CN109401779A - A kind of method and apparatus using next door tower cutting F- T synthesis light oil - Google Patents
A kind of method and apparatus using next door tower cutting F- T synthesis light oil Download PDFInfo
- Publication number
- CN109401779A CN109401779A CN201810900872.1A CN201810900872A CN109401779A CN 109401779 A CN109401779 A CN 109401779A CN 201810900872 A CN201810900872 A CN 201810900872A CN 109401779 A CN109401779 A CN 109401779A
- Authority
- CN
- China
- Prior art keywords
- tower
- king
- next door
- fraction
- section
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims abstract description 45
- 238000005520 cutting process Methods 0.000 title claims abstract description 15
- 230000015572 biosynthetic process Effects 0.000 title claims description 46
- 238000003786 synthesis reaction Methods 0.000 title claims description 46
- 238000000926 separation method Methods 0.000 claims abstract description 144
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 17
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 17
- 238000005192 partition Methods 0.000 claims abstract description 9
- 238000010992 reflux Methods 0.000 claims description 57
- 238000000605 extraction Methods 0.000 claims description 44
- 239000012071 phase Substances 0.000 claims description 37
- 239000007791 liquid phase Substances 0.000 claims description 36
- 239000002994 raw material Substances 0.000 claims description 28
- 229930195733 hydrocarbon Natural products 0.000 claims description 25
- 150000002430 hydrocarbons Chemical class 0.000 claims description 24
- 150000001336 alkenes Chemical class 0.000 claims description 10
- 239000004711 α-olefin Substances 0.000 claims description 7
- 239000004215 Carbon black (E152) Substances 0.000 claims description 6
- 150000001924 cycloalkanes Chemical class 0.000 claims description 5
- 150000001925 cycloalkenes Chemical class 0.000 claims description 5
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims description 5
- 238000001704 evaporation Methods 0.000 claims 2
- 239000000463 material Substances 0.000 claims 1
- 238000005516 engineering process Methods 0.000 abstract description 6
- 230000008901 benefit Effects 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000009835 boiling Methods 0.000 abstract 1
- 238000000746 purification Methods 0.000 abstract 1
- 238000011084 recovery Methods 0.000 abstract 1
- 239000000047 product Substances 0.000 description 33
- 239000007789 gas Substances 0.000 description 28
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 6
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 6
- AFABGHUZZDYHJO-UHFFFAOYSA-N 2-Methylpentane Chemical compound CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 5
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 5
- 239000002283 diesel fuel Substances 0.000 description 5
- GXDHCNNESPLIKD-UHFFFAOYSA-N 2-methylhexane Natural products CCCCC(C)C GXDHCNNESPLIKD-UHFFFAOYSA-N 0.000 description 4
- 150000001335 aliphatic alkanes Chemical class 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical class CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 description 3
- 239000002253 acid Chemical class 0.000 description 3
- 150000001299 aldehydes Chemical class 0.000 description 3
- 150000001875 compounds Chemical class 0.000 description 3
- 239000012043 crude product Substances 0.000 description 3
- 150000002148 esters Chemical class 0.000 description 3
- 150000002576 ketones Chemical class 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 239000003502 gasoline Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 2
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 2
- 239000003915 liquefied petroleum gas Substances 0.000 description 2
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- NHTMVDHEPJAVLT-UHFFFAOYSA-N Isooctane Chemical compound CC(C)CC(C)(C)C NHTMVDHEPJAVLT-UHFFFAOYSA-N 0.000 description 1
- 241000772415 Neovison vison Species 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- -1 alkene Hydrocarbon Chemical class 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- JVSWJIKNEAIKJW-UHFFFAOYSA-N dimethyl-hexane Natural products CCCCCC(C)C JVSWJIKNEAIKJW-UHFFFAOYSA-N 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 125000001972 isopentyl group Chemical group [H]C([H])([H])C([H])(C([H])([H])[H])C([H])([H])C([H])([H])* 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen 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
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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
Landscapes
- 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. The process can adopt the flow of three single dividing wall columns, or two double 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
Cut F- T synthesis light oil using next door tower the present invention relates to a kind of, obtain the method for each carbon number fraction section product with
Device, the cutting especially suitable for the F- T synthesis light oil mainly comprising C6-C10 fraction.
Background technique
F- T synthesis, that is, ICL for Indirect Coal Liquefaction process, the synthesis gas for generating coal gasification under the conditions of existing for the catalyst (CO,
H2) it is converted into gasoline, diesel oil and other hydrocarbon products.Reacting crude product is mainly light oil, mink cell focus and heavy wax.Fischer-Tropsch closes
At product commonly used to the further products such as production gasoline, diesel oil, naphtha, need to carry out hydrotreating to alkene therein,
Cause the waste of the higher alpha-olefin component of added value.The n-alkane that main matter in F- T synthesis light oil is C6-C10
And normal olefine, olefin component are mostly alpha-olefin, have the characteristics that sulfur content is low, is practically free of aromatic hydrocarbons.If can be using appropriate
Method the substance in Fischer-Tropsch synthetic respectively is isolated by refine utilize, further produce high value added product, make
Diesel oil minimizing, product fining, will greatly improve economic benefit.
Patent CN107267212A proposes a kind of separating technology by F- T synthesis crude product, which includes feedstock oil
Multiple processing steps such as product crude separation, oil plus hydrogen, lighter hydrocarbons essence divide, wax adds hydrogen, cerotin point, synthesize temperature according to F- T synthesis crude product
The difference of degree can obtain naphtha, pentane, n-hexane, normal heptane, the normal octane, C50, C70, C80 series of different number
A variety of high value added products such as wax, H1 and H105 series wax.C5-C8 fraction is obtained by raw material oil product crude separation first, is sent
The essence point of lighter hydrocarbons is carried out to light component knockout tower；Light component separation column overhead distillates C5 and C6, and tower reactor distillates C7 and C8, tower top and
Tower reactor logistics respectively enters C5 knockout tower and C7 knockout tower, obtains C5, C6, C7, C8 component, and respectively enters each carbon number alkane and mention
Pure tower finally obtains pentane, n-hexane, normal heptane, normal octane product that purity is greater than 99.9wt%, while obtaining isoamyl
The byproducts such as alkane, isohexane, isoheptane, isooctane.Patent CN107325838A is similar with the process of above-mentioned patent, raw material oil product
Crude separation obtains C5-C7 fraction, then gets pentane, the n-hexane, positive heptan that purity is greater than 99.9wt% by lighter hydrocarbons essence
Alkane product, while obtaining the byproducts such as isopentane, isohexane, isoheptane.
Patent CN107916127A is related to a kind of rectification process for Fischer-Tropsch synthetic separation, which uses
After three separation, then pass through the separation of four tower rectifying five sections of fractions of realization.Fischer-Tropsch product raw material passes through first-stage condenser, level-one respectively
Separator, two-stage water-cooling device, second-stage separator, three-level deep freezer, three-level separator, by oily mutually separated from the water, level-one, two
Grade, three-level separator upper phase are respectively heavy hydrocarbon, light hydrocarbon and lighter hydrocarbons, respectively enter dry gas rectifying column；Successively through overdrying
Four rectifying columns such as gas rectifying column, liquefied petroleum gas rectifying column, C5-C10 rectifying column, C11-C19 rectifying column, respectively obtain dry gas
(C1-C2), five kinds of products such as liquefied petroleum gas (C3-C4), C5-C10 fraction section, C11-C19 fraction section, C20+ fraction section.
Patent CN101275080A is related to a kind of separation method of Fischer-Tropsch reaction product, and it is anti-mainly to solve existing F- T synthesis
The problem for answering product vapour, diesel oil separation difficult.The present invention is by being passed through separator for the hydrocarbon product obtained after Fischer-Tropsch reaction；
Product is obtained after separator separates containing vapour, the hydro carbons of diesel oil and heavy hydrocarbons product, the separator include hot trap tower and
Heater, for heater in the lower part of hot trap tower, hot trap column bottom temperature control range is 120~400 DEG C, the control of hot trap tower top temperature
The technical solution that range is 25~150 DEG C.
The problems such as above-mentioned generally existing products therefrom fraction section of document is unintelligible, and product is difficult to further utilization, furthermore exists
Process is complicated, energy consumption and the higher defect of cost of equipment.The invention proposes a kind of energy-efficient separation from Fischer-Tropsch oil is each
The new process and device of carbon number fraction section product.
Summary of the invention
Present invention aim to address the defects of the above-mentioned prior art, propose a kind of energy-efficient by F- T synthesis lightweight
The method and apparatus of each carbon number fraction section product separating-purifying in oil.
Process proposed by the present invention carries out each carbon number fraction section to F- T synthesis light oil using next door tower technology and produces
The cutting of product respectively obtains C6-C10 fraction section product.
The process of three single next door towers can be used in this technique, and the stream of two double next door towers or a five next door towers can also be used
Journey.Wherein the process of three single next door towers and the process of two double next doors towers can use different separation sequences, detailed process
It is as follows.
(1) three single next door tower process
(a) the first separation sequence (such as Fig. 1-1)
F- T synthesis light oil raw material (S01) enter T11 pre-separation tower, T11 overhead extraction ratio C6 lighter fraction (S02),
T11 tower reactor produces the fraction (S08) heavier than C10, and C6-C10 fraction (S09) is from T11 king-tower side take-off, and it is pre- to enter T12
Knockout tower；T12 overhead extraction C6 fraction section (S03), T12 tower reactor produce C10 fraction section (S07), and C7-C9 fraction (S10) is from T12
King-tower side take-off, and enter T13 pre-separation tower；T13 column overhead produces C7 fraction section (S04), and T13 tower reactor produces C9 fraction section
(S06), C8 fraction section (S05) is from T13 king-tower side take-off.
(b) the second separation sequence (such as Fig. 1-2)
F- T synthesis light oil raw material (S01) enter T11 pre-separation tower, T11 overhead extraction ratio C6 lighter fraction (S02),
T11 tower reactor produces C9 and heavier fraction (S11), and C6-C8 fraction (S12) divides in advance from T11 king-tower side take-off, and into T12
From tower, and enter T13 pre-separation tower；T12 overhead extraction C6 fraction section (S03), tower reactor produce C8 fraction section (S05), C7 fraction
Section (S04) is from T12 king-tower side take-off；T13 column overhead produces C9 fraction section (S06), and tower reactor produces the fraction heavier than C10
(S08), C10 fraction section (S07) is from T13 king-tower side take-off.
(c) third separation sequence (such as Fig. 1-3)
F- T synthesis light oil raw material (S01) enters T11 pre-separation tower, T11 overhead extraction ratio C7 and lighter fraction
(S13), and enter T12 pre-separation tower, T11 tower reactor produces the fraction (S08) heavier than C10, and C8-C10 fraction (S14) is from T11
King-tower side take-off, and enter T13 pre-separation tower；T12 overhead extraction ratio C6 lighter fraction (S02), tower reactor produce C7 fraction
Section (S04), C6 fraction section (S03) is from T12 king-tower side take-off；T13 column overhead produces C8 fraction section (S05), and tower reactor produces C10
Fraction section (S07), C9 fraction section is from T13 king-tower side take-off (S06).
(d) the 4th separation sequence (picture 1-4)
F- T synthesis light oil raw material (S01) enters T11 pre-separation tower, T11 overhead extraction C7 and lighter fraction (S13),
And entering T12 pre-separation tower, T11 tower reactor produces C9 and heavier fraction (S11), and enters T13 pre-separation tower, C8 fraction section
(S05) from T11 king-tower side take-off；T12 overhead extraction ratio C6 lighter fraction (S02), tower reactor produce C7 fraction section (S04),
C6 fraction section (S03) is from T12 king-tower side take-off；T13 column overhead produces C9 fraction section (S06), and tower reactor extraction is heavier than C10
Fraction section (S08), C10 fraction section (S07) is from T13 king-tower side take-off.
(2) two double next doors tower processes
(a) the first separation sequence (such as Fig. 2-1)
F- T synthesis light oil raw material (S01) enter T21 pre-separation tower, T21 overhead extraction ratio C6 lighter fraction (S02),
C6-C9 fraction (S15) enters T22 pre-separation tower from side take-off on T21 king-tower, and C10 fraction section (S07) is under T21 king-tower
Side take-off, T21 tower reactor produce the fraction (S08) heavier than C10；T22 overhead extraction C6 fraction section (S03), respectively from T22 master
Side line and lower side take-off C7 fraction section (S04), C8 fraction section (S05) on tower, T22 tower reactor produce C9 fraction section (S06).
(b) the second separation sequence (such as Fig. 2-2)
F- T synthesis light oil raw material (S01) enter T21 pre-separation tower, T21 overhead extraction ratio C6 lighter fraction (S02),
For C6 fraction section (S03) from side take-off on T21 king-tower, C7-C10 fraction (S16) enters T22 from side take-off under T21 king-tower
Pre-separation tower, T21 tower reactor produce the fraction (S08) heavier than C10；T22 overhead extraction C7 fraction section (S04), respectively from T22 master
Side line and lower side take-off C8 fraction section (S05), C9 fraction section (S06) on tower, T22 tower reactor produce C10 fraction section (S07).
(c) third separation sequence (such as Fig. 2-3)
F- T synthesis light oil raw material (S01) enter T21 pre-separation tower, T21 overhead extraction ratio C6 lighter fraction (S02),
Respectively from side line on T21 king-tower and lower side take-off, T21 tower reactor produces C8 and more for C6 fraction section (S03), C7 fraction section (S04)
The fraction (S17) of weight, and enter T22 pre-separation tower；T22 overhead extraction C8 fraction section (S05), respectively from side line on T22 king-tower
With lower side take-off C9 fraction section (S06), C10 fraction section (S07), T22 tower reactor produces the fraction (S08) heavier than C10.
(d) the 4th separation sequence (such as Fig. 2-4)
F- T synthesis light oil raw material (S01) enters T21 pre-separation tower, T21 overhead extraction C6 and lighter fraction (S18),
And enter T22 pre-separation tower, respectively from side line on T21 king-tower and lower side take-off C9 fraction section (S06), C10 fraction section
(S07), T21 tower reactor produces the fraction (S08) heavier than C10；T22 overhead extraction ratio C6 lighter fraction (S02), respectively from
Side line and lower side take-off C6 fraction section (S03), C7 fraction section (S04) on T22 king-tower, T22 tower reactor produce C8 fraction section
(S05)。
(3) five next door tower processes (such as Fig. 3)
F- T synthesis light oil raw material (S01) enters T3 pre-separation tower, by w11, w21-22, w31-33, w41- in tower
44, the more a partitions of w51-55 are separated, and final T3 tower top obtains the component (S02) lighter than C6, top-down five sides
Line respectively obtains the product (S03-S07) of C6-C10 fraction section, and tower reactor obtains the component (S08) heavier than C10.
In process (1), pre-separation tower (region a in Fig. 4-1) theoretical cam curve of the mono- next door tower of T11 is 10~200, main
Tower (region b in Fig. 4-1) theoretical cam curve is 10~200, and public rectifying section (region c in Fig. 4-1) theoretical cam curve is 0
~100, public stripping section (region d in Fig. 4-1) theoretical cam curve is 0~100, and liquid-phase reflux enters the quality of pre-separation tower
Dividing rate is 0.01~0.99, and the mass fraction that gas phase flows back into pre-separation tower is 0.01~0.99, and reflux ratio is 0.1~20,
Operating pressure is 0.05~5atm；Pre-separation tower (region a in Fig. 4-1) theoretical cam curve of the mono- next door tower of T12 be 10~
200, king-tower (region b in Fig. 4-1) theoretical cam curve is 10~200, the theoretical tower of public rectifying section (region c in Fig. 4-1)
Plate number is 0~100, and public stripping section (region d in Fig. 4-1) theoretical cam curve is 0~100, and liquid-phase reflux enters pre-separation
The mass fraction of tower is 0.01~0.99, and the mass fraction that gas phase flows back into pre-separation tower is 0.01~0.99, and reflux ratio is
0.1~20, operating pressure is 0.05~5atm；Pre-separation tower (region a in Fig. 4-1) theoretical cam curve of the mono- next door tower of T13
It is 10~200, king-tower (region b in Fig. 4-1) theoretical cam curve is 10~200, public rectifying section (region c in Fig. 4-1)
Theoretical cam curve is 0~100, and public stripping section (region d in Fig. 4-1) theoretical cam curve is 0~100, and liquid-phase reflux enters
The mass fraction of pre-separation tower is 0.01~0.99, and the mass fraction that gas phase flows back into pre-separation tower is 0.01~0.99, is returned
For stream than being 0.1~20, operating pressure is 0.05~5atm.
In process (2), pre-separation tower (region e in Fig. 4-2) theoretical cam curve of the bis- next door towers of T21 is 10~200, the
One king-tower (region f in Fig. 4-2) theoretical cam curve is 10~200, and the first public rectifying section (region g in Fig. 4-2) is theoretical
The number of plates is 0~100, and the first public stripping section (region h in Fig. 4-2) theoretical cam curve is 0~100, and liquid-phase reflux enters
The mass fraction of pre-separation tower is 0.01~0.99, and the mass fraction that gas phase flows back into pre-separation tower is 0.01~0.99, the
Two king-towers (5 regions in Fig. 4-2) theoretical cam curve is 10~200, third king-tower (region j in Fig. 4-2) theoretical cam curve
It is 10~200, the second public rectifying section (region k in Fig. 4-2) theoretical cam curve is 0~100, the second public stripping section (figure
The region l in 4-2) theoretical cam curve be 0~100, liquid-phase reflux enters pre-separation tower and the mass fraction of the first king-tower is
0.01~0.99, the mass fraction that gas phase flows back into pre-separation tower and the first king-tower is 0.01~0.99, reflux ratio is 0.1~
20, operating pressure is 0.05~5atm；Pre-separation tower (region e in Fig. 4-2) theoretical cam curve of the bis- next door towers of T22 be 10~
200, the first king-tower (region f in Fig. 4-2) theoretical cam curve is 10~200, the first public rectifying section (area g in Fig. 4-2
Domain) theoretical cam curve be 0~100, the first public stripping section (region h in Fig. 4-2) theoretical cam curve be 0~100, liquid phase return
Stream enter pre-separation tower mass fraction be 0.01~0.99, gas phase flow back into pre-separation tower mass fraction be 0.01~
0.99, the second king-tower (5 regions in Fig. 4-2) theoretical cam curve is 10~200, and third king-tower (region j in Fig. 4-2) is theoretical
The number of plates is 10~200, and the second public rectifying section (region k in Fig. 4-2) theoretical cam curve is 0~100, the second public stripping
Section (region l in Fig. 4-2) theoretical cam curve is 0~100, and liquid-phase reflux enters the mass fraction of pre-separation tower and the first king-tower
It is 0.01~0.99, it is 0.01~0.99 that gas phase, which flows back into pre-separation tower and the mass fraction of the first king-tower, reflux ratio 0.1
~20, operating pressure is 0.05~5atm.
In process (3), pre-separation tower (1 region in Fig. 4-3) theoretical cam curve of five next door tower of T3 is 10~200, the
One king-tower (2 regions in Fig. 4-3) theoretical cam curve is 10~200, and the first public rectifying section (3 regions in Fig. 4-3) is theoretical
The number of plates is 0~100, and the first public stripping section (4 regions in Fig. 4-3) theoretical cam curve is 0~100, and liquid-phase reflux enters
The mass fraction of pre-separation tower is 0.01~0.99, and the mass fraction that gas phase flows back into pre-separation tower is 0.01~0.99；The
Two king-towers (5 regions in Fig. 4-3) theoretical cam curve is 10~200, third king-tower (6 regions in Fig. 4-3) theoretical cam curve
It is 10~200, the second public rectifying section (7 regions in Fig. 4-3) theoretical cam curve is 0~100, the second public stripping section (figure
8 regions in 4-3) theoretical cam curve be 0~100, liquid-phase reflux enters pre-separation tower and the mass fraction of the first king-tower is
0.01~0.99, it is 0.01~0.99 that gas phase, which flows back into pre-separation tower and the mass fraction of the first king-tower,；4th king-tower (Fig. 4-
9 regions in 3) theoretical cam curve be 10~200, the 5th king-tower (10 regions in Fig. 4-3) theoretical cam curve be 10~200,
6th king-tower (11 regions in Fig. 4-3) theoretical cam curve is 10~200, the public rectifying section of third (12 regions in Fig. 4-3)
Theoretical cam curve is 0~100, and the public stripping section of third (13 regions in Fig. 4-3) theoretical cam curve is 0~100, liquid-phase reflux
Mass fraction into pre-separation tower, the first king-tower and the second king-tower is 0.01~0.99, and gas phase flows back into pre-separation tower, the
The mass fraction of one king-tower and the second king-tower is 0.01~0.99；7th king-tower (14 regions in Fig. 4-3) theoretical cam curve is
10~200, the 8th king-tower (15 regions in Fig. 4-3) theoretical cam curve is 10~200, the 9th king-tower (16th area Fig. 4-3 Zhong
Domain) theoretical cam curve be 10~200, the tenth king-tower (17 regions in Fig. 4-3) theoretical cam curve be 10~200, the 4th is public
Rectifying section (18 regions in Fig. 4-3) theoretical cam curve is 0~100, and the 4th public stripping section (19 regions in Fig. 4-3) is theoretical
The number of plates is 0~100, and the mass fraction that liquid-phase reflux enters pre-separation tower, the first king-tower, the second king-tower and the 4th king-tower is
0.01~0.99, gas phase flow back into pre-separation tower, the first king-tower, the second king-tower and the 4th king-tower mass fraction be 0.01~
0.99；11st king-tower (20 regions in Fig. 4-3) theoretical cam curve is the 10~200, the 12nd king-tower (21st area Fig. 4-3 Zhong
Domain) theoretical cam curve is that the 10~200, the 13rd king-tower (22 regions in Fig. 4-3) theoretical cam curve is the 10~200, the 14th
King-tower (23 regions in Fig. 4-3) theoretical cam curve is the 10~200, the 15th king-tower (24 regions in Fig. 4-3) theoretical tray
Number is 10~200, and the 5th public rectifying section (25 regions in Fig. 4-3) theoretical cam curve is 0~100, the 5th public stripping section
(26 regions in Fig. 4-3) theoretical cam curve is 0~100, and liquid-phase reflux enters pre-separation tower, the first king-tower, the second king-tower, the
The mass fraction of four king-towers and the 11st king-tower is 0.01~0.99, and gas phase flows back into pre-separation tower, the first king-tower, the second master
The mass fraction of tower, the 4th king-tower and the 11st king-tower is 0.01~0.99；Reflux ratio is 0.1~20, operating pressure 0.05
~5atm.
Device of the present invention mainly includes three single next door towers or two double next door towers or a five next door towers.
The method and apparatus of the present invention that each carbon number fraction section product is separated from F- T synthesis light oil, advantage
It is clearly isolate the product of each carbon number fraction section, further utilization, while energy consumption from F- T synthesis light oil and sets
Standby expense is lower, can create higher economic benefit, and then improve the market competitiveness of industry and enterprise.
Detailed description of the invention
Fig. 1-1 to Fig. 1-4 is respectively the separating technology flow diagram of three single next door tower difference separation sequences.
Fig. 2-1 to Fig. 2-4 is respectively the separating technology flow diagram of two double next doors tower difference separation sequences.
Fig. 3 is the separating technology flow diagram of a five next door towers.
Fig. 4-1 to Fig. 4-3 is respectively the structural schematic diagram of single next door tower, the next door double next door Ta Hewu tower.
The single next door tower of T11- first, the single next door tower of T12- second, T13- third list next door tower, first pair of next door tower of T21-,
Second pair of next door tower of T22-, five next door tower of T3-.
S01- F- T synthesis light oil raw material, S02- ratio C6 lighter fraction, S03-C6 fraction section, S04-C7 fraction section,
S05-C8 fraction section, S06-C9 fraction section, S07-C10 fraction section, S08- ratio C10 heavier fraction, 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 evaporate
Divide, S15-C7-C10 fraction, S16-C8 and heavier fraction, S17-C8 and lighter fraction.
Specific embodiment
Method and device provided by the present invention is further detailed with reference to the accompanying drawing, it is still, of the invention
Range is not only limited to the range that embodiment is covered.
F- T synthesis light oil raw material (S01) that the present invention uses is mainly comprising carbon number range for the hydro carbons of C6-C10 and micro-
The oxygenatedchemicals of amount.Wherein hydro carbons mainly includes n-alkane and alpha-olefin, further includes some isoparaffins, internal olefin, branch
Olefine, and a small amount of cycloalkane, aromatic hydrocarbons, cycloolefin.
Embodiment 1
The present invention is used for the narrow fraction cutting process of F- T synthesis light oil, as Figure 1-1, including first single next door
Tower (T11), second single next door tower (T12), third list next door tower (T13), condenser, reboiler, pump and relevant feed pipe
Line and the pipeline for connecting the above equipment.Raw material is 1000g Fischer-Tropsch synthesis oil light oil, the hydro carbons for being C6-C10 comprising carbon number range
And micro oxygenatedchemicals.Wherein hydro carbons mainly includes n-alkane and alpha-olefin, further includes some isoparaffins, interior alkene
Hydrocarbon, branched-chain alkene, and a small amount of cycloalkane, aromatic hydrocarbons, cycloolefin.Oxygenatedchemicals includes alcohol, aldehyde, ketone, acid, ester type compound
It is one or more.First single next door tower (T11) pre-separation tower (region a in Fig. 4-1) theoretical cam curve is 10, king-tower (Fig. 4-1
In the region b) theoretical cam curve be 200, public rectifying section (region c in Fig. 4-1) theoretical cam curve be 0, public stripping section
(region d in Fig. 4-1) theoretical cam curve is 100, and the mass fraction that liquid-phase reflux enters pre-separation tower is 0.01, gas phase reflux
Mass fraction into pre-separation tower is 0.01, reflux ratio 0.1, operating pressure 0.05atm；Second single next door tower (T12)
Pre-separation tower (region a in Fig. 4-1) theoretical cam curve be 200, king-tower (region b in Fig. 4-1) theoretical cam curve be 10,
Public rectifying section (region c in Fig. 4-1) theoretical cam curve is 100, public stripping section (region d in Fig. 4-1) theoretical tray
Number is 0, and the mass fraction that liquid-phase reflux enters pre-separation tower is 0.99, and the mass fraction that gas phase flows back into pre-separation tower is
0.99, reflux ratio 20, operating pressure 5atm；The pre-separation tower (region a in Fig. 4-1) of third list next door tower (T13) is managed
It is 100 by the number of plates, king-tower (region b in Fig. 4-1) theoretical cam curve is 100, public rectifying section (region c in Fig. 4-1)
Theoretical cam curve is 50, and public stripping section (region d in Fig. 4-1) theoretical cam curve is 50, and liquid-phase reflux enters pre-separation tower
Mass fraction be 0.5, the mass fraction that gas phase flows back into pre-separation tower is 0.5, and reflux ratio 10, operating pressure is
2.5atm.The purity of C6-C10 fraction section product (S05, S08, S10, S09, S06) is respectively 99.1%, 99.5%, 99.2%,
99.7%, 99.0%, yield is respectively 95.1%, 95.0%, 95.9%, 95.1%, 96.0%.Wherein product purity refers to the carbon
The gross mass content of all hydro carbons of number.
Embodiment 2
The present invention is used for the narrow fraction cutting process of F- T synthesis light oil, as shown in Fig. 2-1, including first pair of next door
Tower (T21), second pair of next door tower (T22), condenser, reboiler, pump and relevant feeding line and the above equipment of connection
Pipeline.Raw material is 1000g Fischer-Tropsch synthesis oil light oil, the hydro carbons and micro oxygen-containing chemical combination for being C6-C10 comprising carbon number range
Object.Wherein hydro carbons mainly includes n-alkane and alpha-olefin, further includes some isoparaffins, internal olefin, branched-chain alkene, and few
Measure cycloalkane, aromatic hydrocarbons, cycloolefin.Oxygenatedchemicals include alcohol, aldehyde, ketone, acid, ester type compound it is one or more.First pair
Pre-separation tower (region e in Fig. 4-2) theoretical cam curve of next door tower (T21) is 10, the first king-tower (region f in Fig. 4-2)
Theoretical cam curve is 200, and the first public rectifying section (region g in Fig. 4-2) theoretical cam curve is 0, the first public stripping section (figure
The region h in 4-2) theoretical cam curve be 100, liquid-phase reflux enter pre-separation tower mass fraction be 0.99, gas phase flows back into
The mass fraction for entering pre-separation tower is 0.01, and the second king-tower (region i in Fig. 4-2) theoretical cam curve is 200, third king-tower
(region j in Fig. 4-2) theoretical cam curve is 10, and the second public rectifying section (region k in Fig. 4-2) theoretical cam curve is 0, the
Two public stripping section (region l in Fig. 4-2) theoretical cam curves are 100, and liquid-phase reflux enters pre-separation tower and the first king-tower
Mass fraction is 0.01, and it is 0.99 that gas phase, which flows back into pre-separation tower and the mass fraction of the first king-tower, reflux ratio 0.1, behaviour
Making pressure is 0.05atm.Pre-separation tower (region e in Fig. 4-2) theoretical cam curve of second pair of next door tower (T22) is 200, the
One king-tower (region f in Fig. 4-2) theoretical cam curve is 10, the first public rectifying section (region g in Fig. 4-2) theoretical cam curve
It is 100, the first public stripping section (region h in Fig. 4-2) theoretical cam curve is 0, and liquid-phase reflux enters the quality of pre-separation tower
Dividing rate is 0.01, and the mass fraction that gas phase flows back into pre-separation tower is 0.99, and the second king-tower (region i in Fig. 4-2) is theoretical
The number of plates is 10, and third king-tower (region j in Fig. 4-2) theoretical cam curve is 200, the second public rectifying section (k in Fig. 4-2
Region) theoretical cam curve be 100, the second public stripping section (region l in Fig. 4-2) theoretical cam curve be 0, liquid-phase reflux enter
The mass fraction of pre-separation tower and the first king-tower is 0.99, and gas phase flows back into pre-separation tower and the mass fraction of the first king-tower is
0.01, reflux ratio 20, operating pressure 5atm.The purity of C6-C10 fraction section product (S06, S07, S8, S09, S04) is distinguished
It is 99.0%, 99.7%, 99.2%, 99.3%, 99.5%, yield is respectively 95.5%, 95.3%, 95.2%, 95.8%,
95.0%.Wherein product purity refers to the gross mass content of all hydro carbons of the carbon number.
Embodiment 3
The present invention is used for the narrow fraction cutting process of F- T synthesis light oil, as shown in figure 3, including five next door towers
(T3), the pipeline of condenser, reboiler, pump and relevant feeding line and the above equipment of connection.Raw material is the conjunction of 1000g Fischer-Tropsch
At oily light oil, the hydro carbons and micro oxygenatedchemicals for being C6-C10 comprising carbon number range.Wherein hydro carbons mainly includes just
Structure alkane and alpha-olefin further include some isoparaffins, internal olefin, branched-chain alkene, and a small amount of cycloalkane, aromatic hydrocarbons, cycloolefin.
Oxygenatedchemicals include alcohol, aldehyde, ketone, acid, ester type compound it is one or more.Pre-separation tower (Fig. 4-3 of five next door towers (T3)
In 1 region) theoretical cam curve be 200, the first king-tower (2 regions in Fig. 4-3) theoretical cam curve be 10, the first public rectifying
Section (3 regions in Fig. 4-3) theoretical cam curve is 100, and the first public stripping section (4 regions in Fig. 4-3) theoretical cam curve is
100, the mass fraction that liquid-phase reflux enters pre-separation tower is 0.01, and the mass fraction that gas phase flows back into pre-separation tower is
0.01；Second king-tower (5 regions in Fig. 4-3) theoretical cam curve is 10, third king-tower (6 regions in Fig. 4-3) theoretical tray
Number is 200, and the second public rectifying section (7 regions in Fig. 4-3) theoretical cam curve is 50, and the second public stripping section is (in Fig. 4-3
8 regions) theoretical cam curve is 50, the mass fraction that liquid-phase reflux enters pre-separation tower and the first king-tower is 0.2, and gas phase flows back into
The mass fraction for entering pre-separation tower and the first king-tower is 0.2；4th king-tower (9 regions in Fig. 4-3) theoretical cam curve is 100,
5th king-tower (10 regions in Fig. 4-3) theoretical cam curve is 100, the 6th king-tower (11 regions in Fig. 4-3) theoretical cam curve
It is 100, the public rectifying section of third (12 regions in Fig. 4-3) theoretical cam curve is 70, and the public stripping section of third is (in Fig. 4-3
13 regions) theoretical cam curve be 30, liquid-phase reflux enter pre-separation tower, the first king-tower and the second king-tower mass fraction be 0.5,
The mass fraction that gas phase flows back into pre-separation tower, the first king-tower and the second king-tower is 0.5；7th king-tower (14th area Fig. 4-3 Zhong
Domain) theoretical cam curve be 30, the 8th king-tower (15 regions in Fig. 4-3) theoretical cam curve be 150, the 9th king-tower is (in Fig. 4-3
16 regions) theoretical cam curve be 60, the tenth king-tower (17 regions in Fig. 4-3) theoretical cam curve be 800, the 4th public rectifying section
(18 regions in Fig. 4-3) theoretical cam curve is 20, and the 4th public stripping section (19 regions in Fig. 4-3) theoretical cam curve is
90, the mass fraction that liquid-phase reflux enters pre-separation tower, the first king-tower, the second king-tower and the 4th king-tower is 0.7, and gas phase flows back into
The mass fraction for entering pre-separation tower, the first king-tower, the second king-tower and the 4th king-tower is 0.7；11st king-tower (20 in Fig. 4-3
Region) theoretical cam curve is that the 30, the 12nd king-tower (21 regions in Fig. 4-3) theoretical cam curve is the 70, the 13rd king-tower (Fig. 4-
22 regions in 3) theoretical cam curve is that the 40, the 14th king-tower (23 regions in Fig. 4-3) theoretical cam curve is the 100, the 15th
King-tower (24 regions in Fig. 4-3) theoretical cam curve is 200, the 5th public rectifying section (25 regions in Fig. 4-3) theoretical tray
Number is 50, and the 5th public stripping section (26 regions in Fig. 4-3) theoretical cam curve is 30, and liquid-phase reflux enters pre-separation tower, the
One king-tower, the second king-tower, the 4th king-tower and the 11st king-tower mass fraction be 0.9, gas phase flows back into pre-separation tower, first
King-tower, the second king-tower, the 4th king-tower and the 11st king-tower mass fraction be 0.9；Reflux ratio is 10, operating pressure 1atm.
The purity of C6-C10 fraction section product (S06, S07, S8, S09, S04) is respectively 99.0%, 99.1%, 99.2%, 99.3%,
99.4%, yield is respectively 95.1%, 95.3%, 95.2%, 95.0%, 95.0%.Wherein product purity refers to that the carbon number is all
The gross mass content of hydro carbons.
Claims (7)
1. a kind of method using next door tower cutting F- T synthesis light oil, obtains the technique side of each carbon number fraction section product of C6-C10
Method and device, it is characterised in that: using the process of three single next door towers, or using two double next doors towers, or using one five every
The process of wall tower, detailed process are as follows:
Process using three single next door towers includes following three concomitant regimens:
Scheme 1: using three single next door towers, F- T synthesis light oil raw material (S01) enters first single next door tower (T11), and first is single
Next door tower (T11) top produces the fraction (S02) lighter than C6, and first single next door tower (T11) kettle produces the fraction heavier than C10
(S08), C6-C10 fraction (S09) is from first single next door tower (T11) king-tower side take-off, and enters second single next door tower (T12)；
Second single next door tower (T12) overhead extraction C6 fraction section (S03), pre-separation tower (T12) tower reactor produce C10 fraction section (S07),
C7-C9 fraction (S10) enters third list next door tower (T13) from T12 king-tower side take-off；Third list next door tower (T13) tower tower
Top extraction C7 fraction section (S04), third list next door tower (T13) tower reactor produce C9 fraction section (S06), and C8 fraction section (S05) is from T13
King-tower side take-off；
Scheme 2: using three single next door towers, F- T synthesis light oil raw material (S01) enters first single next door tower (T11), and first is single
Next door tower (T11) overhead extraction ratio C6 lighter fraction (S02), first single next door tower (T11) tower reactor extraction C9 and heavier evaporates
Divide (S11), C6-C8 fraction (S12) enters second single next door tower from first single next door tower (T11) king-tower side take-off
(T12), and enter third list next door tower (T13)；T12 overhead extraction C6 fraction section (S03), tower reactor produce C8 fraction section (S05),
C7 fraction section (S04) is produced from the second king-tower side (T12) line；Third list next door tower (T13) overhead extraction C9 fraction section (S06),
Tower reactor produces the fraction (S08) heavier than C10, and C10 fraction section (S07) is from third list next door tower (T13) king-tower side take-off；
Scheme 3: using three single next door towers, F- T synthesis light oil raw material (S01) enters the first pre-separation (T11), and T11 tower top is adopted
Out than C7 and lighter fraction (S13), and enter the second pre-separation (T12), T11 tower reactor produces the fraction heavier than C10
(S08), C8-C10 fraction (S14) is from T11 king-tower side take-off, and enters third pre-separation (T13)；T12 overhead extraction ratio C6
Lighter fraction (S02), tower reactor produce C7 fraction section (S04), and C6 fraction section (S03) is from T12 king-tower side take-off；T13 tower tower
Top extraction C8 fraction section (S05), tower reactor produce C10 fraction section (S07), and C9 fraction section is from T13 king-tower side take-off (S06)；
Or, F- T synthesis light oil raw material (S01) enters the first pre-separation (T11), T11 overhead extraction using three single next door towers
C7 and lighter fraction (S13), and enter the second pre-separation (T12), T11 tower reactor produces C9 and heavier fraction (S11), goes forward side by side
Enter third pre-separation (T13), C8 fraction section (S05) is from T11 king-tower side take-off；T12 overhead extraction ratio C6 lighter fraction
(S02), tower reactor extraction C7 fraction section (S04), C6 fraction section (S03) is from T12 king-tower side take-off；T13 column overhead extraction C9 evaporates
It is segmented (S06), tower reactor produces the fraction section (S08) heavier than C10, and C10 fraction section (S07) is from T13 king-tower side take-off；
It include following three schemes, pre-separation tower using two double next doors towers
Scheme 1: using two double next doors towers, F- T synthesis light oil raw material (S01) enters first pair of next door tower (T21), and first pair
Next door tower (T21) overhead extraction ratio C6 lighter fraction (S02), C6-C9 fraction (S15) is from first pair of next door tower (T21) king-tower
Upper side take-off, and enter second pair of next door tower (T22) pre-separation tower, C10 fraction section (S07) is from first pair of next door tower (T21)
Side take-off under king-tower, first pair of next door tower (T21) tower reactor produce the fraction (S08) heavier than C10；Second pair of next door tower
(T22) overhead extraction C6 fraction section (S03) is evaporated from side line and lower side take-off C7 on second pair of next door tower (T22) king-tower respectively
It is segmented (S04), C8 fraction section (S05), second pair of next door tower (T22) tower reactor produces C9 fraction section (S06)；
Scheme 2: using two double next doors towers, F- T synthesis light oil raw material (S01) enters first pair of next door tower (T21), and first pair
Next door tower (T21) overhead extraction ratio C6 lighter fraction (S02), C6 fraction section (S03) is from first pair of next door tower (T21) king-tower
Side take-off, C7-C10 fraction (S16) enter second pair of next door tower from side take-off under first pair of next door tower (T21) king-tower
(T22) pre-separation tower, first pair of next door tower (T21) tower reactor produce the fraction (S08) heavier than C10；Second pair of next door tower (T22)
Overhead extraction C7 fraction section (S04), respectively from side line on T22 king-tower and lower side take-off C8 fraction section (S05), C9 fraction section
(S06), second pair of next door tower (T22) tower reactor extraction C10 fraction section (S07)；
Scheme 3: using two double next doors towers, F- T synthesis light oil raw material (S01) enters first pair of next door tower (T21), and first pair
Next door tower (T21) overhead extraction ratio C6 lighter fraction (S02), C6 fraction section (S03), C7 fraction section (S04) are respectively from first
Side line and lower side take-off on double next door tower (T21) king-towers, first couple of next door tower (T21) tower reactor extraction C8 and heavier fraction
(S17), and enter second pair of next door tower (T22) pre-separation tower；Second pair of next door tower (T22) overhead extraction C8 fraction section (S05),
Respectively from side line and lower side take-off C9 fraction section (S06), C10 fraction section (S07) on second pair of next door tower (T22) king-tower,
Two pairs of next door tower (T22) tower reactors produce the fraction (S08) heavier than C10；
Scheme 4: using two double next doors towers, F- T synthesis light oil raw material (S01) enters first pair of next door tower (T21), and first pair
Next door tower (T21) overhead extraction C6 and lighter fraction (S18), and enter second pair of next door tower (T22) pre-separation tower, respectively from
Side line and lower side take-off C9 fraction section (S06), C10 fraction section (S07) on first pair of next door tower (T21) king-tower, first pair every
Wall tower (T21) tower reactor produces the fraction (S08) heavier than C10；Second couple of next door tower (T22) overhead extraction ratio C6 lighter fraction
(S02), respectively from side line and lower side take-off C6 fraction section (S03), C7 fraction section on second pair of next door tower (T22) king-tower
(S04), second pair of next door tower (T22) tower reactor extraction C8 fraction section (S05)；
Scheme using the process of a five next door towers is as follows:
Using a five next door towers, F- T synthesis light oil raw material (S01) enters five next door tower (T3) of pre-separation tower, by tower
W11, w21-22, w31-33, w41-44, w51-55 are more, and a partition is separated, and final T3 tower top obtains the component lighter than C6
(S02), top-down five side lines respectively obtain the product (S03-S07) of C6-C10 fraction section, and tower reactor obtains heavier than C10
Component (S08).
2. the method according to claim 1 using next door tower cutting F- T synthesis light oil, it is characterised in that: use two
When double next door towers, be placed with two column partitions in each double next doors tower, one piece of partition is placed in feed inlet side, discharge port side place two pieces every
Plate, raw material are added from first pair of next door tower (T21) feed inlet, and feed inlet is arranged in the middle part of next door tower (T21) pre-separation tower；Next door
Tower (T21) overhead stream enters reflux surge tank through condenser, and a part is as reflux, a part extraction；Tower reactor logistics one
Lease making reboiler returns to next door tower (T21), a part extraction；First pair of next door tower (T21) king-tower set there are two height it is different
Discharge port respectively corresponds two pieces of partitions；The structure of second pair of next door tower (T22) is identical as first single next door tower (T21), two towers
Connection type can be varied according to the different separation sequences of use.
3. it is according to claim 1 using next door tower cutting F- T synthesis light oil method, it is characterised in that: using five every
When wall tower, five column partitions are placed in tower, from feed inlet side to discharge port side, each column partition there are 1,2,3,4,5 pieces of partitions respectively, former
Material is added from five next door tower (T3) feed inlets, and feed inlet is arranged in the middle part of next door tower (T3) pre-separation tower；Next door tower (T3) tower top
Logistics enters reflux surge tank through condenser, and a part is as reflux, a part extraction；Tower reactor logistics a part is returned through reboiler
It returns next door tower (T3), a part extraction；First single next door tower (T3) king-tower is equipped with the different discharge port of five height, right respectively
Answer five blocks of column plates of the 5th column.
4. the method according to claim 1 using next door tower cutting F- T synthesis light oil, it is characterised in that: described first
The pre-separation tower theoretical cam curve of single next door tower (T11) is 10~200, and king-tower theoretical cam curve is 10~200, public rectifying section
Theoretical cam curve is 0~100, and public stripping section theoretical cam curve is 0~100, and liquid-phase reflux enters the quality point of pre-separation tower
Rate is 0.01~0.99, and the mass fraction that gas phase flows back into pre-separation tower is 0.01~0.99, and reflux ratio is 0.1~20, behaviour
Making pressure is 0.05~5atm；
The pre-separation tower theoretical cam curve of second single next door tower (T12) is 10~200, king-tower theoretical cam curve is 10~
200, public rectifying section theoretical cam curve is 0~100, and public stripping section theoretical cam curve is 0~100, and liquid-phase reflux enters pre-
The mass fraction of knockout tower is 0.01~0.99, and the mass fraction that gas phase flows back into pre-separation tower is 0.01~0.99, reflux
Than being 0.1~20, operating pressure is 0.05~5atm；
The pre-separation tower theoretical cam curve of third list next door tower (T13) be 10~200, king-tower theoretical cam curve be 10~
200, public rectifying section theoretical cam curve is 0~100, and public stripping section theoretical cam curve is 0~100, and liquid-phase reflux enters pre-
The mass fraction of knockout tower is 0.01~0.99, and the mass fraction that gas phase flows back into pre-separation tower is 0.01~0.99, reflux
Than being 0.1~20, operating pressure is 0.05~5atm.
5. the method according to claim 1 using next door tower cutting F- T synthesis light oil, it is characterised in that: described first
Pre-separation tower (region e in Fig. 4-2) theoretical cam curve of double next door towers (T21) is 10~200, and the first king-tower is (in Fig. 4-2
The region f) theoretical cam curve is 10~200, the first public rectifying section (region g in Fig. 4-2) theoretical cam curve is 0~100, the
One public stripping section (region h in Fig. 4-2) theoretical cam curve is 0~100, and liquid-phase reflux enters the mass fraction of pre-separation tower
It is 0.01~0.99, the mass fraction that gas phase flows back into pre-separation tower is 0.01~0.99, the second king-tower (area i in Fig. 4-2
Domain) theoretical cam curve be 10~200, third king-tower (region j in Fig. 4-2) theoretical cam curve be 10~200, the second public essence
Evaporating section (region k in Fig. 4-2) theoretical cam curve is 0~100, the second public stripping section (region l in Fig. 4-2) theoretical tray
Number is 0~100, and it is 0.01~0.99 that liquid-phase reflux, which enters pre-separation tower and the mass fraction of the first king-tower, and gas phase flows back into
The mass fraction of pre-separation tower and the first king-tower be 0.01~0.99, reflux ratio be 0.1~20, operating pressure be 0.05~
5atm；
Pre-separation tower (region e in Fig. 4-2) theoretical cam curve of second pair of next door tower (T22) is 10~200, and first is main
Tower (region f in Fig. 4-2) theoretical cam curve is 10~200, the first public rectifying section (region g in Fig. 4-2) theoretical tray
Number is 0~100, and the first public stripping section (region h in Fig. 4-2) theoretical cam curve is 0~100, and liquid-phase reflux enters pre- point
Mass fraction from tower is 0.01~0.99, and the mass fraction that gas phase flows back into pre-separation tower is 0.01~0.99, and second is main
Tower (region i in Fig. 4-2) theoretical cam curve is 10~200, and third king-tower (region j in Fig. 4-2) theoretical cam curve is 10
~200, the second public rectifying section (region k in Fig. 4-2) theoretical cam curve is 0~100, and the second public stripping section is (in Fig. 4-2
The region l) theoretical cam curve is 0~100, liquid-phase reflux enter the mass fraction of pre-separation tower and the first king-tower be 0.01~
0.99, it is 0.01~0.99 that gas phase, which flows back into pre-separation tower and the mass fraction of the first king-tower, and reflux ratio is 0.1~20, behaviour
Making pressure is 0.05~5atm.
6. it is according to claim 1 using next door tower cutting F- T synthesis light oil method, it is characterised in that: described five every
Pre-separation tower (1 region in Fig. 4-3) theoretical cam curve of wall tower (T3) is 10~200, the first king-tower (2nd area in Fig. 4-3
Domain) theoretical cam curve be 10~200, the first public rectifying section (3 regions in Fig. 4-3) theoretical cam curve be 0~100, first
Public stripping section (4 regions in Fig. 4-3) theoretical cam curve is 0~100, and the mass fraction that liquid-phase reflux enters pre-separation tower is
0.01~0.99, the mass fraction that gas phase flows back into pre-separation tower is 0.01~0.99；Second king-tower (5th area in Fig. 4-3
Domain) theoretical cam curve be 10~200, third king-tower (6 regions in Fig. 4-3) theoretical cam curve be 10~200, the second public essence
Evaporating section (7 regions in Fig. 4-3) theoretical cam curve is 0~100, the second public stripping section (8 regions in Fig. 4-3) theoretical tray
Number is 0~100, and it is 0.01~0.99 that liquid-phase reflux, which enters pre-separation tower and the mass fraction of the first king-tower, and gas phase flows back into
The mass fraction of pre-separation tower and the first king-tower is 0.01~0.99；4th king-tower (9 regions in Fig. 4-3) theoretical cam curve is
10~200, the 5th king-tower (10 regions in Fig. 4-3) theoretical cam curve is 10~200, the 6th king-tower (11st area Fig. 4-3 Zhong
Domain) theoretical cam curve be 10~200, the public rectifying section of third (12 regions in Fig. 4-3) theoretical cam curve be 0~100, third
Public stripping section (13 regions in Fig. 4-3) theoretical cam curve be 0~100, liquid-phase reflux enter pre-separation tower, the first king-tower and
The mass fraction of second king-tower is 0.01~0.99, and gas phase flows back into the quality of pre-separation tower, the first king-tower and the second king-tower
Dividing rate is 0.01~0.99；7th king-tower (14 regions in Fig. 4-3) theoretical cam curve is 10~200, the 8th king-tower (Fig. 4-3
In 15 regions) theoretical cam curve be 10~200, the 9th king-tower (16 regions in Fig. 4-3) theoretical cam curve be 10~200,
Tenth king-tower (17 regions in Fig. 4-3) theoretical cam curve is 10~200, the 4th public rectifying section (18 regions in Fig. 4-3)
Theoretical cam curve is 0~100, and the 4th public stripping section (19 regions in Fig. 4-3) theoretical cam curve is 0~100, liquid-phase reflux
Mass fraction into pre-separation tower, the first king-tower, the second king-tower and the 4th king-tower is 0.01~0.99, and gas phase flows back into pre-
Knockout tower, the first king-tower, the second king-tower and the 4th king-tower mass fraction be 0.01~0.99；11st king-tower is (in Fig. 4-3
20 regions) theoretical cam curve is that the 10~200, the 12nd king-tower (21 regions in Fig. 4-3) theoretical cam curve is 10~200,
13 king-towers (22 regions in Fig. 4-3) theoretical cam curve is that the 10~200, the 14th king-tower (23 regions in Fig. 4-3) are theoretical
The number of plates is that the 10~200, the 15th king-tower (24 regions in Fig. 4-3) theoretical cam curve is 10~200, the 5th public rectifying section
(25 regions in Fig. 4-3) theoretical cam curve is 0~100, the 5th public stripping section (26 regions in Fig. 4-3) theoretical cam curve
It is 0~100, liquid-phase reflux enters the quality point of pre-separation tower, the first king-tower, the second king-tower, the 4th king-tower and the 11st king-tower
Rate is 0.01~0.99, and gas phase flows back into pre-separation tower, the first king-tower, the second king-tower, the 4th king-tower and the 11st king-tower
Mass fraction is 0.01~0.99；Reflux ratio is 0.1~20, and operating pressure is 0.05~5atm.
7. the method according to claim 1 using next door tower cutting F- T synthesis light oil, it is characterised in that: the Fischer-Tropsch
Synthesize hydro carbons and micro oxygenatedchemicals that light oil raw material (S01) is mainly C6-C10 comprising carbon number range.Wherein hydro carbons
Mainly include n-alkane and alpha-olefin, further includes some isoparaffins, internal olefin, branched-chain alkene, and a small amount of cycloalkane, virtue
Hydrocarbon, cycloolefin.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810900872.1A CN109401779B (en) | 2018-08-09 | 2018-08-09 | A kind of method and device for cutting Fischer-Tropsch synthetic light oil by next-door tower |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810900872.1A CN109401779B (en) | 2018-08-09 | 2018-08-09 | A kind of method and device for cutting Fischer-Tropsch synthetic light oil by next-door tower |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109401779A true CN109401779A (en) | 2019-03-01 |
| CN109401779B CN109401779B (en) | 2021-08-24 |
Family
ID=65463590
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810900872.1A Active CN109401779B (en) | 2018-08-09 | 2018-08-09 | A kind of method and device for cutting Fischer-Tropsch synthetic light oil by next-door tower |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109401779B (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111073677A (en) * | 2019-12-26 | 2020-04-28 | 中国石油化工股份有限公司 | Separation and purification device and separation and purification process for C8-C20 normal paraffin mixed fraction |
| CN111548816A (en) * | 2020-05-29 | 2020-08-18 | 河南中托力合化学有限公司 | Separation and purification device for C8-C20 normal paraffin mixed fraction and thermal coupling process |
| 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 |
| CN112745881A (en) * | 2019-10-31 | 2021-05-04 | 内蒙古伊泰煤制油有限责任公司 | Fischer-Tropsch stable light hydrocarbon deep processing method |
| CN113862020A (en) * | 2020-06-30 | 2021-12-31 | 山西潞安煤基清洁能源有限责任公司 | Olefin separation device for improving quality of coal-made stable heavy oil |
| CN114736093A (en) * | 2021-01-08 | 2022-07-12 | 中国石油天然气股份有限公司 | Process for separating naphtha |
| WO2024229209A1 (en) * | 2023-05-02 | 2024-11-07 | Braskem S.A. | Process for the separation of olefins and low molecular weight hydrocarbons in methanol to olefin processes |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104130094A (en) * | 2014-07-28 | 2014-11-05 | 河北工业大学 | Energy saving method for reduced pressure separation of hexane, heptane and octane by utilizing wall separation tower |
-
2018
- 2018-08-09 CN CN201810900872.1A patent/CN109401779B/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104130094A (en) * | 2014-07-28 | 2014-11-05 | 河北工业大学 | Energy saving method for reduced pressure separation of hexane, heptane and octane by utilizing wall separation tower |
Non-Patent Citations (1)
| Title |
|---|
| 江涵 等: "分隔壁精馏塔节能技术的专利分析", 《吉林工程技术师范学院学报》 * |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112745881A (en) * | 2019-10-31 | 2021-05-04 | 内蒙古伊泰煤制油有限责任公司 | Fischer-Tropsch stable light hydrocarbon deep processing method |
| CN111073677A (en) * | 2019-12-26 | 2020-04-28 | 中国石油化工股份有限公司 | Separation and purification device and separation and purification process for C8-C20 normal paraffin mixed fraction |
| CN111548816A (en) * | 2020-05-29 | 2020-08-18 | 河南中托力合化学有限公司 | Separation and purification device for C8-C20 normal paraffin mixed fraction and thermal coupling process |
| CN113862020A (en) * | 2020-06-30 | 2021-12-31 | 山西潞安煤基清洁能源有限责任公司 | Olefin separation device for improving quality of coal-made stable heavy oil |
| 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 |
| CN114736093A (en) * | 2021-01-08 | 2022-07-12 | 中国石油天然气股份有限公司 | Process for separating naphtha |
| WO2024229209A1 (en) * | 2023-05-02 | 2024-11-07 | Braskem S.A. | Process for the separation of olefins and low molecular weight hydrocarbons in methanol to olefin processes |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109401779B (en) | 2021-08-24 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109401779A (en) | A kind of method and apparatus using next door tower cutting F- T synthesis light oil | |
| US9505678B2 (en) | Process to produce aromatics from crude oil | |
| US4524231A (en) | Production of durene from alcohols and ethers | |
| US4524227A (en) | Coproduction of durene and gasoline from synthesis gas and alcohols and separation of durene-gasoline mixtures | |
| US10113121B2 (en) | Gasoline production process comprising an isomerization step followed by at least two separation steps | |
| CN103827270B (en) | Hydrocracking is used to be prepared the method for alkylbenzene and biofuel altogether by natural oil | |
| CN104611059A (en) | Method for preparing liquid paraffin, paraffin precursor and lubricant base oil precursor from Fischer-Tropsch synthesis products | |
| WO2021041890A1 (en) | Low-sulfur aromatic-rich fuel oil blending component | |
| FR2862311A1 (en) | PROCESS FOR PRODUCING HIGH OCTANE INDEXES FROM A C5 / C6 CUT USING A MENBRANE SEPARATION UNIT | |
| CN207047164U (en) | A kind of following light component piece-rate systems of reformed oil C5 | |
| CN100575320C (en) | Extraction of oxygenates from hydrocarbon stream | |
| US2405393A (en) | Batch distillation | |
| CN102206504B (en) | Separation method of reformate | |
| EP1357165A1 (en) | Process and apparatus for the production of olefins | |
| CN107916132B (en) | A method of aromatic hydrocarbons and isomerization gasoline are produced by C6~C7 alkane | |
| US20190144366A1 (en) | Use of a lewis donor solvent to purify a feedstock that contains ethanol, acetaldehyde, and impurities | |
| RU2478601C1 (en) | Method of separating isopentane-pentane-hexane fraction | |
| RU2691987C1 (en) | Methods for increasing total output of aromatic hydrocarbons and xylenes in complex production of aromatic hydrocarbons | |
| KR20160040641A (en) | Integrated process for gasoline or aromatics production | |
| RU2621349C1 (en) | Method for separation of isophetic-pentan-isohexan-hexane fraction, reducing the share of recycle flows in the system | |
| US20200283355A1 (en) | Methods and systems of upgrading heavy aromatics stream to petrochemical feedstock | |
| CN106190285A (en) | A kind of produce high-flash, the operational approach of high isomerization product | |
| US2463601A (en) | Separation of highly branched paraffins into odorless fractions | |
| US2950241A (en) | Combination crude distillation and olefin production process | |
| CN105579424A (en) | Processes and systems for separating streams to provide a transalkylation feed stream in an aromatics complex |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |