CN108102694A - The reprocessing system and method for F- T synthesis diesel oil distillate - Google Patents
The reprocessing system and method for F- T synthesis diesel oil distillate Download PDFInfo
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- CN108102694A CN108102694A CN201810001051.4A CN201810001051A CN108102694A CN 108102694 A CN108102694 A CN 108102694A CN 201810001051 A CN201810001051 A CN 201810001051A CN 108102694 A CN108102694 A CN 108102694A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
- C10G53/08—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one sorption step
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1022—Fischer-Tropsch products
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
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- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides a kind of reprocessing system and method for F- T synthesis diesel oil distillate, which includes：Raw material surge tank receives C10~C14 aliphatic fractions 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 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 bottom of towe raffinate of adsorbing tower with molecular sieve；Raffinate column is fractionated the material of raffinate feed surge tank.The reprocessing system and method can reprocess C10~C14 aliphatic fractions in F- T synthesis diesel oil technique, so as 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 invention belongs to the reprocessing system and methods of coal chemical technology, particularly F- T synthesis diesel oil distillate.
Background technology
Gradually people is subject to widely to pay close attention in recent years with increasingly scarcity, the indirect coal liquefaction technology of petroleum resources.
The indirect coal liquefaction project gone into operation that is completed domestic at present has the safe 160,000 tons/year of coal liquifaction projects of Inner Mongol gouy, Shanxi the Lushui River peace
160000 tons/year of coal liquifaction projects, 1,000,000 tons/year of coal liquifaction projects of Shaanxi future source of energy and Shenhua 4,000,000 tons/year of coal systems of peaceful coal
Oily project, in addition, also the safe 2,000,000 tons/year of coal liquifaction projects of Inner Mongol gouy, Shanxi the Lushui River pacify 1,800,000 tons/year of coal liquifaction projects,
Rich 6,000,000 tons/year of coal liquifaction projects of the energy of 4,000,000 tons/year of coal liquifaction projects of Yulin Yan Kuang and Guizhou Chongqing etc. are being built or proposed item
Mesh.
However, current China is built, indirect coal liquefaction Project Product is single, and based on fuel diesel, depth is by international crude petroleum
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 is wide, ultralow Nitrogen or sulfur-compounds impurity, low virtue in product
The advantage of hydrocarbon content and clean environment firendly, 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 realize product diversification development, the competitiveness for improving coal liquifaction industry.But mesh
The preceding system for not being suitble to Fischer-Tropsch synthetic is further processed, for example, in F- T synthesis diesel oil technique
C10~C14 aliphatic fractions are typically derived from F- T synthesis hydrofinishing unit and F- T synthesis Hydrocracking unit, are point
Hydrotreated product and isocrackate are not obtained by separating for several times.Only it is to deriving from F- T synthesis hydrogenation essence at present
C10~C14 aliphatic fractions removing isoparaffin of unit processed obtains atoleine, and it is not developed fully to obtain
Obtain finer, more diversification, the higher product of added value.
The content of the invention
It is an object of the invention to provide a kind of reprocessing system and method for F- T synthesis diesel oil distillate, the reprocessing systems
System and method can reprocess F- T synthesis diesel oil distillate, so as to obtain high value added product, and realize the diversification of product
Development.
First purpose to realize the present invention, the technical solution of use 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 fractions in Fischer-Tropsch combined diesel oil technique and delaying to it
Punching；
Raw material pre-rectifying tower for carrying out pre- rectifying to the material from the raw material surge tank, is obtained as overhead materials
The C9 of material-Alkane fraction and C10~C14 aliphatic fractions 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 separated, and the C10~C14 N-alkanes that will be adsorbed in using desorbing agent and irrigation in adsorbent
Hydrocarbon-fraction is desorbed out, obtains the mixing of C10~C14 n-alkanes fraction as tower top Extract, desorbing agent and irrigation
The mixture of object and C10~C14 isoparaffins fraction as bottom of towe raffinate, desorbing agent and irrigation；
Extract feed surge tank, for receiving the tower top Extract from the adsorbing tower with molecular sieve；
Extract tower for being fractionated the material from the Extract feed surge tank, obtains producing as tower top
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 bottom of towe raffinate from the adsorbing tower with molecular sieve；
Raffinate column for being fractionated the material from the raffinate feed surge tank, obtains producing as tower top
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 are different
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 the C14 as tower bottom product+N-alkane fraction；
Isoparaffin knockout tower, the column bottom temperature of the isoparaffin knockout tower is 230~280 DEG C, the isoparaffin
Knockout tower is for separating the tower bottom product from the raffinate column, C10~C14 isoparaffins as overhead product
Solvent naphtha and C10~C14 isoparaffin solvent oils as tower bottom product.
Preferably, the reprocessing system further includes to carry out desorbing agent and irrigation the circular regeneration of circular regeneration
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, 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 the desorbing agent surge tank is inputted；
Filter, for the tower bottom product of the desorbing agent fractionating column to be carried out before the irrigation surge tank is inputted
Filtering.
Preferably, the adsorbing tower with molecular sieve is moving-bed adsorption knockout tower, and adsorbent used is 5A molecular sieves.
Preferably, the desorbing agent is the mixture of pentane and isooctane, wherein, the mass ratio of pentane and isooctane
For (1~4):1, preferably (2~3):1；The flushing liquor is isooctane.
Preferably, the operating condition of the raw material pre-rectifying tower is：80~150 DEG C of tower top temperature, tower top pressure 0.05~
0.25MPa, 240~280 DEG C of column bottom temperature, 0.10~0.35MPa of tower bottom pressure；
The operating condition of the adsorbing tower with molecular sieve is：150~200 DEG C of temperature, 1.5~3.5MPa of pressure；
The operating condition of the Extract tower is：80~120 DEG C, 0.05~0.50MPa of tower top pressure of tower top temperature, bottom of towe
210~270 DEG C of temperature, 0.10~0.30MPa of tower bottom pressure；
The operating condition of the raffinate column is：60~100 DEG C, 0.05~0.30MPa of tower top pressure of tower top temperature, bottom of towe
240~285 DEG C of temperature, 0.10~0.40MPa of tower bottom pressure.
Preferably, the operating condition that the Extract steams tower again is：200~250 DEG C of tower top temperature, tower top pressure 0.001
~0.10MPa, 260~320 DEG C of column bottom temperature, 0.05~0.30MPa of tower bottom pressure；
The operating condition of the isoparaffin knockout tower is：180~230 DEG C of tower top temperature, tower top pressure 0.05~
0.25MPa, 230~280 DEG C of column bottom temperature, 0.05~0.25MPa of tower bottom pressure.
Preferably, the operating condition of the desorbing agent fractionating column is：75~110 DEG C of tower top temperature, tower top pressure 0.10~
0.25MPa, 120~165 DEG C of column bottom temperature, 0.10~0.40MPa of tower bottom pressure.
Another purpose to realize the present invention utilizes above-mentioned reprocessing system to F- T synthesis the present invention also provides a kind of
The method that C10~C14 aliphatic fractions in technique are reprocessed.
The beneficial effects of the present invention are：
The reprocessing system and method for the F- T synthesis diesel oil distillate of the present invention, can be in F- T synthesis diesel oil technique
C10~C14 aliphatic fractions of F- T synthesis hydrofinishing unit and F- T synthesis Hydrocracking unit are reprocessed, so as to
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.
Description of the drawings
Fig. 1 is the flow chart of the reprocessing system of the F- T synthesis diesel oil distillate of the present invention in one embodiment.
Specific embodiment
Technical scheme and its effect are described further below by way of specific embodiment.Following embodiment party
Formula is merely to illustrate present disclosure, and invention is not limited in following embodiments or embodiment.Using the design of the present invention
Simply change to what the present invention carried out all in the scope of protection of present invention.
As shown in Figure 1, the reprocessing system of the F- T synthesis diesel oil distillate of the present invention, is closed including raw material surge tank 1, Fischer-Tropsch
Into hydrofinishing unit 01, raw material pre-rectifying tower 2, adsorbing tower with molecular sieve 3, Extract feed surge tank 4, Extract tower 5, raffinate
Liquid feed surge tank 6 and raffinate column 7.
Raw material surge tank 1, for receiving C10~C14 aliphatic fractions in Fischer-Tropsch combined diesel oil technique and delaying to it
Punching.
C10~C14 aliphatic fractions 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 fractions can be Patent No. 201621478266.8 patent in the first fractionating column one line fraction of side, including C10
~C14 n-alkanes and C10~C14 isoparaffins based on C10~C14 n-alkanes, and also contain a small amount of C9-Component；Come
C10~C14 aliphatic fractions from Fischer-Tropsch hydrogeneration processes Cracking Unit 02 be Patent No. 201621478266.8 patent in
The one line fraction of side of three fractionating columns, including C10~C14 n-alkanes and C10~C14 isoparaffins, with C10~C14 isomeric alkanes
Based on hydrocarbon, 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 for being reprocessed to the product of syrup state bed Fischer Tropsch synthesizer, 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
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 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 to the first cold low separator in first separative element and the first heat
The liquid phase substance of pressure separator is fractionated to obtain fraction 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 to the second cold low separator in second separative element and the second heat
The liquid phase substance of pressure separator is fractionated to obtain fraction and remaining residue.
Wherein, first fractionation unit includes the first fractionating column connected in sequence 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-fractions of the one line fraction of the first fractionating column side；
The after-fractionating unit includes the 3rd fractionating column connected in sequence and the 4th fractionating column；3rd 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-fractions of 3rd fractionating column side, one line fraction.
And F- T synthesis hydrofinishing unit 01 is the hydrogenation essence in the patent for include Patent No. 201621478266.8
Reactor processed, the first separative element and the first fractionation unit；As C10~C14 hydrocarbon-fractions of one line fraction of the first fractionating column side,
As C10~C14 aliphatic fractions from F- T synthesis hydrofinishing unit 01 in the present invention.F- T synthesis Hydrocracking unit
02 includes hydrocracking reactor, the second separative element and the after-fractionating in the patent of Patent No. 201621478266.8
Unit；It is to be split in the present invention from F- T synthesis hydrogenation as C10~C14 hydrocarbon-fractions of one line fraction of the 3rd fractionating column side
Change C10~C14 aliphatic fractions of unit 02.
Raw material pre-rectifying tower 2 for carrying out pre- rectifying to the material from the raw material surge tank 1, is obtained as tower top
The C9 of material-Alkane fraction (that is, the first product lightweight white oil) and C10~C14 aliphatic fractions 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, 0.05~0.25MPa of tower top pressure of tower top temperature, 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, such as 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
Bottom of towe enters, and the gas phase evaporated carries out counter current contacting, during two are in contact, volatile (low boiling point) in lower descending liquid with lower descending liquid
Component is constantly shifted into gas phase, and difficult volatilization (higher boiling) component in gas phase is constantly shifted 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 bottom of towe, difficult volatile component then more enrichment, so as to reach
To the separated purpose of 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 separated, and the positive structures of C10~C14 that will be adsorbed in using desorbing agent and irrigation in adsorbent
Aliphatic fraction is desorbed out, obtains the mixed of C10~C14 n-alkanes fraction as tower top Extract, desorbing agent and irrigation
Close the mixture of object and C10~C14 isoparaffins fraction as bottom of towe raffinate, desorbing agent and irrigation；It is 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 makes the separated device of different material to 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, adsorbent used are 5A molecular sieves；The further preferred desorbing agent is the mixing of pentane and isooctane
Object, wherein, the mass ratio of pentane and isooctane is (1~4):1, preferably (2~3):1, such as 2.5:1；The flushing liquor is
Isooctane, to ensure preferable dewaxing effect.Its process is as follows：The adsorbing tower with molecular sieve 3 utilizes adsorbent (such as 5A molecules
Sieve) selective absorption performance C10~C14 n-alkanes and C10~C14 isoparaffins are separated, the positive structures of C10~C14
After alkane is adsorbed by adsorbent, using desorbing agent, (for example mass ratio is 2.5:1 pentane and the mixture of isooctane), it will just
Structure alkane is desorbed from the duct of adsorbent and comes out, and adsorbent is rinsed with flushing liquor (such as isooctane), by remnants
Desorbing agent develop.
Extract feed surge tank 4, for receiving the tower top Extract from the adsorbing tower with molecular sieve 3 and buffering.
Extract tower 5 for being fractionated to the material from the Extract feed surge tank 4, is obtained as tower top
The desorbing agent of product, C10~C14 as the desorbing agent of side line product and the mixture of irrigation and 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, such as 0.12MPa, bottom of towe 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 bottom of towe raffinate from the adsorbing tower with molecular sieve 3 and buffering.
Raffinate column 7 for being fractionated to the material from the raffinate feed surge tank 6, is obtained as tower top
The desorbing agent of product, C10~C14 as the desorbing agent of side line product and the mixture of irrigation and 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 present invention, can add the F- T synthesis in fischer-tropsch synthesis process
C10~C14 aliphatic fractions of hydrogen refined unit are reprocessed, and so as to obtain high value added product, improve fischer-tropsch synthesis process
Economic interests, and realize the development in pluralism of its product.Wherein, operating condition and preferred operations condition are set in each device
It puts, contributes to the abundant progress of relevant operation in each device, it is different in order to reprocess to obtain C10~C14 aliphatic fractions
High value added product.
The reprocessing system of the F- T synthesis diesel oil distillate of the present invention can simultaneously close the Fischer-Tropsch in fischer-tropsch synthesis process
C10~C14 aliphatic fractions into hydrofinishing unit and F- T synthesis Hydrocracking unit are reprocessed, high attached so as to obtain
Value-added product, improves the economic interests of fischer-tropsch synthesis process, and realizes the development in pluralism of its product.
In one embodiment, the reprocessing system further includes：
Extract steams tower 8 again, for being distilled to the tower bottom product from the Extract tower 5, obtains as tower top
The C13 of product-N-alkane fraction (that is, the 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, the column bottom temperature of the isoparaffin knockout tower 9 is 230~280 DEG C, the isomeric alkane
Hydrocarbon knockout tower 9 is for separating the tower bottom product from the raffinate column 7, C10~C14 isomeries as overhead product
Alkane solvent oil (that is, the 4th product, the percentage shared by the relatively low component of the 4th product mid-boiling point are bigger) and conduct bottom of towe are produced
(that is, the 5th product, the percentage shared by the higher component of the 5th product mid-boiling point compare C10~C14 isoparaffin solvent oils of object
Greatly)；It is preferred that the operating condition of the isoparaffin knockout tower 9 is：180~230 DEG C of tower top temperature, tower top pressure 0.05~
0.25MPa, 230~280 DEG C of column bottom temperature, 0.05~0.25MPa of tower bottom pressure；The further preferred isoparaffin knockout tower
9 operating condition is：190~210 DEG C of tower top temperature, such as 195 DEG C, 0.08~0.15MPa of tower top pressure, such as 0.10MPa,
240~260 DEG C of column bottom temperature, 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 distilling.
It is reprocessed by the tower bottom product of the tower bottom product to Extract tower 5 and raffinate column 7, 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,
Contribute to 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 to carry out circular regeneration to desorbing agent and irrigation
Circular regeneration unit, the circular regeneration unit includes：
Desorbing agent fractionating column 10 separates 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, 0.10~0.25MPa of tower top pressure of tower top temperature, 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
Separated 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 contributes to 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, for by the Extract tower 5, the raffinate column 7 and the desorbing agent fractionating column 10
Overhead product be dried before the desorbing agent surge tank 11 is inputted；
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 present invention 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 fractions are as raw material；Then pre- essence is carried out in raw material C10~C14 aliphatic fractions input raw material pre-rectifying tower 2
It evaporates, obtains the C9 as tower top material-Alkane fraction (that is, the 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-alkanes fraction as tower top Extract, desorbing agent and irrigation,
And the mixture of C10~C14 isoparaffins fraction as bottom of towe raffinate, desorbing agent and irrigation；Adsorbing tower with molecular sieve 3
Tower top Extract input Extract feed surge tank 4 in and buffer；The material input Extract tower of Extract feed surge tank 4
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 fractions as tower bottom product；The bottom of towe raffinate input raffinate of the adsorbing tower with molecular sieve 3
In feed surge tank 6 and buffer；It is fractionated, is obtained as tower in the material input raffinate column 7 of raffinate feed surge tank 6
Push up product desorbing agent, as the desorbing agent of side line product and the mixture of irrigation and as tower bottom product C10~
C14 isoparaffin fractions；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, the second product light liquid paraffin) and the C14 as tower bottom product+N-alkane
Fraction；Separated in the tower bottom product input isoparaffin knockout tower 9 of the raffinate column 7, as overhead product C10~
C14 isoparaffin solvent oils (that is, the 4th product, the percentage shared by the relatively low component of the 4th product mid-boiling point are bigger) and conduct
Tower bottom product C10~C14 isoparaffin solvent oils (that is, the 5th product, hundred shared by the higher component of the 5th product mid-boiling point
Divide bigger)；It is separated in the side line product of the Extract tower 5 and the raffinate column 7 input desorbing agent fractionating column 10,
Obtain the desorbing agent as overhead product and the irrigation as tower bottom product；The Extract tower 5,7 and of the raffinate column
The overhead product of the desorbing agent fractionating column 10 is inputted in the desorbing agent surge tank 11 after the drying of desorbing agent drier 13 and deposited
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 filtered by filter 14
After input in the irrigation surge tank 12 and store, to provide irrigation to the adsorbing tower with molecular sieve 3.
The reprocessing system of the F- T synthesis diesel oil distillate of the present invention, has the advantages that：
(1) C10~C14 aliphatic fractions to F- T synthesis hydrofinishing unit and F- T synthesis Hydrocracking unit are passed through
It is reprocessed, lightweight white oil (the first product), light liquid paraffin (the second product), Paraffin liquid heavy (can be obtained
Three products), C10~C14 isoparaffin solvent oils (the 4th product) of tower top and C10~C14 Isopars of bottom of towe
Five kinds of high value-added products such as oily (the 5th products), realize the diversification of Fischer-Tropsch synthetic, improve F- T synthesis production
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 less than petroleum base processing unit (plant).
(3) in the reprocessing system of F- T synthesis diesel oil distillate of the invention, each device is the dress of petrochemical industry routine
It puts, degree domestic is high, and cost of investment is low.
(4) the reprocessing system of F- T synthesis diesel oil distillate of the invention, can to the desorbing agent that uses and irrigation into
Row recycling, regeneration, recycle.
C10~C14 alkane in fischer-tropsch synthesis process is evaporated using foregoing reprocessing system the present invention also provides a kind of
Divide the method reprocessed.
In one embodiment, the described method includes：
C10~C14 aliphatic fractions in Fischer-Tropsch combined diesel oil technique are received using the raw material surge tank 1 and it is carried out
Buffering；
Pre- rectifying is carried out to the material from the raw material surge tank 1 using the raw material pre-rectifying tower 2, is obtained as tower
Push up the C9 of material-Alkane fraction (the first product) and C10~C14 aliphatic fractions as materials at bottom of tower；
It is adsorbed and is separated to coming from 2 materials at bottom of tower of raw material pre-rectifying tower using the adsorbing tower with molecular sieve 3, made
The mixture of C10~C14 n-alkanes fraction, desorbing agent and irrigation for tower top Extract and conduct bottom of towe raffinate
C10~C14 isoparaffins fraction, the mixture of desorbing agent and irrigation；
The tower top Extract from the adsorbing tower with molecular sieve 3 is received using the Extract feed surge tank 4 and is buffered；
The material from the Extract feed surge tank 4 is fractionated using the Extract tower 5, is obtained as tower
Push up product desorbing agent, as the desorbing agent of side line product and the mixture of irrigation and as tower bottom product C10~
C14 n-alkane fractions；
The bottom of towe raffinate from the adsorbing tower with molecular sieve 3 is received using the raffinate feed surge tank 6 and is buffered；
The material from the raffinate feed surge tank 6 is fractionated using the raffinate column 7, is obtained as tower
Push up product desorbing agent, as the desorbing agent of side line product and the mixture of irrigation and as tower bottom product C10~
C14 isoparaffin fractions.
In one embodiment, the method further includes：
Tower 8 is steamed again using the Extract to distill the tower bottom product from the Extract tower 5, is obtained as tower
Push up the C13 of product-N-alkane fraction (the second product) and the C14 as tower bottom product+N-alkane fraction (third product)；
The tower bottom product from the raffinate column 7 is separated using the isoparaffin knockout tower 9, as tower top
C10~C14 isoparaffin solvent oils (the 4th product) of product and C10~C14 isoparaffin solvent oils as tower bottom product
(the 5th product).
Embodiment
Using reprocessing system the method according to the invention of the present invention to coming from 01 He of F- T synthesis hydrofinishing unit
C10~C14 aliphatic fractions of F- T synthesis Hydrocracking unit 02 are reprocessed, respectively obtain the first product, the second product,
Third product, the 4th product, the 5th product.Wherein,
Adsorbing tower with molecular sieve 3 is moving-bed adsorption knockout tower, and adsorbent used is 5A molecular sieves；The desorbing agent
For pentane and the mixture of 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, tower top pressure 0.12MPa of tower top temperature, column bottom temperature 260
DEG C, tower bottom pressure 0.2MPa；
The operating condition of the Extract tower 5 is：104 DEG C, tower top pressure 0.12MPa of tower top temperature, column bottom temperature 255
DEG C, tower bottom pressure 0.19MPa；
The operating condition of the raffinate column 7 is：80 DEG C, tower top pressure 0.14MPa of tower top temperature, 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, tower top pressure 0.03MPa of tower top temperature, column bottom temperature
290 DEG C, tower bottom pressure 0.10MPa；
The operating condition of the isoparaffin knockout tower 9 is：195 DEG C, tower top pressure 0.10MPa of tower top temperature, bottom of towe 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, tower top pressure 0.18MPa of tower top temperature, 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 and lusters | ≥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 and lusters | ≥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 and lusters | ≥30 |
| Aromatic hydrocarbons contains (mass fraction) % | ≤0.1 |
| Sulfur content (mass fraction) ppm | ≤1 |
| Bromine index mgBr/100mg | ≤50 |
| Flash-point (remaining 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 and lusters | ≥30 |
| Aromatic hydrocarbons contains (mass fraction) % | ≤0.1 |
| Sulfur content (mass fraction) ppm | ≤1 |
| Bromine index mgBr/100mg | ≤50 |
| Flash-point (remaining silent)/DEG C | ≥80 |
| Dynamic viscosity (40 DEG C)/(mm2/s) | 1.958 |
Claims (10)
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 fractions in Fischer-Tropsch combined diesel oil technique and to it into row buffering；
Raw material pre-rectifying tower (2) for carrying out pre- rectifying to the material for coming from the raw material surge tank (1), is obtained as tower top
The C9 of material-Alkane fraction and C10~C14 aliphatic fractions 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 separated, and the positive structures of C10~C14 that will be adsorbed in using desorbing agent and irrigation in adsorbent
Aliphatic fraction is desorbed out, obtains the mixed of C10~C14 n-alkanes fraction as tower top Extract, desorbing agent and irrigation
Close the mixture of object and C10~C14 isoparaffins fraction as bottom of towe raffinate, 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) for being fractionated to the material for coming from the Extract feed surge tank (4), is obtained as tower top
The desorbing agent of product, C10~C14 as the desorbing agent of side line product and the mixture of irrigation and as tower bottom product
N-alkane fraction；
Raffinate feed surge tank (6), for receiving the bottom of towe raffinate from the adsorbing tower with molecular sieve (3)；
Raffinate column (7) for being fractionated to the material for coming from the raffinate feed surge tank (6), is obtained as tower top
The desorbing agent of product, C10~C14 as the desorbing agent of side line product and the mixture of irrigation and 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 being distilled to the tower bottom product for coming from the Extract tower (5), obtains as tower top
The C13 of product-N-alkane fraction and the C14 as tower bottom product+N-alkane fraction；
Isoparaffin knockout tower (9), the column bottom temperature of the isoparaffin knockout tower (9) is 230~280 DEG C, the isomeric alkane
Hydrocarbon knockout tower (9) is used to separate the tower bottom product for coming from the raffinate column (7), obtains the C10 as overhead product
~C14 isoparaffin solvent oils and C10~C14 isoparaffin solvent oils 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) divides for the side line product to 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), for by the Extract tower (5), the raffinate column (7) and the desorbing agent fractionating column
(10) overhead product is dried before the desorbing agent surge tank (11) is inputted；
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 moved for simulation
Bed absorptive separation column, adsorbent used are 5A molecular sieves.
6. reprocessing system according to claim 1, which is characterized in that the desorbing agent is the mixed of pentane and isooctane
Object is closed, wherein, the mass ratio of pentane and isooctane is (1~4):1, preferably (2~3):1；The flushing liquor is isooctane.
7. reprocessing system according to claim 1 or 2, which is characterized in that
The operating condition of the raw material pre-rectifying tower (2) is：80~150 DEG C, 0.05~0.25MPa of tower top pressure of tower top temperature,
240~280 DEG C of column bottom temperature, 0.10~0.35MPa of tower bottom pressure；
The operating condition of the adsorbing tower with molecular sieve (3) is：150~200 DEG C of temperature, 1.5~3.5MPa of pressure；
The operating condition of the Extract tower (5) is：80~120 DEG C, 0.05~0.50MPa of tower top pressure of tower top temperature, bottom of towe
210~270 DEG C of temperature, 0.10~0.30MPa of tower bottom pressure；
The operating condition of the raffinate column (7) is：60~100 DEG C, 0.05~0.30MPa of tower top pressure of tower top temperature, bottom of towe
240~285 DEG C of temperature, 0.10~0.40MPa of tower bottom pressure.
8. reprocessing system according to claim 2, which is characterized in that
The operating condition that the Extract steams tower (8) again is：200~250 DEG C of tower top temperature, tower top pressure 0.001~
0.10MPa, 260~320 DEG C of column bottom temperature, 0.05~0.30MPa of tower bottom pressure；
The operating condition of the isoparaffin knockout tower (9) is：180~230 DEG C of tower top temperature, tower top pressure 0.05~
0.25MPa, 230~280 DEG C of column bottom temperature, 0.05~0.25MPa of tower bottom pressure.
9. reprocessing system according to claim 4, which is characterized in that
The operating condition of the desorbing agent fractionating column (10) is：75~110 DEG C, 0.10~0.25MPa of tower top pressure of tower top temperature,
120~165 DEG C of column bottom temperature, 0.10~0.40MPa of tower bottom pressure.
10. it is a kind of using as claimed in any one of claims 1-9 wherein reprocessing system to the C10 in fischer-tropsch synthesis process~
The method that C14 aliphatic fractions are reprocessed.
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109161398A (en) * | 2018-10-11 | 2019-01-08 | 内蒙古伊泰宁能精细化工有限公司 | A kind of liquid hydrocarbon composition containing isoparaffin component |
| CN109161396A (en) * | 2018-10-11 | 2019-01-08 | 内蒙古伊泰宁能精细化工有限公司 | Solvent fluid composition |
| CN109161397A (en) * | 2018-10-11 | 2019-01-08 | 内蒙古伊泰宁能精细化工有限公司 | A kind of isoparaffin solvent oil composition |
| CN109161399A (en) * | 2018-10-11 | 2019-01-08 | 内蒙古伊泰宁能精细化工有限公司 | A kind of liquid hydrocarbon composition containing isoparaffin component |
| CN109456793A (en) * | 2018-10-11 | 2019-03-12 | 内蒙古伊泰宁能精细化工有限公司 | It is a kind of to synchronize industrial co-production |
| CN111471488A (en) * | 2019-01-23 | 2020-07-31 | 内蒙古伊泰宁能精细化工有限公司 | High-purity environment-friendly isoparaffin solvent oil and application thereof |
| CN112546675A (en) * | 2020-12-28 | 2021-03-26 | 大连福佳·大化石油化工有限公司 | Improved steam stripping structure of adsorption tower for leaking agent from bed layer |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2035337A1 (en) * | 1991-01-31 | 1992-08-01 | Santi Kulprathipanja | Normal paraffin adsorptive separation using non-normal hydrocarbon pre-pulse stream |
| CN208166931U (en) * | 2018-01-02 | 2018-11-30 | 神华集团有限责任公司 | The reprocessing system of F- T synthesis diesel oil distillate |
-
2018
- 2018-01-02 CN CN201810001051.4A patent/CN108102694A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2035337A1 (en) * | 1991-01-31 | 1992-08-01 | Santi Kulprathipanja | Normal paraffin adsorptive separation using non-normal hydrocarbon pre-pulse stream |
| CN208166931U (en) * | 2018-01-02 | 2018-11-30 | 神华集团有限责任公司 | The reprocessing system of F- T synthesis diesel oil distillate |
Non-Patent Citations (1)
| Title |
|---|
| 侯祥麟: "《中国炼油技术》", 31 August 1997, 中国石化出版社 * |
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| CN109161396A (en) * | 2018-10-11 | 2019-01-08 | 内蒙古伊泰宁能精细化工有限公司 | Solvent fluid composition |
| CN109161397A (en) * | 2018-10-11 | 2019-01-08 | 内蒙古伊泰宁能精细化工有限公司 | A kind of isoparaffin solvent oil composition |
| CN109161399A (en) * | 2018-10-11 | 2019-01-08 | 内蒙古伊泰宁能精细化工有限公司 | A kind of liquid hydrocarbon composition containing isoparaffin component |
| CN109456793A (en) * | 2018-10-11 | 2019-03-12 | 内蒙古伊泰宁能精细化工有限公司 | It is a kind of to synchronize industrial co-production |
| CN109161397B (en) * | 2018-10-11 | 2019-07-30 | 内蒙古伊泰宁能精细化工有限公司 | A kind of isoparaffin solvent oil composition |
| CN109161399B (en) * | 2018-10-11 | 2019-07-30 | 内蒙古伊泰宁能精细化工有限公司 | A kind of liquid hydrocarbon composition containing isoparaffin component |
| CN109161398B (en) * | 2018-10-11 | 2019-07-30 | 内蒙古伊泰宁能精细化工有限公司 | A kind of liquid hydrocarbon composition containing isoparaffin component |
| CN109456793B (en) * | 2018-10-11 | 2021-02-26 | 内蒙古伊泰宁能精细化工有限公司 | Synchronous industrial co-production method |
| CN111471488A (en) * | 2019-01-23 | 2020-07-31 | 内蒙古伊泰宁能精细化工有限公司 | High-purity environment-friendly isoparaffin solvent oil and application thereof |
| CN112546675A (en) * | 2020-12-28 | 2021-03-26 | 大连福佳·大化石油化工有限公司 | Improved steam stripping structure of adsorption tower for leaking agent from bed layer |
| CN112546675B (en) * | 2020-12-28 | 2023-10-13 | 大连福佳·大化石油化工有限公司 | Improved structure of adsorption tower stripping of bed leakage agent |
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