CN208166931U - The reprocessing system of F- T synthesis diesel oil distillate - Google Patents
The reprocessing system of F- T synthesis diesel oil distillate Download PDFInfo
- Publication number
- CN208166931U CN208166931U CN201820001501.5U CN201820001501U CN208166931U CN 208166931 U CN208166931 U CN 208166931U CN 201820001501 U CN201820001501 U CN 201820001501U CN 208166931 U CN208166931 U CN 208166931U
- Authority
- CN
- China
- Prior art keywords
- tower
- product
- desorbing agent
- surge tank
- extract
- 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.)
- Active
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model provides a kind of reprocessing system of F- T synthesis diesel oil distillate, which includes：Raw material surge tank receives C10~C14 aliphatic fraction in Fischer-Tropsch combined diesel oil technique；Raw material pre-rectifying tower carries out pre- rectifying to the material from raw material surge tank；Adsorbing tower with molecular sieve is adsorbed and is separated to raw material pre-rectifying tower materials at bottom of tower；Extract feed surge tank receives the tower top Extract of adsorbing tower with molecular sieve；Extract tower is fractionated the material of Extract feed surge tank；Raffinate feed surge tank receives the tower bottom raffinate of adsorbing tower with molecular sieve；Raffinate column is fractionated the material of raffinate feed surge tank.The reprocessing system can reprocess C10~C14 aliphatic fraction in F- T synthesis diesel oil technique, to obtain high value added product, improve the economic interests of F- T synthesis diesel oil technique, and realize the development in pluralism of its product.
Description
Technical field
The utility model belongs to the reprocessing system of coal chemical technology, especially F- T synthesis diesel oil distillate.
Background technique
As increasingly scarcity, the indirect coal liquefaction technology of petroleum resources are gradually widely paid close attention to by people in recent years.
The indirect coal liquefaction project gone into operation that is completed domestic at present has the safe 160,000 tons/year of coal oil projects of Inner Mongol gouy, Shanxi the Lushui River peace
160000 tons/year of coal oil projects, 1,000,000 tons/year of coal oil projects of Shaanxi future source of energy and Shenhua 4,000,000 tons/year of coal systems of peaceful coal
Oily project, in addition, there are also the safe 2,000,000 tons/year of coal oil projects of Inner Mongol gouy, Shanxi the Lushui River pacify 1,800,000 tons/year of coal oil projects,
4,000,000 tons/year of coal oil projects of Yulin Yan Kuang and the Guizhou 6,000,000 tons/year of coal oil projects of the rich energy etc. that change are being built or proposed item
Mesh.
However, the built indirect coal liquefaction Project Product in China is single at present, it is deep by international crude petroleum based on fuel diesel
The restriction in market, and production cost and refined products market competitiveness cannot temporarily contend with oil refining industry.
And since indirect coal liquefaction technology has raw material range wide, ultralow Nitrogen or sulfur-compounds impurity, low virtue in product
The advantage of hydrocarbon content and clean and environmental protection, therefore extensible Fischer-Tropsch synthetic chain, develop high value added product, such as environmentally friendly solvent
The products such as oil, atoleine and lightweight white oil, the competitiveness realized product diversification development, improve coal oil industry.But mesh
Preceding there is no the systems for being suitble to that Fischer-Tropsch synthetic is further processed, for example, in F- T synthesis diesel oil technique
C10~C14 aliphatic fraction is typically derived from F- T synthesis hydrofinishing unit and F- T synthesis Hydrocracking unit, is point
Hydrotreated product and isocrackate are not obtained by separating for several times.It is only to add hydrogen smart to from F- T synthesis at present
C10~C14 aliphatic fraction removing isoparaffin of unit processed obtains atoleine, and is not developed it to obtain fully
Obtain finer, more diversification, the higher product of added value.
Utility model content
The purpose of this utility model is to provide a kind of reprocessing system of F- T synthesis diesel oil distillate, the reprocessing systems
F- T synthesis diesel oil distillate can be reprocessed, to obtain high value added product, and realize the development in pluralism of product.
To realize the purpose of this utility model, the technical solutions adopted are as follows：
A kind of reprocessing system of F- T synthesis diesel oil distillate, including：
Raw material surge tank, for receiving C10~C14 aliphatic fraction in Fischer-Tropsch combined diesel oil technique and delaying to it
Punching；
Raw material pre-rectifying tower is obtained for carrying out pre- rectifying to the material from the raw material surge tank as overhead materials
The C9 of material-Alkane fraction and C10~C14 aliphatic fraction as materials at bottom of tower；
Adsorbing tower with molecular sieve, for using adsorbent to C10~C14 in the materials at bottom of tower of the raw material pre-rectifying tower just
Structure aliphatic fraction is adsorbed and is separated, and the C10~C14 N-alkanes that will be adsorbed in adsorbent using desorbing agent and irrigation
Hydrocarbon-fraction is desorbed out, obtains the mixing of C10~C14 n-alkane fraction, desorbing agent and irrigation as tower top Extract
Object, and as C10~C14 isoparaffin fraction of tower bottom raffinate, the mixture of desorbing agent and irrigation；
Extract feed surge tank, for receiving the tower top Extract from the adsorbing tower with molecular sieve；
Extract tower obtains producing as tower top for being fractionated the material from the Extract feed surge tank
The desorbing agent of object, C10~C14 as the desorbing agent of side line product and the mixture of irrigation, and as tower bottom product is just
Structure aliphatic fraction；
Raffinate feed surge tank, for receiving the tower bottom raffinate from the adsorbing tower with molecular sieve；
Raffinate column obtains producing as tower top for being fractionated the material from the raffinate feed surge tank
The desorbing agent of object, it is different as the desorbing agent of side line product and the mixture of irrigation, and C10~C14 as tower bottom product
Structure aliphatic fraction.
Preferably, the reprocessing system further includes：
Extract steams tower again, for distilling the tower bottom product from the Extract tower, obtains producing as tower top
The C13 of object-N-alkane fraction and C14 as tower bottom product+N-alkane fraction；
Isoparaffin knockout tower, for being separated to the tower bottom product from the raffinate column, as overhead product
C10~C14 isoparaffin solvent oil and C10~C14 isoparaffin solvent oil as tower bottom product.
Preferably, the reprocessing system further includes the circular regeneration for carrying out circular regeneration to desorbing agent and irrigation
Unit, the circular regeneration unit include：
Desorbing agent fractionating column is separated for the side line product to the Extract tower and the raffinate column, is obtained
Desorbing agent as overhead product and the irrigation as tower bottom product；
Desorbing agent surge tank, for receiving the tower of the Extract tower, the raffinate column and the desorbing agent fractionating column
Product is pushed up, to provide desorbing agent to the adsorbing tower with molecular sieve；
Irrigation surge tank, for receiving the tower bottom product of the desorbing agent fractionating column, with to the adsorbing tower with molecular sieve
Irrigation is provided.
Preferably, the circular regeneration unit further includes：
Desorbing agent drier, for by the tower top of the Extract tower, the raffinate column and the desorbing agent fractionating column
Product is dried before inputting the desorbing agent surge tank；
Filter, for carrying out the tower bottom product of the desorbing agent fractionating column before inputting the irrigation surge tank
Filtering.
Preferably, the adsorbing tower with molecular sieve is moving-bed adsorption knockout tower.
The beneficial effects of the utility model are：
The reprocessing system of the F- T synthesis diesel oil distillate of the utility model, can be to taking in F- T synthesis diesel oil technique
C10~C14 aliphatic fraction of support hydrogeneration processes refined unit and F- T synthesis Hydrocracking unit is reprocessed, thus
To high value added product, the economic interests of F- T synthesis diesel oil technique are improved, and realize the development in pluralism of its product.
Detailed description of the invention
Fig. 1 is the process of the reprocessing system of the F- T synthesis diesel oil distillate of the utility model in one embodiment
Figure.
Specific embodiment
The technical solution of the utility model and its effect are described further below by way of specific embodiment.Following reality
The mode of applying is merely to illustrate the content of the utility model, and utility model is not limited in following embodiments or embodiment.Using
The design of the utility model to the utility model carry out it is simple change all the requires of the utility model protect in the range of.
As shown in Figure 1, the reprocessing system of the F- T synthesis diesel oil distillate of the utility model, including raw material surge tank 1, take
Hold in the palm hydrogeneration processes refined unit 01, raw material pre-rectifying tower 2, adsorbing tower with molecular sieve 3, Extract feed surge tank 4, Extract tower 5,
Raffinate feed surge tank 6 and raffinate column 7.
Raw material surge tank 1, for receiving C10~C14 aliphatic fraction in Fischer-Tropsch combined diesel oil technique and delaying to it
Punching.
C10~C14 aliphatic fraction of input raw material surge tank 1 can come from the F- T synthesis in F- T synthesis diesel oil technique
Hydrofinishing unit 01 and/or F- T synthesis Hydrocracking unit 02；C10 from F- T synthesis hydrofinishing unit 01~
C14 aliphatic fraction can be the one line fraction of side of the first fractionating column in the patent of Patent No. 201621478266.8, including
C10~C14 n-alkane and C10~C14 isoparaffin based on C10~C14 n-alkane, and also contain a small amount of C9-Group
Point；C10~C14 aliphatic fraction from F- T synthesis Hydrocracking unit 02 is the patent of Patent No. 201621478266.8
The one line fraction of side of middle third fractionating column, including C10~C14 n-alkane and C10~C14 isoparaffin, it is different with C10~C14
Based on structure alkane, and also contain a small amount of C9-Component.
Wherein, the patent partial content of Patent No. 201621478266.8 is as follows：
A kind of system that the product for syrup state bed Fischer Tropsch synthesizer is reprocessed, including：
Oil-gas Separation unit obtains gas gas-phase objects for carrying out Oil-gas Separation to the top product from F- T synthesis device
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
Separation, to isolate insoluble gas, obtains 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
Support synthesis waxy stone, and hydrofining reaction is carried out to it and obtains refined products；
First separative unit, for being separated to the refined products from the hydrofining reactor；
First separative unit 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
The gaseous substance of one thermal low-pressure separators carries out gas-liquid separation；
First fractionation unit, for in first separative unit the first cold low separator and first heat it is low
The liquid phase substance of pressure separator is fractionated to obtain fraction and remaining residue；
Hydrocracking reactor is obtained for carrying out hydrocracking reaction to the residue from first fractionation unit
Crackate；
Second separative unit, for being separated to the crackate from the hydrocracking reactor；
Second separative unit 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
The gaseous substance of two thermal low-pressure separators carries out gas-liquid separation；
After-fractionating unit, for in second separative unit the second cold low separator and second heat it is low
The liquid phase substance of pressure separator is fractionated to obtain fraction and remaining residue.
Wherein, first fractionation unit includes sequentially connected first fractionating column and after-fractionating tower；Described first point
Tower is evaporated for being fractionated to the liquid phase substance from the first cold low separator and the first thermal low-pressure separators, is made
For C10~C14 hydrocarbon-fraction of first fractionating column side, one line fraction；
The after-fractionating unit includes sequentially connected third fractionating column and the 4th fractionating column；The third fractionating column is used
It is fractionated, is obtained as described in the liquid phase substance from the second cold low separator and the second thermal low-pressure separators
C10~C14 hydrocarbon-fraction of one line fraction of third fractionating column side.
And F- T synthesis hydrofinishing unit 01 is in the patent including Patent No. 201621478266.8 plus hydrogen essence
Reactor, the first separative unit and the first fractionation unit processed；As C10~C14 hydrocarbon-fraction of one line fraction of the first fractionating column side,
C10~C14 aliphatic fraction from F- T synthesis hydrofinishing unit 01 as in the utility model.F- T synthesis is hydrocracked
Unit 02 is hydrocracking reactor, the second separative unit and second in the patent including Patent No. 201621478266.8
Fractionation unit；As C10~C14 hydrocarbon-fraction of one line fraction of third fractionating column side, closed as in the utility model from Fischer-Tropsch
At C10~C14 aliphatic fraction of Hydrocracking unit 02.
Raw material pre-rectifying tower 2 is obtained for carrying out pre- rectifying to the material from the raw material surge tank 1 as tower top
The C9 of material-Alkane fraction (that is, first product lightweight white oil) and C10~C14 aliphatic fraction as materials at bottom of tower；It is preferred that institute
The operating condition for stating raw material pre-rectifying tower 2 is：80~150 DEG C of tower top temperature, 0.05~0.25MPa of tower top pressure, column bottom temperature
240~280 DEG C, 0.10~0.35MPa of tower bottom pressure；The operating condition of the further preferred raw material pre-rectifying tower 2 is：Tower top
100~140 DEG C of temperature, such as 120 DEG C, 0.10~0.20MPa of tower top pressure, for example, 0.12MPa, column bottom temperature 250~270
DEG C, such as 260 DEG C, 0.15~0.30MPa of tower bottom pressure, such as 0.2MPa.
Raw material pre-rectifying tower is rectifying column, and rectifying column is a kind of tower vapor-liquid contacting apparatus for carrying out rectifying, steam by
Tower bottom enters, the gas phase that evaporates and lower descending liquid carry out counter current contacting, and two are in contact, volatile (low boiling point) in lower descending liquid
Component is constantly shifted into gas phase, and difficult volatilization (higher boiling) component in gas phase constantly shifts in downward descending liquid, and gas phase is cured
Close to tower top, volatile components concentration is higher, and lower descending liquid is closer to tower bottom, difficult volatile component then more enrichment, to reach
The purpose separated to component.
Adsorbing tower with molecular sieve 3, for utilizing adsorbent to C10~C14 in the materials at bottom of tower of the raw material pre-rectifying tower 2
N-alkane fraction is adsorbed and is separated, and the positive structure of C10~C14 that will be adsorbed in adsorbent using desorbing agent and irrigation
Aliphatic fraction is desorbed out, obtains the mixed of C10~C14 n-alkane fraction as tower top Extract, desorbing agent and irrigation
Object is closed, and as C10~C14 isoparaffin fraction of tower bottom raffinate, the mixture of desorbing agent and irrigation；It is preferred that described
The operating condition of adsorbing tower with molecular sieve 3 is：150~200 DEG C of temperature, 1.5~3.5MPa of pressure；The further preferred molecular sieve
The operating condition of adsorption tower 3 is：160~185 DEG C of temperature, such as 175 DEG C, 2~3MPa of pressure, such as 2.73MPa.
Adsorbing tower with molecular sieve belongs to moving-bed adsorption separator, such as moving-bed adsorption knockout tower, be with
Molecular sieve is adsorbent, and the device for separating different material the selective absorption of material using adsorbent；After feed separation,
The material being adsorbed in adsorbent is desorbed out using desorbing agent.It is preferred that the adsorbing tower with molecular sieve 3 is Simulation moving bed
Absorptive separation column, preferably adsorbent used are 5A molecular sieve；The further preferred desorbing agent is pentane and isooctane
Mixture, wherein the mass ratio of pentane and isooctane is (1~4):1, preferably (2~3):1, such as 2.5:1；The flushing
Liquid is isooctane, to guarantee preferable dewaxing effect.Its process is as follows：The adsorbing tower with molecular sieve 3 utilizes adsorbent (such as 5A
Molecular sieve) selective absorption performance C10~C14 n-alkane and C10~C14 isoparaffin are separated, C10~C14
After n-alkane is adsorbed by adsorbent, using desorbing agent, (for example mass ratio is 2.5:1 pentane and the mixture of isooctane),
N-alkane is desorbed from the duct of adsorbent and is come out, adsorbent is rinsed with flushing liquor (such as isooctane), it will
Remaining desorbing agent develops.
Extract feed surge tank 4, for receiving the tower top Extract from the adsorbing tower with molecular sieve 3 and buffering.
Extract tower 5 is obtained for being fractionated to the material from the Extract feed surge tank 4 as tower top
The desorbing agent of product, as the desorbing agent of side line product and the mixture of irrigation, and C10~C14 as tower bottom product
N-alkane fraction；It is preferred that the operating condition of the Extract tower 5 is：80~120 DEG C of tower top temperature, tower top pressure 0.05~
0.50MPa, 210~270 DEG C of column bottom temperature, 0.10~0.30MPa of tower bottom pressure；The behaviour of the further preferred Extract tower 5
It is as condition：90~110 DEG C of tower top temperature, such as 104 DEG C, 0.10~0.35MPa of tower top pressure, for example, 0.12MPa, tower bottom temperature
230~260 DEG C of degree, such as 255 DEG C, 0.15~0.25MPa of tower bottom pressure, such as 0.19MPa.
Raffinate feed surge tank 6, for receiving the tower bottom raffinate from the adsorbing tower with molecular sieve 3 and buffering.
Raffinate column 7 is obtained for being fractionated to the material from the raffinate feed surge tank 6 as tower top
The desorbing agent of product, as the desorbing agent of side line product and the mixture of irrigation, and C10~C14 as tower bottom product
Isoparaffin fraction；It is preferred that the operating condition of the raffinate column 7 is：60~100 DEG C of tower top temperature, tower top pressure 0.05~
0.30MPa, 240~285 DEG C of column bottom temperature, 0.10~0.40MPa of tower bottom pressure；The behaviour of the further preferred raffinate column 7
It is as condition：70~90 DEG C of tower top temperature, such as 80 DEG C, 0.10~0.24MPa of tower top pressure such as 0.14MPa, column bottom temperature
250~275 DEG C, such as 265 DEG C, 0.15~0.30MPa of tower bottom pressure, such as 0.20MPa.
Extract tower 5 and raffinate column 7 are fractionating column.
The reprocessing system of the F- T synthesis diesel oil distillate of the utility model can close the Fischer-Tropsch in fischer-tropsch synthesis process
It is reprocessed at C10~C14 aliphatic fraction of hydrofinishing unit, to obtain high value added product, improves F- T synthesis
The economic interests of technique, and realize the development in pluralism of its product.Wherein, operating condition and preferred operations condition in each device
Setting, facilitates the abundant progress of relevant operation in each device, in order to reprocess C10~C14 aliphatic fraction to obtain difference
High value added product.
The reprocessing system of the F- T synthesis diesel oil distillate of the utility model, can be simultaneously to taking in fischer-tropsch synthesis process
C10~C14 aliphatic fraction of support hydrogeneration processes refined unit and F- T synthesis Hydrocracking unit is reprocessed, thus
To high value added product, the economic interests of fischer-tropsch synthesis process are improved, and realize the development in pluralism of its product.
In one embodiment, the reprocessing system further includes：
Extract steams tower 8 again, for distilling to the tower bottom product from the Extract tower 5, obtains as tower top
The C13 of product-N-alkane fraction (that is, second product light liquid paraffin) and the C14 as tower bottom product+N-alkane evaporates
Part (that is, third product Paraffin liquid heavy)；It is preferred that the operating condition that the Extract steams tower 8 again is：Tower top temperature 200~
250 DEG C, 0.001~0.10MPa of tower top pressure, 260~320 DEG C of column bottom temperature, 0.05~0.30MPa of tower bottom pressure；Further
It is preferred that the operating condition that the Extract steams tower 8 again is：220~240 DEG C of tower top temperature, such as 230 DEG C, tower top pressure 0.01
~0.08MPa, such as 0.03MPa, 270~300 DEG C of column bottom temperature, such as 290 DEG C, 0.08~0.20MPa of tower bottom pressure, such as
0.10MPa；
Isoparaffin knockout tower 9 is produced for separating to the tower bottom product from the raffinate column 7 as tower top
(that is, the 4th product, percentage shared by the 4th lower component of product mid-boiling point compares C10~C14 isoparaffin solvent oil of object
Greatly) and C10~C14 isoparaffin solvent oil as tower bottom product is (that is, the 5th product, the 5th higher group of product mid-boiling point
Percentage shared by point is bigger)；It is preferred that the column bottom temperature of the isoparaffin knockout tower 9 is 230~280 DEG C；It is preferred that described different
The operating condition of structure alkane separation tower 9 is：180~230 DEG C of tower top temperature, 0.05~0.25 MPa of tower top pressure, column bottom temperature
230~280 DEG C, 0.05~0.25MPa of tower bottom pressure；The operating condition of the further preferred isoparaffin knockout tower 9 is：Tower
190~210 DEG C of temperature of top, such as 195 DEG C, 0.08~0.15MPa of tower top pressure, such as 0.10MPa, column bottom temperature 240~260
DEG C, such as 250 DEG C, 0.09~0.20MPa of tower bottom pressure, such as 0.12MPa.
Extract steams tower 8 again and isoparaffin knockout tower 9 is the device that feed separation is realized by distillation.
It is reprocessed by the tower bottom product of tower bottom product and raffinate column 7 to Extract tower 5, is more had respectively
High value-added product is conducive to increase economic efficiency.Wherein, in each device operating condition and preferred operations condition setting,
Facilitate the abundant progress of relevant operation in each device, in order to further obtain different high value added products.
In one embodiment, the reprocessing system further includes for carrying out circular regeneration to desorbing agent and irrigation
Circular regeneration unit, the circular regeneration unit includes：
Desorbing agent fractionating column 10 is separated for the side line product to the Extract tower 5 and the raffinate column 7,
Obtain the desorbing agent as overhead product and the irrigation as tower bottom product；It is preferred that the operation item of the desorbing agent fractionating column 10
Part is：75~110 DEG C of tower top temperature, 0.10~0.25MPa of tower top pressure, 120~165 DEG C of column bottom temperature, tower bottom pressure 0.10
~0.40MPa；The operating condition of the further preferred desorbing agent fractionating column 10 is：85~100 DEG C of tower top temperature, such as 95
DEG C, 0.15~0.20MPa of tower top pressure, for example, 0.18MPa, 130~150 DEG C of column bottom temperature, such as 140 DEG C, tower bottom pressure
0.15~0.30MPa, such as 0.20MPa；Desorbing agent fractionating column is to be carried out the mixture of desorbing agent and irrigation by fractionation
Isolated device, to realize the circular regeneration to desorbing agent and irrigation；
Desorbing agent surge tank 11, for receiving the Extract tower 5, the raffinate column 7 and the desorbing agent fractionating column
10 overhead product, to provide desorbing agent to the adsorbing tower with molecular sieve 3；
Irrigation surge tank 12, for receiving the tower bottom product of the desorbing agent fractionating column 10, to be inhaled to the molecular sieve
Attached tower 3 provides irrigation.
The setting of circular regeneration unit facilitates circular regeneration desorbing agent and irrigation, to save desorbing agent and irrigation,
Reduce waste.
In one embodiment, the circular regeneration unit further includes：
Desorbing agent drier 13 is used for the Extract tower 5, the raffinate column 7 and the desorbing agent fractionating column 10
Overhead product be dried before inputting the desorbing agent surge tank 11；
Filter 14, for by the tower bottom product of the desorbing agent fractionating column 10 input the irrigation surge tank 12 it
Before be filtered.
The operational process of the reprocessing system of the F- T synthesis diesel oil distillate of the utility model is as shown in Figure 1：
Raw material surge tank 1 is received from F- T synthesis hydrofinishing unit 01 and F- T synthesis Hydrocracking unit 02
C10~C14 aliphatic fraction is as raw material；Then pre- essence is carried out in raw material C10~C14 aliphatic fraction input raw material pre-rectifying tower 2
It evaporates, obtains the C9 as tower top material-Alkane fraction (that is, first product lightweight white oil) and C10~C14 as materials at bottom of tower
Aliphatic fraction (that is, third product Paraffin liquid heavy)；The materials at bottom of tower of raw material pre-rectifying tower 2 input adsorbing tower with molecular sieve 3 into
Row absorption and separation, obtain the mixture of C10~C14 n-alkane fraction as tower top Extract, desorbing agent and irrigation,
And as C10~C14 isoparaffin fraction of tower bottom raffinate, the mixture of desorbing agent and irrigation；Adsorbing tower with molecular sieve 3
Tower top Extract input Extract feed surge tank 4 in and buffer；The material of Extract feed surge tank 4 inputs Extract tower
It is fractionated in 5, obtains the desorbing agent as overhead product, as the desorbing agent of side line product and the mixture of irrigation, with
And C10~C14 n-alkane fraction as tower bottom product；The tower bottom raffinate of the adsorbing tower with molecular sieve 3 inputs raffinate
In feed surge tank 6 and buffer；It is fractionated in the material input raffinate column 7 of raffinate feed surge tank 6, obtains conduct
The desorbing agent of overhead product, as the desorbing agent of side line product and the mixture of irrigation, and as tower bottom product C10~
C14 isoparaffin fraction；The tower bottom product input Extract of the Extract tower 5 steams again to be distilled in tower 8, is obtained as tower
Push up the C13 of product-N-alkane fraction (that is, second product light liquid paraffin) and the C14 as tower bottom product+N-alkane
Fraction；The raffinate column 7 tower bottom product input isoparaffin knockout tower 9 in separated, as overhead product C10~
C14 isoparaffin solvent oil (that is, the 4th product, percentage shared by the 4th lower component of product mid-boiling point is bigger) and make
For C10~C14 isoparaffin solvent oil (that is, the 5th product, shared by the 5th higher component of product mid-boiling point of tower bottom product
Percentage is bigger)；Divided in the side line product of the Extract tower 5 and the raffinate column 7 input desorbing agent fractionating column 10
From obtaining the desorbing agent as overhead product and the irrigation as tower bottom product；The Extract tower 5, the raffinate column 7
It is inputted in the desorbing agent surge tank 11 after desorbing agent drier 13 is dry with the overhead product of the desorbing agent fractionating column 10
Storage, to provide desorbing agent to the adsorbing tower with molecular sieve 3；The tower bottom product of the desorbing agent fractionating column 10 is through 14 mistake of filter
It inputs in the irrigation surge tank 12 and stores after filter, to provide irrigation to the adsorbing tower with molecular sieve 3.
The reprocessing system of the F- T synthesis diesel oil distillate of the utility model, has the advantages that：
(1) it is evaporated by C10~C14 alkane to F- T synthesis hydrofinishing unit and F- T synthesis Hydrocracking unit
Divide and is reprocessed, available lightweight white oil (the first product), light liquid paraffin (the second product), Paraffin liquid heavy
C10~C14 the isoparaffin solvent oil (the 4th product) and C10~C14 isoparaffin of tower bottom of (third product), tower top are molten
Five kinds of high value-added products such as agent oil (the 5th product), realize the diversification of Fischer-Tropsch synthetic, improve F- T synthesis
The added value of product extends Fischer-Tropsch synthetic chain, improves the economic benefit of F- T synthesis diesel oil technique.
(2) since the diesel oil distillate that F- T synthesis hydrofinishing unit and F- T synthesis hydrogenation Cracking Unit generate has
There is the advantages of low-sulfur, low nitrogen, low aromatic hydrocarbons, low impurity, working process is simple, and processing cost is lower than petroleum base processing unit (plant).
(3) in the reprocessing system of the F- T synthesis diesel oil distillate of the utility model, each device is petrochemical industry routine
Device, degree domestic is high, and cost of investment is low.
(4) the reprocessing system of the F- T synthesis diesel oil distillate of the utility model, can be to the desorbing agent and flushing used
Agent is recycled, is regenerated, and is recycled.
Embodiment
Add hydrogen to from F- T synthesis hydrofinishing unit 01 and F- T synthesis using the reprocessing system of the utility model
C10~C14 aliphatic fraction of Cracking Unit 02 is reprocessed, and the first product, the second product, third product, are respectively obtained
Four products, the 5th product.Wherein,
Adsorbing tower with molecular sieve 3 is moving-bed adsorption knockout tower, and adsorbent used is 5A molecular sieve；The desorbing agent
For the mixture of pentane and isooctane, and the mass ratio of pentane and isooctane is 2.5:1；The flushing liquor is isooctane；
Operating condition is：175 DEG C of temperature, pressure 2.73MPa；
The operating condition for stating raw material pre-rectifying tower 2 is：120 DEG C of tower top temperature, 0.12 MPa of tower top pressure, column bottom temperature
260 DEG C, tower bottom pressure 0.2MPa；
The operating condition of the Extract tower 5 is：104 DEG C of tower top temperature, tower top pressure 0.12MPa, column bottom temperature 255
DEG C, tower bottom pressure 0.19MPa；
The operating condition of the raffinate column 7 is：80 DEG C of tower top temperature, tower top pressure 0.14MPa, 265 DEG C of column bottom temperature,
Tower bottom pressure 0.20Mpa；
The operating condition that the Extract steams tower 8 again is：230 DEG C of tower top temperature, tower top pressure 0.03MPa, column bottom temperature
290 DEG C, tower bottom pressure 0.10MPa；
The operating condition of the isoparaffin knockout tower 9 is：195 DEG C of tower top temperature, tower top pressure 0.10MPa, tower bottom temperature
240 DEG C of degree, tower bottom pressure 0.12MPa；
The operating condition of the desorbing agent fractionating column 10 is：95 DEG C of tower top temperature, tower top pressure 0.18MPa, column bottom temperature
140 DEG C, tower bottom pressure 0.20MPa.
Obtained first product, the second product, third product, the 4th product and the 5th product testing result respectively such as
Shown in table 1-5.
The testing result of 1 first product of table
| Project | Testing result |
| Initial boiling point/DEG C | 168 |
| The end point of distillation/DEG C | 259 |
| Arene content (mass fraction)/% | ≤0.5 |
| Density (20 DEG C)/(kg/m3) | 750~775 |
| Sulfur content (mass fraction)/ppm | ≤0.4 |
| Distribution of normal alkanes (mass fraction)/% | 85~90 |
| Bromine index (mgBr/100mg) | ≤0.5 |
| Mechanical admixture and moisture | Nothing |
The testing result of 2 second product of table
| Project | Testing result |
| Sai Shi color | ≥30 |
| Bromine index (mgBr/100mg) | ≤15 |
| Aromatic hydrocarbons contains (mass fraction)/% | ≤0.1 |
| Sulfur content (mass fraction)/ppm | ≤1 |
| Total n-alkane (mass fraction)/% | ≥98.5 |
| Distribution of normal alkanes (mass fraction)/%≤C9 | ≤0.5 |
| Distribution of normal alkanes (mass fraction)/% >=C14 | ≤0.5 |
The testing result of 3 third product of table
| Project | Testing result |
| Sai Shi color | ≥30 |
| Bromine index (mgBr/100mg) | ≤15 |
| Aromatic hydrocarbons contains (mass fraction)/% | ≤0.1 |
| Sulfur content (mass fraction)/ppm | ≤1 |
| Total n-alkane (mass fraction)/% | ≥98.5 |
| Distribution of normal alkanes (mass fraction)/%≤C13 | ≤5 |
The testing result of the 4th product of table 4
| Project | Testing result |
| Initial boiling point/DEG C | 184 |
| The end point of distillation/DEG C | 265 |
| Sai Shi color | ≥30 |
| Aromatic hydrocarbons contains (mass fraction) % | ≤0.1 |
| Sulfur content (mass fraction) ppm | ≤1 |
| Bromine index mgBr/100mg | ≤50 |
| Flash-point (silent)/DEG C | ≥60 |
| Dynamic viscosity (40 DEG C)/(mm2/s) | 1.360 |
The Testing index of the 5th product of table 5
| Project | Testing result |
| Initial boiling point/DEG C | 232 |
| The end point of distillation/DEG C | 265 |
| Sai Shi color | ≥30 |
| Aromatic hydrocarbons contains (mass fraction) % | ≤0.1 |
| Sulfur content (mass fraction) ppm | ≤1 |
| Bromine index mgBr/100mg | ≤50 |
| Flash-point (silent)/DEG C | ≥80 |
| Dynamic viscosity (40 DEG C)/(mm2/s) | 1.958 |
Claims (5)
1. a kind of reprocessing system of F- T synthesis diesel oil distillate, which is characterized in that including：
Raw material surge tank (1), for receiving C10~C14 aliphatic fraction in Fischer-Tropsch combined diesel oil technique and being buffered to it；
Raw material pre-rectifying tower (2) is obtained for carrying out pre- rectifying to the material from the raw material surge tank (1) as tower top
The C9 of material-Alkane fraction and C10~C14 aliphatic fraction as materials at bottom of tower；
Adsorbing tower with molecular sieve (3), for utilizing adsorbent to C10~C14 in the materials at bottom of tower of the raw material pre-rectifying tower (2)
N-alkane fraction is adsorbed and is separated, and the positive structure of C10~C14 that will be adsorbed in adsorbent using desorbing agent and irrigation
Aliphatic fraction is desorbed out, obtains the mixed of C10~C14 n-alkane fraction as tower top Extract, desorbing agent and irrigation
Object is closed, and as C10~C14 isoparaffin fraction of tower bottom raffinate, the mixture of desorbing agent and irrigation；
Extract feed surge tank (4), for receiving the tower top Extract from the adsorbing tower with molecular sieve (3)；
Extract tower (5) is obtained for being fractionated to the material from the Extract feed surge tank (4) as tower top
The desorbing agent of product, as the desorbing agent of side line product and the mixture of irrigation, and C10~C14 as tower bottom product
N-alkane fraction；
Raffinate feed surge tank (6), for receiving the tower bottom raffinate from the adsorbing tower with molecular sieve (3)；
Raffinate column (7) is obtained for being fractionated to the material from the raffinate feed surge tank (6) as tower top
The desorbing agent of product, as the desorbing agent of side line product and the mixture of irrigation, and C10~C14 as tower bottom product
Isoparaffin fraction.
2. reprocessing system according to claim 1, which is characterized in that the reprocessing system further includes：
Extract steams tower (8) again, for distilling to the tower bottom product from the Extract tower (5), obtains as tower top
The C13 of product-N-alkane fraction and C14 as tower bottom product+N-alkane fraction；
Isoparaffin knockout tower (9) is obtained for separating to the tower bottom product from the raffinate column (7) as tower
Push up C10~C14 isoparaffin solvent oil of product and C10~C14 isoparaffin solvent oil as tower bottom product.
3. reprocessing system according to claim 1 or 2, which is characterized in that the reprocessing system further include for pair
Desorbing agent and irrigation carry out the circular regeneration unit of circular regeneration, and the circular regeneration unit includes：
Desorbing agent fractionating column (10), for dividing the side line product of the Extract tower (5) and the raffinate column (7)
From obtaining the desorbing agent as overhead product and the irrigation as tower bottom product；
Desorbing agent surge tank (11), for receiving the Extract tower (5), the raffinate column (7) and desorbing agent fractionation
The overhead product of tower (10), to provide desorbing agent to the adsorbing tower with molecular sieve (3)；
Irrigation surge tank (12), for receiving the tower bottom product of the desorbing agent fractionating column (10), to be inhaled to the molecular sieve
Attached tower (3) provides irrigation.
4. reprocessing system according to claim 3, which is characterized in that the circular regeneration unit further includes：
Desorbing agent drier (13) is used for the Extract tower (5), the raffinate column (7) and the desorbing agent fractionating column
(10) overhead product is dried before inputting the desorbing agent surge tank (11)；
Filter (14), for the tower bottom product of the desorbing agent fractionating column (10) to be inputted the irrigation surge tank (12)
It is filtered before.
5. reprocessing system according to claim 1, which is characterized in that the adsorbing tower with molecular sieve (3) is simulation movement
Bed absorptive separation column.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820001501.5U CN208166931U (en) | 2018-01-02 | 2018-01-02 | The reprocessing system of F- T synthesis diesel oil distillate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820001501.5U CN208166931U (en) | 2018-01-02 | 2018-01-02 | The reprocessing system of F- T synthesis diesel oil distillate |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN208166931U true CN208166931U (en) | 2018-11-30 |
Family
ID=64387176
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201820001501.5U Active CN208166931U (en) | 2018-01-02 | 2018-01-02 | The reprocessing system of F- T synthesis diesel oil distillate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN208166931U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108102694A (en) * | 2018-01-02 | 2018-06-01 | 神华集团有限责任公司 | The reprocessing system and method for F- T synthesis diesel oil distillate |
| CN111471484A (en) * | 2019-01-23 | 2020-07-31 | 内蒙古伊泰宁能精细化工有限公司 | Process for preparing isoparaffin composition |
| WO2021047040A1 (en) * | 2019-09-10 | 2021-03-18 | 南京延长反应技术研究院有限公司 | System and process for enhancing coal indirect liquefaction on basis of micro-interface |
-
2018
- 2018-01-02 CN CN201820001501.5U patent/CN208166931U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108102694A (en) * | 2018-01-02 | 2018-06-01 | 神华集团有限责任公司 | The reprocessing system and method for F- T synthesis diesel oil distillate |
| CN111471484A (en) * | 2019-01-23 | 2020-07-31 | 内蒙古伊泰宁能精细化工有限公司 | Process for preparing isoparaffin composition |
| WO2021047040A1 (en) * | 2019-09-10 | 2021-03-18 | 南京延长反应技术研究院有限公司 | System and process for enhancing coal indirect liquefaction on basis of micro-interface |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108102694A (en) | The reprocessing system and method for F- T synthesis diesel oil distillate | |
| CN208166931U (en) | The reprocessing system of F- T synthesis diesel oil distillate | |
| RU2662814C2 (en) | Improved hydrogen extraction | |
| Li et al. | Process optimization of heat-integrated extractive dividing-wall columns for energy-saving separation of CO2 and hydrocarbons | |
| CN103146426B (en) | Method of converting fischer-tropsch synthesis products into naphtha, diesel and liquefied petroleum gas | |
| TWI651407B (en) | Process for the hydrotreatent of a gas oil in a series of reactors with recycling of hydrogen | |
| Li et al. | Absorption–hydration hybrid method for ethylene recovery from refinery dry gas: Simulation and evaluation | |
| CN106699501A (en) | Method for producing elemental N-alkanes | |
| CN102146298A (en) | Hydrocarbon hydrogenation conversion process combined method | |
| CN105733647A (en) | Method for recovering liquefied petroleum gas from Fischer-Tropsch synthesis tail gas | |
| CN104178197B (en) | The method that coal tar and coal coreaction prepare liquid fuel | |
| US2608270A (en) | Method of separating light hydrocarbon from high-pressure gas | |
| CN109355100B (en) | Coal tar processing and coal co-refining combined process | |
| CN105623703A (en) | Thermal high-pressure dissociating gas dust removal method for three-phase product of hydrocarbon material hydrogenation reaction | |
| CN206512159U (en) | System for being reprocessed to Fischer-Tropsch synthetic | |
| CN113122314B (en) | Gas-liquid separation process for hydrogenation reaction product | |
| CN113789190A (en) | Multi-stage countercurrent-cross-flow combined extraction device and method for catalyzing diesel polycyclic aromatic hydrocarbon by using ionic liquid | |
| CN113817496A (en) | Crude oil or heavy oil pretreatment method | |
| CN103789025B (en) | Heavy benzene hydro-upgrading method | |
| CN101823931B (en) | Method for deeply processing C5 raffinate raw material separated from diolefin | |
| US9809761B2 (en) | Hydrocarbon processing apparatuses and methods of refining hydrocarbons with absorptive recovery of C3+ hydrocarbons | |
| RU2793029C1 (en) | Method for producing diesel fuel with low-temperature properties | |
| CN106554824B (en) | A kind of processing method of Fischer-Tropsch synthetic | |
| CN203540300U (en) | Biabsorption and bidesorption hydrogen and light hydrocarbon comprehensive recovering system | |
| CN112011363B (en) | Method for producing high-quality mesophase pitch raw material by circularly extracting heavy oil products |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |