CN103254932B - Extract C4 ~ C6 normal paraffin coproduction iso-pentane and isomery hexane technique in light naphthar - Google Patents
Extract C4 ~ C6 normal paraffin coproduction iso-pentane and isomery hexane technique in light naphthar Download PDFInfo
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Abstract
The present invention relates to a kind of chemical separating technique, particularly relate to C4 ~ C6 normal paraffin coproduction iso-pentane and the present invention of isomery hexane technique in a kind of extraction light naphthar and adopt multi-tower variable pressure adsorption and rectifying separation coupling technique.Gas phase C4 ~ C6 positive isomery hydro carbons mixing raw material passes into absorption tower adsorbs and is separated, using the normal paraffin of gas phase C7 ~ C9 as strippant, desorb is carried out to bed after having adsorbed, desorb material enters rectifying tower and isolates products C 4 ~ C6 normal paraffin and strippant C7 ~ C9 normal paraffin, strippant recycles, re-use and do not carried out manipulation of regeneration by the adsorption tower of C4 ~ C6 isoparaffin to absorption C7 ~ C9 normal paraffin adsorbed, regeneration feed, through twice rectifying separation, obtains high purity strippant C7 ~ C9 normal paraffin and high purity iso-pentane and isomery hexane.The present invention can be separated positive isoparaffin effectively, and adsorbent reactivation is easy, technical process simple, high financial profit, greatly reduces relative to other separating process energy consumption.
Description
Technical field:
The present invention relates to a kind of chemical separating technique, particularly relate to C4 ~ C6 normal paraffin coproduction iso-pentane and isomery hexane technique in a kind of extraction light naphthar.
Background technology:
Light naphthar is one of product of hydrocracking in Aromatic Hydrocarbon United Plant, and because present most of device for producing hydrogen adopts natural gas hydrogen preparation, therefore light naphthar is mainly used as cracking ethylene preparation raw material and gasoline blending stock.Because in this petroleum naphtha, isoparaffin is too high, the not too suitable raw material as preparing ethylene by steam cracking; As gasoline blending stock, again because its normal paraffin content is higher, affect oil product octane value.Therefore be rationally separated in light naphthar that positive isoparaffin is for the comprehensive utilization value improving light naphthar, the light naphthar resource of integrated optimization, increases the economic benefit of petroleum chemical enterprise, significant.
CN101148390A sets forth technique for extracting high-pure normal hexane product by pressure swing adsorption, adopts four towers to heat pressure-variable adsorption flow process, realizes the desorption of sorbent material normal hexane under vacuum, obtains the normal hexane that purity is greater than 99% after rectifying tower is separated.
CN101134703A has invented pressure-variable adsorption and has extracted normal heptane coproduction octane technique, multitower is adopted to heat pressure-variable adsorption flow process, while vacuum desorption, add rare gas element purge, make bed obtain sufficient desorb, coproduction obtains normal heptane and the octane that purity is all greater than 99%.
CN1634812A proposes the method for separating normal alkane from C5 ~ C6 alkane isomerization product, achieve the separation under liquid-phase condition, employing rectification method removes the iso-pentane in raw material, re-use the positive isoparaffin mixture of absorption method fractionation by adsorption, using octane as liquid phase strippant, bed is resolved.
CN101148390A, CN101134703A are the invention achievement in this laboratory, require that subsequent condensation temperature reaches subzero, requires that condensing pressure is higher owing to adopting rare gas element desorption, energy consumption and facility investment larger.And adopt gas phase high-carbon C4 ~ C6 normal paraffin as strippant, isoparaffin is that the associating separating process of regenerator has no report, and technique can co-producing high-purity iso-pentane and isomery hexane as required, and energy consumption reduces greatly, therefore, on the basis of laboratory study, this technique is invented.
Summary of the invention:
The object of the invention is to provide C4 ~ C6 normal paraffin coproduction iso-pentane and isomery hexane technique in extraction light naphthar to improve the deficiencies in the prior art.The present invention adopts multi-tower variable pressure adsorption and rectifying separation coupling technique.
Technical scheme of the present invention is: C4 ~ C6 normal paraffin coproduction iso-pentane and isomery hexane technique in a kind of extraction light naphthar, from the first adsorption tower T1 adsorbs, four towers simultaneously continuous adsorption desorption are separated, concrete steps are as follows: (1) adsorbs, the positive isoparaffin mixing raw material of C4 ~ C6 exports from raw material storage tank V3, after gasification, enter the first adsorption tower T1 adsorb, normal paraffin in raw material is adsorbed, non-absorbed component is exported by the first adsorption tower T1 tower top, regenerates the second adsorption tower T2 completing equal voltage rise; (2) all pressure drops, the first adsorption tower T1 completing absorption and the 3rd adsorption tower T3 completing desorb all press; (3) bed displacement, use inert gas replacement to go out the material of dead space in the first adsorption tower T1, material obtains middle runnings through condensation; (4) desorb, C7 ~ C9 normal paraffin single component or two or more blending ingredients have entered the first adsorption tower T1 of displacement after gasification, separate sucking-off by the C4 ~ C6 normal paraffin adsorbed, desorb material input Second distillation column T6; (5) all voltage rises, the 3rd adsorption tower T3 now completing absorption and the first adsorption tower T1 completing desorb all press; (6) bed regeneration, the isoparaffin do not adsorbed by the 4th adsorption tower T4 tower top carrying out adsorbing is as regenerator, desorption goes out C7 ~ C9 normal paraffin of the first adsorption tower T1 internal adsorption, and realize the regeneration of the first adsorption tower T1 internal adsorption agent, the regeneration feed obtained enters the first rectifying tower T5; (7) associating rectifying, the desorb material input Second distillation column T6 that the first adsorption tower T1 obtains, tower top obtains products C 4 ~ C6 normal paraffin, and tower reactor obtains strippant C7 ~ C9 normal paraffin, and C7 ~ C9 normal paraffin recycles; The regeneration feed that first adsorption tower T1 obtains enters the first rectifying tower T5, tower top obtains C4 ~ C6 isoparaffin, tower reactor obtains strippant C7 ~ C9 normal paraffin and recycles, tower top C4 ~ C6 isoparaffin by the 3rd rectifying tower T7 again rectifying obtain iso-pentane and isomery hexane product respectively.
More detailed step is as follows: (1) adsorbs, C4 ~ C6 paraffinic feedstock in raw material storage tank V3 enters first adsorption tower T1 absorption by the first pipeline 1 by the second constant-flux pump P3 after the 3rd interchanger E3 gasifies, and (in T1 adsorption process, the second adsorption tower T2 successively carries out equal pressure drop and regeneration, 3rd adsorption tower carries out desorb, 4th adsorption tower successively carries out equal pressure drop and displacement), C4 ~ C6 normal paraffin is adsorbed, and C4 ~ C6 isoparaffin enters the second adsorption tower T2 and regenerates, (2) all pressure drops, the first adsorption tower T1 completing absorption and the 3rd adsorption tower T3 completing desorb are by all pressure drops of the 5th pipeline 5, (3) bed displacement, the rare gas element in displacement gas nitrogen storage tank V2 displaces the material of dead space in the first adsorption tower T1 by the 4th pipeline 4, and this material enters intermediates storage tank V5 by the 3rd pipeline 3, the 8th pipeline the 8 and the 11 pipeline pipeline 11, (4) desorb, C7 ~ C9 normal paraffin strippant (single component or two or more blending ingredients) in strippant C7 ~ C9 normal paraffin storage tank V1 enters by the 6th pipeline 6 the first adsorption tower T1 just completing displacement by the first constant-flux pump P1 after First Heat Exchanger E1 gasifies heat exchange, separate sucking-off by the C4 ~ C6 normal paraffin adsorbed, the desorb material obtained enters Second distillation column T6 by second pipe 2 and the 9th pipeline 9, (5) all voltage rises, now complete the 3rd adsorption tower T3 of absorption to completing the first adsorption tower T1 of desorb by all voltage rises of the 5th pipeline 5, (6) bed regeneration, now the 4th adsorption tower T4 adsorbs, C4 ~ C6 the isoparaffin do not adsorbed is mixed together input first adsorption tower T1 by the 5th pipeline 5 and regenerator in the regenerator isoparaffin storage tank V4 through gasifying, mixed gaseous C4 ~ C6 isoparaffin regenerates the first adsorption tower T1 just completing equal voltage rise as regenerator, purge the C7 ~ C9 normal paraffin separating sucking-off first adsorption tower T1 internal adsorption, realize the regeneration of the first adsorption tower T1 internal adsorption agent, the regeneration feed obtained is by the 3rd pipeline 3, 8th pipeline the 8 and the 12 pipeline 12 enters the first rectifying tower T5, (7) associating rectifying, obtain desorb material during the first adsorption tower T1 desorb and enter Second distillation column T6, Second distillation column T6 tower top obtain product purity be 99.0% ~ 99.5% C4 ~ C6 normal paraffin enter C4 ~ C6 normal paraffin product storage tank V6, Second distillation column T6 tower reactor obtains C7 ~ C9 normal paraffin strippant that purity is 99.0% ~ 99.5%, and C7 ~ C9 normal paraffin inputs strippant C7 ~ C9 normal paraffin storage tank V1 for recycling by the 7th pipeline 7, the regeneration feed obtained during the first adsorption tower bed regeneration inputs the first rectifying tower T5, T5 tower top obtains C4 ~ C6 isoparaffin of purity 99.0% ~ 99.5%, part C4 ~ C6 isoparaffin is diverted to C4 ~ C6 isoparaffin product storage tank V7, C4 ~ C6 isoparaffin of C4 ~ C6 isoparaffin product storage tank V7 inputs in V4 storage tank again, as regenerator, T5 tower reactor obtains C7 ~ C9 normal paraffin of purity 99.0% ~ 99.5%, C7 ~ C9 normal paraffin inputs V1 for recycling by the 7th pipeline 7, C4 ~ C6 the isoparaffin not being diverted to C4 ~ C6 isoparaffin product storage tank V7 enters the 3rd rectifying tower T7, T7 tower top obtains purity 99.0% ~ 99.8% iso-pentane product, input iso-pentane storage tank V9, T7 tower reactor obtains purity 99.5% ~ 99.8% isomery hexane product, isomery hexane produces input isomery hexane storage tank V8.So far, complete a pressure swing adsorption cycles, four adsorption towers continuously carry out simultaneously.
Preferred C4 ~ C6 the paraffinic feedstock of the present invention is for being hydrocracked naphtha, reforming topped oil or cat cracked naphtha, the petroleum fractions of 60 DEG C ~ 165 DEG C.
In adsorption process of the present invention, adsorption temp is preferably 150 ~ 450 DEG C, gas phase air speed 40 ~ 2000h
-1, adsorptive pressure is 0 ~ 3Mpa(gauge pressure).
Bed displacement rare gas element of the present invention is preferably nitrogen, helium, carbonic acid gas or hydrogen, and air speed is at 15 ~ 500h
-1.
In desorption process of the present invention, desorption temperature is preferably 120 ~ 450 DEG C, pressure 0 ~ 1Mpa(gauge pressure), gas phase air speed 40 ~ 2000h
-1, the desorption method adopted is for purging desorb, and the strippant adopted is C7 ~ C9 single component normal paraffin or two or more blending ingredients.
The regenerator of bed regeneration of the present invention is preferably rare gas element N
2, H
2, He, CO
2or the isoparaffin of C4 ~ C6, be more preferably the isoparaffin of C4 ~ C6, regeneration is for purging regeneration, and regeneration temperature is preferably 120 ~ 450 DEG C, and pressure is preferably 0 ~ 2Mpa(gauge pressure), gas phase air speed is preferably 40 ~ 2000h
-1.
The present invention uses rectifying tower T6 rectifying separation to go out C4 ~ C6 normal paraffin and C7 ~ C9 normal paraffin, bottom temperature is preferably 80 ~ 200 DEG C, tower top temperature is preferably 50 ~ 200 DEG C, theoretical plate number is preferably 40 ~ 120 pieces, tower top obtain product purity 99.0% ~ 99.5% C4 ~ C6 normal paraffin, tower reactor obtain purity 99.0% ~ 99.5% C7 ~ C9 normal paraffin, C7 ~ C9 normal paraffin inputs V1 use to be recycled by the 7th pipeline 7.
The present invention uses rectifying tower T5 rectifying separation to go out C4 ~ C6 isoparaffin and C7 ~ C9 normal paraffin strippant, bottom temperature 80 ~ 200 DEG C, tower top temperature 60 ~ 200 DEG C, theoretical plate number 35 ~ 120 pieces, tower top obtains C4 ~ C6 isoparaffin of purity 99.0% ~ 99.5%, tower reactor obtains C7 ~ C9 normal paraffin of purity 99.0% ~ 99.5%, and C7 ~ C9 normal paraffin inputs V1 use to be recycled by pipeline 7.
The present invention uses rectifying tower T7 rectifying sub-argument to go out iso-pentane and isomery hexane, bottom temperature 50 ~ 200 DEG C, tower top temperature 40 ~ 200 DEG C, theoretical plate number 40 ~ 150 pieces, tower top obtains purity 99.0% ~ 99.8% iso-pentane product, and tower reactor obtains purity 99.5% ~ 99.8% isomery hexane product.
The positive isoparaffin technique of above-mentioned pressure-variable adsorption separation of C 4 ~ C6 is that multi-tower variable pressure adsorption combines with rectifying separation process.Multi-tower variable pressure adsorption optimal process two tower to ten four tower pressure-variable adsorption flow process, the best is four tower pressure swing adsorption process.
Beneficial effect:
The present invention is for adopting gas phase high-carbon normal paraffin as strippant, and isoparaffin is the associating separating process of regenerator, co-production high purity iso-pentane and isomery hexane.Relative to traditional rectifying separation, fractionation by adsorption energy consumption reduces greatly, and the resolution of positive isoparaffin is high; Relative to vacuum desorption, the security of this technique is remarkable; Relative to inert gas purge desorb, desorption rate of the present invention is obviously accelerated, and energy consumption significantly reduces.Therefore, this technique has great industrial advantages.
Accompanying drawing illustrates:
Fig. 1 is the process flow sheet that the present invention is separated positive isoparaffin; Wherein T1 is the first adsorption tower, and T2 is the second adsorption tower, and T3 is the 3rd adsorption tower, and T4 is the 4th adsorption tower; T5 is the first rectifying tower, and T6 is Second distillation column, and T7 is the 3rd rectifying tower; P1 is the first constant-flux pump, P3 second constant-flux pump, and P4 is the 3rd constant-flux pump, and P2 is the first mass flowmeter; E1 First Heat Exchanger, E2 is the second interchanger, and E3 is the 3rd interchanger, and E4 is the 4th interchanger; V1 is strippant C7 ~ C9 normal paraffin storage tank, V2 is displacement gas nitrogen storage tank, V3 is raw material storage tank, V4 is regenerator isoparaffin storage tank, V5 is intermediates storage tank, and V6 is C4 ~ C6 normal paraffin product storage tank, and V7 is C4 ~ C6 isoparaffin product storage tank, V8 is isomery hexane storage tank, and V9 is iso-pentane storage tank; 1 is the first pipeline, and 2 is second pipe, and 3 is the 3rd pipeline, and 4 is the 4th pipeline, and 5 is the 5th pipeline, and 6 is the 6th pipeline, and 7 is the 7th pipeline, and 8 is the 8th pipeline, and 9 is the 9th pipeline, and 10 is the tenth pipeline, and 11 is the 11 pipeline, and 12 is the 12 pipeline.
The change curve of two constituent mass marks in desorb material when Fig. 2 is normal heptane desorb Skellysolve A.
Fig. 3 is isoparaffin when regenerating bed, the concentration curve of normal heptane in regeneration feed.
Fig. 4 be liquid phase normal heptane desorb C4 ~ C6 normal paraffin and gas phase normal heptane desorb C4 ~ C6 normal paraffin time stripping liquid in C4 ~ C6 normal paraffin massfraction change curve.
Embodiment:
Case study on implementation 1: certain petroleum chemical enterprise's hydrocracking light naphthar is raw material, and light naphthar mainly forms as shown in table 1:
Table 1 light naphthar forms
Four tower pressure swing adsorption cycles time devided modulation are as shown in table 2: a pressure swing adsorption cycles cycle is 24min, and each stage, concrete time devided modulation was as table 2.
Table 2 four tower pressure swing adsorption cycles timetable
[note]: A-adsorbs, the equal pressure drop of ED-, and R-replaces, V-desorb, the equal voltage rise of ER-, and H-regenerates
Be separated n-alkane in Light Naphtha technical process Fig. 1 according to pressure-variable adsorption, absorption: V3 storage tank light naphthar raw material, input vaporizing chamber E3 through constant-flux pump P3,150 DEG C and 0.4MPa(gauge pressure) condition gasified, the light naphthar of gasification 1 enters T1 by the road; Equal pressure drop, after having adsorbed, by pipeline 5, T1 internal pressure is all put into T2, T1 pressure tower drops to 0.18MPa, and T2 pressure tower is raised to 0.2MPa; Bed replace, now nitrogen storage tank V2 nitrogen through under meter P2 measure after with air speed 30h
-1enter preheater E2,150 DEG C and 0.4Mpa(gauge pressure) preheating under condition, displace the material in T1 dead space through pipeline 4, input storage tank 5 by pipeline 3,8 and 11 and collect and obtain middle runnings; Desorb, after having replaced, the normal heptane of storage tank V1 inputs vaporizer E1 through constant-flux pump P1,150 DEG C and 0Mpa(gauge pressure) condition gasified, through pipeline 6 with 40h
-1air speed enters adsorption column T1, separate sucking-off by the C4 ~ C6 normal paraffin adsorbed, desorb material inputs rectifying tower T6 through pipeline 2 and 9, rectifying tower T6 number of effective plate 40 pieces, obtain C4 ~ C6 normal paraffin and purity 99.4% normal heptane of purity 99.5%, normal heptane is transported to V1 through pipeline 7 and recycles; Equal voltage rise, has all dropped to the T1 of desorb, has realized the equal voltage rise of T1 through pipeline 5 by the pressure completing the T3 of absorption; Bed regenerates, and the isoparaffin do not adsorbed in the T4 now adsorbed enters T1 through pipeline 5, for the normal heptane of desorption absorption, realizes the regeneration of bed, and isoparaffin air speed is 40h
-1, supplemented by V4 when the isoparaffin in T4 is in shortage, obtain fresh molecular sieve; Associating rectifying, regenerated liquid enters rectifying tower T5 through pipeline 3,8 and 12, T5 number of effective plate is 35 pieces, tower top obtains the isoparaffin of purity 99.3% and tower reactor obtains purity 99.3% normal heptane, normal heptane recycles through pipeline 7, and T5 tower top obtains isoparaffin and inputs rectifying tower T7 again, and T7 number of effective plate is 40 pieces, it is 99.3% iso-pentane that tower top obtains purity, and it is 99.7% isomery hexane that tower reactor obtains purity.So far, a pressure swing adsorption cycles is completed.According to this order, four adsorption towers carry out simultaneously continuously.
As shown in Figure 2, normal heptane can separate sucking-off Skellysolve A to the concentration curve of normal heptane desorb Skellysolve A in first 25 minutes, and normal heptane self does not reach breakthrough point.
When isoparaffin regenerates bed, in regeneration feed, the massfraction change curve of normal heptane as shown in Figure 3, and as can be seen from Figure 3, isoparaffin is fast to normal heptane regeneration rate, and bed regeneration rate reaches more than 90%, meets the requirement of next circulation.
The each product purity of table 3 for obtaining after rectifying.
Each compositional purity after table 3 rectifying
Case study on implementation 2: certain petroleum chemical enterprise's catalytic pyrolysis petroleum naphtha is separated.Technical process and example 1 similar.
Adsorption temp is 450 DEG C, adsorptive pressure 3MPa(gauge pressure), desorption temperature 450 DEG C, desorption pressures 1MPa(gauge pressure), desorb air speed 2000h
-1, regeneration temperature 450 DEG C, regeneration pressure 2MPa(gauge pressure), regeneration air speed 2000h-1, strippant is the mass mixing such as normal heptane and normal hexane component, uses C4 ~ C6 isoparaffin to carry out the regeneration of bed after desorb completes.It is 120,120 and 150 pieces that rectifying tower T5, T6 and T7 number of effective plate is respectively, and finally obtains product purity as shown in table 4.
Each compositional purity after table 4 rectifying
Case study on implementation 3: adopt certain factory's reforming topped oil to be raw material, raw material composition is as shown in table 5.
Table 5 reforming topped oil forms
Still adopt four tower pressure-variable adsorption separating technologies, absorbing process is similar, adopts the stronger octane of adsorption as desorbing agent during desorption, compared for gas phase and liquid phase desorption rate and desorption effect.Bed regeneration uses iso-pentane as regenerator.
When equivalent liquid phase flow rate strippant carries out desorb, through gasifying, the desorb of laggard promoting the circulation of qi phase and direct liquid phase desorption rate contrast as shown in Figure 4, as can be seen from Figure 4, gas phase desorption rate is obviously greater than liquid phase desorption rate, maximum desorption rate is just reached in 5min, and liquid phase desorption rate is little, after 25min, also do not reach maximum desorption rate.
Case study on implementation 4: with certain petroleum chemical enterprise's shortening petroleum naphtha for raw material.With example 1 similarly, employing octane is strippant, desorption temperature 300 DEG C, pressure 0.2MPa(gauge pressure), gas phase air speed 40h
-1carry out desorb under condition, it is that 102,98 and 114 pieces of the finished product purity are as shown in table 6 that rectifying tower T5, T6 and T7 number of effective plate is respectively.
Each compositional purity after table 6 rectifying
Claims (2)
1. one kind is extracted C4 ~ C6 normal paraffin coproduction iso-pentane and isomery hexane technique in light naphthar, from the first adsorption tower T1 adsorbs, four towers simultaneously continuous adsorption desorption are separated, concrete steps are as follows: (1) adsorbs, the positive isoparaffin mixing raw material of C4 ~ C6 exports from raw material storage tank V3, after gasification, enter the first adsorption tower T1 adsorb, normal paraffin in raw material is adsorbed, non-absorbed component is exported by the first adsorption tower T1 tower top, regenerates the second adsorption tower T2 completing equal voltage rise; (2) all pressure drops, the first adsorption tower T1 completing absorption and the 3rd adsorption tower T3 completing desorb all press; (3) bed displacement, use inert gas replacement to go out the material of dead space in the first adsorption tower T1, material obtains middle runnings through condensation; (4) desorb, C7 ~ C9 normal paraffin single component or two or more blending ingredients have entered the first adsorption tower T1 of displacement after gasification, separate sucking-off by the C4 ~ C6 normal paraffin adsorbed, desorb material input Second distillation column T6; (5) all voltage rises, the 3rd adsorption tower T3 now completing absorption and the first adsorption tower T1 completing desorb all press; (6) bed regeneration, the isoparaffin do not adsorbed by the 4th adsorption tower T4 tower top carrying out adsorbing is as regenerator, desorption goes out C7 ~ C9 normal paraffin of the first adsorption tower T1 internal adsorption, realize the regeneration of the first adsorption tower T1 internal adsorption agent, the regeneration feed obtained enters the first rectifying tower T5; (7) associating rectifying, the desorb material input Second distillation column T6 that the first adsorption tower T1 obtains, tower top obtains products C 4 ~ C6 normal paraffin, and tower reactor obtains strippant C7 ~ C9 normal paraffin, and C7 ~ C9 normal paraffin recycles; The regeneration feed that first adsorption tower T1 obtains enters the first rectifying tower T5, tower top obtains C4 ~ C6 isoparaffin, tower reactor obtains strippant C7 ~ C9 normal paraffin and recycles, tower top C4 ~ C6 isoparaffin by the 3rd rectifying tower T7 again rectifying obtain iso-pentane and isomery hexane product respectively; Wherein the positive isoparaffin blending ingredients of C4 ~ C6 is hydrocracked naphtha, reforming topped oil or cat cracked naphtha, the petroleum fractions of 60 DEG C ~ 165 DEG C; Adsorption temp 150 ~ 450 DEG C; Gas phase air speed 40 ~ 2000h
-1; Pressure 0 ~ 3MPa; Desorption temperature 120 ~ 450 DEG C; Pressure 0 ~ 1MPa; Gas phase air speed 40 ~ 2000h
-1; The desorption method adopted is for purging desorb, and the strippant adopted is C7 ~ C9 single component normal paraffin or two or more blending ingredients; Regeneration is for purging regeneration; Regeneration temperature 120 ~ 450 DEG C; Pressure 0 ~ 2MPa; Gas phase air speed is 40 ~ 2000h
-1.
2. the technique according to right 1, is characterized in that the rare gas element of replacing is nitrogen, helium, carbonic acid gas or hydrogen; Air speed is at 15 ~ 500h
-1.
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| EP3204468B1 (en) * | 2014-10-09 | 2020-07-29 | Basf Se | Process for adsorber regeneration |
| WO2016054787A1 (en) * | 2014-10-09 | 2016-04-14 | Basf Se | Product recovery process for adsorber regeneration |
| CN106316754A (en) * | 2015-06-30 | 2017-01-11 | 中国石油化工股份有限公司 | Method for producing isopentane product |
| CN106318459A (en) * | 2015-07-01 | 2017-01-11 | 中国石化扬子石油化工有限公司 | Optimized utilization method for light naphtha |
| CN107746366B (en) * | 2017-10-11 | 2021-03-12 | 中石化上海工程有限公司 | Method for extracting isopentane from naphtha |
| CN109053352A (en) * | 2018-08-07 | 2018-12-21 | 黑龙江莱睿普思环境科技发展有限公司 | The method of pressure-variable adsorption extraction normal heptane coproduction normal octane |
| CN110724023A (en) * | 2019-11-07 | 2020-01-24 | 岳阳金瀚高新技术股份有限公司 | Preparation method of 2-methylpentane, 3-methylpentane and n-hexane |
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| CN1267388C (en) * | 2003-12-25 | 2006-08-02 | 中国石油化工股份有限公司 | Method for separating n-alkane from C5 to C6 alkane isomerized products |
| CN101148390B (en) * | 2007-10-12 | 2010-11-24 | 中国石化扬子石油化工有限公司 | Technique for extracting high-pure normal hexane product by pressure swing adsorption |
| CN102452885B (en) * | 2010-10-25 | 2014-12-03 | 中国石油化工股份有限公司 | Adsorption and separation method of C5 and C6 isomerization product |
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