CN109401779B - A kind of method and device for cutting Fischer-Tropsch synthetic light oil by next-door tower - Google Patents
A kind of method and device for cutting Fischer-Tropsch synthetic light oil by next-door tower Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 27
- 238000005520 cutting process Methods 0.000 title claims abstract description 10
- 238000000926 separation method Methods 0.000 claims abstract description 160
- 238000005192 partition Methods 0.000 claims abstract description 97
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 16
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 16
- 238000010992 reflux Methods 0.000 claims description 94
- 238000003786 synthesis reaction Methods 0.000 claims description 42
- 230000015572 biosynthetic process Effects 0.000 claims description 41
- 239000007789 gas Substances 0.000 claims description 40
- 239000012071 phase Substances 0.000 claims description 38
- 239000007791 liquid phase Substances 0.000 claims description 37
- 239000002994 raw material Substances 0.000 claims description 27
- 229930195733 hydrocarbon Natural products 0.000 claims description 22
- 150000002430 hydrocarbons Chemical class 0.000 claims description 22
- 150000001336 alkenes Chemical class 0.000 claims description 12
- 238000004821 distillation Methods 0.000 claims description 12
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 8
- 150000001875 compounds Chemical class 0.000 claims description 8
- -1 cyclic olefins Chemical class 0.000 claims description 8
- 229910052760 oxygen Inorganic materials 0.000 claims description 8
- 239000001301 oxygen Substances 0.000 claims description 8
- 239000004711 α-olefin Substances 0.000 claims description 7
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 3
- GGQQNYXPYWCUHG-RMTFUQJTSA-N (3e,6e)-deca-3,6-diene Chemical compound CCC\C=C\C\C=C\CC GGQQNYXPYWCUHG-RMTFUQJTSA-N 0.000 claims 1
- 238000007599 discharging Methods 0.000 claims 1
- 230000008901 benefit Effects 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000005516 engineering process Methods 0.000 abstract description 2
- 238000000746 purification Methods 0.000 abstract description 2
- 238000009835 boiling Methods 0.000 abstract 1
- 238000011084 recovery Methods 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 39
- 239000000047 product Substances 0.000 description 36
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 15
- 239000004215 Carbon black (E152) Substances 0.000 description 9
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 description 9
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 6
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 6
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 6
- 239000002283 diesel fuel Substances 0.000 description 5
- 239000012188 paraffin wax Substances 0.000 description 5
- 239000001993 wax Substances 0.000 description 5
- GXDHCNNESPLIKD-UHFFFAOYSA-N 2-methylhexane Natural products CCCCC(C)C GXDHCNNESPLIKD-UHFFFAOYSA-N 0.000 description 4
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 4
- 239000003502 gasoline Substances 0.000 description 4
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 4
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- 239000002253 acid Substances 0.000 description 3
- 150000001299 aldehydes Chemical class 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 150000002576 ketones Chemical class 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 239000012043 crude product Substances 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000005984 hydrogenation reaction Methods 0.000 description 2
- 239000003915 liquefied petroleum gas Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- NHTMVDHEPJAVLT-UHFFFAOYSA-N Isooctane Chemical compound CC(C)CC(C)(C)C NHTMVDHEPJAVLT-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- JVSWJIKNEAIKJW-UHFFFAOYSA-N dimethyl-hexane Natural products CCCCCC(C)C JVSWJIKNEAIKJW-UHFFFAOYSA-N 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1022—Fischer-Tropsch products
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
本发明涉及一种用于利用隔壁塔切割费托合成轻油，得到各碳数馏分段产品的方法与装置，该工艺可采用三个单隔壁塔的流程，也可采用两个双隔壁塔或一个五隔壁塔的流程，其中三个单隔壁塔的流程和两个双隔壁塔的流程可以采用不同的分离序列。经该工艺分离提纯后，C6‑C10馏分段产品的质量含量可以达到99％以上，回收率可以达到95％以上。本发明的特点是借助隔壁塔技术，将不同沸点的产品分离，可大大降低能耗及设备费用，创造较高的经济效益。
The invention relates to a method and a device for cutting Fischer-Tropsch synthetic light oil by using a dividing wall column to obtain fractional products of various carbon numbers. A five-partition-wall column process, three single-partition-wall column processes and two double-partition-wall column processes can employ different separation sequences. After separation and purification by this process, the mass content of the C6-C10 fractionated products can reach more than 99%, and the recovery rate can reach more than 95%. The feature of the invention is that the products with different boiling points are separated by means of the partition tower technology, which can greatly reduce the energy consumption and equipment cost and create higher economic benefits.
Description
Technical Field
The invention relates to a method and a device for cutting Fischer-Tropsch synthesis light oil by a bulkhead tower to obtain products of each carbon number fraction section, which are particularly suitable for cutting Fischer-Tropsch synthesis light oil mainly containing C6-C10 fractions.
Background
Fischer-Tropsch synthesis, i.e. an indirect coal liquefaction process, in the presence of a catalyst, gasifying the synthesis gas (CO, H)2) Converting into gasoline, diesel oil and other hydrocarbon products. The crude reaction products mainly comprise light oil, heavy oil and heavy wax. The Fischer-Tropsch synthesis product is usually used for further producing products such as gasoline, diesel oil, naphtha and the like, and olefin in the products needs to be subjected to hydrotreating, so that waste of alpha-olefin components with higher added values is caused. The main substances in the Fischer-Tropsch synthesis light oil are normal paraffin and normal olefin of C6-C10, the olefin component is mostly alpha-olefin, and the Fischer-Tropsch synthesis light oil has the characteristics of low sulfur content, almost no aromatic hydrocarbon and the like. If the substances in the Fischer-Tropsch synthesis product can be separated and refined by adopting a proper method, high value-added products can be further produced, the diesel oil is reduced, the products are refined, and the economic benefit is greatly improved.
The patent CN107267212A provides a separation process of Fischer-Tropsch synthesized crude products, which comprises a plurality of process steps of raw oil crude separation, oil hydrogenation, light hydrocarbon fine separation, wax hydrogenation, wax fine separation and the like, and according to the difference of the synthesis temperature of the Fischer-Tropsch synthesized crude products, various high value-added products such as naphtha, n-pentane, n-hexane, n-heptane, n-octane, C50, C70, C80 series wax, H1, H105 series wax and the like with different quantities can be obtained. Firstly, crude separation is carried out on raw oil products to obtain C5-C8 fraction, and the fraction is sent to a light component separation tower to carry out fine separation on light hydrocarbon; distilling C5 and C6 from the top of the light component separation tower, distilling C7 and C8 from the bottom of the tower, respectively feeding the material flows from the top of the tower and the bottom of the tower into a C5 separation tower and a C7 separation tower to obtain C5, C6, C7 and C8 components, respectively feeding the C5, C6, C7 and C8 components into alkane purification towers with carbon number, and finally obtaining products of n-pentane, n-hexane, n-heptane and n-octane with the purity of more than 99.9 wt%, and simultaneously obtaining byproducts of isopentane, isohexane, isoheptane, isooctane and the like. The patent CN107325838A is similar to the flow of the above patent, crude separation of raw oil products is carried out to obtain C5-C7 fraction, then products of n-pentane, n-hexane and n-heptane with purity of more than 99.9 wt% are obtained by fine separation of light hydrocarbon, and byproducts of isopentane, isohexane, isoheptane and the like are obtained at the same time.
The patent CN107916127A relates to a rectification process for Fischer-Tropsch synthesis product separation, and the rectification process adopts three-stage separation and then realizes five-stage fraction separation through four-tower rectification. Separating the oil phase from the water phase by the Fischer-Tropsch product raw material respectively passing through a first-stage condenser, a first-stage separator, a second-stage water cooler, a second-stage separator, a third-stage deep cooler and a third-stage separator, wherein upper liquid phases of the first-stage separator, the second-stage separator and the third-stage separator are respectively heavy hydrocarbon, light hydrocarbon and respectively enter a dry gas rectifying tower; the crude oil sequentially passes through four rectifying towers, namely a dry gas rectifying tower, a liquefied petroleum gas rectifying tower, a C5-C10 rectifying tower, a C11-C19 rectifying tower and the like to respectively obtain five products, namely dry gas (C1-C2), liquefied petroleum gas (C3-C4), C5-C10 fraction section, C11-C19 fraction section, C20+ fraction section and the like.
The patent CN101275080A relates to a separation method of Fischer-Tropsch reaction products, and mainly solves the problem that the separation of gasoline and diesel oil which are the products of the existing Fischer-Tropsch synthesis reaction is difficult. The hydrocarbon product obtained after the Fischer-Tropsch reaction is introduced into a separation device; and separating the product by a separating device to obtain a hydrocarbon and heavy hydrocarbon product containing gasoline and diesel oil, wherein the separating device comprises a hot trap tower and a heater, the heater is arranged at the lower part of the hot trap tower, the temperature control range of the bottom of the hot trap tower is 120-400 ℃, and the temperature control range of the top of the hot trap tower is 25-150 ℃.
The above documents generally have the problems of unclear fractionation section of the obtained product, difficulty in fine utilization of the product, and the like, and have the defects of complicated flow, and high energy consumption and equipment cost. The invention provides a novel process method and a novel device for separating products of each carbon number fraction section from Fischer-Tropsch oil with high efficiency and energy saving.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provides a high-efficiency and energy-saving method and device for separating and purifying products in each carbon number fraction section in Fischer-Tropsch synthesis light oil.
The technical method provided by the invention adopts a bulkhead tower technology to cut products of each carbon number fraction section of Fischer-Tropsch synthesis light oil, so as to respectively obtain products of C6-C10 fraction sections.
The process can adopt the flow of three single partition wall towers, and also can adopt the flow of two double partition wall towers or one five partition wall tower. Wherein, the flow of three single-partition towers and the flow of two double-partition towers can adopt different separation sequences, and the specific flow is as follows.
(1) Three single dividing wall tower process
(a) First separation sequence (see FIG. 1-1)
Feeding a Fischer-Tropsch synthesis light oil raw material (S01) into a T11 pre-separation tower, taking a fraction lighter than C6 from the top of the T11 (S02), taking a fraction heavier than C10 from the bottom of the T11 tower (S08), taking a C6-C10 fraction (S09) from the main tower side line of the T11, and feeding the fraction into the T12 pre-separation tower; c6 fraction (S03) is extracted from the top of the T12 tower, C10 fraction (S07) is extracted from the bottom of the T12 tower, and C7-C9 fraction (S10) is extracted from the main tower side line of the T12 and enters a T13 pre-separation tower; a C7 fraction (S04) is extracted from the top of the T13 tower, a C9 fraction (S06) is extracted from the bottom of the T13 tower, and a C8 fraction (S05) is extracted from the side of the T13 main tower.
(b) Second separation sequence (see FIGS. 1-2)
Feeding a Fischer-Tropsch synthesis light oil raw material (S01) into a T11 pre-separation tower, taking a fraction lighter than C6 from the top of the T11 (S02), taking a fraction C9 and heavier from the bottom of the T11 tower (S11), taking a fraction C6-C8 (S12) from the main tower side line of the T11, feeding the fraction into the T12 pre-separation tower, and feeding the fraction into a T13 pre-separation tower; a C6 fraction section (S03) is extracted from the top of the T12 tower, a C8 fraction section (S05) is extracted from the bottom of the tower, and a C7 fraction section (S04) is extracted from the side of the T12 main tower; the top of the T13 column was taken as a C9 cut (S06), the bottom was taken as a heavier than C10 cut (S08), and the side of the T13 column was taken as a C10 cut (S07).
(c) Third separation sequence (see FIGS. 1-3)
Feeding a Fischer-Tropsch synthesis light oil raw material (S01) into a T11 pre-separation tower, taking a fraction (S13) lighter than C7 at the top of the T11 tower, feeding the fraction into a T12 pre-separation tower, taking a fraction (S08) heavier than C10 at the bottom of the T11 tower, taking a C8-C10 fraction (S14) from the side line of the T11 main tower, and feeding the fraction into a T13 pre-separation tower; the T12 takes a fraction lighter than C6 at the top (S02), takes a C7 fraction section (S04) at the bottom, and takes a C6 fraction section (S03) from the main column side of the T12; the top of the T13 column was taken as the C8 cut (S05), the bottom was taken as the C10 cut (S07), and the C9 cut was taken from the main side of the T13 column (S06).
(d) Fourth separation sequence (see FIGS. 1-4)
The Fischer-Tropsch synthesis light oil raw material (S01) enters a T11 pre-separation tower, C7 and lighter fractions (S13) are extracted from the top of the T11 and enter a T12 pre-separation tower, C9 and heavier fractions (S11) are extracted from the bottom of the T11 tower and enter a T13 pre-separation tower, and C8 fractions (S05) are extracted from the side line of the T11 main tower; the T12 takes a fraction lighter than C6 at the top (S02), takes a C7 fraction section (S04) at the bottom, and takes a C6 fraction section (S03) from the main column side of the T12; a C9 fraction (S06) is taken from the top of the T13 column, a fraction heavier than C10 is taken from the bottom of the T3578 column (S08), and a C10 fraction (S07) is taken from the main column side of the T13 column.
(2) Two double dividing wall tower flow
(a) First separation sequence (see FIG. 2-1)
Feeding a Fischer-Tropsch synthesis light oil raw material (S01) into a T21 pre-separation tower, extracting a fraction lighter than C6 from the top of the T21 (S02), extracting a C6-C9 fraction (S15) from the upper side line of a T21 main tower, feeding the fraction into a T22 pre-separation tower, extracting a C10 fraction section (S07) from the lower side line of the T21 main tower, and extracting a fraction heavier than C10 from the bottom of a T21 tower (S08); the top of the T22 is provided with a C6 fraction (S03), the upper side and the lower side of the T22 main column are provided with a C7 fraction (S04), a C8 fraction (S05) and the bottom of the T22 column is provided with a C9 fraction (S06).
(b) Second separation sequence (see FIG. 2-2)
Feeding a Fischer-Tropsch synthesis light oil raw material (S01) into a T21 pre-separation tower, extracting a fraction lighter than C6 (S02) from the top of the T21 tower, extracting a C6 fraction section (S03) from the upper side line of a T21 main tower, extracting a C7-C10 fraction (S16) from the lower side line of a T21 main tower, feeding the fraction into the T22 pre-separation tower, and extracting a fraction heavier than C10 from the bottom of a T21 tower (S08); the top of the T22 is provided with a C7 fraction (S04), the upper side and the lower side of the T22 main column are provided with a C8 fraction (S05), a C9 fraction (S06) and the bottom of the T22 column is provided with a C10 fraction (S07).
(c) Third separation sequence (see FIGS. 2-3)
Feeding a Fischer-Tropsch synthesis light oil raw material (S01) into a T21 pre-separation tower, extracting a fraction (S02) lighter than C6 from the top of the T21 tower, extracting a C6 distillation section (S03) and a C7 distillation section (S04) from the upper side line and the lower side line of a T21 main tower respectively, extracting a C8 fraction and a heavier fraction (S17) from the bottom of the T21 tower, and feeding the fractions into a T22 pre-separation tower; a C8 fraction (S05) is taken out from the top of the T22 column, a C9 fraction (S06) and a C10 fraction (S07) are taken out from the upper side line and the lower side line of the T22 main column, and a fraction heavier than C10 is taken out from the bottom of the T22 column (S08).
(d) Fourth separation sequence (see FIGS. 2-4)
The Fischer-Tropsch synthesis light oil raw material (S01) enters a T21 pre-separation tower, C6 and lighter fractions (S18) are extracted from the top of the T21 pre-separation tower and enter a T22 pre-separation tower, C9 distillation sections (S06) and C10 distillation sections (S07) are extracted from the upper side line and the lower side line of a T21 main tower respectively, and fractions heavier than C10 are extracted from the bottom of a T21 tower (S08); the top of the T22 column is provided with lighter fractions than C6 (S02), C6 fraction (S03) and C7 fraction (S04) are provided from the upper side and the lower side of the T22 main column, and C8 fraction (S05) is provided from the bottom of the T22 column.
(3) A five-compartment tower process (as shown in figure 3)
The Fischer-Tropsch synthesis light oil raw material (S01) enters a T3 pre-separation tower, is separated by a plurality of clapboards w11, w21-22, w31-33, w41-44 and w51-55 in the tower, finally, a component lighter than C6 is obtained at the top of the T3 tower (S02), products of C6-C10 fractional segments (S03-S07) are respectively obtained from five side lines from top to bottom, and a component heavier than C10 is obtained at the bottom of the tower (S08).
In the process (1), the theoretical plate number of a pre-separation tower (area a in figure 4-1) of a T11 single-partition wall tower is 10-200, the theoretical plate number of a main tower (area b in figure 4-1) is 10-200, the theoretical plate number of a common rectification section (area c in figure 4-1) is 0-100, the theoretical plate number of a common stripping section (area d in figure 4-1) is 0-100, the mass fraction of a liquid phase reflux entering the pre-separation tower is 0.01-0.99, the mass fraction of a gas phase reflux entering the pre-separation tower is 0.01-0.99, the reflux ratio is 0.1-20, and the operation pressure is 0.05-5 atm; the number of theoretical plates of a pre-separation tower (area a in figure 4-1) of the T12 single-partition wall tower is 10-200, the number of theoretical plates of a main tower (area b in figure 4-1) is 10-200, the number of theoretical plates of a common rectification section (area c in figure 4-1) is 0-100, the number of theoretical plates of a common stripping section (area d in figure 4-1) is 0-100, the mass fraction of a liquid phase reflux entering the pre-separation tower is 0.01-0.99, the mass fraction of a gas phase reflux entering the pre-separation tower is 0.01-0.99, the reflux ratio is 0.1-20, and the operating pressure is 0.05-5 atm; the number of theoretical plates of a pre-separation tower (area a in figure 4-1) of the T13 single-partition wall tower is 10-200, the number of theoretical plates of a main tower (area b in figure 4-1) is 10-200, the number of theoretical plates of a common rectification section (area c in figure 4-1) is 0-100, the number of theoretical plates of a common stripping section (area d in figure 4-1) is 0-100, the mass fraction of a liquid phase reflux entering the pre-separation tower is 0.01-0.99, the mass fraction of a gas phase reflux entering the pre-separation tower is 0.01-0.99, the reflux ratio is 0.1-20, and the operating pressure is 0.05-5 atm.
In the flow (2), the number of theoretical plates of a pre-separation column (region e in FIG. 4-2) of a T21 double-dividing-wall column is 10 to 200, the number of theoretical plates of a first main column (region f in FIG. 4-2) is 10 to 200, the number of theoretical plates of a first common rectification section (region g in FIG. 4-2) is 0 to 100, the number of theoretical plates of a first common stripping section (region h in FIG. 4-2) is 0 to 100, the mass fraction of a liquid phase reflux entering the pre-separation column is 0.01 to 0.99, the mass fraction of a gas phase reflux entering the pre-separation column is 0.01 to 0.99, the number of theoretical plates of a second main column (region 5 in FIG. 4-2) is 10 to 200, the number of theoretical plates of a third main column (region j in FIG. 4-2) is 10 to 200, the number of theoretical plates of a second common column (region k in FIG. 4-2) is 0 to 100, and the number of theoretical plates of l in a second common stripping section (region 4-2) is 0 to 100, the mass fraction of the liquid phase reflux entering the pre-separation tower and the first main tower is 0.01-0.99, the mass fraction of the gas phase reflux entering the pre-separation tower and the first main tower is 0.01-0.99, the reflux ratio is 0.1-20, and the operating pressure is 0.05-5 atm; t22 double dividing wall column has a pre-separation column (region e in FIG. 4-2) theoretical plate number of 10-200, a first main column (region f in FIG. 4-2) theoretical plate number of 10-200, a first common rectification section (region g in FIG. 4-2) theoretical plate number of 0-100, a first common stripping section (region h in FIG. 4-2) theoretical plate number of 0-100, a liquid phase reflux entering the pre-separation column of 0.01-0.99, a gas phase reflux entering the pre-separation column of 0.01-0.99, a second main column (region 5 in FIG. 4-2) theoretical plate number of 10-200, a third main column (region j in FIG. 4-2) theoretical plate number of 10-200, a second common rectification section (region k in FIG. 4-2) theoretical plate number of 0-100, a second common stripping section (region l in FIG. 4-2) theoretical plate number of 0-100, the mass fraction of the liquid phase reflux entering the pre-separation tower and the first main tower is 0.01-0.99, the mass fraction of the gas phase reflux entering the pre-separation tower and the first main tower is 0.01-0.99, the reflux ratio is 0.1-20, and the operating pressure is 0.05-5 atm.
In the flow (3), the theoretical plate number of a pre-separation tower (area 1 in fig. 4-3) of a T3 five-partition wall tower is 10-200, the theoretical plate number of a first main tower (area 2 in fig. 4-3) is 10-200, the theoretical plate number of a first common rectification section (area 3 in fig. 4-3) is 0-100, the theoretical plate number of a first common stripping section (area 4 in fig. 4-3) is 0-100, the mass fraction of a liquid phase reflux entering the pre-separation tower is 0.01-0.99, and the mass fraction of a gas phase reflux entering the pre-separation tower is 0.01-0.99; the theoretical plate number of the second main tower (5 regions in fig. 4-3) is 10-200, the theoretical plate number of the third main tower (6 regions in fig. 4-3) is 10-200, the theoretical plate number of the second common rectification section (7 regions in fig. 4-3) is 0-100, the theoretical plate number of the second common stripping section (8 regions in fig. 4-3) is 0-100, the mass fraction of the liquid phase reflux entering the pre-separation tower and the first main tower is 0.01-0.99, and the mass fraction of the gas phase reflux entering the pre-separation tower and the first main tower is 0.01-0.99; the theoretical plate number of the fourth main tower (area 9 in fig. 4-3) is 10-200, the theoretical plate number of the fifth main tower (area 10 in fig. 4-3) is 10-200, the theoretical plate number of the sixth main tower (area 11 in fig. 4-3) is 10-200, the theoretical plate number of the third common rectification section (area 12 in fig. 4-3) is 0-100, the theoretical plate number of the third common stripping section (area 13 in fig. 4-3) is 0-100, the mass fraction of the liquid phase reflux entering the pre-separation tower, the first main tower and the second main tower is 0.01-0.99, and the mass fraction of the gas phase reflux entering the pre-separation tower, the first main tower and the second main tower is 0.01-0.99; the theoretical plate number of the seventh main tower (14 regions in fig. 4-3) is 10-200, the theoretical plate number of the eighth main tower (15 regions in fig. 4-3) is 10-200, the theoretical plate number of the ninth main tower (16 regions in fig. 4-3) is 10-200, the theoretical plate number of the tenth main tower (17 regions in fig. 4-3) is 10-200, the theoretical plate number of the fourth common rectification section (18 regions in fig. 4-3) is 0-100, the theoretical plate number of the fourth common rectification section (19 regions in fig. 4-3) is 0-100, the mass fraction of the liquid phase reflux entering the pre-separation tower plate, the first main tower, the second main tower and the fourth main tower is 0.01-0.99, and the mass fraction of the gas phase reflux entering the pre-separation tower, the first main tower, the second main tower and the fourth main tower is 0.01-0.99; the number of theoretical plates of an eleventh main column (20 regions in FIGS. 4-3) is 10 to 200, the number of theoretical plates of a twelfth main column (21 regions in FIGS. 4-3) is 10 to 200, the number of theoretical plates of a thirteenth main column (22 regions in FIGS. 4-3) is 10 to 200, the number of theoretical plates of a fourteenth main column (23 regions in FIGS. 4-3) is 10 to 200, the number of theoretical plates of a fifteenth main column (24 regions in FIGS. 4-3) is 10 to 200, the number of theoretical plates of a fifth common rectification section (25 regions in FIGS. 4-3) is 0 to 100, the number of theoretical plates of a fifth common stripping section (26 regions in FIGS. 4-3) is 0 to 100, the mass fraction of a liquid phase reflux into the pre-separation column, the first main column, the second main column, the fourth main column and the eleventh main column is 0.01 to 0.99, and a gas phase reflux into the pre-separation column, the first main column, The mass fractions of the second main tower, the fourth main tower and the eleventh main tower are 0.01-0.99; the reflux ratio is 0.1-20, and the operation pressure is 0.05-5 atm.
The device mainly comprises three single-partition towers or two double-partition towers or a five-partition tower.
The method and the device for separating the products of each carbon number fraction section from the Fischer-Tropsch synthesis light oil have the advantages that the products of each carbon number fraction section can be clearly separated from the Fischer-Tropsch synthesis light oil, the products are finely utilized, meanwhile, the energy consumption and the equipment cost are low, higher economic benefits can be created, and further, the market competitiveness of industries and enterprises is improved.
Drawings
FIGS. 1-1 to 1-4 are schematic diagrams of separation processes of different separation sequences of three single-wall towers, respectively.
FIGS. 2-1 to 2-4 are schematic diagrams of the separation processes of two double-wall towers in different separation sequences.
FIG. 3 is a schematic diagram of a separation process for a five-divided wall column.
FIGS. 4-1 to 4-3 are schematic structural views of a single-divided wall column, a double-divided wall column and a five-divided wall column, respectively.
T11-first single dividing wall column, T12-second single dividing wall column, T13-third single dividing wall column, T21-first double dividing wall column, T22-second double dividing wall column, T3-five dividing wall column.
S01 Fischer-Tropsch synthesis light oil raw material, S02-the fraction lighter than C6, S03-C6 fraction section, S04-C7 fraction section, S05-C8 fraction section, S06-C9 fraction section, S07-C10 fraction section, S08-the fraction heavier than C10, S09-C6-C10 fraction, S10-C7-C9 fraction, S11-C9 and heavier fraction, S12-C6-C8 fraction, S13-C7 and lighter fraction, S14-C6-C9 fraction, S15-C7-C10 fraction, S16-C8 and heavier fraction, S17-C8 and lighter fraction.
Detailed Description
The method and apparatus provided by the present invention will be further described with reference to the accompanying drawings, but the scope of the present invention is not limited to the embodiments.
The Fischer-Tropsch synthesis light oil raw material (S01) adopted by the invention mainly comprises hydrocarbons with the carbon number range of C6-C10 and a trace amount of oxygen-containing compounds. The hydrocarbons mainly comprise normal paraffin and alpha-olefin, and also comprise some isoparaffin, internal olefin, branched olefin, and small amount of naphthene, aromatic hydrocarbon and cyclic olefin.
Example 1
The invention is used in the narrow cut cutting process of Fischer-Tropsch synthesis light oil, and comprises a first single-wall tower (T11), a second single-wall tower (T12), a third single-wall tower (T13), a condenser, a reboiler, a pump, related feed lines and lines connecting the above devices, as shown in figure 1-1. The raw material is 1000g of Fischer-Tropsch synthetic oil light oil, and the light oil comprises hydrocarbons with the carbon number ranging from C6 to C10 and a trace amount of oxygen-containing compounds. The hydrocarbons mainly comprise normal paraffin and alpha-olefin, and also comprise some isoparaffin, internal olefin, branched olefin, and small amount of naphthene, aromatic hydrocarbon and cyclic olefin. The oxygen-containing compound comprises one or more of alcohol, aldehyde, ketone, acid and ester compounds. The theoretical plate number of a pre-separation tower (area a in figure 4-1) of a first single-partition wall tower (T11) is 10, the theoretical plate number of a main tower (area b in figure 4-1) is 200, the theoretical plate number of a common rectification section (area c in figure 4-1) is 0, the theoretical plate number of a common stripping section (area d in figure 4-1) is 100, the mass fraction of a liquid phase reflux entering the pre-separation tower is 0.01, the mass fraction of a gas phase reflux entering the pre-separation tower is 0.01, the reflux ratio is 0.1, and the operating pressure is 0.05 atm; the theoretical plate number of the pre-separation column (region a in fig. 4-1) of the second single-dividing wall column (T12) was 200, the theoretical plate number of the main column (region b in fig. 4-1) was 10, the theoretical plate number of the common rectification section (region c in fig. 4-1) was 100, the theoretical plate number of the common stripping section (region d in fig. 4-1) was 0, the mass fraction of the liquid phase reflux entering the pre-separation column was 0.99, the mass fraction of the gas phase reflux entering the pre-separation column was 0.99, the reflux ratio was 20, and the operating pressure was 5 atm; the theoretical plate number of the pre-separation column (region a in fig. 4-1) of the third single-dividing wall column (T13) was 100, the theoretical plate number of the main column (region b in fig. 4-1) was 100, the theoretical plate number of the common rectification section (region c in fig. 4-1) was 50, the theoretical plate number of the common stripping section (region d in fig. 4-1) was 50, the mass fraction of the liquid phase reflux entering the pre-separation column was 0.5, the mass fraction of the gas phase reflux entering the pre-separation column was 0.5, the reflux ratio was 10, and the operating pressure was 2.5 atm. The purities of C6-C10 fraction products (S05, S08, S10, S09 and S06) are respectively 99.1%, 99.5%, 99.2%, 99.7% and 99.0%, and the yields are respectively 95.1%, 95.0%, 95.9%, 95.1% and 96.0%. Wherein the product purity refers to the total mass content of all hydrocarbons of that carbon number.
Example 2
The invention is used in the narrow cut cutting process of Fischer-Tropsch synthesis light oil, and comprises a first double-wall tower (T21), a second double-wall tower (T22), a condenser, a reboiler, a pump, related feeding pipelines and pipelines for connecting the above devices, as shown in figure 2-1. The raw material is 1000g of Fischer-Tropsch synthetic oil light oil, and the light oil comprises hydrocarbons with the carbon number ranging from C6 to C10 and a trace amount of oxygen-containing compounds. The hydrocarbons mainly comprise normal paraffin and alpha-olefin, and also comprise some isoparaffin, internal olefin, branched olefin, and small amount of naphthene, aromatic hydrocarbon and cyclic olefin. The oxygen-containing compound comprises one or more of alcohol, aldehyde, ketone, acid and ester compounds. The theoretical plate number of the pre-separation column (region e in FIG. 4-2) of the first double divided wall column (T21) was 10, the theoretical plate number of the first main column (region f in FIG. 4-2) was 200, the theoretical plate number of the first common rectification section (region g in FIG. 4-2) was 0, the theoretical plate number of the first common stripping section (region h in FIG. 4-2) was 100, the mass fraction of the liquid phase reflux entering the pre-separation column was 0.99, the mass fraction of the gas phase reflux entering the pre-separation column was 0.01, the theoretical plate number of the second main column (region i in FIG. 4-2) was 200, the theoretical plate number of the third main column (region j in FIG. 4-2) was 10, the theoretical plate number of the second common rectification section (region k in FIG. 4-2) was 0, the theoretical plate number of the second common stripping section (region l in FIG. 4-2) was 100, the mass fraction of the liquid phase reflux entering the pre-separation tower and the first main tower is 0.01, the mass fraction of the gas phase reflux entering the pre-separation tower and the first main tower is 0.99, the reflux ratio is 0.1, and the operating pressure is 0.05 atm. The theoretical plate number of the pre-separation column (region e in FIG. 4-2) of the second double divided wall column (T22) was 200, the theoretical plate number of the first main column (region f in FIG. 4-2) was 10, the theoretical plate number of the first common rectification section (region g in FIG. 4-2) was 100, the theoretical plate number of the first common stripping section (region h in FIG. 4-2) was 0, the mass fraction of the liquid phase reflux entering the pre-separation column was 0.01, the mass fraction of the gas phase reflux entering the pre-separation column was 0.99, the theoretical plate number of the second main column (region i in FIG. 4-2) was 10, the theoretical plate number of the third main column (region j in FIG. 4-2) was 200, the theoretical plate number of the second common rectification section (region k in FIG. 4-2) was 100, the theoretical plate number of the second common stripping section (region l in FIG. 4-2) was 0, the mass fraction of the liquid phase reflux entering the pre-separation tower and the first main tower is 0.99, the mass fraction of the gas phase reflux entering the pre-separation tower and the first main tower is 0.01, the reflux ratio is 20, and the operating pressure is 5 atm. The purities of C6-C10 fraction products (S06, S07, S8, S09 and S04) are respectively 99.0%, 99.7%, 99.2%, 99.3% and 99.5%, and the yields are respectively 95.5%, 95.3%, 95.2%, 95.8% and 95.0%. Wherein the product purity refers to the total mass content of all hydrocarbons of that carbon number.
Example 3
The invention is used in the narrow cut cutting process of Fischer-Tropsch synthesis light oil, and comprises a five-wall column (T3), a condenser, a reboiler, a pump, related feed lines and lines connecting the above devices, as shown in FIG. 3. The raw material is 1000g of Fischer-Tropsch synthetic oil light oil, and the light oil comprises hydrocarbons with the carbon number ranging from C6 to C10 and a trace amount of oxygen-containing compounds. The hydrocarbons mainly comprise normal paraffin and alpha-olefin, and also comprise some isoparaffin, internal olefin, branched olefin, and small amount of naphthene, aromatic hydrocarbon and cyclic olefin. The oxygen-containing compound comprises one or more of alcohol, aldehyde, ketone, acid and ester compounds. The theoretical plate number of a pre-separation column (region 1 in fig. 4-3) of the five-divided wall column (T3) was 200, the theoretical plate number of the first main column (region 2 in fig. 4-3) was 10, the theoretical plate number of the first common rectification section (region 3 in fig. 4-3) was 100, the theoretical plate number of the first common stripping section (region 4 in fig. 4-3) was 100, the mass fraction of the liquid phase reflux entering the pre-separation column was 0.01, and the mass fraction of the gas phase reflux entering the pre-separation column was 0.01; the theoretical plate number of the second main column (5 regions in fig. 4-3) is 10, the theoretical plate number of the third main column (6 regions in fig. 4-3) is 200, the theoretical plate number of the second common rectification section (7 regions in fig. 4-3) is 50, the theoretical plate number of the second common stripping section (8 regions in fig. 4-3) is 50, the mass fraction of the liquid phase reflux entering the pre-separation column and the first main column is 0.2, and the mass fraction of the gas phase reflux entering the pre-separation column and the first main column is 0.2; the theoretical plate number of the fourth main column (region 9 in fig. 4-3) is 100, the theoretical plate number of the fifth main column (region 10 in fig. 4-3) is 100, the theoretical plate number of the sixth main column (region 11 in fig. 4-3) is 100, the theoretical plate number of the third common rectification section (region 12 in fig. 4-3) is 70, the theoretical plate number of the third common stripping section (region 13 in fig. 4-3) is 30, the mass fraction of the liquid phase reflux entering the pre-separation column, the first main column and the second main column is 0.5, and the mass fraction of the gas phase reflux entering the pre-separation column, the first main column and the second main column is 0.5; the theoretical plate number of the seventh main column (14 regions in fig. 4-3) was 30, the theoretical plate number of the eighth main column (15 regions in fig. 4-3) was 150, the theoretical plate number of the ninth main column (16 regions in fig. 4-3) was 60, the theoretical plate number of the tenth main column (17 regions in fig. 4-3) was 800, the theoretical plate number of the fourth common rectifying section (18 regions in fig. 4-3) was 20, the theoretical plate number of the fourth common stripping section (19 regions in fig. 4-3) was 90, the mass fraction of the liquid phase reflux into the pre-separation column, the first main column, the second main column and the fourth main column was 0.7, and the mass fraction of the gas phase reflux into the pre-separation column, the first main column, the second main column and the fourth main column was 0.7; the theoretical plate number of the eleventh main column (20 regions in FIGS. 4-3) was 30, the theoretical plate number of the twelfth main column (21 regions in FIGS. 4-3) was 70, the theoretical plate number of the thirteenth main column (22 regions in FIGS. 4-3) was 40, the theoretical plate number of the fourteenth main column (23 regions in FIGS. 4-3) was 100, the theoretical plate number of the fifteenth main column (24 regions in FIGS. 4-3) was 200, the theoretical plate number of the fifth common rectification section (25 regions in FIGS. 4-3) was 50, the theoretical plate number of the fifth common stripping section (26 regions in FIGS. 4-3) was 30, the mass fraction of the liquid phase reflux into the pre-separation column, the first main column, the second main column, the fourth main column and the eleventh main column was 0.9, the gas phase reflux into the pre-separation column, the mass fraction of the first main column, the second main column, the fourth main column and the eleventh main column is 0.9; the reflux ratio was 10 and the operating pressure was 1 atm. The purities of C6-C10 fraction products (S06, S07, S8, S09 and S04) are respectively 99.0%, 99.1%, 99.2%, 99.3% and 99.4%, and the yields are respectively 95.1%, 95.3%, 95.2%, 95.0% and 95.0%. Wherein the product purity refers to the total mass content of all hydrocarbons of that carbon number.
Claims (2)
1. A method for cutting Fischer-Tropsch synthesis light oil by using a bulkhead tower is characterized by comprising the following steps: the method adopts a flow of three single-partition towers, or adopts two double-partition towers, or adopts a flow of one five-partition tower, and the specific flow is as follows:
the flow process using three single-dividing-wall towers comprises the following three parallel schemes:
scheme 1: three single-partition towers are adopted, the Fischer-Tropsch synthesis light oil raw material (S01) enters a first single-partition tower (T11), the top of the first single-partition tower (T11) produces a fraction (S02) lighter than C6, the bottom of the first single-partition tower (T11) produces a fraction (S08) heavier than C10, and C6-C10 fractions (S09) are produced from the main tower side line of the first single-partition tower (T11) and enter a second single-partition tower (T12); c6 fraction (S03) is extracted from the top of the second single-partition column (T12), C10 fraction (S07) is extracted from the bottom of the pre-separation column (T12), C7-C9 fraction (S10) is extracted from the side of the main column of T12 and enters a third single-partition column (T13); a C7 fraction (S04) is extracted from the tower top of the third single-partition tower (T13), a C9 fraction (S06) is extracted from the tower bottom of the third single-partition tower (T13), and a C8 fraction (S05) is extracted from the main tower side line of the T13;
scheme 2: adopting three single-partition towers, feeding Fischer-Tropsch synthesis light oil raw material (S01) into a first single-partition tower (T11), extracting a fraction (S02) lighter than C6 from the top of the first single-partition tower (T11), extracting C9 and heavier fractions (S11) from the bottom of the first single-partition tower (T11) and feeding the fractions into a third single-partition tower (T13), and extracting C6-C8 fractions (S12) from the main tower side line of the first single-partition tower (T11) and feeding the fractions into a second single-partition tower (T12); a C6 fraction section (S03) is extracted from the top of the T12 tower, a C8 fraction section (S05) is extracted from the bottom of the tower, and a C7 fraction section (S04) is extracted from a line on the second main tower side (T12); a C9 fraction (S06) is extracted from the top of the third single-partition column (T13), a fraction heavier than C10 is extracted from the bottom of the column (S08), and a C10 fraction (S07) is extracted from the main column side line of the third single-partition column (T13);
scheme 3: three single-partition towers are adopted, Fischer-Tropsch synthesis light oil raw materials (S01) enter a first pre-separation (T11), fractions lighter than C7 and C7 are extracted from the top of the T11 tower (S13) and enter a second pre-separation (T12), fractions heavier than C10 are extracted from the bottom of the T11 tower (S08), C8-C10 fractions (S14) are extracted from the side of the T11 main tower and enter a third pre-separation (T13); the T12 takes a fraction lighter than C6 at the top (S02), takes a C7 fraction section (S04) at the bottom, and takes a C6 fraction section (S03) from the main column side of the T12; a C8 fraction is extracted from the top of the T13 tower (S05), a C10 fraction is extracted from the bottom of the tower (S07), and a C9 fraction is extracted from the side of the T13 main tower (S06);
or, three single-bulkhead towers are adopted, the Fischer-Tropsch synthesis light oil raw material (S01) enters a first pre-separation (T11), C7 and lighter fractions (S13) are extracted from the top of the T11 tower and enter a second pre-separation (T12), C9 and heavier fractions (S11) are extracted from the bottom of the T11 tower and enter a third pre-separation (T13), and C8 fractions (S05) are extracted from the side of the T11 main tower; the T12 takes a fraction lighter than C6 at the top (S02), takes a C7 fraction section (S04) at the bottom, and takes a C6 fraction section (S03) from the main column side of the T12; a C9 fraction section (S06) is extracted from the tower top of the T13, a fraction section (S08) heavier than C10 is extracted from the tower bottom, and a C10 fraction section (S07) is extracted from the main tower side line of the T13;
the adoption of two double-partition wall towers comprises the following three schemes:
scheme 1: adopting two double-partition towers, feeding Fischer-Tropsch synthesis light oil raw material (S01) into a first double-partition tower (T21), extracting a fraction (S02) lighter than C6 from the top of the first double-partition tower (T21), extracting a C6-C9 fraction (S15) from the upper side line of a main tower of the first double-partition tower (T21), feeding the fraction into a pre-separation tower of a second double-partition tower (T22), extracting a C10 fraction section (S07) from the lower side line of the main tower of the first double-partition tower (T21), and extracting a fraction (S08) heavier than C10 from the bottom of the first double-partition tower (T21); a C6 distillation section (S03) is extracted from the top of the second double-partition column (T22), a C7 distillation section (S04) and a C8 distillation section (S05) are respectively extracted from the upper side line and the lower side line of the main column of the second double-partition column (T22), and a C9 distillation section (S06) is extracted from the bottom of the second double-partition column (T22);
scheme 2: adopting two double-partition towers, feeding Fischer-Tropsch synthesis light oil raw materials (S01) into a first double-partition tower (T21), extracting a fraction (S02) lighter than C6 from the top of the first double-partition tower (T21), extracting a C6 fraction (S03) from the upper side line of a main tower of the first double-partition tower (T21), extracting a C7-C10 fraction (S16) from the lower side line of the main tower of the first double-partition tower (T21) and feeding the C6 fraction into a pre-separation tower of a second double-partition tower (T22), and extracting a fraction (S08) heavier than C10 from the bottom of the first double-partition tower (T21); a C7 distillation section (S04) is extracted from the top of the second double-partition wall tower (T22), a C8 distillation section (S05) and a C9 distillation section (S06) are respectively extracted from the upper side line and the lower side line of the T22 main tower, and a C10 distillation section (S07) is extracted from the bottom of the second double-partition wall tower (T22);
scheme 3: two double-partition towers are adopted, a Fischer-Tropsch synthesis light oil raw material (S01) enters a first double-partition tower (T21), a fraction (S02) lighter than C6 is extracted from the top of the first double-partition tower (T21), a C6 fraction (S03) and a C7 fraction (S04) are respectively extracted from the upper side line and the lower side line of a main tower of the first double-partition tower (T21), and a C8 and a heavier fraction (S17) are extracted from the bottom of the first double-partition tower (T21) and enter a pre-separation tower of a second double-partition tower (T22); a C8 fraction (S05) is extracted from the top of the second double-partition column (T22), a C9 fraction (S06) and a C10 fraction (S07) are extracted from the upper side line and the lower side line of the main column of the second double-partition column (T22), and a fraction heavier than C10 is extracted from the bottom of the second double-partition column (T22) (S08);
or, two double-partition towers are adopted, the Fischer-Tropsch synthesis light oil raw material (S01) enters a first double-partition tower (T21), C6 and lighter fractions (S18) are extracted from the top of the first double-partition tower (T21), the first double-partition tower enters a second double-partition tower (T22) pre-separation tower, C9 fraction (S06) and C10 fraction (S07) are extracted from the upper side line and the lower side line of a main tower of the first double-partition tower (T21), and fractions heavier than C10 (S08) are extracted from the bottom of the first double-partition tower (T21); a fraction lighter than C6 is extracted from the top of the second double-partition column (T22) (S02), a C6 fraction (S03) and a C7 fraction (S04) are extracted from the upper side line and the lower side line of the main column of the second double-partition column (T22), and a C8 fraction (S05) is extracted from the bottom of the second double-partition column (T22);
when two double-partition wall towers are adopted, two rows of partition plates are arranged in each double-partition wall tower, one partition plate is arranged on the side of a feeding port, two partition plates are arranged on the side of a discharging port, raw materials are added from a feeding port of a first double-partition wall tower (T21), and the feeding port is arranged in the middle of a pre-separation tower of the double-partition wall tower (T21); the overhead stream of the dividing wall tower (T21) enters a reflux buffer tank through a condenser, one part of the overhead stream is used as reflux, and the other part of the overhead stream is extracted; part of the tower bottom material flow returns to the dividing wall tower (T21) through the reboiler, and part is extracted; the main tower of the first double-partition tower (T21) is provided with two discharge ports with different heights, which respectively correspond to the two partition boards; the second double dividing wall column (T22) has the same structure as the first single dividing wall column (T21);
the flow scheme using a five-compartment column is as follows:
adopting a five-partition tower, enabling Fischer-Tropsch synthesis light oil raw materials (S01) to enter a five-partition tower (T3) of a pre-separation tower, separating by virtue of a plurality of partitions w11, w21 w, w31, w32, w33, w41, w42, w43, w44, w51, w52, w53, w54 and w5 in the tower, finally obtaining lighter components (S02) than C6 at the top of the T3 tower, respectively obtaining products (S03-S07) of C6-C10 fraction sections from five side lines from top to bottom, and obtaining heavier components (S08) than C10 at the bottom of the tower; when a five-partition-wall tower is adopted, five rows of partition plates are arranged in the tower, each row of partition plates is provided with 1,2,3,4 and 5 partition plates from the side of a feed inlet to the side of a discharge outlet, raw materials are added from a feed inlet of the five-partition-wall tower (T3), and the feed inlet is arranged in the middle of a pre-separation tower of the five-partition-wall tower (T3); the overhead stream of the dividing wall tower (T3) enters a reflux buffer tank through a condenser, one part of the overhead stream is used as reflux, and the other part of the overhead stream is extracted; part of the tower bottom material flow returns to the dividing wall tower (T3) through the reboiler, and part is extracted; the main tower of the first single-partition tower (T3) is provided with five discharge ports with different heights, which respectively correspond to five tower plates in a fifth row;
the number of theoretical plates of a pre-separation tower of the first single-partition wall tower (T11) is 10-200, the number of theoretical plates of a main tower is 10-200, the number of theoretical plates of a common rectification section is 0-100, the number of theoretical plates of a common stripping section is 0-100, the mass fraction of liquid phase reflux entering the pre-separation tower is 0.01-0.99, the mass fraction of gas phase reflux entering the pre-separation tower is 0.01-0.99, the reflux ratio is 0.1-20, and the operating pressure is 0.05-5 atm;
the number of theoretical plates of a pre-separation tower of the second single-partition wall tower (T12) is 10-200, the number of theoretical plates of a main tower is 10-200, the number of theoretical plates of a common rectification section is 0-100, the number of theoretical plates of a common stripping section is 0-100, the mass fraction of liquid phase reflux entering the pre-separation tower is 0.01-0.99, the mass fraction of gas phase reflux entering the pre-separation tower is 0.01-0.99, the reflux ratio is 0.1-20, and the operating pressure is 0.05-5 atm;
the theoretical plate number of a pre-separation tower of the third single-partition tower (T13) is 10-200, the theoretical plate number of a main tower is 10-200, the theoretical plate number of a common rectification section is 0-100, the theoretical plate number of a common stripping section is 0-100, the mass fraction of a liquid phase reflux entering the pre-separation tower is 0.01-0.99, the mass fraction of a gas phase reflux entering the pre-separation tower is 0.01-0.99, the reflux ratio is 0.1-20, and the operating pressure is 0.05-5 atm;
the number of theoretical plates of a pre-separation tower of the first double-partition wall tower (T21) is 10-200, the number of theoretical plates of a first main tower is 10-200, the number of theoretical plates of a first public rectification section is 0-100, the number of theoretical plates of a first public stripping section is 0-100, the mass fraction of liquid phase reflux entering the pre-separation tower is 0.01-0.99, the mass fraction of gas phase reflux entering the pre-separation tower is 0.01-0.99, the number of theoretical plates of a second main tower is 10-200, the number of theoretical plates of a third main tower is 10-200, the theoretical number of theoretical plates of a second public rectification section is 0-100, the theoretical plates of the second public stripping section is 0-100, the mass fraction of liquid phase reflux entering the pre-separation tower and the first main tower is 0.01-0.99, the mass fraction of gas phase reflux entering the pre-separation tower and the first main tower is 0.01-0.99, the reflux ratio is 0.1-20, and the operating pressure is 0.05-5 atm;
the number of theoretical plates of a pre-separation tower of the second double-partition wall tower (T22) is 10-200, the number of theoretical plates of a first public rectification section is 0-100, the number of theoretical plates of a first public stripping section is 0-100, the mass fraction of liquid phase reflux entering the pre-separation tower is 0.01-0.99, the mass fraction of gas phase reflux entering the pre-separation tower is 0.01-0.99, the number of theoretical plates of a second main tower is 10-200, the number of theoretical plates of a third main tower is 10-200, the number of theoretical plates of a second public rectification section is 0-100, the number of theoretical plates of a second public stripping section is 0-100, the mass fraction of liquid phase reflux entering the pre-separation tower and the first main tower is 0.01-0.99, the mass fraction of gas phase reflux entering the pre-separation tower and the first main tower is 0.01-0.99, the reflux ratio is 0.1-20, and the operating pressure is 0.05-5 atm;
the number of theoretical plates of a pre-separation tower of the five-partition-wall tower (T3) is 10-200, the number of theoretical plates of a first main tower is 10-200, the number of theoretical plates of a first public rectification section is 0-100, the number of theoretical plates of a first public stripping section is 0-100, the mass fraction of liquid phase reflux entering the pre-separation tower is 0.01-0.99, and the mass fraction of gas phase reflux entering the pre-separation tower is 0.01-0.99; the number of theoretical plates of the second main tower is 10-200, the number of theoretical plates of the third main tower is 10-200, the number of theoretical plates of the second public rectification section is 0-100, the number of theoretical plates of the second public stripping section is 0-100, the mass fraction of liquid phase reflux entering the pre-separation tower and the first main tower is 0.01-0.99, and the mass fraction of gas phase reflux entering the pre-separation tower and the first main tower is 0.01-0.99; the theoretical plate number of the fourth main tower is 10-200, the theoretical plate number of the fifth main tower is 10-200, the theoretical plate number of the sixth main tower is 10-200, the theoretical plate number of the third public rectifying section is 0-100, the theoretical plate number of the third public stripping section is 0-100, the mass fraction of the liquid phase reflux entering the pre-separation tower, the first main tower and the second main tower is 0.01-0.99, and the mass fraction of the gas phase reflux entering the pre-separation tower, the first main tower and the second main tower is 0.01-0.99; the theoretical plate number of a seventh main tower is 10-200, the theoretical plate number of an eighth main tower is 10-200, the theoretical plate number of a ninth main tower is 10-200, the theoretical plate number of a tenth main tower is 10-200, the theoretical plate number of a fourth public rectification section is 0-100, the theoretical plate number of a fourth public stripping section is 0-100, the mass fraction of a liquid phase reflux entering the pre-separation tower, the first main tower, the second main tower and the fourth main tower is 0.01-0.99, and the mass fraction of a gas phase reflux entering the pre-separation tower, the first main tower, the second main tower and the fourth main tower is 0.01-0.99; the theoretical plate number of an eleventh main tower is 10-200, the theoretical plate number of a twelfth main tower is 10-200, the theoretical plate number of a thirteenth main tower is 10-200, the theoretical plate number of a fourteenth main tower is 10-200, the theoretical plate number of a fifteenth main tower is 10-200, the theoretical plate number of a fifth public rectification section is 0-100, the theoretical plate number of a fifth public stripping section is 0-100, the mass fraction of a liquid phase reflux entering the pre-separation tower, the first main tower, the second main tower, the fourth main tower and the eleventh main tower is 0.01-0.99, and the mass fraction of a gas phase reflux entering the pre-separation tower, the first main tower, the second main tower, the fourth main tower and the eleventh main tower is 0.01-0.99; the reflux ratio is 0.1-20, and the operation pressure is 0.05-5 atm.
2. The method for cutting fischer-tropsch synthesis light oil by using a divided wall column as set forth in claim 1, wherein: the Fischer-Tropsch synthesis light oil raw material (S01) mainly comprises hydrocarbons with the carbon number range of C6-C10 and trace oxygen-containing compounds, wherein the hydrocarbons mainly comprise normal paraffins and alpha-olefins, and also comprise some isoparaffins, internal olefins and branched olefins, and a small amount of naphthenes, aromatic hydrocarbons and cyclic olefins.
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| CN111996027A (en) * | 2020-08-27 | 2020-11-27 | 河北工业大学 | A kind of method and device for separating Fischer-Tropsch synthetic heavy oil by using next-door tower |
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