and the step (2) is used to do the thermal source of other hot traps, thereby the energy of raffinate tower and Extract tower obtains recycling;
(4) operating parameters of adjustment Extract tower and raffinate tower, the influence behind the rounding backflow heat-obtaining;
The extraction optimum seeking site of column plate liquid phase described in the step (1) is from down several the 9th～11 block of plates of cat head;
The home position of the column plate liquid phase described in the step (1) after the cooling is preferably from down several the 7th～9 block of plates of cat head;
Distance between described extraction position and the home position be at least 2 plate spacings from;
The extraction optimum seeking site of column plate liquid phase described in the step (2) is from down several the 8th～10 block of plates of cat head;
The home position of the column plate liquid phase described in the step (2) after the cooling is preferably from down several the 6th～8 block of plates of cat head;
Distance between described extraction position and the home position be at least 2 plate spacings from;
The method of adjusting the operating parameters of Extract tower and raffinate tower described in the step (4) is preferably the flowsheeting technology of utilizing, implement raffinate tower and simulation of Extract tower whole process and optimization after the stage casing backflow is set up, with operating parameterss such as corresponding adjustment cold reflux amounts, guarantee product yield and quality;
Realize the device of described method, comprise raffinate tower and Extract tower, wherein, stage casing reflux I is set above the opening for feed of raffinate tower, stage casing reflux II is set above the opening for feed of Extract tower; Stage casing reflux I comprises and extracts out mouthful, returns tower mouth and heat-exchanger rig, extracts out mouthful and returns the tower mouth and be connected with the raffinate tower; Stage casing reflux II comprises and extracts out mouthful, returns tower mouth and heat-exchanger rig, extracts out mouthful and returns the tower mouth and be connected with the Extract tower;
Described stage casing reflux I is preferably it and extracts mouth out and be arranged at the 9th～11 Board position (first block of plate of cat head is numbered 1) at the raffinate tower, returns the tower mouth and is arranged at the 7th～9 block of plate at the raffinate tower; Return the tower mouth with extract out mouth be separated by at least 2 plate spacings from;
Described stage casing reflux II is preferably it and extracts mouth out and be arranged at the 8th～10 Board position (first block of plate of cat head is numbered 1) at the Extract tower, returns the tower mouth and is arranged at the 6th～8 block of plate at the Extract tower; Return the tower mouth with extract out mouth be separated by at least 2 plate spacings from;
The heat-exchanger rig of described stage casing reflux I is preferably interchanger;
The heat-exchanger rig of described stage casing reflux II is preferably interchanger.
Principle of the present invention is: raffinate tower and Extract tower are behind stage casing backflow heat-obtaining, but equivalent reduces the cat head cooling load.Because the stage number of raffinate tower and Extract tower is more, the stage casing reflux is set does not influence product yield and quality substantially, and its fluctuation can obtain rounding by adjusting operating parameterss such as cat head cold reflux.
The present invention has following advantage and beneficial effect with respect to prior art:
1, the present invention has realized raffinate tower and the upgrading of Extract tower energy, the unrenewable cat head waste heat of script is changed into the stage casing backflow heat of the suitable higher potential temperature that reclaims;
2, the present invention has reduced the cat head cooling load of raffinate tower and Extract tower, helps overcoming the shortcomings such as fluctuation of service that summer environment temperature height, cooling difficulty cause simultaneously;
3, among the present invention reflux and exported net heat in the stage casing of raffinate tower and Extract tower, for other hot traps provide thermal source;
4, workflow reengineering of the present invention is simple, feasible, and newly-increased stage casing recuperator can be arranged in ground, need not increase the heat exchange framework newly.
Description of drawings
Fig. 1 is the raffinate tower and the Extract tower process schema of prior art: wherein
The 1-raffinate, 2-raffinate tower, 3-cat head oil gas, the 4-cold reflux, 5-contains isomery C
8More desorbing agent, 6-raffinate tower side line, isoparaffin at the bottom of the 7-tower, the 8-Extract, the washing fluid that 9-is new, 10-Extract tower, 11-cat head oil gas, the 12-cold reflux, 13-contains positive structure C
5More desorbing agent, 14-Extract tower side line, normal paraffin at the bottom of the 15-tower, the 16-stripper overhead gas, 17-washing fluid, reboiler at the bottom of the 18-raffinate Tata, reboiler at the bottom of the 19-Extract Tata, 20-raffinate column overhead air cooling device, 21-raffinate column overhead water cooling plant, 22-raffinate column overhead is divided flow container, 23-Extract column overhead air cooling device, 24-Extract column overhead water cooling plant, 25-Extract column overhead is divided flow container, the washing fluid that 26-is new; Mark is that collinear represents it is logistics among the figure, other shapes be equipment configuration.
Fig. 2 is raffinate tower of the present invention and Extract tower process schema:
Wherein: 1～26 same Fig. 1,27-stage casing reflux I, 28-stage casing reflux II, 29-interchanger, 30-interchanger; Mark is that collinear represents it is logistics among the figure, other shapes be equipment configuration.
Embodiment
The present invention is described in further detail below in conjunction with embodiment and accompanying drawing, but the working of an invention mode is not limited thereto.
Comparative example (the raffinate tower of prior art and Extract tower process flow process, as shown in Figure 1)
Enter the 30th plate of raffinate tower 2 from the next raffinate 1 (166.0 ℃, 67.2t/h) of tempering tank, under reboiler at the bottom of charging and the raffinate Tata 18 effect, the cat head oil gas 3 of formation (flow is 100.3t/h, 97.5 ℃, 0.12MPaG) is cooled to 53 ℃ through raffinate column overhead air cooling device 20 and raffinate column overhead water cooling plant 21 and enters the raffinate column overhead and divide flow container 22 (the total cooling load of cat head is 985.0 * 10
4Kcal/h), obtain containing isomery C
8More desorbing agent (liquid phase).The part of this desorbing agent is returned raffinate column overhead (flow is 79.4t/h) as cold reflux 4, and remaining desorbing agent (promptly contains isomery C
8More desorbing agent 5) reclaims (flow is 20.9t/h) as product; Raffinate tower side line 6 (34.3t/h, 141.0 ℃) is extracted out from the 11st plate, enters stripping tower.Isoparaffin 7 at the bottom of the tower (31.9t/h, 252.0 ℃) send the tank field after heat exchange, cooling.Full tower provides heat 663.0 * 10 by tower bottom reboiler 18
4Kcal/h.
After converging, raffinate tower side line 6 (34.3t/h, 141.0 ℃) and Extract tower side line 14 (10.3t/h, 130.0 ℃) enter the stripping tower top, new washing fluid 26 (1.9t/h, 148 ℃) Zi Tadi enters stripping tower, stripper overhead gas 16 (20.3t/h, 146 ℃) return the raffinate tower, obtain (26.3t/h, 154 ℃) washing fluid 17 at the bottom of the tower.
Embodiment 1:
Present embodiment raffinate tower and Extract tower process flow process as shown in Figure 2, compared to the comparative example flow implementation following improvement, the same comparative example of other steps:
(1) above the opening for feed of raffinate tower and Extract tower, the stage casing reflux is set respectively, is specially stage casing reflux I (27) is set above the opening for feed of raffinate tower, stage casing reflux II (28) is set above the opening for feed of Extract tower; Stage casing reflux I (27) comprises and extracts out mouthful, returns tower mouth and interchanger, extracts out mouthful and returns the tower mouth and be connected with the raffinate tower; Stage casing reflux II (28) comprises and extracts out mouthful, returns tower mouth and interchanger, extracts out mouthful and returns the tower mouth and be connected with the Extract tower;
Raffinate tower 2 from cat head down number the 10th Board position (promptly extract out mouthful) extraction stage casing backflow 160.0t/h, extract 137.9 ℃ of temperature out, by returning the 8th block of plate (promptly returning the tower mouth) after the interchanger 29 among the reflux I of stage casing and 65 ℃ of hot water heat exchange, return 92.9 ℃ of temperature, heat removal 442.0 * 10
4Kcal/h, heat-obtaining medial temperature are 115.4 ℃, the 7th block of column plate dry plate not in this process; The 9th Board position (promptly extracting mouth out) at the Extract tower located extraction stage casing backflow 125.0t/h, extracting temperature out is 125.2 ℃, by returning the 7th block of plate (promptly returning the tower mouth) after the interchanger 30 among the reflux II of stage casing and 65 ℃ of hot water heat exchange, return 95.2 ℃ of temperature, heat removal 229.0 * 10
4Kcal/h, the heat-obtaining medial temperature is 110.2 ℃, the 6th block of column plate dry plate not in this process.
(2) utilize reflux heat that 85 ℃～95 ℃ heat medium waters take place, with its heating low temperature de-mineralized water;
With the 65 ℃ hot water 220t/hs of above-mentioned reflux heat heating, be heated 95 ℃ and send heat power plant's heating de-mineralized water back to from heat power plant.In the present embodiment, the 130t/h of heat power plant, 35 ℃ of de-mineralized waters are former ℃ to advance the deoxygenation of normal pressure deoxygenator with 1.0MPa steam heating to 104, consumes steam 16.0t/h, now changes into and is heated to 86.6 ℃ with hot water earlier, and therefore steam concurrent heating then reduces steam consumption 12t/h.
(3) adjust raffinate tower and Extract tower operating parameters;
Behind the reflux heat of extraction stage casing, raffinate column overhead cold reflux 4 is reduced to 34.6t/h by 79.4t/h; Extract column overhead cold reflux 12 is reduced to 23.6t/h by 45.7t/h;
Other flow processs, controlled variable and equipment all do not change, and is consistent with comparative example.
The raffinate tower of employing present embodiment and Extract tower operational circumstances and effect are as follows:
A, the total cooling load 545.0 * 10 of raffinate column overhead
4Kcal/h is with comparative example 985.0 * 10
4The kcal/h contrast reduces by 440.0 * 10
4Kcal/h descends 44.7%; Extract column overhead cooling load 621.0 * 10
4Kcal/h is with comparative example 841.0 * 10
4The kcal/h contrast reduces by 220.0 * 10
4Kcal/h descends 26.2%;
Hot reboiler 663.0 * 10 at the bottom of B, the raffinate Tata
4Kcal/h is with comparative example 663.0 * 10
4The kcal/h contrast does not change; Reboiler 398.0 * 10 at the bottom of the Extract Tata
4Kcal/h is with comparative example 389.0 * 10
4The kcal/h contrast, basic not variation;
Isoparaffin amount 31.9t/h at the bottom of C, the raffinate Tata with comparative example 31.9t/h contrast, does not change, and quality remains unchanged simultaneously; Normal paraffin amount 15.1t/h at the bottom of the Extract Tata with comparative example 15.1t/h contrast, does not change, and quality remains unchanged simultaneously;
D, raffinate column overhead contain isomery C
8More desorption dosage is 20.9t/h, with comparative example 20.9t/h contrast, does not change, and quality remains unchanged simultaneously; The Extract column overhead contains positive structure C
5More desorption dosage is 38.4t/h, with comparative example 38.4t/h contrast, does not change, and quality remains unchanged simultaneously;
E, raffinate column overhead cold reflux amount 34.6t/h with comparative example 79.4t/h contrast, reduce 44.8t/h; Extract column overhead cold reflux amount 23.6t/h with comparative example 45.7t/h contrast, reduces 22.1t/h;
F, the de-mineralized water deoxygenation steam consumption 4.0t/h of heat power plant with comparative example 16t/h contrast, reduce by 75%.
Embodiment 2:
Present embodiment raffinate tower and Extract tower process flow process as shown in Figure 2, compared to the comparative example flow implementation following improvement, the same comparative example of other steps:
(1) above the opening for feed of raffinate tower and Extract tower, the stage casing reflux is set respectively, is specially stage casing reflux I (27) is set above the opening for feed of raffinate tower, stage casing reflux II (28) is set above the opening for feed of Extract tower; Stage casing reflux I (27) comprises and extracts out mouthful, returns tower mouth and interchanger, extracts out mouthful and returns the tower mouth and be connected with the raffinate tower; Stage casing reflux II (28) comprises and extracts out mouthful, returns tower mouth and interchanger, extracts out mouthful and returns the tower mouth and be connected with the Extract tower;
Locate extraction stage casing backflow 160.0t/h at the 10th Board position (first block of plate of cat head is numbered 1) of raffinate tower, extract 137.9 ℃ of temperature out, by returning the 8th block of plate after the interchanger 29 among the reflux I of stage casing and 65 ℃ of hot water heat exchange, return 92.9 ℃ of temperature, heat removal 442.0 * 10
4Kcal/h, heat-obtaining medial temperature are 115.4 ℃, the 7th block of column plate dry plate not in this process; At the 9th Board position place extraction stage casing backflow 125.0t/h of Extract tower, extracting temperature out is 125.2 ℃, by returning the 7th block of plate after interchanger among the reflux II of stage casing 30 and the virgin kerosene heat exchange, returns 95.2 ℃ of temperature, heat removal 229.0 * 10
4Kcal/h, the heat-obtaining medial temperature is 110.2 ℃, the 6th block of column plate dry plate not in this process.
(2) utilize raffinate tower reflux heat that 85 ℃～95 ℃ heat medium waters take place, with its heating low temperature de-mineralized water; Utilize Extract tower reflux virgin kerosene;
With the 65 ℃ hot water 147.0t/hs of above-mentioned reflux heat heating, be heated 95 ℃ and send heat power plant's heating de-mineralized water back to from heat power plant.In the present embodiment, the 130t/h of heat power plant, 35 ℃ of de-mineralized waters are former ℃ to advance the deoxygenation of normal pressure deoxygenator with 1.0MPa steam heating to 104, consumes steam 16.0t/h, now changes into and is heated to 69.1 ℃ with hot water earlier, and therefore steam concurrent heating then reduces steam consumption 7.8t/h.
Will be from the 25.0 ℃ of virgin kerosene 100t/h and the newly-increased Extract midsection backflow heat exchange in head tank district, raw material is heated to 70 ℃ and walks at the bottom of former flow process and the preliminary fractionator oil heat exchange to 146.0 and ℃ advance preliminary fractionator, therefore improves 37.5 ℃ of feeding temperatures, reduces reboiler furnace thermal load 226.0 * 10 at the bottom of the prefractionation Tata
4Kcal/h increases preliminary fractionator cat head cooling load 4.3 * 10 simultaneously
4Kcal/h, basic not variation;
(3) adjust raffinate tower and Extract tower operating parameters;
Behind the reflux heat of extraction stage casing, raffinate column overhead cold reflux amount is reduced to 34.6t/h by 79.4t/h; Extract column overhead cold reflux amount is reduced to 23.6t/h by 45.7t/h;
Other flow processs, controlled variable and equipment all do not change, and is consistent with comparative example.
The raffinate tower of employing present embodiment and Extract tower operational circumstances and effect are as follows:
A, raffinate column overhead cooling load 545.0 * 10
4Kcal/h is with comparative example 985.0 * 10
4The kcal/h contrast reduces by 440.0 * 10
4Kcal/h descends 44.7%; Extract column overhead cooling load 621.0 * 10
4Kcal/h is with comparative example 841.0 * 10
4The kcal/h contrast reduces by 220.0 * 10
4Kcal/h descends 26.2%;
Hot reboiler 663.0 * 10 at the bottom of B, the raffinate Tata
4Kcal/h is with comparative example 663.0 * 10
4The kcal/h contrast does not change; Reboiler 398.0 * 10 at the bottom of the Extract Tata
4Kcal/h is with comparative example 389.0 * 10
4The kcal/h contrast does not change;
The isoparaffin amount is 31.9t/h at the bottom of C, the raffinate Tata, with comparative example 31.9t/h contrast, does not change, and quality remains unchanged simultaneously; The normal paraffin amount is 15.1t/h at the bottom of the Extract Tata, with comparative example 15.1t/h contrast, does not change, and quality remains unchanged simultaneously;
D, raffinate column overhead contain isomery C
8More desorption dosage is 20.9t/h, with comparative example 20.9t/h contrast, does not change, and quality remains unchanged simultaneously; The Extract column overhead contains positive structure C
5More desorption dosage is 38.4t/h, with comparative example 38.4t/h contrast, does not change, and quality remains unchanged simultaneously;
E, raffinate column overhead cold reflux amount 34.6t/h with comparative example 79.4t/h contrast, reduce 44.8t/h; Extract column overhead cold reflux amount 23.6t/h with comparative example 45.7t/h contrast, reduces 22.1t/h;
F, the de-mineralized water deoxygenation steam consumption 8.2t/h of heat power plant with comparative example 16t/h contrast, reduce by 48.8%;
G, preliminary fractionator tower bottom reboiler load 485.2 * 10
4Kcal/h is with comparative example 711.2 * 10
4The kcal/h contrast reduces by 226.0 * 10
4Kcal/h has descended 31.8%.
To sum up, embodiment of the invention raffinate tower and Extract column overhead cooling load reduce, the energy of upgrade recycling raffinate tower and Extract tower, and product is guaranteed simultaneously, and the tower bottom reboiler load is constant substantially.Workflow reengineering is simple, feasible, and economic benefit is obvious.
The foregoing description is a preferred implementation of the present invention; but embodiments of the present invention are not restricted to the described embodiments; other any do not deviate from change, the modification done under spirit of the present invention and the principle, substitutes, combination, simplify; all should be the substitute mode of equivalence, be included within protection scope of the present invention.
Claims (7)
1. the method for raffinate tower and the upgrade recycling of Extract tower energy is characterized in that comprising following steps:
(1) carries out the heat exchange cooling, the rising of heating medium temperature from raffinate tower column plate liquid phase of extracting out and the heating medium that temperature is lower than the column plate liquid phase; Column plate liquid phase after the cooling turns back on the column plate of raffinate tower again, and promptly the column plate liquid phase turns back to and returns on the column plate; The extraction amount of column plate liquid phase is according to returning column plate and near the column plate of cat head dry plate not for guaranteeing to be next to;
(2) carry out the heat exchange cooling, the rising of heating medium temperature from Extract tower column plate liquid phase of extracting out and the heating medium that temperature is lower than the column plate liquid phase; Column plate liquid phase after the cooling is returned on the column plate of Extract tower again, and promptly the column plate liquid phase turns back to and returns on the column plate; The extraction amount of column plate liquid phase is according to returning column plate and near the column plate of cat head dry plate not for guaranteeing to be next to;
(3) heating medium of the rising of the temperature in step (1) and the step (2) is used to do the thermal source of hot trap, thereby the energy of raffinate tower and Extract tower obtains recycling;
(4) operating parameters of adjustment Extract tower and raffinate tower, the influence behind the rounding backflow heat-obtaining.
2. method according to claim 1 is characterized in that: the extraction position of column plate liquid phase described in the step (1) is from down several the 9th～11 block of plates of cat head; The home position of the column plate liquid phase described in the step (1) after the cooling is from down several the 7th～9 block of plates of cat head; Distance between described extraction position and the home position be at least 2 plate spacings from.
3. method according to claim 1 is characterized in that: the extraction position of column plate liquid phase described in the step (2) is from down several the 8th～10 block of plates of cat head; The home position of the column plate liquid phase described in the step (2) after the cooling is from down several the 6th～8 block of plates of cat head; Distance between described extraction position and the home position be at least 2 plate spacings from.
4. realize the device of each described method of claim 1～3, comprise raffinate tower and Extract tower, it is characterized in that: stage casing reflux I is set above the opening for feed of raffinate tower, stage casing reflux II is set above the opening for feed of Extract tower; Stage casing reflux I comprises and extracts out mouthful, returns tower mouth and heat-exchanger rig, extracts out mouthful and returns the tower mouth and be connected with the raffinate tower; Stage casing reflux II comprises and extracts out mouthful, returns tower mouth and heat-exchanger rig, extracts out mouthful and returns the tower mouth and be connected with the Extract tower.
5. device according to claim 4 is characterized in that: the extraction mouth of described stage casing reflux I is arranged at the 9th～11 column plate position of down calculating from cat head, returns the tower mouth and is arranged at the 7th～9 block of plate of down calculating from cat head; Return the tower mouth with extract out mouth be separated by at least 2 plate spacings from.
6. device according to claim 4 is characterized in that: the extraction mouth of described stage casing reflux II is arranged at the 8th～10 Board position of down calculating from cat head, returns the tower mouth and is arranged at the 6th～8 block of plate of down calculating from cat head; Return the tower mouth with extract out mouth be separated by at least 2 plate spacings from.
7. device according to claim 4 is characterized in that: the heat-exchanger rig of described stage casing reflux I is an interchanger; The heat-exchanger rig of described stage casing reflux II is an interchanger.
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