CN102485708B - C5 fraction separation method employing hypergravity extractive distillation apparatus - Google Patents
C5 fraction separation method employing hypergravity extractive distillation apparatus Download PDFInfo
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Abstract
The invention discloses a C5 fraction separation method employing a hypergravity extractive distillation apparatus. A first segment of extractive distillation and a second segment of extractive distillation employ the hypergravity extractive distillation apparatus for extractive distillation. The apparatus comprises a hypergravity rectifying section, a hypergravity stripping section and a solvent recovery section. The method comprises steps of: (1) mixing a gas phase material and steam from the hypergravity stripping section and carrying out counter current contact with an extractant in a hypergravity rectifying section; (2) introducing extracted gas phase material into the solvent recovery section; (3) subjecting the part of the material led out from the solvent recovery section to the subsequent procedures, and condensing part of the material and introducing the condensed part of the material into the solvent recovery section; (4) mixing the extractant from the recovery section with the extractant from a solvent pump and making the mixed extractant from the recovery section with the extractant from a solvent pump enter into the hypergravity rectifying section and the hypergravity stripping section; (5) re-boiling part of the solvent material led out from a liquid outlet of the hypergravity stripping section by a reboiler and providing uprising steam for the hypergravity stripping section. The method of the invention can increase output and yield of an isoprene product and reduce energy consumption.
Description
Technical field
The present invention relates to petrochemical industry, say further, relate to a kind of C5 fraction separation method that adopts hypergravity extracting rectifying device.
Background technology
Carbon five (being called for short C5) cut is the by product producing in petrochemical complex oil refining apparatus, catalytic cracking unit and heavy hydrocarbon feedstocks steam cracking process of producing ethylene, the component that in C5 fraction, utility value is higher and content is more is isoprene (IP), cyclopentadiene (CPD) and m-pentadiene (PD), and in cracked C 5 fraction, three accounts for 40%～60%.These diolefins are due to its special molecular structure, and chemical property is active, can synthesize many important high value added products, and as spices, coating, resin, synthetic rubber, medicine, agricultural chemicals etc., be the precious resources of chemical utilization.
Along with the development of petrochemical complex, ethylene producing device maximizes, and economic benefit and the social benefit of by-product C5 fraction processing and utilization highlight especially day by day.Yet, C5 fraction forms complicated, there is the close component of a twenty or thirty boiling point, easily form again each other binary and ternary azeotrope, in addition C 5 diene is easy to polymerization, the method of employing conventional distillation is difficult to obtain the product of high-purity high-yield, and the main flow technique of our times various countries is all the separation that slective extraction rectificating method carries out C5 fraction.
Cracked C 5 fraction separation both at home and abroad at present all adopts the method for two-section extraction rectifying to obtain polymerization grade isoprene product, one of them extracting system completes the separated of C 5 monoolefin, alkane and C 5 diene, another extracting system is removed alkynes and cyclopentadiene in isoprene material, obtains polymerization grade isoprene product.Extraction solvent mainly adopts dimethyl formamide (DMF), acetonitrile (ACN) or N-Methyl pyrrolidone (NMP).Domestic only a set of 2.5 ten thousand tons/year of carbon five tripping devices also adopt two-section extraction rectification method, and employing dimethyl formamide is extraction solvent, and this covering device is that China studies foundation voluntarily.
Figure 1 shows that the industrial experiment device schema of the C5 fraction separation method of typical employing DMF two-section extraction rectification process, comprise altogether 5 unit, i.e. raw materials pretreatment unit, the first extracting rectifying unit, the second extracting rectifying unit, m-pentadiene and dicyclopentadiene refined unit and solvent treatment unit.That pretreatment unit comprises is pre-de-light, dimerization reaction, de-heavy three parts in advance.C5 fraction raw material in pre-lightness-removing column T-101, remove raw material in the low boiling component such as most of alkynes, then enter dipolymer reactor R-101, most of cyclopentadiene dimerization in raw material is dicyclopentadiene, and the raw material of being derived by dipolymer reactor enters pre-weight-removing column T-102 by dicyclopentadiene, m-pentadiene and isoprene initial gross separation.Pre-weight-removing column tower top material enters the first extractive distillation column T-201, and the first extracting rectifying column overhead is isolated C 5 alkane and monoolefine, and the solvent that tower reactor is dissolved with isoprene enters the first stripping tower T-202, returns to the first extractive distillation column after the solvent analysis.The C5 fraction materials such as the isoprene parsing, m-pentadiene and cyclopentadiene enter weight-removing column T-203, at this isoprene, further remove cyclopentadiene and m-pentadiene.The thick isoprene that weight-removing column tower top is derived enters the second extractive distillation column T-301, removes a small amount of cyclopentadiene and valylene, and the solvent that the second extractive distillation column tower reactor derives recycles after the second steam stripping unit T-302 is resolved.The isoprene of the second extracting rectifying column overhead enters that lightness-removing column T-303 is further refining to be removed crotonylene and obtain polymerization grade isoprene product.From the material of pre-weight-removing column and the extraction of weight-removing column tower reactor, be sent to m-pentadiene and dicyclopentadiene refined unit carries out separation and purification.In extracting rectifying process, need to extract out partial solvent refines to guarantee extracting rectifying (especially two extractions) effect to solvent treatment unit.
Two-section extraction rectification process flow process is longer, complicated operation difficulty; Extraction agent consumption is larger, need carry out stripping recovery, and energy consumption is high; Extracting rectifying tower is huge, and facility investment is large, and process cost is high; In sepn process, isoprene and m-pentadiene are because dimerization reaction loss is more.
For improving two-section extraction rectification process, scientific research personnel has carried out a large amount of research work.
CN1160033A is disclosed carries out separated processing method by the C5 diolefin in pyrolysis C 5 with other the component such as alkane, alkene, its feature is, before C 5 fraction carries out extracting and separating, by rectifying, first the alkynes such as isoamyl alkene, crotonylene are removed, make whole C5 separating technology get rid of the danger of alkynes blast, guarantee safety in production, reduced the processing load of post-order process and the usage quantity of extraction solvent, improve the processing power of whole Production Flow Chart.
CN1160034A is disclosed carries out separated processing method by the C5 diolefin in C5 cracking cut with other the component such as alkane, alkene, its feature is, two stripping towers are at least set in the first extracting system and remove water and the dimer in extracting system, improved the quality of circulating solvent, can avoid the localized accumulated of dipolymer and water, improve the operation of Analytic Tower, guaranteed the normal stable of whole separating technology.
The separation method of diolefin in the disclosed cracked C 5 fraction of CN101108782A, first that isoprene in raw material C5 fraction is separated with cyclopentadiene by adopting, cyclopentadiene enters hot dipolymer reactor and generates dicyclopentadiene and the technical scheme separated with m-pentadiene, in order to solve the polymerization losses problem of isoprene and cyclopentadiene in dimerization.
In two-section extraction rectifying C5 fraction separation process scheme, two extracting rectifying unit (tower) are the most key parts, it is for the ultimate yield of C 5 diene, the treatment capacity of product purity and even whole device and energy expenditure can produce a very large impact, and are the soul places of whole carbon five separation process.Above-mentioned patent documentation improves two-section extraction rectification process flow process from multiple angles, but to extracting rectifying unit (tower) itself upgrading and improve to rarely have and relate to.
Reality is, extracting rectifying is than conventional rectification, and liquid phase (extraction solvent) internal circulating load is very large, and the liquid phase load of extractive distillation column and stripping tower is very large, makes the energy expenditure of whole extracting rectifying unit very surprising; The plate efficiency of extractive distillation column is but very low simultaneously, is only 30-40%, and for reaching separation requirement, the stage number needing is a lot, normally adopts in practice the separation of the mode realize target component of multitower series connection.In whole flow process, required equipment is numerous, bulky, and complicated operation.
Another large problem C5 fraction polymerization of (especially the second extractive distillation column) in extractive distillation column in two-section extraction rectification process.Because the second extractive distillation column system temperature is high, in charging, thick isoprene feed purity has reached more than 95%, and C5 fraction residence time in the second extractive distillation column causes C5 fraction high temperature polymerization compared with length, and the loss of the isoprene causing is very serious; The black bits that polymerisate and solvent system effect produce simultaneously can cause column plate to stop up, and have greatly reduced plate efficiency, need cleaning during shutdown when severe obstruction.
On the whole, the separated two-section extraction distillation process of existing carbon five exists that energy consumption is high, solvent-oil ratio is large, extracting rectifying flow process easily produces black bits, environmental pollution is serious, operation expense is high, the shortcomings such as complicated operation, therefore existing extracting rectifying unit is optimized to upgrading and technological transformation just seems very necessary, has realistic meaning.
Summary of the invention
For solving problems of the prior art, the invention provides a kind of C5 fraction separation method that adopts hypergravity extracting rectifying device.The problem existing for extracting rectifying unit in existing carbon five separation process is improved and optimizes, and has improved output and the yield of isoprene product, has reduced energy consumption.
High-gravity technology is the patent of strengthening sepn process that Britain at end of the seventies ICI Imperial Chemical Industries (ICI) proposes, and hypergravity machine is the novel appts that utilizes super gravity field (centrifuge field) strengthening transport chemical process.English name Higee, also claims rotating packed bed, Rotating Packed Bed, abbreviation RPB.
The centrifugal force simulation super gravity field environment that high-gravity technology utilization rotation produces, greatly strengthens the contact between gas-liquid, mass transfer enhancement and reaction efficiency, thus significantly reduce equipment volume, reduce facility investment, be a kind of typical process intensification technology.
High-gravity technology both can be used for mass transfer sepn process, can be used for again heterogeneous reaction process.Its handled medium is varied, and according to difference, needing can be that solution-air two-phase can be also liquid-liquid two-phase, can also be gas-liquid-solid three-phase, can be and stream, adverse current or cross-flow operation.Compare hypergravity with traditional tower equipment and demonstrate its unique advantage, that is:
1. mass transfer intensity is high, can reduce significantly equipment volume, reduces facility investment;
The residence time short, be applicable to the processing of heat-sensitive material and selectivity and absorb;
3. be not afraid of vibrations and tilt, being applicable in playground, as used on offshore oil platform;
4. easy to foaming and not higher centrifugal force, is applicable to treat surface active substance and high viscosity substance;
5. liquid holdup is little, is applicable to process precious material;
6. spotting out is high, is applicable to the occasion of atm number, high gas speed;
7. filler is difficult for stopping up, and is applicable to process the system containing solid particulate or impurity;
8., during for the treatment of corrosive medium, can greatly save expensive corrosion resistant material;
9. start-stop appearance of vehicle is easy, can in several minutes, reach steady state.
The object of this invention is to provide a kind of C5 fraction separation method that adopts hypergravity extracting rectifying device.Wherein one-section abstraction rectifying and two-stage extraction rectifying adopt hypergravity extracting rectifying device to carry out extracting rectifying, with hypergravity extracting rectifying device, substitute the first extractive distillation column of the prior art and the second extractive distillation column;
Hypergravity extracting rectifying device comprises: hypergravity rectifying section, hypergravity stripping section and solvent recuperation section;
Hypergravity rectifying section and hypergravity stripping section are completed by hypergravity machine;
Solvent recuperation section is completed by hypergravity machine or gas-liquid separation device, preferably by hypergravity machine, is completed;
Described method comprises following steps:
(1) gaseous phase materials with from after the vapor mixing of hypergravity stripping section in hypergravity rectifying section and extraction agent counter current contact;
(2) gaseous phase materials after extraction enters solvent recuperation section, and the extraction agent of carrying secretly in gaseous phase materials is recovered;
(3) material of deriving from solvent recuperation section, a part enters down-stream, and a part enters solvent recuperation section after condensation;
(4) extraction agent of recovery zone enters hypergravity rectifying section and hypergravity stripping section successively with after extraction agent from solvent pump mixes;
(5) the solvent material part that hypergravity stripping section liquid exit is derived enters follow-up solvent stripper plant; A part after reboiler boils again for hypergravity stripping section provides rising steam.
Wherein said hypergravity rectifying extraction plant pressure is 0.1～0.4MPa, and hypergravity stripping section reboiler temperature is 100～135 ℃, and the reflux ratio of hypergravity extraction plant is 3～9, and the throughput ratio of extraction agent and carbon five materials is 2～5;
In described hypergravity stripping section, hypergravity machine rotor speed is 450～1200rmin
-1, in hypergravity rectifying section, hypergravity machine rotor speed is 400～1200rmin
-1, in solvent recuperation section, hypergravity machine rotor speed is 400～600rmin
-1;
For improving effect of extracting, the hypergravity machine of hypergravity rectifying section and hypergravity stripping section can 2～5 series connection;
Above-described hypergravity machine preferred filler is wire packing, and voidage is 90%～98%, and specific surface area is 200m
2m
-3～5000m
2m
-3.
Concrete scheme is as follows:
Figure 2 shows that the hypergravity extracting rectifying device in the present invention, in order to replace the first extractive distillation column T-201 and the second extractive distillation column T-301 in Fig. 1, in the present invention, except extractive distillation column, all the other flow process parts are not all made any change, shown in Fig. 1.
Below in conjunction with Fig. 2 second extracting rectifying of take, be partly example, illustrate the implementation procedure of hypergravity extracting rectifying.
The same with common rectifying tower, hypergravity rectifying is also divided into stripping section and rectifying section, for extracting rectifying, considers and has increased an extraction process, and hypergravity extracting rectifying device also need to increase an extraction agent recovery unit accordingly.
Thick isoprene gas phase from weight-removing column tower top enters hypergravity rectifying section RPB-1 gas inlet end, the extraction solvent counter current contact of upgrading with high dispersing, the continuous fragmentation of specific surface in filler, in this process, in thick isoprene material, cyclopentadiene and valylene are constantly extracted rectifying in extraction agent, and in gas phase, isoprene concentration is promoted step by step.
In like manner, in hypergravity stripping section RPB-2 part, the extraction solvent that contains isoprene material contacts with the steam counter-flow from reboiler H-101, in this process, isoprene in extraction solvent constantly gasification shifts in gas phase, and the cyclopentadiene in extraction solvent and valylene concentration get a promotion.
At extracting rectifying, cross therefrom, may have a small amount of extraction solvent to be gone out by Vapor Entrainment, consider this kind of situation, in the present invention, increased solvent recuperation section RPB-3, guarantee not contain extraction solvent through the isoprene cut of two extractions.This section can be completed by overweight machine, also can complete by conventional gas-liquid separation device, and the former is that preferably the latter can be used as alternative use in the present invention.
The material part deriving from solvent recovery unit enters the de-T-303 of lightness-removing column can obtain polymerization grade isoprene product except crotonylene, and another part enters solvent recovery unit and uses as the backflow of whole extracting rectifying device after C-101 condensation.
The solvent material part being derived by hypergravity stripping section liquid exit enters follow-up solvent stripper plant and resolves cyclopentadiene and valylene, reclaims solvent simultaneously; A part enters reboiler H-101 and provides rising steam for hypergravity stripping section.
In the present invention, designing hypergravity extracting rectifying device technique pressure is 0.1～0.4MPa, and stripping section reboiler temperature is 100～135 ℃, and the reflux ratio of hypergravity extraction plant is 3～9, and the throughput ratio of extraction agent and carbon five materials is 2～5.
Stripping section hypergravity machine rotor speed is 450～1200rmin
-1, rectifying section hypergravity machine rotor speed is 400～1200rmin
-1, solvent recovery unit hypergravity machine rotor speed is 400～600rmin
-1.
Expansion ground, stripping section can be realized by 2～5 hypergravity machine series connection that do not wait according to rotating speed is different with rotor radius with rectifying section unit, and each logical block physically can be by many hypergravity machine flexible combination.
Above-mentioned three part hypergravity machines filler model used is identical, is wire packing, and voidage is 90%～98%, and specific surface area is 200m
2m
-3～5000m
2m
-3.
In the present invention, any solvent that extraction agent can select carbon five extracting rectifying fields to use, as DMF, NMP, ACN etc.
The present invention compares with existing two-stage method C5 fraction separation process, has the following advantages:
1, high-gravity technology is applied to extracting rectifying field, this process intensification mass transfer and heat transfer, not only can equally realize separation and purification function with traditional tower, and there is higher vapour-liquid ratio (carbon five materials/extraction agent) compared with traditional tower, therefore under the constant condition of extraction agent flow, the treatment capacity of raw material is larger, in the constant situation of inlet amount, the consumption (internal circulating load) of extraction agent can reduce greatly in other words, reduce the energy expenditure of extracting rectifying process and stripping process, the object that reach energy-saving and cost-reducing, reduces production and operation cost.
2, in whole extracting rectifying process, the duration of contact of gas-liquid in the super gravity field of high temperature, the residence time was very short in other words, the dimerization reaction of C5 fraction is greatly suppressed, solved black bits problem, the operation stability of whole carbon five separation process is obviously promoted, improved output and the yield of isoprene product, the severity of solvent steam stripping unit and solvent treatment unit operation and operation reduces greatly simultaneously, and energy consumption obviously reduces.
Accompanying drawing explanation
The C5 fraction extracting rectifying schema that Fig. 1 is traditional
Fig. 2 hypergravity extracting rectifying of the present invention setting drawing
Description of reference numerals:
The pre-lightness-removing column of T-101; R-101 dipolymer reactor; The pre-weight-removing column of T-102; T-201 the first extractive distillation column; T-202 the first steam stripping unit; T-203 weight-removing column; T-301 the second extractive distillation column; T-303 lightness-removing column; T-302 the second steam stripping unit; T-401 carbon five steams tower; T-402 m-pentadiene treating tower; T-403 dicyclopentadiene treating tower; E-501 solvent regeneration tower; The burnt matter dilution of V-501 tower; T-501 solvent treatment tower RPB-1 hypergravity rectifying section; RPB-2 hypergravity stripping section; RPB-3 solvent recuperation section; P-101 solvent pump; C-101 condenser; H-101 reboiler
Embodiment
Below in conjunction with embodiment, further illustrate the present invention.
Embodiment
In conjunction with Fig. 1, Fig. 2, be specifically described.
In embodiment, with hypergravity extracting rectifying device, replace extractive distillation column of the prior art, specifically by one section, hypergravity extracting rectifying device, replace the first extractive distillation column T-201, two sections of replacement second extractive distillation column T-301 of hypergravity extracting rectifying device;
First raw material C5 fraction enters pre-lightness-removing column T-101, and the components such as most of alkynes, carbon four and iso-pentane remove from pre-lightness-removing column T-101 top, and tower reactor extraction material is sent to dipolymer reactor R-101.Pre-lightness-removing column T-101 stage number is 90, and reflux ratio is 18, controls pre-lightness-removing column T-101 tower top isoprene content and is no more than 1%.
From pre-lightness-removing column T-101 tower reactor extraction material, carry out dimerization reaction in dipolymer reactor R-101, the cyclopentadiene in material is converted into dicyclopentadiene, and reaction pressure is controlled at 1.2MPa, 86 ℃ of temperature of reaction, and gate ring pentadiene transformation efficiency reaches 90-95%.
C5 fraction enters pre-weight-removing column T-102 after dimerization reaction, from tower reactor extraction, remove the heavy constituents such as dicyclopentadiene, m-pentadiene, from overhead extraction isoprene material, pre-weight-removing column T-102 stage number is 90, trim the top of column ratio is 10, control m-pentadiene, cyclopentadiene and dicyclopentadiene tower reactor yield and be not less than 90%, isoprene yield is greater than 95%.
Material from pre-weight-removing column T-102 tower top enters one section, hypergravity extracting rectifying device, in hypergravity rectifying section gas outlet end, remove C 5 alkane and monoolefine component, the solvent that contains isoprene enters the first steam stripping unit T-202 after by the extraction of hypergravity stripping section liquid exit end and parses C5 fraction.The reflux ratio of controlling one section, extracting rectifying device is 3, the throughput ratio 4 of extraction agent and carbon five materials, the stage number that hypergravity extracting rectifying device is one section is 120, working pressure is 0.2MPa, 110 ℃ of the temperature of hypergravity stripping section reboiler, rectifying section, stripping section hypergravity machine rotor speed are 650rmin
-1, what solvent recuperation section adopted is hypergravity machine, rotor speed is 600rmin
-1, rectifying section, stripping section and solvent recuperation section hypergravity machine filler model used is identical, is wire packing, and voidage is 93%, and specific surface area is 900m
2m
-3.
The first steam stripping unit T-202 stage number is 45, and tower internal pressure is 0.02MPa, 150 ℃ of tower reactor temperature, reflux ratio 2.
The C5 fraction being parsed by the first steam stripping unit T-202 tower top enters weight-removing column T-203, and tower reactor is isolated the material containing heavy constituents such as m-pentadiene, dicyclopentadiene.Weight-removing column T-203 stage number is 120, and tower internal pressure is 0.2MPa, and reflux ratio is 15, controls weight-removing column T-203 tower top isoprene yield and is not less than 97%, and tower reactor m-pentadiene, dicyclopentadiene yield reach 98-99%.
Weight-removing column T-203 tower top material enters two sections, hypergravity extracting rectifying device, remove after a small amount of cyclopentadiene and alkynes by the extraction of hypergravity rectifying section gas outlet end, by the solvent containing cyclopentadiene and alkynes of hypergravity stripping section liquid exit end extraction, enter after the second steam stripping unit T-302 resolves and recycle.Two sections of stage number of hypergravity extracting rectifying device are 130, and working pressure is 0.2MPa, and reflux ratio is 5,125 ℃ of the temperature of hypergravity stripping section reboiler, and the throughput ratio of extraction agent and carbon five materials is 3, rectifying section, stripping section hypergravity machine rotor speed are 650rmin
-1, what solvent recuperation section adopted is hypergravity machine, rotor speed is 600rmin
-1, rectifying section, stripping section and solvent recuperation section hypergravity machine filler model used is identical, is wire packing, and voidage is 93%, and specific surface area is 900m
2m
-3.
The second stripping tower T-302: atmospheric stripping part stage number is 40, tower reactor temperature is 150 ℃, reflux ratio is 4; Decompression stripping part stage number is 40, and tower reactor temperature is 90 ℃, reflux ratio 45.
Through the material of two sections of extraction of hypergravity extracting rectifying device, enter lightness-removing column T-303 and remove light constituent, at tower reactor side line, place obtains polymerization grade isoprene, and purity is 99.5%.Lightness-removing column T-303 stage number is 110, and tower internal pressure is 0.2MPa, and trim the top of column ratio is 50, and tower reactor temperature is 70 ℃.
M-pentadiene refined unit T-402, dicyclopentadiene refined unit T-403 and solvent treatment part is substantially identical with China existing C5 fraction tripping device, in this not specifically narration, this part equipment can not put into main flow, and this area scientific research personnel can carry out design calculation as the case may be.
Table 1 polymerization grade isoprene product forms
Claims (8)
1. a C5 fraction separation method that adopts hypergravity extracting rectifying device, is characterized in that:
In described method, one-section abstraction rectifying and two-stage extraction rectifying adopt hypergravity extracting rectifying device to carry out extracting rectifying;
Described hypergravity extracting rectifying device comprises: hypergravity rectifying section, hypergravity stripping section and solvent recuperation section;
Described hypergravity rectifying section and hypergravity stripping section are completed by hypergravity machine;
Described solvent recuperation section is completed by hypergravity machine or gas-liquid separation device.
2. the C5 fraction separation method of employing hypergravity extracting rectifying device as claimed in claim 1, is characterized in that:
Described solvent recuperation section is completed by hypergravity machine.
3. the C5 fraction separation method of the employing hypergravity extracting rectifying device as described in one of claim 1～2, comprises following steps:
(1) gaseous phase materials with from after the vapor mixing of hypergravity stripping section in hypergravity rectifying section and extraction agent counter current contact;
(2) gaseous phase materials after extraction enters solvent recuperation section, and the extraction agent of carrying secretly in gaseous phase materials is recovered;
(3) material of deriving from solvent recuperation section, a part enters down-stream, and a part enters solvent recuperation section after condensation;
(4) extraction agent of recovery zone enters hypergravity rectifying section and hypergravity stripping section successively with after extraction agent from solvent pump mixes;
(5) the solvent material part that hypergravity stripping section liquid exit is derived enters follow-up solvent stripper plant; A part after reboiler boils again for hypergravity stripping section provides rising steam.
4. the C5 fraction separation method of employing hypergravity extracting rectifying device as claimed in claim 3, is characterized in that:
Described hypergravity extracting rectifying device pressure is 0.1～0.4MPa, and hypergravity stripping section reboiler temperature is 100～135 ℃, and the reflux ratio of hypergravity extraction plant is 3～9, and the throughput ratio of extraction agent and carbon five materials is 2～5.
5. the C5 fraction separation method of employing hypergravity extracting rectifying device as claimed in claim 3, is characterized in that:
In described hypergravity stripping section, hypergravity machine rotor speed is 450～1200rmin
-1, in hypergravity rectifying section, hypergravity machine rotor speed is 400～1200rmin
-1.
6. the C5 fraction separation method of employing hypergravity extracting rectifying device as claimed in claim 2, is characterized in that:
In described solvent recuperation section, hypergravity machine rotor speed is 400～600rmin
-1.
7. the C5 fraction separation method of employing hypergravity extracting rectifying device as claimed in claim 3, is characterized in that:
The hypergravity machine of described hypergravity rectifying section and hypergravity stripping section is 2～5 series connection.
8. the C5 fraction separation method of the employing hypergravity extracting rectifying device as described in one of claim 4～7, is characterized in that:
The filler of described hypergravity machine is wire packing, and voidage is 90%～98%, and specific surface area is 200m
2m
-3～5000m
2m
-3.
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| CN107827750A (en) * | 2017-08-11 | 2018-03-23 | 南京揽博环境技术有限公司 | A kind of technique for separating tert-butyl acetate in medicine solvent slop using the rectification under vacuum of hypergravity bed |
| CN110642692B (en) * | 2019-09-11 | 2022-04-22 | 中北大学 | Device and method for purifying cyclopropyl methyl ketone by salt extraction and rectification |
| CN114470854A (en) * | 2022-02-11 | 2022-05-13 | 赤峰福纳康生物技术有限公司 | Method for removing residual solvent in oil by using supergravity rotating bed gas extraction method |
| CN115108880B (en) * | 2022-08-08 | 2023-12-19 | 万华化学集团股份有限公司 | Method for separating methylcyclopentane and methylenecyclopentane |
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