CN106701183A

CN106701183A - System and method for reprocessing Fischer-Tropch synthesized product

Info

Publication number: CN106701183A
Application number: CN201611253125.0A
Authority: CN
Inventors: 安良成; 袁炜; 罗春桃; 王峰; 张安贵; 黄斌; 邵光涛; 袁华; 李增杰; 刘素丽; 梁雪美
Original assignee: Shenhua Group Corp Ltd; Shenhua Ningxia Coal Industry Group Co Ltd
Current assignee: China Energy Investment Corp Ltd; Shenhua Ningxia Coal Industry Group Co Ltd
Priority date: 2016-12-30
Filing date: 2016-12-30
Publication date: 2017-05-24

Abstract

The invention provides a system and a method for reprocessing a Fischer-Tropch synthesized product. The system comprises an oil-gas separation unit, a low temperature oil washing unit, a hydrogenation refining reactor, a first separation unit, a first fractionation unit, a hydrocracking reactor, a second separation unit and a second fractionation unit, wherein the first separation unit comprises a first high pressure hot separator, a first high pressure cold separator, a first low pressure cold separator and a first low pressure hot separator; the second separation unit comprises a second high pressure hot separator, a second high pressure cold separator, a second low pressure cold separator and a second low pressure hot separator. The method is to reprocess the Fischer-Tropch synthesized product by using the system. According to the system and the method, the Fischer-Tropch synthesized product can be respectively converted into various high-value-added products through reprocessing, so that the structure of the product can be optimized, and diversified development of the product can be realized; furthermore, the product can be further refined into a high-end chemical, and the market competitiveness of a Fischer-Tropch synthesized oil product is improved.

Description

System and method for being reprocessed to Fischer-Tropsch synthetic

Technical field

The invention belongs to coal chemical technology, and in particular to for the system reprocessed to Fischer-Tropsch synthetic and side Method.

Background technology

Coal in China reserves are more oily, gas reserves relative abundance, and coal is converted into liquid on a large scale with the technique of clean and effective The industrialization of fluid fuel and chemicals, advantageously reduces dependence of the China to Imported oil resource, improves China's oil product and chemistry The basic self-supporting ability of product.At present, because F- T synthesis technology has raw material range wide, product is mainly by alkane and alkene structure Into, and with sulphur, nitrogen and arene content is low, clean environment firendly the features such as, realize industrial applications in China.Wherein, thrown That produces has Inner Mongol group of gouy Thailand, 180,000 tons/year of dresses of 160,000 tons/year of Shanxi Lu Anmeiji artificial oils Co., Ltd and Shenhua Group Put；Project in construction has 4,000,000 tons/year of Ning Mei groups of Shenhua, 1,200,000 tons/year of Inner Mongol gouy Thailand, Shanxi the Lushui River to pacify 1,800,000 tons/year The projects such as rich 2,000,000 tons/year of the energy of (1,000,000 tons/year of a phase), 1,000,000 tons/year of Shandong Yan Kuang and Chongqing.Be expected to the year two thousand twenty I State's Fischer-Tropsch synthesis oil industry will form about 31,000,000 tons/year of production capacity.

At present, most F- T synthesis devices use the technology (CN of Zhong Ke artificial oils Co., Ltd 103146426 B), with liquefied gas, naphtha and diesel component as major product.However, because the demand in market is limited, entirely The production of the large fuel of state is impacted to petrochemical industry, causes the intensified competition to petrochemical industry, and necessarily coal enterprise is passed through Battalion's build-up of pressure.Therefore, domestic many scholars and technical staff are devoted to producing fuel as little as possible by existing apparatus, give birth to more Produce high valuable chemicals and adapt to product diversification development trend, so as to improve enterprise competitiveness.Such as Chinese patent CN 104611059 A, CN 102533329 B, CN 104178219 B etc. be each provided with Fischer-Tropsch synthetic or therein one The method that product is converted into certain high value added product is planted, such as, by the thick cured production microwax of F- T synthesis, uses Fischer Tropsch waxes Production lube base oil, or produce atoleine, paraffin precursor and lube base oil precursor with Fischer-Tropsch synthetic.But It is the method for not being provided with that Fischer-Tropsch synthetic is fully converted into various high value added products, corresponding system is not more provided System.

The content of the invention

It is an object of the invention to provide a kind of system and method for being reprocessed to Fischer-Tropsch synthetic, can Fischer-Tropsch synthetic is fully converted into various high valuable chemicals.

To realize the one side of the object of the invention, the present invention provides a kind of for being reprocessed to Fischer-Tropsch synthetic System, using following technical scheme：

A kind of system for being reprocessed to Fischer-Tropsch synthetic, including：

Oil-gas Separation unit, for carrying out Oil-gas Separation to the top product from F- T synthesis device, obtains gas gas-phase objects Material and the first Fischer-Tropsch oil；

Low temperature oil wash unit, for receiving the gaseous phase materials from the Oil-gas Separation unit and carrying out low temperature oil wash to it Separate, to isolate insoluble gas, obtain the second Fischer-Tropsch oil；

Hydrofining reactor, for receiving the first Fischer-Tropsch oil, the second Fischer-Tropsch oil and taking from F- T synthesis device Synthesis waxy stone is held in the palm, and hydrofining reaction is carried out to it and obtain refined products；

First separative element, for being separated to the refined products from the hydrofining reactor；

First separative element includes：

First high pressure hot separator, for carrying out gas-liquid separation to the refined products from the hydrofining reactor；

First cold high pressure separator, for carrying out gas-liquid point to the gaseous substance from first high pressure hot separator From；

First thermal low-pressure separators, for carrying out gas-liquid point to the liquid phase substance from first high pressure hot separator From；With

First cold low separator, for the liquid phase substance from first cold high pressure separator and from described The gaseous substance of one thermal low-pressure separators carries out gas-liquid separation；

First fractionation unit, for low from the first cold low separator in first separative element and the first heat The liquid phase substance of pressure separator be fractionated and obtains cut and remaining residue；

Hydrocracking reactor, obtains for carrying out hydrocracking reaction to the residue from first fractionation unit Crackate；

Second separative element, for being separated to the crackate from the hydrocracking reactor；

Second separative element includes：

Second high pressure hot separator, for carrying out gas-liquid separation to the crackate from the hydrocracking reactor；

Second cold high pressure separator, for carrying out gas-liquid point to the gaseous substance from second high pressure hot separator From；

Second thermal low-pressure separators, for carrying out gas-liquid point to the liquid phase substance from second high pressure hot separator From；With

Second cold low separator, for the liquid phase substance from second cold high pressure separator and from described The gaseous substance of two thermal low-pressure separators carries out gas-liquid separation；

After-fractionating unit, for low from the second cold low separator in second separative element and the second heat The liquid phase substance of pressure separator be fractionated and obtains cut and remaining residue.

Preferably, first fractionation unit includes the first fractionating column and after-fractionating tower that are sequentially connected with；

First fractionating column is used for the liquid phase from the first cold low separator and the first thermal low-pressure separators Material is fractionated, to obtain C5~C12 hydrocarbon-fractions as the first fractionation column tops, as the described first fractionation C10~C14 hydrocarbon-fractions of the line cut of tower side one, C14~C18 hydrocarbon-fractions as the first fractionating column side two wires cut and remaining Under residue；

The after-fractionating tower be used for vacuum fractionation is carried out to the residue from first fractionating column, using obtain as C19~C21 hydrocarbon-fractions of the line cut of the after-fractionating tower side one, as after-fractionating tower side two wires cut C21~ C25 hydrocarbon-fractions, the C25~C40 hydrocarbon-fractions as the line cut of the after-fractionating tower side three, as the after-fractionating tower side four The C40+ hydrocarbon-fractions and remaining residue of line cut.

Preferably, the after-fractionating unit includes the 3rd fractionating column and the 4th fractionating column that are sequentially connected with；

3rd fractionating column is used for the liquid phase from the second cold low separator and the second thermal low-pressure separators Material is fractionated, and obtains C10~C14 hydrocarbon-fractions as the line cut of the 3rd fractionating column side one, as described 3rd point Evaporate C14~C18 hydrocarbon-fractions of tower side two wires cut, C3~C11 hydrocarbon-fractions as the 3rd fractionation column tops and remaining Under residue；

4th fractionating column is used to be fractionated the residue from the 3rd fractionating column, obtains as described the C10~C15 hydrocarbon-fractions of the line cut of four fractionating column side one, evaporated as C16~C31 hydrocarbon of the 4th fractionating column side two wires cut Divide and as the C31+ hydrocarbon-fractions of the 4th fractionating column tower bottom distillate.

Preferably, the system also includes naphtha separative element, for evaporating the tower top from first fractionating column Separated, to obtain solvent oil product after isolating light component.

Preferably, the system also includes dewaxing unit, for evaporating the line of side one from first fractionating column respectively Point and side two wires cut separated, to remove isoparaffin, respectively obtain as liquid paraffin,light product C11-C13 just Structure paraffins mixture and the C14-C18 normal paraffin mixtures as Paraffin liquid heavy product.

Preferably, the system also includes hydro dewaxing reactor, for the line of side one from the after-fractionating tower Cut and side two wires cut carry out hydro dewaxing and are reacted to give pour point depression product.

Preferably, the system also includes solvent deoiling unit, for evaporating the line of side three from the after-fractionating tower Dividing carries out de-oiling to obtain the C25-C40 hydrocarbon mixtures as solid paraffin product.

Preferably, the system also includes white oil machining cell, for evaporating the side two wires from the 4th fractionating column Dividing carries out hydrofinishing and stripping, to obtain white oil product.

Preferably, the system also includes lubricating oil machining cell, for evaporating the bottom of towe from the 4th fractionating column Dividing carries out dewaxing and hydrofinishing to obtain lube base oil.

Preferably, the system also include catalyst cracking unit, for the insoluble gas from the low temperature oil wash unit, Light component from the naphtha separative element and the overhead fraction from the 3rd fractionating column carry out catalytic pyrolysis.

Preferably, the system also includes Fischer-Tropsch wax machining cell, for the line of side three from the after-fractionating tower Cut is processed to obtain Fischer-Tropsch wax.

To realize second aspect of the object of the invention, the present invention provides one kind using said system to Fischer-Tropsch synthetic The method reprocessed, the technical scheme of use is as follows：

A kind of method reprocessed to Fischer-Tropsch synthetic using said system, including：

Oil-gas Separation is carried out to the top product from F- T synthesis device using Oil-gas Separation unit and obtains gaseous phase materials With the first Fischer-Tropsch oil；The gaseous phase materials from the Oil-gas Separation unit are carried out with low temperature oil wash point using low temperature oil wash unit From to isolate insoluble gas, obtaining the second Fischer-Tropsch oil；

Using hydrofining reactor to the first Fischer-Tropsch oil, the second Fischer-Tropsch oil and the Fischer-Tropsch from F- T synthesis device close Hydrofining reaction is carried out into waxy stone；

The refined products from the hydrofining reactor are separated using the first separative element；Wherein, utilize First high pressure hot separator carries out gas-liquid separation to the refined products from the hydrofining reactor；Using the first cold anticyclone Separator carries out gas-liquid separation to the gaseous substance from first high pressure hot separator；Using the first thermal low-pressure separators, Gas-liquid separation is carried out to the liquid phase substance from first high pressure hot separator；Using the first cold low separator to from institute The liquid phase substance and the gaseous substance from first thermal low-pressure separators for stating the first cold high pressure separator carry out gas-liquid separation；

Using the first fractionation unit to low from the first cold low separator in first separative element and the first heat The liquid phase substance of pressure separator be fractionated and obtains cut and remaining residue；

Hydrocracking reaction is carried out using hydrocracking reactor to the residue from first fractionation unit to obtain Crackate；

The crackate from the hydrocracking reactor is separated using the second separative element；Wherein, utilize Second high pressure hot separator carries out gas-liquid separation to the crackate from the hydrocracking reactor；Using the second cold anticyclone Separator carries out gas-liquid separation to the gaseous substance from second high pressure hot separator；Using the second thermal low-pressure separators pair Liquid phase substance from second high pressure hot separator carries out gas-liquid separation；Using the second cold low separator to from described The liquid phase substance of the second cold high pressure separator and the gaseous substance from second thermal low-pressure separators carry out gas-liquid separation；

Using after-fractionating unit to low from the second cold low separator in second separative element and the second heat The liquid phase substance of pressure separator be fractionated and obtains cut and remaining residue.

Preferably, first fractionation unit includes the first fractionating column and after-fractionating tower that are sequentially connected with；Described second Fractionation unit includes the 3rd fractionating column and the 4th fractionating column that are sequentially connected with；Methods described includes：

Using the first fractionating column to the liquid phase substance from the first cold low separator and the first thermal low-pressure separators It is fractionated, is obtained C5~C12 hydrocarbon-fractions as the first fractionation column tops, as the first fractionating column side one C14~C18 hydrocarbon-fractions and remaining residual of C10~C14 hydrocarbon-fractions of line cut and the first fractionating column side two wires cut Thing；

Vacuum fractionation is carried out to the residue from first fractionating column using after-fractionating tower, to obtain as described C19~C21 hydrocarbon-fractions of the line cut of after-fractionating tower side one, the C21~C25 hydrocarbon as after-fractionating tower side two wires cut Cut, the C25~C40 hydrocarbon-fractions as the line cut of the after-fractionating tower side three, evaporated as the line of after-fractionating tower side four The C40+ hydrocarbon-fractions and remaining residue for dividing；

Using the 3rd fractionating column to the liquid phase substance from the second cold low separator and the second thermal low-pressure separators It is fractionated, is obtained C10~C14 hydrocarbon-fractions as the line cut of the 3rd fractionating column side one, as the 3rd fractionating column C14~C18 hydrocarbon-fractions of side two wires cut, C3~C11 hydrocarbon-fractions as the 3rd fractionation column tops and remaining Residue；

The residue from the 3rd fractionating column is fractionated using the 4th fractionating column, is obtained as described 4th point Evaporate C10~C15 hydrocarbon-fractions of the line cut of tower side one, the C16~C31 hydrocarbon-fractions as the 4th fractionating column side two wires cut and As the C31+ hydrocarbon-fractions of the 4th fractionating column tower bottom distillate.

Preferably, methods described includes：

The overhead fraction from first fractionating column is separated using naphtha separative element, sub-argument goes out light component After obtain solvent naphtha；The light component is C5-C8 hydrocarbon mixtures, and the solvent naphtha is C9-C12 hydrocarbon mixtures；

The line cut of side one and side two wires cut from first fractionating column are separated respectively using dewaxing unit, To remove isoparaffin, respectively obtain as the C11-C13 normal paraffin mixtures of liquid paraffin,light product and as heavy The C14-C18 normal paraffin mixtures of atoleine product；

The line cut of side one and side two wires cut from the after-fractionating tower are faced using hydro dewaxing reactor The reaction of hydrogen pour point depression obtains pour point depression product；

De-oiling is carried out using solvent deoiling unit to the line cut of side three from the after-fractionating tower to obtain as solid The C25-C40 hydrocarbon mixtures of paraffin wax product；

Hydrofinishing and stripping are carried out to the side two wires cut from the 4th fractionating column using white oil machining cell, with Obtain white oil product；

The tower bottom distillate from the 4th fractionating column is dewaxed using lubricating oil machining cell and hydrofinishing is obtained To lube base oil；

Using catalyst cracking unit to the insoluble gas from the low temperature oil wash unit, from the naphtha separative element Light component and the overhead fraction from the 3rd fractionating column carry out catalytic pyrolysis, produce ethene, propylene and gasoline group Point.

Preferably, methods described also includes：

The line cut of side three from the after-fractionating tower is processed using Fischer-Tropsch wax machining cell obtains Fischer-Tropsch wax.

Preferably, the reaction condition of the hydrofining reactor is：Temperature be 300~400 DEG C, pressure be 4.5~ 9.5MPa, cumulative volume air speed is 1.0~4.0h^-1, entrance hydrogen to oil volume ratio is 300~700；

The reaction condition of the hydrocracking reactor is：Temperature is 280~450 DEG C, and pressure is 6.0~13.0MPa, always 1.0~3.5h of volume space velocity^-1, entrance hydrogen to oil volume ratio 400~800；

The reaction condition of the hydro dewaxing reactor is：Temperature is 280~450 DEG C, and pressure is 6.0~13.0MPa, always 1.0~4.0h of volume space velocity^-1, entrance hydrogen to oil volume ratio 400~800；

The operating condition of first high pressure hot separator is：Temperature is 200~300 DEG C, and pressure is 3.5~9.0MPa；

The operating condition of first cold high pressure separator is：Temperature is 40~80 DEG C, and pressure is 3.5~9.0MPa；

The operating condition of second high pressure hot separator is：Temperature is 230~300 DEG C, and pressure is 6.5~13.0MPa；

The operating condition of second cold high pressure separator is：Temperature is 40~80 DEG C, and pressure is 6.0~13.0MPa；

The operating condition of the first cold low separator and the second cold low separator is：Temperature is 40~80 DEG C, pressure is 1.0~3.0MPa；

The operating condition of first thermal low-pressure separators and second thermal low-pressure separators is：Temperature is 200~300 DEG C, pressure is 1.0~3.0MPa.

The beneficial effects of the present invention are：

(1) system and method for being reprocessed to Fischer-Tropsch synthetic of the invention, can be different by three kinds Fischer-Tropsch synthetic by reprocessing be changed into respectively low-carbon alkene, lube base oil, white oil, Fischer Tropsch waxes, solvent naphtha, The high value added products such as paraffin, gasoline, can optimize product structure, and realize that product diversification develops, and can further refine and be High-end chemicals, improves the market competitiveness of oil from Fischer-Tropsch synthesis；

(2) system and method for being reprocessed to Fischer-Tropsch synthetic of the invention, use same set of catalytic pyrolysis Unit carries out catalytic pyrolysis to the product from multiple systems, produces low-carbon alkene and gasoline component, realizes processing unit (plant) comprehensive Close and utilize, reduce investment outlay；

(3) system and method for being reprocessed to Fischer-Tropsch synthetic of the invention, can be by adjusting temperature, pressure The operating conditions such as power, cut out the product frac for meeting processing unit (plant), and device operating flexibility is big；

(4) only need on original device spare interface, flexibly select the processing unit (plant) set up by actual conditions, transformation letter It is single, it is easy to accomplish.

Brief description of the drawings

Fig. 1 is the signal for the system reprocessed to Fischer-Tropsch synthetic in one embodiment of the invention Figure；

Fig. 2 is the first separative element in the system reprocessed to Fischer-Tropsch synthetic of the invention in one kind Schematic diagram in implementation method；

Fig. 3 is the second separative element in the system reprocessed to Fischer-Tropsch synthetic of the invention in one kind Schematic diagram in implementation method.

Specific embodiment

Technical solution of the present invention and its effect are described further below by way of specific embodiment.Implementation below Present disclosure is merely to illustrate, the protection domain being not intended to limit the invention.Using design of the invention to the present invention The simple change for carrying out is all in the scope of protection of present invention.

As shown in figure 1, the system for being reprocessed to Fischer-Tropsch synthetic of the invention, including：

Oil-gas Separation unit 17, for carrying out Oil-gas Separation to the top product from F- T synthesis device 3, obtains gas phase Material and the first Fischer-Tropsch oil；

Low temperature oil wash unit 15, for receiving the gaseous phase materials from the Oil-gas Separation unit 17 and carrying out low temperature to it Oil wash is separated, and to isolate insoluble gas, obtains the second Fischer-Tropsch oil；The low temperature oil wash unit 15 mainly includes absorption tower, desorption Tower, stabilizer and regenerator；Absorbed with from tower in gaseous phase materials input absorption tower from the Oil-gas Separation unit 17 Oil wash dry gas is isolated on top, and (oil wash dry gas is with CO and H₂Based on, tail gas device for producing hydrogen is input into, for hydrogen retrieval), absorbing tower bottom Liquid is input into desorption tower to desorb C2 classes gas (C2 classes mixture), and desorption tower tower bottom liquid input stabilizer is separated with from tower top Go out liquefied gas, stabilizer tower bottom liquid input regenerator obtains light naphthar, heavy naphtha is obtained from bottom of towe with from tower top, middle stone A cerebrol part returns to absorption tower as absorbent, and another part is with light naphthar together as the second Fischer-Tropsch oil input hydrogenation essence In reactor processed 1；The insoluble gas that low temperature oil wash is isolated is that the Fischer-Tropsch oil of liquefied gas second is included from low temperature oil wash unit 15 Regenerate the light naphthar and the part heavy naphtha from regenerator bottom of towe in low temperature oil wash unit 15 of column overhead；

Hydrofining reactor 1, for reception the first Fischer-Tropsch oil, the second Fischer-Tropsch oil and from F- T synthesis device 3 F- T synthesis waxy stone, and hydrofining reaction is carried out to it obtain refined products；It is preferred that the reaction of the hydrofining reactor 1 Condition is：Temperature is 300~400 DEG C, such as 340~365 DEG C；Pressure is 4.5~9.5MPa, such as 5.5~8.0MPa；It is overall Product air speed is 1.0~4.0h^-1, such as 2.0~3.0h^-1；Entrance hydrogen to oil volume ratio is 300~700, such as 450~600；

First separative element 2, for being separated to the refined products from the hydrofining reactor 1；

First separative element 2 includes：

First high pressure hot separator 21, for the refined products from the hydrofining reactor 1 to be carried out with gas-liquid point From；It is preferred that the operating condition of first high pressure hot separator 21 is：Temperature is 200~300 DEG C, such as 230~260 DEG C；Pressure Power is 3.5~9.0MPa, such as 6.0~7.0MPa；

First cold high pressure separator 22, for carrying out gas-liquid to the gaseous substance from first high pressure hot separator 21 Separate；It is preferred that the operating condition of first cold high pressure separator 22 is：Temperature is 40~80 DEG C, such as 50~70 DEG C；Pressure Be 3.5~9.0MPa, such as 6.0~7.0MPa；

First thermal low-pressure separators 24, for carrying out gas-liquid to the liquid phase substance from first high pressure hot separator 21 Separate；It is preferred that the operating condition of first thermal low-pressure separators 24 is：Temperature is 200~300 DEG C, such as 230~260 DEG C； Pressure is 1.0~3.0MPa, such as 1.5~2.5MPa；With

First cold low separator 23, for the liquid phase substance from first cold high pressure separator 22 and from institute The gaseous substance for stating the first thermal low-pressure separators 24 carries out gas-liquid separation；It is preferred that the operation bar of the first cold low separator 23 Part is：Temperature is 40~80 DEG C, such as 50~70 DEG C；Pressure is 1.0~3.0MPa, such as 1.5~2.5MPa；

First fractionation unit 4, for from the first cold low separator 23 and first in first separative element 2 The liquid phase substance of thermal low-pressure separators 24 is fractionated, and to be partitioned into different fractions product, is conducive to being processed further obtaining not Same product；

Hydrocracking reactor 5, obtains for carrying out hydrocracking reaction to the residue from first fractionation unit 4 To crackate；It is preferred that the reaction condition of the hydrocracking reactor 5 is：Temperature is 280~450 DEG C, such as 340~400 ℃；Pressure is 6.0~13.0MPa, such as 8.5~10.0MPa；1.0~3.5h of cumulative volume air speed^-1, such as 1.5~3.0h^-1； Entrance hydrogen to oil volume ratio 400~800, such as 550~700；

Second separative element 6, for being separated to the crackate from the hydrocracking reactor 5；

Second separative element 6 includes：

Second high pressure hot separator 61, for carrying out gas-liquid point to the crackate from the hydrocracking reactor 5 From；It is preferred that the operating condition of second high pressure hot separator 61 is：Temperature is 230~300 DEG C, such as 230~260 DEG C；Pressure Power is 6.5~13.0MPa, such as 8.5~10.0MPa；

Second cold high pressure separator 62, for carrying out gas-liquid to the gaseous substance from second high pressure hot separator 61 Separate；It is preferred that the operating condition of second cold high pressure separator 62 is：Temperature is 40~80 DEG C, such as 50~70 DEG C；Pressure Be 6.0~13.0MPa, such as 9.0~10.5MPa；

Second thermal low-pressure separators 64, for carrying out gas-liquid to the liquid phase substance from second high pressure hot separator 61 Separate；It is preferred that the operating condition of second thermal low-pressure separators 64 is：Temperature is 200~300 DEG C, such as 230~260 DEG C； Pressure is 1.0~3.0MPa, such as 1.5~2.5MPa；With

Second cold low separator 63, for the liquid phase substance from second cold high pressure separator 62 and from institute The gaseous substance for stating the second thermal low-pressure separators 64 carries out gas-liquid separation；It is preferred that the operation bar of the second cold low separator 63 Part is：Temperature is 40~80 DEG C, such as 50~70 DEG C；Pressure is 1.0~3.0MPa, such as 1.5~2.5MPa；

After-fractionating unit 7, for from the second cold low separator 63 and second in second separative element 6 The liquid phase substance of thermal low-pressure separators 64 is fractionated, and to be partitioned into different fractions product, is conducive to being processed further obtaining not Same product.

Various devices wherein used are commonly used in the art.

System of the invention, is reprocessed respectively by by several products of F- T synthesis, obtains the product of high added value Product, reduce the wasting of resources；And can cut out and meet the product of processing unit (plant) and evaporate by adjusting the operating conditions such as temperature, pressure Point, device operating flexibility is big.

In one embodiment, first fractionation unit 4 includes the first fractionating column 41 being sequentially connected with and second point Evaporate tower 42；It is preferred that the theoretical cam curve of first fractionating column 41 is 20~40,100~160 DEG C of tower top temperature, column bottom temperature 250~400 DEG C, operating pressure is 0.1~1.0MPa；It is preferred that the theoretical cam curve of the after-fractionating tower 42 is 10~40, tower Top temperature is 50~150 DEG C, and column bottom temperature is 200~350 DEG C, and operating pressure is 0~0.1MPa；

First fractionating column 41 is used for from the first cold low separator 23 and the first thermal low-pressure separators 24 Liquid phase substance be fractionated, to obtain C5~C12 hydrocarbon-fractions as the overhead fraction of the first fractionating column 41, as described C10~C14 hydrocarbon-fractions of the line cut of 41 side of the first fractionating column one, as the side two wires cut of first fractionating column 41 C14~ C18 hydrocarbon-fractions and remaining residue；

The after-fractionating tower 42 is used to carry out vacuum fractionation to the residue from first fractionating column 41, to obtain As C19~C21 hydrocarbon-fractions of the line cut of 42 side of after-fractionating tower one, as the side two wires cut of the after-fractionating tower 42 C21~C25 hydrocarbon-fractions, the C25~C40 hydrocarbon-fractions as the line cut of 42 side of after-fractionating tower three, as described second The C40+ hydrocarbon-fractions and remaining residue of the line cut of 42 side of fractionating column four；

Usually, fractionating column is disposed with tower top outlet, the outlet of the line of side one, the outlet of side two wires, the line of side three from top to bottom Outlet and bottom of towe outlet.Different cuts is fractionated out from different outlets respectively during fractionation.Fractionating column is respectively exported from top to bottom Cut carbon number gradually increases, and operating condition is adjusted as needed can change each outlet Fraction distribution.

The specific setting of the first fractionation unit, helps further to divide the liquid phase substance from the first separative element Evaporate, in order to follow-up reprocessing.

In one embodiment, the after-fractionating unit 7 includes the 3rd fractionating column 71 being sequentially connected with and the 4th point Evaporate tower 72；It is preferred that the theoretical cam curve of first fractionating column 71 is 20~40,100~160 DEG C of tower top temperature, column bottom temperature 250~400 DEG C, operating pressure is 0.1~1.0MPa；It is preferred that the theoretical cam curve of the after-fractionating tower 72 is 10~40, tower Top temperature is 50~150 DEG C, and column bottom temperature is 200~350 DEG C, and operating pressure is 0~0.1MPa；

3rd fractionating column 71 is used for from the second cold low separator 63 and the second thermal low-pressure separators 64 Liquid phase substance be fractionated, obtain C10~C14 hydrocarbon-fractions as the line cut of 71 side of the 3rd fractionating column one, as institute State the side two wires cut of the 3rd fractionating column 71 C14~C18 hydrocarbon-fractions, as the overhead fraction of the 3rd fractionating column 71 C3~ C11 hydrocarbon-fractions and remaining residue；

4th fractionating column 72 is used to be fractionated the residue from the 3rd fractionating column 71, obtains as institute State C10~C15 hydrocarbon-fractions of the line cut of 72 side of the 4th fractionating column one, the C16 as the side two wires cut of the 4th fractionating column 72 ~C31 hydrocarbon-fractions and the C31+ hydrocarbon-fractions as the tower bottom distillate of the 4th fractionating column 72.

The specific setting of after-fractionating unit, helps further to divide the liquid phase substance from the second separative element Evaporate, in order to follow-up reprocessing.

In one embodiment, the system also includes that the system also includes naphtha separative element 8, for coming Separated from the overhead fraction of first fractionating column 41, to obtain solvent oil product after isolating light component.

The setting of naphtha separative element, is conducive to carrying out isolated solvent naphtha to the overhead fraction of the first fractionating column 41 With the C5-C8 hydrocarbon light components for catalytic pyrolysis, conveniently reprocess to obtain high added value product.

In one embodiment, the system also includes dewaxing unit 9, for respectively to from first fractionating column The 41 line cut of side one and side two wires cut is separated, and to remove isoparaffin, is respectively obtained and is produced as liquid paraffin,light The C11-C13 normal paraffin mixtures of product and the C14-C18 normal paraffin mixtures as Paraffin liquid heavy product.

Because though the hydrocarbon after hydrofinishing is saturated alkane, it is the mixture of n-alkane and isoparaffin, is taken off Ceroplastic is n-alkane separating technology, is that n-alkane is separated with isoparaffin, obtains the n-alkane of high-purity, i.e., It is atoleine, wherein, it is light liquids to what is obtained after the line ends removal isoparaffin of side one of first fractionating column 41 Paraffin, is Paraffin liquid heavy to what is obtained after the side two wires ends removal isoparaffin of first fractionating column 41.

In one embodiment, the system also includes hydro dewaxing reactor 10, for from described second point Evaporate the line cut of side one and side two wires cut of tower 42 and carry out hydro dewaxing and be reacted to give pour point depression product, pour point depression product is diesel oil group Point；It is preferred that the reaction condition of the hydro dewaxing reactor 10 is：Temperature is 280~450 DEG C, such as 340~400 DEG C；Pressure Be 6.0~13.0MPa, such as 8.5~10.0MPa；1.0~4.0h of cumulative volume air speed^-1, such as 2.0~3.0h^-1；Entrance hydrogen oil Volume ratio 400~800, such as 550~700.Diesel component of the invention is passed through and blend component reconciliation process according to a certain ratio The diesel oil of national standard can be obtained meeting afterwards, the blend component can be petroleum base poor ignition quality fuel component or direct liquefaction diesel oil Component.Isomerization reaction is substantially carried out in hydro dewaxing reactor 10, while being also carried out further hydrocracking reaction.

In one embodiment, the system also includes solvent deoiling unit 11, for from the after-fractionating The line cut of side three of tower 42 carries out de-oiling, to obtain the C25-C40 hydrocarbon mixtures as solid paraffin product.

The principle of solvent deoiling is that have the characteristic of different solubility to oil, wax using solvent, makes wax in the solution Solubility reduces and crystallizes and separate out, and is then separated oil and wax using mechanical filter or the method for centrifugation.Rich oil solvent is again Oil is desorbed by evaporating or stripping treatment, recycled solvent.

In one embodiment, the system also includes white oil machining cell 13, for from the described 4th fractionation The side two wires cut of tower 72 carries out hydrofinishing and stripping, to obtain white oil product.

It is that industry is white well because the side two wires fraction isomerization degree of the 4th fractionating column 72 is high, flash-point is high, it is low to put just Oily raw material, therefore it is processed using two sections of white oil hydrogenation techniques：First paragraph is raw material hydrofinishing section, for hydrofinishing To remove the sulfur-bearing in raw material, nitrogen-containing compound, and saturated hydrocarbons will be largely converted into, then through stripping, dry after enter the Two sections；Second segment is refining stage after hydrogenation, for carrying out further hydrofinishing to unsaturated aromatic hydrocarbons in first paragraph, by its turn Saturated hydrocarbons is turned to, then white oil product is obtained after stripping, drying.

In one embodiment, the system also includes lubricating oil machining cell 14, for from described 4th point Evaporating the tower bottom distillate of tower 72 carries out dewaxing and hydrofinishing to obtain lube base oil.The lube base oil includes API Group III lube base oil.

The raw material that the tower bottom distillate of the 4th fractionating column 72 can be processed as lube base oil, therefore two-stage process is used to it It is processed：First paragraph is isomerization dewaxing or catalytic dewaxing, and the N-alkanes in raw material is made by selective isomerization and cracking reaction Hydrocarbon isomerization, obtains low hectare of point, the base oil of high viscosity index (HVI)；Second segment by hydrofinishing, reduces by the to be refined after hydrogenation One section processes sulfide, nitride and the residual aromatic hydrocarbons remained in the base oil for obtaining, and puies forward its high oxidation stability and pacifies with color It is qualitative, then lube base oil is obtained by stripping.

In one embodiment, the system also includes catalyst cracking unit 16, for from the low temperature oil wash The insoluble gas of unit 15, the light component from the naphtha separative element 8 and the tower top from the 3rd fractionating column 71 Cut carries out catalytic pyrolysis, produces ethene, propylene and gasoline.

System and method of the present invention for being reprocessed to Fischer-Tropsch synthetic, with same set of catalyst cracking unit pair Product from multiple systems carries out catalytic pyrolysis, produces low-carbon alkene and gasoline component, realizes processing unit (plant) comprehensive utilization, Reduce investment outlay.

In one embodiment, the system also includes Fischer-Tropsch wax machining cell 12, for from described second point The line cut of side three for evaporating tower 42 is processed to obtain Fischer-Tropsch wax.The Fischer-Tropsch wax includes 85#, 95#, 110# Fischer Tropsch waxes Deng.

Three kinds of different Fischer-Tropsch synthetics can be respectively changed into low-carbon (LC) alkene by system of the invention by reprocessing The high value added products such as hydrocarbon, lube base oil, white oil, Fischer Tropsch waxes, solvent naphtha, paraffin, gasoline component, optimize product Structure, realizes product diversification development, improves economic benefit, and it is high-end chemicals that can further refine, and raising takes Hold in the palm the market competitiveness of synthetic oil；And only need on original device spare interface, it is flexibly selecting to set up by actual conditions plus Frock is put, and transformation is simple, it is easy to accomplish.

The present invention also provides a kind of method reprocessed to Fischer-Tropsch synthetic using above-mentioned system, methods described Including：

Oil-gas Separation is carried out using 17 pairs of top products from F- T synthesis device 3 of Oil-gas Separation unit obtain gas gas-phase objects Material and the first Fischer-Tropsch oil；Low-temperature oil is carried out using 15 pairs of gaseous phase materials from the Oil-gas Separation unit 17 of low temperature oil wash unit Separation is washed, to isolate insoluble gas, the second Fischer-Tropsch oil is obtained；

Using 1 pair of the first Fischer-Tropsch oil of hydrofining reactor, the second Fischer-Tropsch oil and the Fischer-Tropsch from F- T synthesis device 3 Synthesis waxy stone carries out hydrofining reaction；

Separated using 2 pairs of refined products from the hydrofining reactor 1 of the first separative element；Wherein, profit Gas-liquid separation is carried out with 21 pairs of refined products from the hydrofining reactor 1 of the first high pressure hot separator；Using first 22 pairs of gaseous substances from first high pressure hot separator 21 of cold high pressure separator carry out gas-liquid separation；It is low using the first heat Pressure separator 24, gas-liquid separation is carried out to the liquid phase substance from first high pressure hot separator 21；Using the first cold low Liquid phase substance of the separator 23 pairs from first cold high pressure separator 22 and from first thermal low-pressure separators 24 Gaseous substance carries out gas-liquid separation；

Using the first fractionation unit 4 pairs from the first cold low separator 23 and first in first separative element 2 The liquid phase substance of thermal low-pressure separators 24 be fractionated and obtains cut and remaining residue；

Hydrocracking reaction is carried out using 5 pairs of residues from first fractionation unit 4 of hydrocracking reactor to obtain To crackate；

Separated using 6 pairs of crackates from the hydrocracking reactor 5 of the second separative element；Wherein, profit Gas-liquid separation is carried out with 61 pairs of crackates from the hydrocracking reactor 5 of the second high pressure hot separator；Using second 62 pairs of gaseous substances from second high pressure hot separator 61 of cold high pressure separator carry out gas-liquid separation；It is low using the second heat Pressure 64 pairs of liquid phase substances from second high pressure hot separator 61 of separator carry out gas-liquid separation；Using the second cold low point 63 pairs from the device liquid phase substances from second cold high pressure separator 62 and the gas from second thermal low-pressure separators 64 Phase material carries out gas-liquid separation；

Using after-fractionating unit 7 pairs from the second cold low separator 63 and second in second separative element 6 The liquid phase substance of thermal low-pressure separators 64 be fractionated and obtains cut and remaining residue.

In one embodiment, first fractionation unit 4 includes the first fractionating column 41 being sequentially connected with and second point Evaporate tower 42；The after-fractionating unit 7 includes the 3rd fractionating column 71 and the 4th fractionating column 72 that are sequentially connected with；Methods described bag Include：

Using 41 pairs of liquid from the first cold low separator 23 and the first thermal low-pressure separators 24 of the first fractionating column Phase material is fractionated, and obtains C5~C12 hydrocarbon-fractions as the overhead fraction of the first fractionating column 41, as described first point Evaporate C10~C14 hydrocarbon-fractions of the line cut of 41 side of tower one and C14~C18 hydrocarbon-fractions of the side two wires cut of first fractionating column 41 With remaining residue；

Carry out vacuum fractionation using 42 pairs of residues from first fractionating column 41 of after-fractionating tower, using obtain as C19~C21 hydrocarbon-fractions of the line cut of 42 side of after-fractionating tower one, as the side two wires cut of the after-fractionating tower 42 C21~C25 hydrocarbon-fractions, the C25~C40 hydrocarbon-fractions as the line cut of 42 side of after-fractionating tower three, as described second point Evaporate the C40+ hydrocarbon-fractions and remaining residue of the line cut of 42 side of tower four；

Using 71 pairs of liquid from the second cold low separator 63 and the second thermal low-pressure separators 64 of the 3rd fractionating column Phase material is fractionated, and obtains C10~C14 hydrocarbon-fractions as the line cut of 71 side of the 3rd fractionating column one, as described C14~C18 hydrocarbon-fractions, the C3~C11 hydrocarbon as the overhead fraction of the 3rd fractionating column 71 of the side two wires cut of three fractionating column 71 Cut and remaining residue；

It is fractionated using 72 pairs of residues from the 3rd fractionating column 71 of the 4th fractionating column, is obtained as described C10~C15 hydrocarbon-fractions of the line cut of four fractionating columns, 72 side one, the C16~C31 as the side two wires cut of the 4th fractionating column 72 Hydrocarbon-fraction and the C31+ hydrocarbon-fractions as the tower bottom distillate of the 4th fractionating column 72.

In one embodiment, methods described includes：

Separated using 8 pairs of overhead fractions from first fractionating column 41 of naphtha separative element, sub-argument goes out gently Solvent naphtha is obtained after component；The light component is C5-C8 hydrocarbon mixtures, and the solvent naphtha is C9-C12 hydrocarbon mixtures；

The line cut of side one and side two wires cut from first fractionating column 41 are divided respectively using dewaxing unit 9 From, to remove isoparaffin, respectively obtain as liquid paraffin,light product C11-C13 normal paraffin mixtures and as weight The C14-C18 normal paraffin mixtures of matter atoleine product；

Entered using hydro dewaxing reactor 10 pairs of the line cuts of side one and side two wires cut from the after-fractionating tower 42 The reaction of row hydro dewaxing obtains pour point depression product；

De-oiling is carried out using 11 pairs of line cuts of side three from the after-fractionating tower 42 of solvent deoiling unit obtain conduct The C25-C40 hydrocarbon mixtures of solid paraffin product；

Hydrofinishing and vapour are carried out using 13 pairs of side two wires cuts from the 4th fractionating column 72 of white oil machining cell Carry, to obtain white oil product；

Dewaxed and be hydrogenated with essence using 14 pairs of tower bottom distillates from the 4th fractionating column 72 of lubricating oil machining cell Lube base oil is obtained；The lube base oil lube base oil such as including API Group IIIs；

Separated using 16 pairs of insoluble gas from the low temperature oil wash unit 15 of catalyst cracking unit, from the naphtha The light component of unit 8 and the overhead fraction from the 3rd fractionating column 71 carry out catalytic pyrolysis, produce ethene, propylene and Gasoline component.Gasoline component can obtain gasoline after being processed through gasoline stabilizer.The operating condition of the gasoline stabilizer is：Tower top Temperature is 50~150 DEG C, such as 109 DEG C；Column bottom temperature is 100~200 DEG C, such as 170 DEG C；Pressure is 1.0~2.0MPa, than Such as 1.75MPa；The number of plates is 20~60, such as 47.

In one embodiment, methods described also includes：

The expense of obtaining is processed using 12 pairs of line cuts of side three from the after-fractionating tower 42 of Fischer-Tropsch wax machining cell Into wax；The Fischer-Tropsch wax Fischer Tropsch waxes such as including 85#, 95#, 110#.

In one embodiment, the reaction condition of the hydrofining reactor 1 is：Temperature is 300~400 DEG C, than Such as 340~365 DEG C；Pressure is 4.5~9.5MPa, such as 5.5~8.0MPa；Cumulative volume air speed is 1.0~4.0h^-1, such as 2.0 ~3.0h^-1；Entrance hydrogen to oil volume ratio is 300~700, such as 450~600；

The reaction condition of the hydrocracking reactor 5 is：Temperature is 280~450 DEG C, such as 340~400 DEG C；Pressure Be 6.0~13.0MPa, such as 8.5~10.0MPa；1.0~3.5h of cumulative volume air speed^-1, such as 1.5~3.0h^-1；Entrance hydrogen oil Volume ratio 400~800, such as 550~700；

The reaction condition of the hydro dewaxing reactor 10 is：Temperature is 280~450 DEG C, such as 340~400 DEG C；Pressure Be 6.0~13.0MPa, such as 8.5~10.0MPa；1.0~4.0h of cumulative volume air speed^-1, such as 2.0~3.0h^-1；Entrance hydrogen oil Volume ratio 400~800, such as 550~700；

The operating condition of first high pressure hot separator 21 is：Temperature is 200~300 DEG C, such as 230~260 DEG C；Pressure Power is 3.5~9.0MPa, such as 6.0~7.0MPa；

The operating condition of first cold high pressure separator 22 is：Temperature is 40~80 DEG C, such as 50~70 DEG C；Pressure is 3.5~9.0MPa, such as 6.0~7.0MPa；

The operating condition of second high pressure hot separator 61 is：Temperature is 230~300 DEG C, such as 230~260 DEG C；Pressure Power is 6.5~13.0MPa, such as 8.5~10.0MPa；

The operating condition of second cold high pressure separator 62 is：Temperature is 40~80 DEG C, such as 50~70 DEG C；Pressure is 6.0~13.0MPa, such as 9.0~10.5MPa；

The operating condition of the first cold low separator 23 and the second cold low separator 63 is：Temperature be 40~ 80 DEG C, such as 50~70 DEG C；Pressure is 1.0~3.0MPa, such as 1.5~2.5MPa；

The operating condition of first thermal low-pressure separators 24 and second thermal low-pressure separators 64 is：Temperature is 200 ~300 DEG C, such as 230~260 DEG C；Pressure is 1.0~3.0MPa, such as 1.5~2.5MPa.

Fischer-Tropsch synthetic is carried out to add again using the system for reprocessing Fischer-Tropsch synthetic of the invention The method of work, process is as follows：

Oil-gas Separation is carried out in the top product input Oil-gas Separation unit 17 from Fischer-Tropsch synthesis unit 3 to obtain To gaseous phase materials and the first Fischer-Tropsch oil；Gaseous phase materials from the Oil-gas Separation unit 17 are input into the low temperature oil wash unit 15 In carry out low temperature oil wash, and isolate insoluble gas, obtain the second Fischer-Tropsch oil；The first Fischer-Tropsch oil from Oil-gas Separation unit 17, F- T synthesis waxy stone from Fischer-Tropsch synthesis unit 3 and the second Fischer-Tropsch oil input from the low temperature oil wash unit 15 add Hydrofining reaction is carried out in hydrogen finishing reactor 1, refined products are obtained；Refined product from the hydrofining reactor 1 Thing is input into first high pressure hot separator 21 and carries out gas-liquid separation；Gas gas-phase objects from first high pressure hot separator 21 Matter is input into first cold high pressure separator 22 and carries out gas-liquid separation；Liquid phase thing from first high pressure hot separator 21 Matter is input into first thermal low-pressure separators 24 and carries out gas-liquid separation；Liquid phase thing from first cold high pressure separator 22 Matter and the gaseous substance from first thermal low-pressure separators 24 are input into the first cold low separator 23 and carry out gas-liquid Separate；Liquid phase substance input described first from the first cold low separator 23 and first thermal low-pressure separators 24 Carry out being fractionated in fractionating column 41 obtain C5~C12 hydrocarbon-fractions as the overhead fraction of the first fractionating column 41, as described C10~C14 hydrocarbon-fractions of the line cut of one fractionating column, 41 side one, the C14~C18 as the side two wires cut of first fractionating column 41 Hydrocarbon-fraction and remaining residue；Residue from first fractionating column 41 is input into the after-fractionating tower 42 and is divided Evaporate, obtain C19~C21 hydrocarbon-fractions as the line cut of 42 side of after-fractionating tower one, as the side of after-fractionating tower 42 C21~C25 hydrocarbon-fractions of two wires cut, C25~C40 hydrocarbon-fractions, conduct as the line cut of 42 side of after-fractionating tower three The C40+ hydrocarbon-fractions and remaining residue of the line cut of 42 side of after-fractionating tower four；From the residual of the after-fractionating tower 42 Stay thing to be input into carries out hydrocracking reaction and obtains crackate in the hydrocracking reactor 5；It is hydrocracked instead from described Answering the crackate of device 5 to be input into second high pressure hot separator 61 carries out gas-liquid separation；From second thermal high point Being input into second cold high pressure separator 62 from the gaseous substance of device 61 carries out gas-liquid separation；From second thermal high point Being input into second thermal low-pressure separators 64 from the liquid phase substance of device 61 carries out gas-liquid separation；From second cold anticyclone point Liquid phase substance from device 62 and the gaseous substance from second thermal low-pressure separators 64 are input into second cold low and separate Gas-liquid separation is carried out in device 63；Liquid phase substance from the second cold low separator 63 and the second thermal low-pressure separators 64 is defeated To enter be fractionated in the 3rd fractionating column 71, obtain being evaporated as C10~C14 hydrocarbon of the line cut of 71 side of the 3rd fractionating column one Point, the C14~C18 hydrocarbon-fractions as the side two wires cut of the 3rd fractionating column 71, evaporated as the tower top of the 3rd fractionating column 71 C3~C11 the hydrocarbon-fractions and remaining residue for dividing；Residue input the 4th fractionation from the 3rd fractionating column 71 It is fractionated in tower 72, is obtained C10~C15 hydrocarbon-fractions as the line cut of 72 side of the 4th fractionating column one, as described C16~C31 hydrocarbon-fractions of the side two wires cut of four fractionating column 72 and evaporated as the C31+ hydrocarbon of the tower bottom distillate of the 4th fractionating column 72 Point；Overhead fraction from first fractionating column 41 is input into after isolating light component in the naphtha separative element 8 and obtains Solvent oil product；The line cut of side one and side two wires cut from first fractionating column 41 are input into the dewaxing unit 9 respectively In separated, remove isoparaffin, respectively obtain as liquid paraffin,light product C11-C13 normal paraffin mixtures and As the C14-C18 normal paraffin mixtures of Paraffin liquid heavy product；The line cut of side one from the after-fractionating tower 42 Pour point depression product is obtained with hydro dewaxing reaction is carried out in the side two wires cut input hydro dewaxing reactor 10；From described De-oiling is carried out in the line cut input solvent deoiling unit 11 of side three of two fractionating columns 42 to obtain as solid paraffin product C25-C40 hydrocarbon mixtures；The line cut of side three from the after-fractionating tower 42 is input into the Fischer-Tropsch wax machining cell 12 It is processed and obtains Fischer-Tropsch wax；Side two wires cut from the 4th fractionating column 72 is input into the white oil machining cell 13 Row hydrofinishing and stripping, to obtain white oil product；Tower bottom distillate from the 4th fractionating column 72 is input into the lubricating oil Dewaxing is carried out in machining cell 14 and hydrofinishing obtains lube base oil；From the insoluble of the low temperature oil wash unit 15 The input of gas, the light component from the naphtha separative element 8 and the overhead fraction from the 3rd fractionating column 71 is described Catalytic pyrolysis is carried out in catalyst cracking unit 16, ethene, propylene and gasoline component is produced.

Claims

1. a kind of system that product for syrup state bed Fischer Tropsch synthesizer is reprocessed, it is characterised in that the system Including：

Oil-gas Separation unit (17), for carrying out Oil-gas Separation to the top product from F- T synthesis device (3), obtains gas phase Material and the first Fischer-Tropsch oil；

Low temperature oil wash unit (15), for receiving the gaseous phase materials from the Oil-gas Separation unit (17) and carrying out low temperature to it Oil wash is separated, and to isolate insoluble gas, obtains the second Fischer-Tropsch oil；

Hydrofining reactor (1), for reception the first Fischer-Tropsch oil, the second Fischer-Tropsch oil and from F- T synthesis device (3) F- T synthesis waxy stone, and hydrofining reaction is carried out to it obtain refined products；

First separative element (2), for being separated to the refined products from the hydrofining reactor (1)；

First separative element (2) includes：

First high pressure hot separator (21), for the refined products from the hydrofining reactor (1) to be carried out with gas-liquid point From；

First cold high pressure separator (22), for carrying out gas-liquid to the gaseous substance from first high pressure hot separator (21) Separate；

First thermal low-pressure separators (24), for carrying out gas-liquid to the liquid phase substance from first high pressure hot separator (21) Separate；With

First cold low separator (23), for the liquid phase substance from first cold high pressure separator (22) and from institute The gaseous substance for stating the first thermal low-pressure separators (24) carries out gas-liquid separation；

First fractionation unit (4), for from the first cold low separator (23) in first separative element (2) and The liquid phase substance of one thermal low-pressure separators (24) be fractionated and obtains cut and remaining residue；

Hydrocracking reactor (5), obtains for carrying out hydrocracking reaction to the residue from first fractionation unit (4) To crackate；

Second separative element (6), for being separated to the crackate from the hydrocracking reactor (5)；

Second separative element (6) includes：

Second high pressure hot separator (61), for carrying out gas-liquid point to the crackate from the hydrocracking reactor (5) From；

Second cold high pressure separator (62), for carrying out gas-liquid to the gaseous substance from second high pressure hot separator (61) Separate；

Second thermal low-pressure separators (64), for carrying out gas-liquid to the liquid phase substance from second high pressure hot separator (61) Separate；With

Second cold low separator (63), for the liquid phase substance from second cold high pressure separator (62) and from institute The gaseous substance for stating the second thermal low-pressure separators (64) carries out gas-liquid separation；

After-fractionating unit (7), for from the second cold low separator (63) in second separative element (6) and The liquid phase substance of two thermal low-pressure separators (64) be fractionated and obtains cut and remaining residue.

2. system according to claim 1, it is characterised in that

First fractionation unit (4) includes the first fractionating column (41) and after-fractionating tower (42) that are sequentially connected with；

First fractionating column (41) is for from the first cold low separator (23) and the first thermal low-pressure separators (24) liquid phase substance is fractionated, to obtain C5~C12 hydrocarbon-fractions, work as the first fractionating column (41) overhead fraction Evaporated for C10~C14 hydrocarbon-fractions of the line cut of the first fractionating column (41) side one, as the first fractionating column (41) side two wires C14~C18 the hydrocarbon-fractions and remaining residue for dividing；

The after-fractionating tower (42) for carrying out vacuum fractionation to the residue from first fractionating column (41), to obtain As C19~C21 hydrocarbon-fractions of the line cut of after-fractionating tower (42) side one, as after-fractionating tower (42) the side two wires C21~C25 hydrocarbon-fractions of cut, the C25~C40 hydrocarbon-fractions as the line cut of after-fractionating tower (42) side three, as institute State the C40+ hydrocarbon-fractions and remaining residue of the line cut of after-fractionating tower (42) side four.

3. system according to claim 2, it is characterised in that

The after-fractionating unit (7) includes the 3rd fractionating column (71) being sequentially connected with and the 4th fractionating column (72)；

3rd fractionating column (71) is for from the second cold low separator (63) and the second thermal low-pressure separators (64) liquid phase substance is fractionated, obtain C10~C14 hydrocarbon-fractions as the line cut of the 3rd fractionating column (71) side one, Evaporated as C14~C18 hydrocarbon-fractions of the 3rd fractionating column (71) side two wires cut, as the 3rd fractionating column (71) tower top C3~C11 the hydrocarbon-fractions and remaining residue for dividing；

4th fractionating column (72) is obtained as institute for being fractionated to the residue from the 3rd fractionating column (71) State C10~C15 hydrocarbon-fractions of the line cut of the 4th fractionating column (72) side one, as the 4th fractionating column (72) side two wires cut C16~C31 hydrocarbon-fractions and the C31+ hydrocarbon-fractions as the 4th fractionating column (72) tower bottom distillate.

4. system according to claim 3, it is characterised in that the system also includes naphtha separative element (8), is used for Overhead fraction from first fractionating column (41) is separated, to obtain solvent oil product after isolating light component.

5. the system according to claim 3 or 4, it is characterised in that the system also includes dewaxing unit (9), for point It is other that the line cut of side one and side two wires cut from first fractionating column (41) are separated, to remove isoparaffin, point Do not obtain as the C11-C13 normal paraffin mixtures and the C14- as Paraffin liquid heavy product of liquid paraffin,light product C18 normal paraffin mixtures.

6. system according to claim 5, it is characterised in that the system also includes hydro dewaxing reactor (10), uses Pour point depression is reacted to give in hydro dewaxing is carried out to the line cut of side one and side two wires cut from the after-fractionating tower (42) Product.

7. system according to claim 6, it is characterised in that the system also includes solvent deoiling unit (11), is used for De-oiling is carried out to obtain the C25-C40 hydrocarbon as solid paraffin product to the line cut of side three from the after-fractionating tower (42) Class mixture.

8. the system according to claim 6 or 7, it is characterised in that the system also includes white oil machining cell (13), uses In hydrofinishing and stripping is carried out to the side two wires cut from the 4th fractionating column (72), to obtain white oil product.

9. system according to claim 8, it is characterised in that the system also includes lubricating oil machining cell (14), uses Dewax with hydrofinishing to obtain lube base oil in the tower bottom distillate from the 4th fractionating column (72).

10. the system according to any one of claim 6-7 or 9, it is characterised in that the system also includes catalytic pyrolysis Unit (16), for the insoluble gas from the low temperature oil wash unit (15), from the light of the naphtha separative element (8) Component and the overhead fraction from the 3rd fractionating column (71) carry out catalytic pyrolysis.

11. systems according to claim 10, it is characterised in that the system also includes Fischer-Tropsch wax machining cell (12), For being processed to obtain Fischer-Tropsch wax to the line cut of side three from the after-fractionating tower (42).

The side that a kind of 12. systems using as any one of claim 1-11 are reprocessed to Fischer-Tropsch synthetic Method, it is characterised in that methods described includes：

Oil-gas Separation is carried out to the top product from F- T synthesis device (3) using Oil-gas Separation unit (17) and obtains gas gas-phase objects Material and the first Fischer-Tropsch oil；The gaseous phase materials from the Oil-gas Separation unit (17) are carried out using low temperature oil wash unit (15) low Warm oil wash is separated, and to isolate insoluble gas, obtains the second Fischer-Tropsch oil；

Using hydrofining reactor (1) to the first Fischer-Tropsch oil, the second Fischer-Tropsch oil and the Fischer-Tropsch from F- T synthesis device (3) Synthesis waxy stone carries out hydrofining reaction；

The refined products from the hydrofining reactor (1) are separated using the first separative element (2)；Wherein, profit Gas-liquid separation is carried out to the refined products from the hydrofining reactor (1) with the first high pressure hot separator (21)；Utilize First cold high pressure separator (22) carries out gas-liquid separation to the gaseous substance from first high pressure hot separator (21)；Utilize First thermal low-pressure separators (24), gas-liquid separation is carried out to the liquid phase substance from first high pressure hot separator (21)；Profit With the first cold low separator (23) to the liquid phase substance from first cold high pressure separator (22) and from described first The gaseous substance of thermal low-pressure separators (24) carries out gas-liquid separation；

Using the first fractionation unit (4) to from the first cold low separator (23) in first separative element (2) and The liquid phase substance of one thermal low-pressure separators (24) be fractionated and obtains cut and remaining residue；

Hydrocracking reaction is carried out using hydrocracking reactor (5) to the residue from first fractionation unit (4) to obtain To crackate；

The crackate from the hydrocracking reactor (5) is separated using the second separative element (6)；Wherein, profit Gas-liquid separation is carried out to the crackate from the hydrocracking reactor (5) with the second high pressure hot separator (61)；Utilize Second cold high pressure separator (62) carries out gas-liquid separation to the gaseous substance from second high pressure hot separator (61)；Utilize Second thermal low-pressure separators (64) carry out gas-liquid separation to the liquid phase substance from second high pressure hot separator (61)；Utilize Second cold low separator (63) is to the liquid phase substance from second cold high pressure separator (62) and from the described second heat The gaseous substance of low pressure separator (64) carries out gas-liquid separation；

Using after-fractionating unit (7) to from the second cold low separator (63) in second separative element (6) and The liquid phase substance of two thermal low-pressure separators (64) be fractionated and obtains cut and remaining residue.

13. methods according to claim 12, it is characterised in that first fractionation unit (4) is including what is be sequentially connected with First fractionating column (41) and after-fractionating tower (42)；The after-fractionating unit (7) includes the 3rd fractionating column that is sequentially connected with And the 4th fractionating column (72) (71)；Methods described includes：

Using the first fractionating column (41) to from the first cold low separator (23) and the first thermal low-pressure separators (24) Liquid phase substance is fractionated, and obtains C5~C12 hydrocarbon-fractions as the first fractionating column (41) overhead fraction, as described C10~C14 hydrocarbon-fractions of the line cut of one fractionating column (41) side one and the C14 of first fractionating column (41) side two wires cut~ C18 hydrocarbon-fractions and remaining residue；

Vacuum fractionation is carried out to the residue from first fractionating column (41) using after-fractionating tower (42), using obtain as C19~C21 hydrocarbon-fractions of the line cut of after-fractionating tower (42) side one, as after-fractionating tower (42) side two wires cut C21~C25 hydrocarbon-fractions, the C25~C40 hydrocarbon-fractions as the line cut of after-fractionating tower (42) side three, as described The C40+ hydrocarbon-fractions and remaining residue of the line cut of two fractionating columns (42) side four；

Using the 3rd fractionating column (71) to from the second cold low separator (63) and the second thermal low-pressure separators (64) Liquid phase substance is fractionated, and obtains C10~C14 hydrocarbon-fractions as the line cut of the 3rd fractionating column (71) side one, as institute State C14~C18 hydrocarbon-fractions, the C3 as the 3rd fractionating column (71) overhead fraction of the 3rd fractionating column (71) side two wires cut ~C11 hydrocarbon-fractions and remaining residue；

The residue from the 3rd fractionating column (71) is fractionated using the 4th fractionating column (72), is obtained as described C10~C15 hydrocarbon-fractions, the C16 as the 4th fractionating column (72) side two wires cut of the line cut of four fractionating columns (72) side one ~C31 hydrocarbon-fractions and the C31+ hydrocarbon-fractions as the 4th fractionating column (72) tower bottom distillate.

14. methods according to claim 13, it is characterised in that methods described includes：

The overhead fraction from first fractionating column (41) is separated using naphtha separative element (8), sub-argument goes out gently Solvent naphtha is obtained after component；The light component is C5-C8 hydrocarbon mixtures, and the solvent naphtha is C9-C12 hydrocarbon mixtures；

The line cut of side one and side two wires cut from first fractionating column (41) are divided respectively using dewaxing unit (9) From, to remove isoparaffin, respectively obtain as liquid paraffin,light product C11-C13 normal paraffin mixtures and as weight The C14-C18 normal paraffin mixtures of matter atoleine product；

The line cut of side one and side two wires cut from the after-fractionating tower (42) are entered using hydro dewaxing reactor (10) The reaction of row hydro dewaxing obtains pour point depression product；

De-oiling is carried out to the line cut of side three from the after-fractionating tower (42) using solvent deoiling unit (11) and obtains conduct The C25-C40 hydrocarbon mixtures of solid paraffin product；

Hydrofinishing and vapour are carried out to the side two wires cut from the 4th fractionating column (72) using white oil machining cell (13) Carry, to obtain white oil product；

The tower bottom distillate from the 4th fractionating column (72) is dewaxed and is hydrogenated with essence using lubricating oil machining cell (14) Lube base oil is obtained；

Separated to the insoluble gas from the low temperature oil wash unit (15), from the naphtha using catalyst cracking unit (16) The light component of unit (8) and the overhead fraction from the 3rd fractionating column (71) carry out catalytic pyrolysis, produce ethene, third Alkene and gasoline component；

Preferably, methods described also includes：

The expense of obtaining is processed to the line cut of side three from the after-fractionating tower (42) using Fischer-Tropsch wax machining cell (12) Support wax.

15. methods according to claim 14, it is characterised in that

The reaction condition of the hydrofining reactor (1) is：Temperature is 300~400 DEG C, and pressure is 4.5~9.5MPa, overall Product air speed is 1.0~4.0h^-1, entrance hydrogen to oil volume ratio is 300~700；

The reaction condition of the hydrocracking reactor (5) is：Temperature is 280~450 DEG C, and pressure is 6.0~13.0MPa, always 1.0~3.5h of volume space velocity^-1, entrance hydrogen to oil volume ratio 400~800；

The reaction condition of the hydro dewaxing reactor (10) is：Temperature is 280~450 DEG C, and pressure is 6.0~13.0MPa, always 1.0~4.0h of volume space velocity^-1, entrance hydrogen to oil volume ratio 400~800；

The operating condition of first high pressure hot separator (21) is：Temperature is 200~300 DEG C, and pressure is 3.5~9.0MPa；

The operating condition of first cold high pressure separator (22) is：Temperature is 40~80 DEG C, and pressure is 3.5~9.0MPa；

The operating condition of second high pressure hot separator (61) is：Temperature is 230~300 DEG C, and pressure is 6.5~13.0MPa；

The operating condition of second cold high pressure separator (62) is：Temperature is 40~80 DEG C, and pressure is 6.0~13.0MPa；

The operating condition of the first cold low separator (23) and the second cold low separator (63) is：Temperature be 40~ 80 DEG C, pressure is 1.0~3.0MPa；

The operating condition of first thermal low-pressure separators (24) and second thermal low-pressure separators (64) is：Temperature is 200 ~300 DEG C, pressure is 1.0~3.0MPa.