CN101134703A - Process for skellysolve C abstraction with combined production of octane product by pressure swing adsorption - Google Patents
Process for skellysolve C abstraction with combined production of octane product by pressure swing adsorption Download PDFInfo
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- 238000001179 sorption measurement Methods 0.000 title claims abstract description 129
- 238000000034 method Methods 0.000 title claims abstract description 101
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 title claims abstract description 99
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 title claims abstract description 46
- 238000004519 manufacturing process Methods 0.000 title claims description 21
- 238000000926 separation method Methods 0.000 claims abstract description 8
- 238000010438 heat treatment Methods 0.000 claims abstract description 5
- 239000000203 mixture Substances 0.000 claims description 32
- 230000009466 transformation Effects 0.000 claims description 28
- 238000003795 desorption Methods 0.000 claims description 22
- ZJKABZNFELLAQQ-UHFFFAOYSA-N octane Chemical compound CCCCCCCC.CCCCCCCC ZJKABZNFELLAQQ-UHFFFAOYSA-N 0.000 claims description 19
- 239000003921 oil Substances 0.000 claims description 18
- 239000007789 gas Substances 0.000 claims description 16
- 239000002994 raw material Substances 0.000 claims description 16
- 230000008016 vaporization Effects 0.000 claims description 16
- 239000007788 liquid Substances 0.000 claims description 14
- 239000002808 molecular sieve Substances 0.000 claims description 13
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 13
- 239000002594 sorbent Substances 0.000 claims description 13
- 239000002904 solvent Substances 0.000 claims description 12
- 238000010521 absorption reaction Methods 0.000 claims description 10
- 229930195733 hydrocarbon Natural products 0.000 claims description 10
- 150000002430 hydrocarbons Chemical class 0.000 claims description 10
- 239000004215 Carbon black (E152) Substances 0.000 claims description 9
- 238000009834 vaporization Methods 0.000 claims description 9
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 8
- 238000009833 condensation Methods 0.000 claims description 8
- 230000005494 condensation Effects 0.000 claims description 8
- 238000002407 reforming Methods 0.000 claims description 8
- 230000000994 depressogenic effect Effects 0.000 claims description 7
- 241000282326 Felis catus Species 0.000 claims description 5
- 238000009835 boiling Methods 0.000 claims description 5
- 238000010926 purge Methods 0.000 claims description 5
- 229910019142 PO4 Inorganic materials 0.000 claims description 4
- 239000004411 aluminium Substances 0.000 claims description 4
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 4
- 229910052782 aluminium Inorganic materials 0.000 claims description 4
- 229910021529 ammonia Inorganic materials 0.000 claims description 4
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 239000012188 paraffin wax Substances 0.000 claims description 4
- 239000003208 petroleum Substances 0.000 claims description 4
- 239000010452 phosphate Substances 0.000 claims description 4
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims description 2
- 229910052799 carbon Inorganic materials 0.000 claims description 2
- 125000004432 carbon atom Chemical group C* 0.000 claims description 2
- 238000006073 displacement reaction Methods 0.000 claims description 2
- 229910052680 mordenite Inorganic materials 0.000 claims description 2
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 claims description 2
- 239000000463 material Substances 0.000 claims 1
- 239000000126 substance Substances 0.000 abstract description 4
- 238000003860 storage Methods 0.000 description 17
- 239000000543 intermediate Substances 0.000 description 8
- 230000000274 adsorptive effect Effects 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 239000000284 extract Substances 0.000 description 2
- UAEPNZWRGJTJPN-UHFFFAOYSA-N methylcyclohexane Chemical compound CC1CCCCC1 UAEPNZWRGJTJPN-UHFFFAOYSA-N 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- 239000003905 agrochemical Substances 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000003747 fuel oil additive Substances 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- GYNNXHKOJHMOHS-UHFFFAOYSA-N methyl-cycloheptane Natural products CC1CCCCCC1 GYNNXHKOJHMOHS-UHFFFAOYSA-N 0.000 description 1
- 230000003533 narcotic effect Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000012454 non-polar solvent Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000012925 reference material Substances 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 239000005060 rubber Substances 0.000 description 1
- 238000002336 sorption--desorption measurement Methods 0.000 description 1
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- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
Abstract
The present invention relates to chemical separation process, and is especially one pressure swing adsorption process for extracting n-heptane and co-produced n-octane. N-heptane and co-produced n-octane are extracted through one combined multiple tower heating pressure swing adsorption and rectifying separation process. The advanced technological process is simple, low in power consumption and high in automation, and can produce high purity n-heptane while producing high purity n-octane.
Description
Affiliated technical field:
The present invention relates to a kind of chemical separating method, especially relate to a kind of process for skellysolve C abstraction with combined production of octane product by pressure swing adsorption method.
Background technology:
Normal heptane is typical non-polar solvent, is commonly used for the standard of measuring octane value, narcotic, organic synthesis raw material etc., also is widely used in industries such as medicine, agricultural chemicals, rubber is synthetic, chemical fibre synthesizes, reagent, electronics cleanings.Octane also is used for organic synthesis as solvent and stratographic analysis reference material.Along with the fast development of relevant industries such as chemical industry, medicine, electronics, China will increase year by year to the demand of normal heptane, and especially the high purity normal heptane has vast market prospect.Normal heptane mainly is present in 90～100 ℃ of petroleum fractionss, reforming raffinate oil and No. 120 solvent oils.At present industrial main employing rectificating method is produced normal heptane, because normal heptane very close with C7 cut boiling point (as: 98.43 ℃ of normal heptane boiling points, 100.93 ℃ of methylcyclohexane boiling points, boiling-point difference have only 2.5 ℃) is difficult to its separation with conventional distillation; With precise distillation energy consumption height, production cost is higher, and yield is lower, and is difficult to obtain high purity normal heptane (〉 99%); Use the special extract rectification method, cost is higher, the process complexity.Though absorption method is separated at the positive isomery of hydrocarbon mixture, improve aspect industrialization such as gasoline octane rating and ethylene raw optimization, but the production technique report that extracts one-component alkane product about the employing absorption method from petroleum fractions, reforming raffinate oil and solvent wet goods complicated hydrocarbons class mixture is very few, and not seeing has the report that adopts the skellysolve C abstraction with combined production of octane product by pressure swing adsorption producing and manufacturing technique.
Summary of the invention:
The production technique that the purpose of this invention is to provide a kind of new pressure swing adsorption process skellysolve C abstraction with combined production of octane product from the hydrocarbon mixture that contains normal heptane, all right co-producing high-purity octane product in production high purity normal heptane product, and can significantly improve the octane value of inhaling surplus liquid, avoid rectification method energy consumption height, low, the process complicated problems of yield.
Technical scheme of the present invention is a kind of process for skellysolve C abstraction with combined production of octane product by pressure swing adsorption method, its concrete steps are as follows: the hydrocarbon mixture that (A) will contain normal heptane, pass through psa unit, obtain normal heptane or normal heptane and octane mixture, normal heptane can be used as high purity normal heptane product, and normal heptane and octane mixture carry out later separation; (B) above-mentioned gained normal heptane and octane mixture are delivered to rectifying tower, the rectifying tower cat head obtains highly purified normal heptane product, obtains highly purified octane product at the bottom of the rectifying Tata.
Above-mentioned psa unit is made up of three ADSORPTION IN A FIXED BED towers that load sorbent material at least, be the multitower transformation adsorption process of heating, may further comprise the steps: (1) adsorption process, the hydrocarbon mixture raw material that contains normal heptane enters the ADSORPTION IN A FIXED BED tower that loads sorbent material continuously after the vaporizing chamber vaporization, normal heptane in the raw material and octane are adsorbed agent absorption, and all the other components are collected as at overhead condensation inhales surplus liquid; (2) all pressure drops, put pressure, above-mentioned adsorption tower is after finishing adsorption process, and its adsorption column pressure is used to another is finished the adsorption tower of desorption process and all presses, again through forward put pressure, reverse putting is depressed into (absolute pressure) about normal pressure 0.1Mpa; (3) desorption process is depressed into non-pressurized adsorption tower and carries out desorb above-mentioned putting, and obtains normal heptane or normal heptane and octane mixture, and normal heptane can be used as high purity normal heptane product, and normal heptane and octane mixture carry out later separation; (4) all voltage rises, pressurising, finishing the adsorption tower of desorption process is all pressed by another adsorption tower of finishing adsorption process, inhale residual air to this adsorption tower pressurising with residual gas behind unstripped gas or absorption extracting normal heptane and the octane again, prepare to enter next round-robin adsorption process; So far, this tower has been finished the transformation sorption cycle one time.
The present invention delivers to rectifying tower with desorption process gained normal heptane with the octane mixture and separates, and rectifying tower top obtains the normal heptane product that content is 95%～99.9% (wt), preferred normal heptane 〉=99% (wt); Obtaining content at the bottom of the rectifying tower is the octane product of 95%～99.9% (wt), preferred octane 〉=99% (wt).
The above-mentioned hydrocarbon mixture that contains normal heptane that is used for skellysolve C abstraction with combined production of octane product is reforming raffinate oil, petroleum fractions or No. 120 solvent oils of 90～120 ℃.
Aforesaid method pressure-swing adsorption process processing condition are: 120～450 ℃ of vaporizing chamber vaporization temperatures, 120～450 ℃ of adsorption tower temperature, adsorption process pressure is 0.1～1.7MPa (absolute pressure), and desorption process pressure is 0.1～100kPa (absolute pressure), and the transformation sorption cycle cycle is 4～60min.
The sorbent material that above-mentioned pressure-swing adsorption process is used is mordenite, ZSM type molecular sieve, type T molecular sieve, 5A molecular sieve or phosphate aluminium molecular sieve, preferred phosphate aluminium molecular sieve.
Process for skellysolve C abstraction with combined production of octane product by pressure swing adsorption desorption process of the present invention is that desorption process is to carry out under 120～450 ℃ of adsorption temps, and the desorption method that is adopted is: vacuumize desorb; Vacuumize and be lower than 25 ℃ non-condensable gases (N simultaneously with boiling point under the normal pressure
2, H
2, A
r, H
e, CH
4, CO
2) or purge desorb with low carbon atom normal paraffin (Skellysolve A or normal hexane); Vacuumize simultaneously with product gas (normal heptane or normal heptane and octane mixture), usefulness ammonia, water vapour or ammonia and water vapor displacement desorption.
Said extracted normal heptane product coproduction octane product process flow is the heat combination of transformation adsorption process (or being called transformation heat of adsorption method flow process) and rectifying separation flow process of multitower.Preferred three towers to ten tower of multitower transformation adsorption process (or being called transformation heat of adsorption method flow process) the transformation adsorption process of heating, the best are the four towers transformation adsorption process of heating.
Do detailed explanation below in conjunction with 1 pair of technological process of the present invention of accompanying drawing, 1. the hydrocarbon mixture that contains normal heptane among the raw material storage tank V1 is entered vaporizing chamber H1 through feedstock pump P1, unstripped gas after the vaporization reaches 120～450 ℃ of adsorption temps, pressure is 0.1～1.7MPa, enter the adsorption tower T1 that finishes pressurising, in the adsorption tower temperature is 120～450 ℃, pressure is under 0.1～1.7MPa, normal heptane in the unstripped gas or normal heptane and octane mixture are adsorbed agent absorption, all the other components or suction residual air are 2. through interchanger E1 condensation, enter and inhale surplus liquid storage tank V2, according to use raw material difference, this inhales surplus liquid and can be used as further deep processing or separate raw materials, or still can be used as product (No. 120 solvent oils) sale.After adsorption process finishes, adsorption tower T1 and the adsorption tower T3 that finishes desorption and regeneration all press, again through forward put pressure, reverse putting is depressed into 0.1MPa, forward puts pressure, reverse putting presses the product (being called intermediates) obtain 3. after interchanger E2 condensation, enters intermediates storage tank V3.Forward put pressure, reverse put press finish after, under adsorption tower T1 desorption pressures 0.1～100kPa, separate sucking-off normal heptane or normal heptane and octane mixture 4., through interchanger E3 condensation, normal heptane can be used as the normal heptane product that content is 95%～99.9% (wt), preferred normal heptane 〉=99% (wt) high purity product, the normal heptane of separating sucking-off enters rectifying tower T5 with the octane mixture to be separated, rectifying tower T5 cat head obtain content be 95%～99.9% normal heptane product 5., preferred normal heptane 〉=99% (wt); Obtain content at the bottom of the rectifying tower T5 tower and be 95%～99.9% octane product 6., preferred octane 〉=99% (wt).The adsorption tower T1 that finishes desorption process is done after the adsorption tower T3 of adsorption process all presses, again with raw material or inhale residual air and finally be pressurized to adsorptive pressure.So far, adsorption tower T1 has finished a transformation sorption cycle, and other adsorption tower distributed according to transformation sorption cycle process and time, was in the various process of transformation sorption cycle respectively.
Beneficial effect:
Skellysolve C abstraction with combined production of octane product by pressure swing adsorption production method of the present invention is that a kind of equipment is simple, easy to operate, energy consumption is low, level of automation is high, easy to operate, the vanguard technology that is rich in characteristics such as the market competitiveness.Not only technology is simple, but co-producing high-purity octane product also in production high purity normal heptane product, the octane value of inhaling surplus liquid significantly improves, inhaling surplus liquid can directly sell as product (as: No. 120 solvent oils), also can be used as high-quality fuel oil additives, or as further deep processing raw material.The present invention can significantly improve C
7The level of resources utilization has good economic worth and social benefit.
Description of drawings:
Fig. 1 is four tower process for skellysolve C abstraction with combined production of octane product by pressure swing adsorption schematic flow sheets, wherein V1 is that raw material storage tank, V2 are that product storage tank between surplus liquid storage tank, V3 are, V4 are that high purity normal heptane product storage tank, V5 are purity octane product storage tank, T1, T2, T3, T4 are four ADSORPTION IN A FIXED BED towers that sorbent material is housed, T5 is a rectifying tower, H1 is the feed vaporization chamber, E1, E2, E3 are respectively three interchanger, and P1 is a feedstock pump, and P2 is a vacuum pump; 1. being raw material, for inhaling residual air, 3. is intermediates gas 2., 4. is high purity normal heptane product or normal heptane and octane mixture, 5. high purity normal heptane product, 6. high purity octane product.
Fig. 2 adopts for desorb and vacuumizes four tower process for skellysolve C abstraction with combined production of octane product by pressure swing adsorption schematic flow sheets of nitrogen purging mode simultaneously, removes many one road N of four ADSORPTION IN A FIXED BED column overhead among the figure
2Purge pipeline, other flow process is identical with Fig. 1.
Fig. 3 is seven tower process for skellysolve C abstraction with combined production of octane product by pressure swing adsorption schematic flow sheets, wherein V1 is that raw material storage tank, V2 are that product storage tank between surplus liquid storage tank, V3 are, V4 are that high purity normal heptane product storage tank, V5 are purity octane product storage tank, T1, T2, T3, T4, T5, T6, T7 are seven ADSORPTION IN A FIXED BED towers that load sorbent material, T8 is a rectifying tower, H1 is the feed vaporization chamber, E1, E2, E3 are respectively three interchanger, and P1 is a feedstock pump, and P2 is a vacuum pump; 1. being raw material, for inhaling residual air, 3. is intermediates gas 2., 4. is high purity normal heptane product or normal heptane and octane mixture, 5. high purity normal heptane product, 6. high purity octane product.
Embodiment:
Embodiment 1: adopting No. 120 solvent oils is raw material,, the SAPO-34 molecular sieve is a sorbent material, and No. 120 solvent oil typical case composition is as shown in table 1, and the four tower pressure swing adsorption process schematic flow sheet is as shown in Figure 1.
Table 1120 solvent oil is formed
| The component title | Normal paraffin content (wt%) | Isoparaffin content (wt%) |
| C6 C7 C8 C9 total content (wt%) | — 13.45 2.01 — 15.46 | 21.27 51.08 10.97 1.22 84.54 |
Four towers (T1, T2, T3, T4) transformation sorption cycle process and time distribute as shown in table 2, and a transformation sorption cycle cycle is 16min, wherein adsorbs 4min, and all pressure drop 2min is put and pressed 2min, desorb 4min, equal voltage rise 2min, pressurising 2min.
Table 2 four tower transformation sorption cycle processes and time distribute
| Time/min | 4 | 2 | 2 | 4 | 2 | 2 |
| T1 | A | ED | CD | V | ER | R |
| T2 | ER | R | A | ED | CD | V | ||
| T3 | V | ER | R | A | ED | CD | ||
| T4 | ED | CD | V | ER | R | A | ||
[notes]: A-attached, ED-all pressure drops, CD-put pressure, V-desorb, ER-all voltage rises, R-pressurising.
According to process for skellysolve C abstraction with combined production of octane product by pressure swing adsorption schematic flow sheet 1,1. No. 120 solvent oils enter vaporizing chamber H1 through feedstock pump P1 among the head tank V1, under 260 ℃, 1.4MPa, vaporize, vaporization back unstripped gas enters the adsorption tower T1 that finishes pressurising, under 260 ℃, 1.4MPa, normal heptane in the unstripped gas or normal heptane and octane mixture are by the SAPO-34 molecular sieve adsorption, inhale residual air and 2. be condensed into the surplus liquid of suction through interchanger E1, enter and inhale surplus liquid storage tank V2, this is inhaled surplus liquid and still can be used as No. 120 solvent oils sales.After absorption finished, adsorption tower T1 and the adsorption tower T3 that finishes regenerative process all pressed, and reduce to 0.7MPa, and reverse the putting of adsorption tower T1 is depressed into 0.1MPa then, and reverse putting presses the product (being called intermediates) that obtains 3. to enter intermediates storage tank V3 after interchanger E2 condensation.Reverse put press finish after, adsorption tower T1 is evacuated to desorption pressures 30kPa, the mixture of separating sucking-off normal heptane and octane enters rectifying tower T5 and separates (see figure 1) 4. through interchanger E3 condensation, the normal heptane product that rectifying tower T5 cat head obtains content 99% is 5.; The octane product that obtains content 99% at the bottom of the rectifying tower T5 tower 6..The adsorption tower T1 that finishes desorption and regeneration all presses with the adsorption tower T3 that finishes adsorption process, rises to 0.7MPa, with unstripped gas this adsorption tower is pressurized to adsorptive pressure 1.4MPa then, prepares to enter next round-robin adsorption process.So far, this tower has been finished the transformation sorption cycle one time.Other three tower distributed according to transformation sorption cycle process and time, was in the various process of transformation sorption cycle respectively.
Embodiment 2, as shown in Figure 2.Transformation adsorption process, specific operation process and step are equal to embodiment 1, and what they were different is: adsorption temp is 160 ℃, and desorb is adopted to vacuumize and used N simultaneously
2Purge, desorption pressures is 40kPa.
Embodiment 3, and the employing reforming raffinate oil is a raw material, and the 5A molecular sieve is a sorbent material, and reforming raffinate oil is formed as shown in table 3, and seven tower pressure swing adsorption technique schematic flow sheets as shown in Figure 3.
Table 3 reforming raffinate oil is formed
| The component title | Normal paraffin content (wt%) | Isoparaffin content (wt%) |
| C6 C7 C8 C9 total content (wt%) | — 6.81 1.04 — 7.85 | 20.48 52.08 16.37 3.22 92.15 |
Seven towers (T1, T2, T3, T4, T5, T6, T7) transformation sorption cycle process and time distribute as shown in table 4, and a transformation sorption cycle cycle is 21min, wherein adsorbs 6min, one all, three be 2min, put and press 2min, desorb 3min.
Table 4 seven tower transformation sorption cycle processes and time distribute
| Time/min | 6 | 1 | 2 | 1 | 2 | 3 | 1 | 2 | 1 | 2 | ||||
| T1 | A | ED1 | ED2 | ED3 | CD | V | ER1 | ER2 | ER3 | R | ||||
| T2 | ER3 | R | A | ED1 | ED2 | ED3 | CD | V | ER1 | ER2 | ||||
| T3 | ER1 | ER2 | ER3 | R | A | ED1 | ED2 | ED3 | CD | V | ||||
| T4 | V | ER1 | ER2 | ER3 | R | A | ED1 | ED2 | ED3 | CD | ||||
| T5 | ED3 | CD | V | ER1 | ER2 | ER3 | R | A | ED1 | ED2 | ||||
| T6 | ED1 | ED2 | ED3 | CD | V | ER1 | ER2 | ER3 | R | A | ||||
| T7 | A | ED1 | ED2 | ED3 | CD | V | ER1 | ER2 | ER3 | R | A | |||
[notes]: A-absorption, ED1-one equal pressure drop, ED2-two equal pressure drops, ED3-three equal pressure drops, CD-is put pressure, V-desorb, the equal voltage rise of ER1-, ER2-two equal voltage rises, ER3-three equal voltage rises, R-pressurising.
As Fig. 3,1. reforming raffinate oil among the head tank V1 enters vaporizing chamber H1 through feedstock pump P1, under 380 ℃, 1.6MPa, vaporize, vaporization back unstripped gas enters the adsorption tower T1 that finishes pressurising, under 380 ℃, 1.6MPa, normal heptane in the unstripped gas or normal heptane and octane mixture are adsorbed agent absorption, inhale residual air and 2. are condensed into the surplus liquid of suction through interchanger E1, enter and inhale surplus liquid storage tank V2; Adsorption tower T1 finishes after the adsorption process at first and finishes the two adsorption tower T4 that all rise and carry out one and all fall, and adsorption tower T1 pressure is reduced to 1.2MPa; Adsorption tower T1 then carries out two with adsorption tower T5 and all falls after finishing the drop pressure first time, and pressure is reduced to 0.8MPa; Adsorption tower T1 carries out three with the adsorption tower T6 that just finishes desorption process again and all falls after finishing the drop pressure second time, and pressure is reduced to 0.4MPa; After adsorption tower T1 finishes three equal pressure drops, forward put again and be depressed into 0.1MPa, 3. (be called intermediates) and after interchanger E2 condensation, enter intermediates storage tank V3 along putting the product that obtains.Along after putting end, T1 is evacuated to 10kPa to adsorption tower, and the mixture of separating sucking-off normal heptane and octane enters rectifying tower T5 and separates (see figure 3) 4. through interchanger E3,5. the normal heptane product that rectifying tower T8 cat head obtains content 99% obtains the octane product of content 99% at the bottom of the rectifying tower T8 tower.Then, adsorption tower T1 is carried out one all rise with having finished the two adsorption tower T3 pressure that all fall process, pressure rises to 0.4MPa; Adsorption tower T1 again with finish an adsorption tower T4 who all falls process and carry out two and all rise, pressure rises to 0.8MPa; After finishing twice equal voltage rise, adsorption tower T1 carries out three with the adsorption tower T5 that just finishes adsorption process and all rises, and pressure rises to 0.8MPa; Finish the adsorption tower T1 that all presses for three times after the pressurising and be pressurized to adsorptive pressure 1.6MPa, prepare to enter next round-robin adsorption process with unstripped gas.So far, this tower has been finished the transformation sorption cycle one time.Other six towers distributed according to transformation sorption cycle process and time, were in the various process of transformation sorption cycle respectively.
Claims (9)
1. process for skellysolve C abstraction with combined production of octane product by pressure swing adsorption method, its concrete steps are as follows: the hydrocarbon mixture that (A) will contain normal heptane, pass through psa unit, obtain normal heptane or normal heptane and octane mixture, normal heptane is as high purity normal heptane product, and normal heptane and octane mixture carry out later separation; (B) above-mentioned gained normal heptane and octane mixture are delivered to rectifying tower, the rectifying tower cat head obtains highly purified normal heptane product, obtains highly purified octane product at the bottom of the rectifying Tata.
2. method according to claim 1, the hydrocarbon mixture that it is characterized in that containing normal heptane are reforming raffinate oil, petroleum fractions or No. 120 solvent oils of 900 ~ 120 ℃.
3. method according to claim 1, it is characterized in that psa unit is made up of three ADSORPTION IN A FIXED BED towers that load sorbent materials at least, be the multitower transformation adsorption process of heating, may further comprise the steps: (1) adsorption process, the hydrocarbon mixture raw material that contains normal heptane enters the ADSORPTION IN A FIXED BED tower that loads sorbent material continuously after the vaporizing chamber vaporization, normal heptane in the raw material and octane are adsorbed agent absorption, and all the other components are collected as at overhead condensation inhales surplus liquid; (2) all pressure drops, put pressure, above-mentioned adsorption tower is after finishing adsorption process, and its adsorption column pressure is used to another is finished the adsorption tower of desorption process and all presses, again through forward put pressure, reverse putting is depressed into normal pressure; (3) desorption process is depressed into non-pressurized adsorption tower and carries out desorb above-mentioned putting, and obtains normal heptane or normal heptane and octane mixture, and normal heptane can be used as high purity normal heptane product, and normal heptane and octane mixture carry out later separation;
(4) all voltage rises, pressurising, finishing the adsorption tower of desorption process is all pressed by another adsorption tower of finishing adsorption process, inhale residual air to this adsorption tower pressurising with residual gas behind unstripped gas or absorption extracting normal heptane and the octane again, prepare to enter next round-robin adsorption process; So far, this tower has been finished the transformation sorption cycle one time.
4. method according to claim 3,120～450 ℃ of vaporization temperatures that it is characterized in that vaporizing chamber, 120～450 ℃ of adsorption tower temperature, adsorption process pressure is 0.1～1.7MPa, desorption process pressure is 0.1～100kPa, and the transformation sorption cycle cycle is 4～60min.
5. method according to claim 3 is characterized in that the sorbent material that the ADSORPTION IN A FIXED BED tower loads is mordenite, ZSM type molecular sieve, type T molecular sieve, 5A molecular sieve or phosphate aluminium molecular sieve.
6. according to the described method of claim 5, it is characterized in that the sorbent material that the ADSORPTION IN A FIXED BED tower loads is a phosphate aluminium molecular sieve.
7. method according to claim 3 is characterized in that desorption process is to carry out under 120～450 ℃ of adsorption temps, the desorption method that is adopted is: vacuumize desorb; Vacuumize simultaneously with product gas, usefulness ammonia, water vapour or ammonia and water vapor displacement desorption; Vacuumize and be lower than 25 ℃ non-condensable gases N simultaneously with boiling point under the normal pressure
2, H
2, Ar, He, CH
4, CO
2Or purge desorb with low carbon atom normal paraffin Skellysolve A, normal hexane.
8. method according to claim 1 is characterized in that the ADSORPTION IN A FIXED BED tower of psa unit loading sorbent material is three towers to ten towers;
9. method according to claim 8 is characterized in that the ADSORPTION IN A FIXED BED tower of psa unit loading sorbent material is four towers.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2012065364A1 (en) * | 2010-11-15 | 2012-05-24 | Zhou Xiangjin | Method for joint production of low octane number gasoline and high octane number gasoline |
| CN103467229A (en) * | 2013-09-18 | 2013-12-25 | 中石化上海工程有限公司 | Method for separating n-alkane from isoparaffin by combining pressure swing adsorption and membrane separation |
| CN107266277A (en) * | 2017-07-04 | 2017-10-20 | 滁州市润达溶剂有限公司 | A kind of removing of the low temperature from solvent naphtha isoparaffin purification normal heptane, the technique of n-hexane |
| 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 |
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2007
- 2007-10-12 CN CN200710133497A patent/CN100575322C/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2012065364A1 (en) * | 2010-11-15 | 2012-05-24 | Zhou Xiangjin | Method for joint production of low octane number gasoline and high octane number gasoline |
| US9428697B2 (en) | 2010-11-15 | 2016-08-30 | Xiangjin Zhou | Method for joint production of low octane number gasoline and high octane number gasoline |
| EA025230B1 (en) * | 2010-11-15 | 2016-12-30 | Сянцзинь Чжоу | Method for joint production of low octane number gasoline and high octane number gasoline |
| CN103467229A (en) * | 2013-09-18 | 2013-12-25 | 中石化上海工程有限公司 | Method for separating n-alkane from isoparaffin by combining pressure swing adsorption and membrane separation |
| CN103467229B (en) * | 2013-09-18 | 2015-01-07 | 中石化上海工程有限公司 | Method for separating n-alkane from isoparaffin by combining pressure swing adsorption and membrane separation |
| CN107266277A (en) * | 2017-07-04 | 2017-10-20 | 滁州市润达溶剂有限公司 | A kind of removing of the low temperature from solvent naphtha isoparaffin purification normal heptane, the technique of n-hexane |
| CN107266277B (en) * | 2017-07-04 | 2021-07-16 | 滁州市润达溶剂有限公司 | Process for purifying n-heptane and n-hexane by removing isoparaffin from solvent oil at low temperature |
| 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 |
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|---|---|
| CN100575322C (en) | 2009-12-30 |
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