CN108165304A - A kind of method and system that special solvent oil is extracted from stable light hydrocarbon - Google Patents
A kind of method and system that special solvent oil is extracted from stable light hydrocarbon Download PDFInfo
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- CN108165304A CN108165304A CN201810084562.7A CN201810084562A CN108165304A CN 108165304 A CN108165304 A CN 108165304A CN 201810084562 A CN201810084562 A CN 201810084562A CN 108165304 A CN108165304 A CN 108165304A
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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
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
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Abstract
The invention discloses a kind of method and system that special solvent oil is extracted from stable light hydrocarbon, belong to oil-refining chemical technical field, this method includes：Raw material stable light hydrocarbon is sent into weight-removing column, obtains light component oil and heavy aromatics；Light component oil is sent into lightness-removing column, obtains byproduct stable light hydrocarbon and C6‑C7Component；By C6‑C7Component is sent into dehexanizer, obtains hexane oil and heptane oil；Hexane oil is sent into hexane oil knockout tower, obtains isohexane and n-hexane；Heptane oil is sent into heptane oil knockout tower, obtains isoheptane and normal heptane.The system includes：Weight-removing column, lightness-removing column, dehexanizer, hexane oil knockout tower and heptane oil knockout tower.The exemplary technical solution of the present invention, realizes the efficient utilization of stable light hydrocarbon, and limited resource is made to play maximum benefit, and enterprise economic benefit while meets the market demand.
Description
Technical field
It is specifically a kind of that special solvent oil is extracted from stable light hydrocarbon the invention belongs to oil-refining chemical technical field
Method and system.
Background technology
Stable light hydrocarbon is one of oil product, may separate out a variety of Organic Ingredients, and in China, stable light hydrocarbon supply is very tight
, oil-refining chemical enterprise is traditionally the means that weight is taken to cut to the utilization of stable light hydrocarbon, using light oil as ethylene raw
Or gasoline blend component, as reformer feed, this Land use systems fail fully to realize its optimization on hydrocarbon system's composition heavy oil
It utilizes：
1st, tower internals is easily blocked after coking containing certain colloid, traditional separation method easy coking in raw material stable light hydrocarbon,
Separation accuracy is not achieved and has an effect on yield；
2nd, ethylene raw（Light oil C3-C6）In containing part cycloalkane and aromatic hydrocarbon, influence triolefin mass yield, and easy green coke；
3rd, reformer feed（Heavy oil C7-C11）In containing part n-alkane, influence reformer operation and liquid quality yield；
4th, current extraction equipment, weight-removing column height is higher, and investment is big, steam consumption is big, of high cost.
Therefore, how to efficiently use limited resource, it is made to play maximum benefit in production, it has also become oil-refining chemical
The major issue that integration firm is faced.
Invention content
In order to solve above-mentioned deficiency of the prior art, extracted from stable light hydrocarbon the purpose of the present invention is to provide one kind
The method and system of special solvent oil fully realize the Optimum utilization of stable light hydrocarbon.
The technical solution adopted by the present invention to solve the technical problems is：
On the one hand, a kind of method that special solvent oil is extracted from stable light hydrocarbon is provided, including：
Raw material stable light hydrocarbon is sent into weight-removing column, after weight-removing column detaches, light component oil is obtained in weight-removing column overhead condensation, de-
Weight tower bottom of towe obtains heavy aromatics, wherein, the operation temperature of weight-removing column tower top is 70-80 DEG C, operating pressure 100-110KPa, is taken off
The operation temperature of weight tower bottom of towe is 140-150 DEG C, operating pressure 155-165KPa；
The light component oil is sent into lightness-removing column, after lightness-removing column detaches, byproduct is obtained in lightness-removing column overhead condensation and stablizes gently
Hydrocarbon obtains C in lightness-removing column bottom of towe6-C7Component, wherein, the operation temperature of lightness-removing column tower top is 55-65 DEG C, operating pressure 235-
245KPa, the operation temperature of lightness-removing column bottom of towe is 110-120 DEG C, operating pressure 290-300KPa；
By the C6-C7Component is sent into dehexanizer, and after dehexanizer detaches, hexane is obtained in dehexanizer overhead condensation
Oil obtains heptane oil in dehexanizer bottom of towe, wherein, the operation temperature of dehexanizer tower top is 60-70 DEG C, operating pressure is
100-110KPa, the operation temperature of dehexanizer bottom of towe is 70-80 DEG C, operating pressure 155-165KPa；
The hexane oil is sent into hexane oil knockout tower, after the separation of hexane oil knockout tower, in the separation column overhead condensation of hexane oil
Isohexane is obtained, n-hexane is obtained in hexane oil knockout tower bottom of towe, wherein, the operation temperature of hexane oil separation column overhead is 85-
95 DEG C, operating pressure 100-110KPa, the operation temperature of hexane oil knockout tower bottom of towe is 100-115 DEG C, operating pressure is
155-165KPa；
The heptane oil is sent into heptane oil knockout tower, after the separation of heptane oil knockout tower, in the separation column overhead condensation of heptane oil
Isoheptane is obtained, normal heptane is obtained in heptane oil knockout tower bottom of towe, wherein, the operation temperature of heptane oil separation column overhead is 70-
80 DEG C, operating pressure 100-110KPa, the operation temperature of heptane oil knockout tower bottom of towe is 140-150 DEG C, operating pressure is
155-165KPa。
Further, the tower of the weight-removing column, lightness-removing column, dehexanizer, hexane oil knockout tower and heptane oil knockout tower
Top, condensed on-condensible gas are sent into out-of-bounds gas recovery system for oil after entering fixed gas surge tank.
Further, the tower of the weight-removing column, lightness-removing column, dehexanizer, hexane oil knockout tower and heptane oil knockout tower
Top, the obtained equal partial reflux of product.
Further, the light component oil is C6And following components.
Further, the heavy aromatics is C8-C12Component.
On the other hand, a kind of system that special solvent oil is extracted from stable light hydrocarbon is provided, including weight-removing column, is taken off gently
Tower, dehexanizer, hexane oil knockout tower and heptane oil knockout tower, the tower top of the weight-removing column is connected with the lightness-removing column, described
The bottom of towe of lightness-removing column is connected with the dehexanizer, and the tower top of the dehexanizer is connected with the hexane oil knockout tower, described
The bottom of towe of dehexanizer is connected with the heptane oil knockout tower；
Wherein, the top inside the weight-removing column is provided with epimere filling batch, and the lower part inside weight-removing column is provided with hypomere and fills out
Expect bed, liquid collecting distributer is provided between the epimere filling batch and hypomere filling batch, the liquid is collected
Distributor includes collecting part and distributed elements, and the distributed elements are mounted on the collecting part and the height of distributed elements
Less than collecting part, the collecting part collects the liquid of epimere filling batch bottom and is conducted into distributed elements, distribution portion
Part makes liquid be evenly distributed on hypomere filling batch.
Further, the collecting part includes the open slot that is made of bottom surface and side wall, the sky inside the open slot
Between be interconnected overall space, the side wall is serpentine-like to be bent and forms end to end closed-loop, and the side wall is located at
The part of inside is bottom inclined inclined surface inwardly, so as to form central collection slot at the middle part of collecting part；Described point
Cloth component is uniformly mounted on the diversion pipe of the side-wall outer side of collecting part, the diversion pipe is vertically-mounted and the top of diversion pipe
Less than the top edge of the side wall of collecting part.
Further, the central collection slot is arranged along a straight line, the sidewall symmetry arrangement of central collection slot both sides.
Further, the tube wall of the diversion pipe crimps in the shape of a spiral.
Further, between the bottom end of the liquid collecting distributer and the top of the hypomere filling batch it is vertical away from
From for H, 900mm≤H≤1100mm.
Further, the tower of the weight-removing column, lightness-removing column, dehexanizer, hexane oil knockout tower and heptane oil knockout tower
Top is equipped with condenser and is connected with fixed gas surge tank.
Further, the tower of the weight-removing column, lightness-removing column, dehexanizer, hexane oil knockout tower and heptane oil knockout tower
Top is respectively connected with return tank.
Further, the fixed gas surge tank is connected to out-of-bounds gas recovery system for oil.
Compared with prior art, beneficial effects of the present invention are：
1st, the exemplary method that special solvent oil is extracted from stable light hydrocarbon of the present invention by separation layer by layer, is realized and is stablized gently
Hydrocarbon makes full use of, and this method improves separation accuracy by the setting to knockout tower operation temperatures at different levels and operating pressure, with
Traditional weight cutting is different, can improve separation accuracy to isolating C6-C7Component and C8-C12Component improves triolefin yield,
The liquid yield reformed and product octane number are improved, the anti-knock properties of product can be improved by improving product octane number, promote product quality.
2nd, the exemplary method that special solvent oil is extracted from stable light hydrocarbon of the present invention, enters after the buffered tank of on-condensible gas
Out-of-bounds gas recovery system for oil, the product of each tower top can partial reflux realize the separation of repetitive cycling, obtain limited raw material
To making full use of to the greatest extent, the maximization of benefit is realized for enterprise, and meets the environmental protection concept of country's promotion.
3rd, the exemplary method that special solvent oil is extracted from stable light hydrocarbon of the present invention, preciseness of separation is high, may separate out
C6-C7Component and C8-C12Subsequent processing is carried out to said components again after component, efficiently separates out the impurity and shakiness in product
Determine part, obtained superior product quality.
4th, the exemplary system that special solvent oil is extracted from stable light hydrocarbon of the present invention, setting weight-removing column, take off oneself at lightness-removing column
Alkane tower, hexane oil knockout tower and heptane oil knockout tower, it is rationally distributed, it is simple and compact for structure, reduce operating severity.
5th, the exemplary system that special solvent oil is extracted from stable light hydrocarbon of the present invention, weight-removing column inside setting liquid are collected
The function of the collection of liquid and distribution is integrated in one by distributor, liquid collecting distributer, and distributed elements are directly installed on collection
It, can be by liquid collecting distributer and hypomere while ensureing that liquid can be evenly distributed on hypomere filling batch on component
Vertical range between filling batch foreshortens to 1000mm or so, reduces the whole height of weight-removing column, so as to reduce investment, section
Steam consumption is saved, reduces device operating cost.
6th, the exemplary system that special solvent oil is extracted from stable light hydrocarbon of the present invention, sets liquid collecting distributer, arrives
Up to hypomere filling batch liquid by traditional in the unordered sprinkling of shape spray, become being uniformly distributed, promote hypomere filling batch
Separative efficiency.
7th, the exemplary system that special solvent oil is extracted from stable light hydrocarbon of the present invention, the collection portion of liquid collecting distributer
Part is equipped with central collection slot, and the side wall around central collection slot is inclined, and coke powder can flow downward along inclined surface, avoid
Coke powder blocks the diversion pipe of liquid collecting distributer.
8th, the exemplary system that special solvent oil is extracted from stable light hydrocarbon of the present invention, central collection slot are arranged along a straight line,
The sidewall symmetry arrangement of central collection slot both sides, and side wall is serpentine bend shape, reaches the maximization of liquid distribution uniformity coefficient.
9th, the exemplary system that special solvent oil is extracted from stable light hydrocarbon of the present invention, the tube wall of diversion pipe are rolled up in the shape of a spiral
Song compared with traditional pipe, not only increases the tie point of diversion pipe and collecting part, increases its installation strength, and to liquid
The distributed effect of body is more preferable.
10th, the exemplary system that special solvent oil is extracted from stable light hydrocarbon of the present invention, setting fixed gas surge tank, reflux
Tank etc., system good operating stability, raw material availability are high.
Description of the drawings
By reading the detailed description made to non-limiting example made with reference to the following drawings, the application's is other
Feature, objects and advantages will become more apparent upon：
Fig. 1 is the schematic diagram of the embodiment of the present invention one；
Fig. 2 is the structure diagram of one weight-removing column of the embodiment of the present invention；
Fig. 3 is the structure diagram of one liquid collecting distributer of the embodiment of the present invention.
In figure：1 weight-removing column, 2 epimere filling batch, 3 liquid collecting distributers, 31 collecting parts, 32 distributed elements, in 33
Heart collecting tank, 4 hypomere filling batch.
Specific embodiment
The application is described in further detail with reference to the accompanying drawings and examples.It is understood that this place is retouched
The specific embodiment stated is used only for explaining related invention rather than the restriction to the invention.It also should be noted that in order to
Convenient for description, illustrated only in attached drawing with inventing relevant part.
It should be noted that in the absence of conflict, the feature in embodiment and embodiment in the application can phase
Mutually combination.The application is described in detail below with reference to the accompanying drawings and in conjunction with the embodiments.
Embodiment one：
As shown in Figure 1, a kind of method that special solvent oil is extracted from stable light hydrocarbon is present embodiments provided, including：
S1：Raw material stable light hydrocarbon is sent into weight-removing column, after weight-removing column detaches, light component oil is obtained in weight-removing column overhead condensation,
Heavy aromatics is obtained in weight-removing column bottom of towe, wherein, the operation temperature of weight-removing column tower top is 70 DEG C, operating pressure 100KPa, takes off weight
The operation temperature of tower bottom of towe is 140 DEG C, operating pressure 155KPa；
S2：The light component oil is sent into lightness-removing column, after lightness-removing column detaches, byproduct is obtained in lightness-removing column overhead condensation and stablizes
Lighter hydrocarbons obtain C in lightness-removing column bottom of towe6-C7Component, wherein, the operation temperature of lightness-removing column tower top is 55 DEG C, operating pressure is
235KPa, the operation temperature of lightness-removing column bottom of towe is 110 DEG C, operating pressure 290KPa；
S3：By the C6-C7Component is sent into dehexanizer, and after dehexanizer detaches, oneself is obtained in dehexanizer overhead condensation
Alkane oil obtains heptane oil in dehexanizer bottom of towe, wherein, the operation temperature of dehexanizer tower top is 60 DEG C, operating pressure is
100KPa, the operation temperature of dehexanizer bottom of towe is 70 DEG C, operating pressure 155KPa；
S4：The hexane oil is sent into hexane oil knockout tower, it is cold in hexane oil separation column overhead after the separation of hexane oil knockout tower
It is solidifying to obtain isohexane, n-hexane is obtained in hexane oil knockout tower bottom of towe, wherein, the operation temperature of hexane oil separation column overhead is 85
DEG C, operating pressure 100KPa, the operation temperature of hexane oil knockout tower bottom of towe is 100 DEG C, operating pressure 155KPa；
S5：The heptane oil is sent into heptane oil knockout tower, it is cold in heptane oil separation column overhead after the separation of heptane oil knockout tower
It is solidifying to obtain isoheptane, normal heptane is obtained in heptane oil knockout tower bottom of towe, wherein, the operation temperature of heptane oil separation column overhead is 70
DEG C, operating pressure 100KPa, the operation temperature of heptane oil knockout tower bottom of towe is 140 DEG C, operating pressure 155KPa.
Weight-removing column, lightness-removing column, dehexanizer, hexane oil knockout tower and heptane oil knockout tower tower top, it is condensed not
Solidifying gas is sent into out-of-bounds gas recovery system for oil after entering fixed gas surge tank, is polluted the environment to avoid fixed gas.
Weight-removing column, lightness-removing column, dehexanizer, hexane oil knockout tower and heptane oil knockout tower tower top, obtained production
The equal partial reflux of product, the product meeting circulating repetition separation of partial reflux so that separation is more thorough, improves triolefin yield, improves heavy
Whole liquid yield.
Light component oil is C6And following components, heavy aromatics C8-C12Component.
It should be noted that although describing the operation of the method for the present invention with particular order in the above-described embodiments, this is simultaneously
It is undesired or imply and must perform these operations according to the particular order or have to carry out operation ability shown in whole
Realize desired result.On the contrary, the step in embodiment, which can change, performs sequence.For example, above-mentioned S4's and S5 performs sequence
It can exchange, first carry out S4, then perform S5.Additionally or alternatively, it is convenient to omit multiple steps are merged into one by certain steps
A step performs and/or a step is decomposed into execution of multiple steps.For example, above-mentioned S4 and S5 can be performed simultaneously.
The present embodiment additionally provides a kind of system that special solvent oil is extracted from stable light hydrocarbon, including weight-removing column, takes off gently
Tower, dehexanizer, hexane oil knockout tower and heptane oil knockout tower, the tower top of the weight-removing column is connected with the lightness-removing column, described
The bottom of towe of lightness-removing column is connected with the dehexanizer, and the tower top of the dehexanizer is connected with the hexane oil knockout tower, described
The bottom of towe of dehexanizer is connected with the heptane oil knockout tower.
As shown in Fig. 2, the top inside weight-removing column 1 is provided with epimere filling batch 2, the lower part setting inside weight-removing column 1
There is hypomere filling batch 4, liquid collecting distributer 3 be provided between the epimere filling batch 2 and hypomere filling batch 4,
As shown in figure 3, the liquid collecting distributer 3 includes collecting part 31 and distributed elements 32, the distributed elements 32 are mounted on
On the collecting part 31 and the height of distributed elements 32 is less than collecting part 31, and the collecting part 31 collects epimere packed bed
The liquid of 2 bottom of layer is simultaneously conducted into distributed elements 32, and distributed elements 32 make liquid be evenly distributed on hypomere filling batch 4.
Such as Fig. 3, collecting part 31 includes the open slot being made of bottom surface and side wall, and the space inside the open slot is phase
Intercommunicated overall space, the side wall is serpentine-like to be bent and forms end to end closed-loop, and the side wall is located inside
Part is bottom inclined inclined surface inwardly, so as to form central collection slot 33 at the middle part of collecting part；The distribution portion
Part 32 is uniformly mounted on the diversion pipe of the side-wall outer side of collecting part 31, the diversion pipe is vertically-mounted and the top of diversion pipe
Less than the top edge of the side wall of collecting part 31.
Central collection slot 33 is arranged along a straight line, the sidewall symmetry arrangement of 33 both sides of central collection slot.The tube wall of diversion pipe is in
Helical form crimps, and as seen from Figure 3, one flaky material of use that helical form curling refers to crimps structure from one end to the other side
Into diversion pipe, when being installed on collecting part 31, outer surface of tube wall forms a fixed connection diversion pipe with collecting part 31, curling
It is located at external one end afterwards also to form a fixed connection with collecting part 31, increases its installation strength, and the distribution of liquid is imitated
Fruit is more preferable.
Vertical range between the bottom end of liquid collecting distributer and the top of the hypomere filling batch is H, 900mm≤
H≤1100mm.H is preferably 1000mm, and after setting liquid collecting distributer 3, liquid on hypomere filling batch 4 has been effectively ensured
Be uniformly distributed, reduce the height of tower body.
Weight-removing column, lightness-removing column, dehexanizer, hexane oil knockout tower and heptane oil knockout tower tower top be equipped with condensation
Device is simultaneously connected with fixed gas surge tank.Fixed gas surge tank can be kept in and be buffered to on-condensible gas, be delayed by fixed gas
The buffering of tank is rushed, fixed gas can enter subsequent device and process with stable air pressure, avoid the impact to system, make system
Work it is more reliable and more stable.
Weight-removing column, lightness-removing column, dehexanizer, hexane oil knockout tower and heptane oil knockout tower tower top be respectively connected with back
Flow tank.Return tank is connected, the product condensed is through return tank partial reflux, partly into subsequent processing, the product meeting of reflux
Circulating repetition detaches, and limited raw material is made to be made full use of to the greatest extent, and the maximization of benefit is realized for enterprise, and
Reduce byproduct and discharge, meet the environmental protection concept of country's promotion.
Fixed gas surge tank is connected to out-of-bounds gas recovery system for oil.Fixed gas in fixed gas surge tank enters out-of-bounds oil gas
Recovery system is recycled, and reduces discharge, Improve Efficiency.
To improve production efficiency, ensure the stable operation of system, in weight-removing column, lightness-removing column, dehexanizer, the separation of hexane oil
The tower top of tower and heptane oil knockout tower sets reflux pump, is pumped at bottom of towe setting bottom and sends cooler outside, so that higher level's product
Next procedure can smoothly be entered, and extend the service life of system.In weight-removing column, lightness-removing column, dehexanizer, the separation of hexane oil
The inside of tower and heptane oil knockout tower is respectively arranged with reboiler.
The material balance table of the present embodiment is shown in Table 1, and can reach high-purity through the obtained alkane product of separation and Extraction
The requirement of degree.
Table 1：Material balance table：
Embodiment two：
A kind of method that special solvent oil is extracted from stable light hydrocarbon is present embodiments provided, including：
S1：Raw material stable light hydrocarbon is sent into weight-removing column, after weight-removing column detaches, light component oil is obtained in weight-removing column overhead condensation,
Heavy aromatics is obtained in weight-removing column bottom of towe, wherein, the operation temperature of weight-removing column tower top is 74.5 DEG C, operating pressure 105KPa, is taken off
The operation temperature of weight tower bottom of towe is 145.4 DEG C, operating pressure 160KPa；
S2：The light component oil is sent into lightness-removing column, after lightness-removing column detaches, byproduct is obtained in lightness-removing column overhead condensation and stablizes
Lighter hydrocarbons obtain C in lightness-removing column bottom of towe6-C7Component, wherein, the operation temperature of lightness-removing column tower top is 58.9 DEG C, operating pressure is
240KPa, the operation temperature of lightness-removing column bottom of towe is 113.6 DEG C, operating pressure 295KPa；
S3：By the C6-C7Component is sent into dehexanizer, and after dehexanizer detaches, oneself is obtained in dehexanizer overhead condensation
Alkane oil obtains heptane oil in dehexanizer bottom of towe, wherein, the operation temperature of dehexanizer tower top is 63 DEG C, operating pressure is
105KPa, the operation temperature of dehexanizer bottom of towe is 77 DEG C, operating pressure 160KPa；
S4：The hexane oil is sent into hexane oil knockout tower, it is cold in hexane oil separation column overhead after the separation of hexane oil knockout tower
It is solidifying to obtain isohexane, n-hexane is obtained in hexane oil knockout tower bottom of towe, wherein, the operation temperature of hexane oil separation column overhead is
91.7 DEG C, operating pressure 105KPa, the operation temperature of hexane oil knockout tower bottom of towe is 107.2 DEG C, operating pressure 160KPa；
S5：The heptane oil is sent into heptane oil knockout tower, it is cold in heptane oil separation column overhead after the separation of heptane oil knockout tower
It is solidifying to obtain isoheptane, normal heptane is obtained in heptane oil knockout tower bottom of towe, wherein, the operation temperature of heptane oil separation column overhead is
74.5 DEG C, operating pressure 105KPa, the operation temperature of heptane oil knockout tower bottom of towe is 145.4 DEG C, operating pressure 160KPa.
Other features of the present embodiment are identical with embodiment one, and details are not described herein.
The material balance table of the present embodiment is shown in Table 2, and can reach high-purity through the obtained alkane product of separation and Extraction
The requirement of degree.
Table 2：Material balance table：
Embodiment three：
A kind of method that special solvent oil is extracted from stable light hydrocarbon is present embodiments provided, including：
S1：Raw material stable light hydrocarbon is sent into weight-removing column, after weight-removing column detaches, light component oil is obtained in weight-removing column overhead condensation,
Heavy aromatics is obtained in weight-removing column bottom of towe, wherein, the operation temperature of weight-removing column tower top is 80 DEG C, operating pressure 110KPa, takes off weight
The operation temperature of tower bottom of towe is 150 DEG C, operating pressure 165KPa；
S2：The light component oil is sent into lightness-removing column, after lightness-removing column detaches, byproduct is obtained in lightness-removing column overhead condensation and stablizes
Lighter hydrocarbons obtain C in lightness-removing column bottom of towe6-C7Component, wherein, the operation temperature of lightness-removing column tower top is 65 DEG C, operating pressure is
245KPa, the operation temperature of lightness-removing column bottom of towe is 120 DEG C, operating pressure 300KPa；
S3：By the C6-C7Component is sent into dehexanizer, and after dehexanizer detaches, oneself is obtained in dehexanizer overhead condensation
Alkane oil obtains heptane oil in dehexanizer bottom of towe, wherein, the operation temperature of dehexanizer tower top is 70 DEG C, operating pressure is
110KPa, the operation temperature of dehexanizer bottom of towe is 80 DEG C, operating pressure 165KPa；
S4：The hexane oil is sent into hexane oil knockout tower, it is cold in hexane oil separation column overhead after the separation of hexane oil knockout tower
It is solidifying to obtain isohexane, n-hexane is obtained in hexane oil knockout tower bottom of towe, wherein, the operation temperature of hexane oil separation column overhead is 95
DEG C, operating pressure 110KPa, the operation temperature of hexane oil knockout tower bottom of towe is 115 DEG C, operating pressure 165KPa；
S5：The heptane oil is sent into heptane oil knockout tower, it is cold in heptane oil separation column overhead after the separation of heptane oil knockout tower
It is solidifying to obtain isoheptane, normal heptane is obtained in heptane oil knockout tower bottom of towe, wherein, the operation temperature of heptane oil separation column overhead is 80
DEG C, operating pressure 110KPa, the operation temperature of heptane oil knockout tower bottom of towe is 150 DEG C, operating pressure 165KPa.
Other features of the present embodiment are identical with embodiment one, and details are not described herein.
The material balance table of the present embodiment is shown in Table 3, and can reach high-purity through the obtained alkane product of separation and Extraction
The requirement of degree.
Table 3：Material balance table：
The preferred embodiment and the explanation to institute's application technology principle that above description is only the application.Those skilled in the art should
Work as understanding, involved invention scope in the application, however it is not limited to the technical solution that the specific combination of above-mentioned technical characteristic forms,
It should also cover in the case where not departing from the inventive concept simultaneously, arbitrary group is carried out by above-mentioned technical characteristic or its equivalent feature
The other technical solutions closed and formed.Such as features described above has the skill of similar functions with (but not limited to) disclosed herein
The technical solution that art feature is replaced mutually and formed.
In addition to the technical characteristic described in specification, remaining technical characteristic is the known technology of those skilled in the art, is prominent
Go out the innovative characteristics of the present invention, details are not described herein for remaining technical characteristic.
Claims (10)
1. a kind of method that special solvent oil is extracted from stable light hydrocarbon, it is characterized in that, including：
Raw material stable light hydrocarbon is sent into weight-removing column, after weight-removing column detaches, light component oil is obtained in weight-removing column overhead condensation, de-
Weight tower bottom of towe obtains heavy aromatics, wherein, the operation temperature of weight-removing column tower top is 70-80 DEG C, operating pressure 100-110KPa, is taken off
The operation temperature of weight tower bottom of towe is 140-150 DEG C, operating pressure 155-165KPa；
The light component oil is sent into lightness-removing column, after lightness-removing column detaches, byproduct is obtained in lightness-removing column overhead condensation and stablizes gently
Hydrocarbon obtains C in lightness-removing column bottom of towe6-C7Component, wherein, the operation temperature of lightness-removing column tower top is 55-65 DEG C, operating pressure 235-
245KPa, the operation temperature of lightness-removing column bottom of towe is 110-120 DEG C, operating pressure 290-300KPa；
By the C6-C7Component is sent into dehexanizer, and after dehexanizer detaches, hexane oil is obtained in dehexanizer overhead condensation,
Heptane oil is obtained in dehexanizer bottom of towe, wherein, the operation temperature of dehexanizer tower top is 60-70 DEG C, operating pressure 100-
110KPa, the operation temperature of dehexanizer bottom of towe is 70-80 DEG C, operating pressure 155-165KPa；
The hexane oil is sent into hexane oil knockout tower, after the separation of hexane oil knockout tower, in the separation column overhead condensation of hexane oil
Isohexane is obtained, n-hexane is obtained in hexane oil knockout tower bottom of towe, wherein, the operation temperature of hexane oil separation column overhead is 85-
95 DEG C, operating pressure 100-110KPa, the operation temperature of hexane oil knockout tower bottom of towe is 100-115 DEG C, operating pressure is
155-165KPa；
The heptane oil is sent into heptane oil knockout tower, after the separation of heptane oil knockout tower, in the separation column overhead condensation of heptane oil
Isoheptane is obtained, normal heptane is obtained in heptane oil knockout tower bottom of towe, wherein, the operation temperature of heptane oil separation column overhead is 70-
80 DEG C, operating pressure 100-110KPa, the operation temperature of heptane oil knockout tower bottom of towe is 140-150 DEG C, operating pressure is
155-165KPa。
2. the method according to claim 1 that special solvent oil is extracted from stable light hydrocarbon, it is characterized in that, the de- weight
Tower, lightness-removing column, dehexanizer, hexane oil knockout tower and heptane oil knockout tower tower top, condensed on-condensible gas enters not
Out-of-bounds gas recovery system for oil is sent into after solidifying gas surge tank.
3. the method according to claim 1 that special solvent oil is extracted from stable light hydrocarbon, it is characterized in that, the de- weight
Tower, lightness-removing column, dehexanizer, hexane oil knockout tower and heptane oil knockout tower tower top, obtained product partly returns
Stream.
4. the method according to claim 1 that special solvent oil is extracted from stable light hydrocarbon, it is characterized in that, the light component
Oil is C6And following components, the heavy aromatics are C8-C12Component.
5. a kind of system that special solvent oil is extracted from stable light hydrocarbon, it is characterized in that, including weight-removing column, lightness-removing column, de- hexane
Tower, hexane oil knockout tower and heptane oil knockout tower, the tower top of the weight-removing column are connected with the lightness-removing column, the tower of the lightness-removing column
Bottom is connected with the dehexanizer, and the tower top of the dehexanizer is connected with the hexane oil knockout tower, the dehexanizer
Bottom of towe is connected with the heptane oil knockout tower；
Wherein, the top inside the weight-removing column is provided with epimere filling batch, and the lower part inside weight-removing column is provided with hypomere and fills out
Expect bed, liquid collecting distributer is provided between the epimere filling batch and hypomere filling batch, the liquid is collected
Distributor includes collecting part and distributed elements, and the distributed elements are mounted on the collecting part and the height of distributed elements
Less than collecting part, the collecting part collects the liquid of epimere filling batch bottom and is conducted into distributed elements, distribution portion
Part makes liquid be evenly distributed on hypomere filling batch.
6. the system according to claim 5 that special solvent oil is extracted from stable light hydrocarbon, it is characterized in that, the collection portion
Part includes the open slot that is made of bottom surface and side wall, and the space inside the open slot be the overall space being interconnected, described
Side wall is serpentine-like to be bent and forms end to end closed-loop, and the part that the side wall is located inside is inclined inwardly for bottom
Inclined surface, so as to form central collection slot at the middle part of collecting part；The distributed elements is uniformly mounted on collecting parts
The diversion pipe of side-wall outer side, the diversion pipe is vertically-mounted and the top of diversion pipe less than the side wall of collecting part top edge.
7. the system according to claim 6 that special solvent oil is extracted from stable light hydrocarbon, it is characterized in that, the center is received
Collection slot is arranged along a straight line, the sidewall symmetry arrangement of central collection slot both sides.
8. the system according to claim 6 that special solvent oil is extracted from stable light hydrocarbon, it is characterized in that, the diversion pipe
Tube wall crimp in the shape of a spiral.
9. the system according to claim 5 that special solvent oil is extracted from stable light hydrocarbon, it is characterized in that, the liquid is received
Integrate the vertical range between the bottom end of distributor and the top of the hypomere filling batch as H, 900mm≤H≤1100mm.
10. the system according to claim 5 that special solvent oil is extracted from stable light hydrocarbon, it is characterized in that, the de- weight
Tower, lightness-removing column, dehexanizer, hexane oil knockout tower and heptane oil knockout tower tower top be equipped with condenser and be connected with not
Solidifying gas surge tank, the fixed gas surge tank are connected to out-of-bounds gas recovery system for oil；
And/or the weight-removing column, lightness-removing column, dehexanizer, hexane oil knockout tower and heptane oil knockout tower tower top connect
It is connected to return tank.
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| CN111471483A (en) * | 2019-01-23 | 2020-07-31 | 内蒙古伊泰宁能精细化工有限公司 | Method for producing series of high-purity isoparaffins |
| CN112225633A (en) * | 2020-10-29 | 2021-01-15 | 洛阳金达石化有限责任公司 | Production method of normal hexane containing heptane raw material |
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| CN106824007A (en) * | 2017-02-22 | 2017-06-13 | 河北工业大学 | A kind of liquid distribution trough with mass transfer function |
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| CN204933481U (en) * | 2015-08-21 | 2016-01-06 | 天津科林泰克科技有限公司 | A kind of band is from the liquid distribution trough of distributed architecture |
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