CN207958177U - From the device for adding hydrogen Residual oil aromatics separation solvent naphtha and naphthalene Related product - Google Patents
From the device for adding hydrogen Residual oil aromatics separation solvent naphtha and naphthalene Related product Download PDFInfo
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- CN207958177U CN207958177U CN201721652399.7U CN201721652399U CN207958177U CN 207958177 U CN207958177 U CN 207958177U CN 201721652399 U CN201721652399 U CN 201721652399U CN 207958177 U CN207958177 U CN 207958177U
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Abstract
The utility model is related to a kind of from the device for adding hydrogen Residual oil aromatics separation solvent naphtha and naphthalene Related product, which includes：A) rectifying column；B) naphthalene tower is taken off, the bottom of tower extraction mouth connection of the de- naphthalene tower and a) the middle final tower kettle product of discharge, including feed inlet in the middle part of de- naphthalene tower, de- naphthalene tower tower reactor reboiler, de- naphthalene column overhead condenser takes off naphthalene column overhead and produces mouth, takes off naphthalene tower bottom of tower and produces mouth, the number of plates of de- naphthalene tower drawdown pump, the de- naphthalene tower is 40 55；C) the sequentially connected crystallization case of overhead extraction mouth of the de- naphthalene tower in and b).The isolated naphthane of device according to the present utility model and naphthalene product meet national standard.Therefore, the device of the utility model can greatly improve the economic benefit for adding hydrogen Residual oil and improve environment from the industrial products for adding extraction high added value in hydrogen Residual oil.
Description
Technical field
The utility model is related to rectifying purification technique fields, and in particular to a kind of from adding hydrogen Residual oil C9+ and C8+ to produce
The device of product aromatics separation solvent naphtha and naphthalene Related product.
Background technology
The production of traditional high boiling aromatic hydrocarbon solvent oil mainly relies on large-scale petrochemical device, to reform C9 and C10 or cracking
C9 is raw material.First pass through plus hydrogen lighting processing after, then to carry out rectifying isolated, complex process and processing cost compared with
It is high.And (Residual oil) C9+ and C8+ that by-product is refined with crude benzole hydrogenation have alkene and benzene content is low, form and aspect are relatively light, harmful substance
Content is low, good security and the advantages that without strong peculiar smell.
It is all to be directly used in petrol and diesel oil reconciliation to add hydrogen Residual oil in the past, some of important industrial chemicals such as trimethylbenzene, four
Hydrogen naphthalene and naphthalene are directly burnt up, and are not reasonably utilized not only, but also burning is not thorough and also pollutes the environment.It is how deep
Degree processing plus hydrogen Residual oil, it is the problem of this field faces at present therefrom to extract high value byproduct.
High boiling aromatic hydrocarbon solvent oil belongs to one kind of solvent naphtha, is mainly used for paint, printing ink and pesticide solvent
Class etc..Compared with the light aromatic solvents oil phase such as benzene and toluene, high boiling aromatic hydrocarbon solvent oil has toxicity low, and solvability is strong, waves
The advantages that sending out slow is more suitable for paint resin solvent and advanced off-set oil.When organic solvent as pesticide, high boiling aromatic hydrocarbons are molten
Agent oil is few to the user of pesticide and producer's health hazard, to environment also without larger hidden danger.Country has also promulgated decoration, agriculture
Medicine industry light aromatic solvent oil limit standard, so market will face bigger to the environment protection type high-boiling-point solvent oil of low benzene content
Demand.
Naphthane is ideal high boiling solvent, can be widely applied to paint, coating, ink and (is used as paint ink
Solvent), hard alloy (be used as hard alloy forming agent), medicine, the industrial circles such as papermaking, it is long-term by a variety of industries in the country
It uses.Naphthane is mainly used as production tetralone, also serves as the solvent of grease, wax, resin and paint, and can be with benzene and ethyl alcohol
Fuel with resulting mixture as internal combustion engine is also used as terebinthine substitute in glazing agent and coating.
Naphthalene is industrial most important hydrocarbon with condensed rings, mainly for the production of phthalic anhydride；Various naphthols；Naphthylamines etc. is production synthesis
Resin；Plasticizer；The intermediate of dyestuff；Surfactant；Synthetic fibers；Coating；Pesticide；Medicine；Fragrance；It rubber chemicals and kills
The raw material of worm agent.The purposes of naphthalene is distributed, and various countries are different.70% is substantially accounted for for produce phthalic anhydride, is used for dyestuff intermediate
Account for about 15% with rubber chemicals, insecticide accounts for about 6%, and tanning extracts accounts for about 4%.Using naphthalene as raw material, by sulfonation；Nitre
Change；Reduction；Amination；The unit operations such as hydrolysis, can be made a variety of intermediates.The application of refined naphthalene is also being widened, the super modeling of new product
Property material, that is, naphthalenesulfonate formaldehyde condensation compound, can be used as cement additive, it is strong without reducing it to increase the plastic deformation of concrete
Degree.
Therefore, naphthane and naphthalene are all the industrial products of high added value, there is various purposes.As can from hydrogen Residual oil is added
Advanced treating obtains the naphthane or naphthalene of high added value, can greatly improve economic benefit and improve environment.
Utility model content
Therefore, the purpose of this utility model is to provide a kind of from adding hydrogen Residual oil aromatics separation solvent naphtha and naphthalene Related product
Device.
One side according to the present utility model, providing one kind, hydrogen Residual oil aromatics separation solvent naphtha is related to naphthalene to be produced from adding
The device of product, which is characterized in that the device includes：
Rectifying column, wherein
It can be used a rectifying column, which includes middle part feed inlet, tower reactor reboiler, overhead condenser, and tower top is adopted
Outlet, tower side produce mouth, and bottom of tower produces mouth, and the number of plates of drawdown pump, the rectifying column is 60-80, or
First rectifying column and Second distillation column can also be used, the first rectifying column includes charging in the middle part of first rectifying column
Mouthful, first rectifying column tower reactor reboiler, first rectifying column overhead condenser, first rectifying column overhead extraction mouth, first rectifying column
Bottom of tower produces mouth, and the number of plates of first rectifying column drawdown pump, the first rectifying column is 45-65；The Second distillation column includes the
Feed inlet in the middle part of two rectifying columns, Second distillation column tower reactor reboiler, Second distillation column overhead condenser, Second distillation column tower top are adopted
Outlet, Second distillation column bottom of tower produce mouth, and the number of plates of Second distillation column drawdown pump, the Second distillation column is 50-70；Described
The first rectifying column bottom of tower extraction mouth of one rectifying column is connect with feed inlet in the middle part of the Second distillation column of the Second distillation column；Or
Third distillation column and the 4th rectifying column can also be used, the third distillation column includes charging in the middle part of third distillation column
Mouthful, third distillation column tower reactor reboiler, third distillation column overhead condenser, third distillation column overhead extraction mouth, third distillation column
Tower side produces mouth, and third distillation column bottom of tower produces mouth, and the number of plates of third distillation column drawdown pump, the third distillation column is 70-85；
4th rectifying column includes feed inlet in the middle part of the 4th rectifying column, and the 4th tower bottom of rectifying tower reboiler, the 4th rectifying column tower top is cold
Condenser, the 4th rectifying column tower top produce mouth, and the 4th rectifying tower bottom produces mouth, the 4th rectifying column drawdown pump, the 4th rectifying column
The number of plates be 50-70；The third distillation column bottom of tower extraction mouth of the third distillation column and the 4th essence of the 4th rectifying column
Evaporate feed inlet connection in the middle part of tower；
De- naphthalene tower, the de- naphthalene tower produce mouth with the bottom of tower that final tower kettle product is discharged in rectifying column and connect, the de- naphthalene
Tower includes feed inlet in the middle part of de- naphthalene tower, takes off naphthalene tower tower reactor reboiler, takes off naphthalene column overhead condenser, takes off naphthalene column overhead and produces mouth, takes off
Naphthalene tower bottom of tower produces mouth, takes off naphthalene tower drawdown pump, and the number of plates of the de- naphthalene tower is 40-55；
Case is crystallized, the crystallization case is connect with the overhead extraction mouth of the de- naphthalene tower.
Preferably, which further includes：
Bleaching tower or decoloration kettle, the bleaching tower or decoloration kettle are connect with the bottom of tower of de- naphthalene tower extraction mouth, wherein
In the case of bleaching tower, the bleaching tower includes feed inlet in the middle part of bleaching tower, bleaching tower tower reactor reboiler, decoloration
Column overhead condenser, bleaching tower overhead extraction mouth, bleaching tower bottom of tower produce mouth, bleaching tower drawdown pump, the number of plates of the bleaching tower
For 10-25；
In the case where decolourizing kettle, which includes heating mantle, condenser.
Preferably, the destilling tower uses the case where only one destilling tower；At this point it is possible to which the energy for reducing reboiler disappears
Consumption.
Preferably, the case where bleaching tower or the selection of decoloration kettle are using decoloration kettle；At this point, it is few with floor space,
Equipment investment is few, advantage easy to operate.
Preferably, in the device of the utility model, further include well known to a person skilled in the art other pumps, flowmeter,
The common element such as pressure gauge, heat exchanger, conduit, purposes and effect with it is in the prior art identical, details are not described herein.
The high boiling solvent 99% that device separation and Extraction according to the present utility model obtains is aromatic hydrocarbons mixture, benzene content
≤ 1%, sulfur content≤5ppm.The high boiling aromatic hydrocarbon solvent oil of different size has different flash-points, mixed aniline point and boiling range
Deng.Isolated naphthane and naphthalene product meets national standard.Therefore, the device of the utility model can be from adding in hydrogen Residual oil
The industrial products for extracting high added value greatly improve the economic benefit for adding hydrogen Residual oil and improve environment.
Device according to the present utility model introduced below is from the side for adding hydrogen Residual oil aromatics separation solvent naphtha and naphthalene Related product
Method.Wherein, described plus hydrogen Residual oil ingredient includes mainly benzene 0.001%-0.05%, toluene 0.08%-0.5%, ethylbenzene
0.057%-7.5%, Mixed XYLENE 0.2%-30.2%, 1,3,5- trimethylbenzene 2.30%-3.5%, 1,2,4- trimethylbenzene
3.32%-3.6%, indane 18.0%-41.52%, naphthane 10.0%-14.0%, naphthalene 6.03%-14.92%, 1- methyl
Naphthalene 0.59%-1.18%, 2- methyl naphthalene 1.56%-3.30%, other impurity 15.0%-17.8% etc. use the side of the device
Method includes：
A) product that boiling point is less than naphthalene is isolated in rectifying column, wherein
Using a rectifying column, described plus hydrogen Residual oil is fed in the middle part of tower, the temperature of tower reactor reboiler
It it is 135-155 DEG C, tower top temperature is 48-52 DEG C, tower top pressure 10-20kPa, reflux ratio 0.5-3.0, number of plates 60-
80, tower kettle product is pumped up into naphthalene rectifying column, overhead extraction S100# aromatic solvent naphthas, and it is 112-120 DEG C that tower side, which produces temperature,
Tower side produces S150# aromatic solvent naphthas；
It is described to add hydrogen Residual oil from first using two rectifying column, that is, first rectifying columns and Second distillation column
The middle part of rectifying column is fed, and the temperature of the tower reactor reboiler of the first rectifying column is 100-115 DEG C, tower top temperature 50-62
DEG C, tower top pressure 10-30kPa, reflux ratio 0.5-5.0, number of plates 45-65, overhead extraction S100# aromatic solvent naphthas,
Tower kettle product is pumped up into the 2nd rectifying column；The temperature of the tower reactor reboiler of 2nd rectifying column is 118-122 DEG C, tower top temperature
Be 75-85 DEG C, tower top pressure 10-30kPa, reflux ratio 1.0-3.0, number of plates 50-70, overhead extraction naphthane or
S150# aromatic solvent naphthas, tower kettle product are pumped up into de- naphthalene tower；Or
Use two rectifying columns in another situation, i.e. third distillation column and when four rectifying columns, described plus hydrogen Residual oil from
The middle part of third distillation column is fed, and the temperature of the tower reactor reboiler of the third distillation column is 100-120 DEG C, and tower top temperature is
35-40 DEG C, tower top pressure 10-30kPa, reflux ratio 1.0-5.0, number of plates 70-85, overhead extraction Mixed XYLENE, tower
It is 55-65 DEG C that side, which produces temperature, and tower side produces S100# aromatic solvent naphthas, and tower kettle product is pumped up into the 4th rectifying column；It is described
The temperature of the tower reactor reboiler of 4th rectifying column is 112-130 DEG C, and tower top temperature is 75-88 DEG C, tower top pressure 10-20kPa,
Reflux ratio is 1.0-5.0, number of plates 50-70, overhead extraction naphthane or S150# aromatic solvent naphthas, and tower kettle product is through pump
It is sent into and takes off naphthalene tower；
B) finally obtained tower kettle product in step a) is fed in the middle part of de- naphthalene tower, the tower reactor reboiler of the de- naphthalene tower
Temperature be 140-170 DEG C, tower top temperature be 95-110 DEG C, tower top pressure 10-60kPa, reflux ratio 0.5-8.0, column plate
Number is 40-55, and tower reactor obtains tower kettle product, and main component is S180# aromatic solvent naphthas；
C) liquid product of the overhead extraction of the de- naphthalene tower in step b) is being maintained the temperature at 85-100 DEG C under normal pressure
In the case of by high-temperature resistant pump be delivered directly to crystallization case in, in crystallizing case, at a temperature of normal pressure, 80-95 DEG C,
It is crystallized under 2.0-6.0m/h flow velocitys, to obtain the naphthalene product of the solid of 95% or more purity.
Preferably, this method further includes：
D) tower kettle product of the de- naphthalene tower is pumped up in bleaching tower or decoloration kettle, wherein
In the case of bleaching tower, the bottom temperature of the bleaching tower is 160-180 DEG C, and tower top temperature is 98-115 DEG C,
Tower top pressure is 10-60kPa, reflux ratio 1.0-5.0, number of plates 10-25, and tower top obtains S180# solvent naphthas, and tower reactor obtains
Tail oil；
In the case where decolourizing kettle, the heating temperature in the decoloration kettle is 160-190 DEG C, and pressure is de- for 10-60 kPa
The product that color kettle steams is S180# solvent naphthas, and the surplus materials of hardly possible evaporation is tail oil.
Preferably in step a), using a rectifying column, described plus hydrogen Residual oil is fed in the middle part of tower,
The temperature of tower reactor reboiler is 140-150 DEG C, and tower top temperature is 49-51 DEG C, tower top pressure 12-18kPa, reflux ratio 0.5-
3.0, number of plates 65-75, tower kettle product are pumped up into naphthalene rectifying column, overhead extraction S100# aromatic solvent naphthas, tower side extraction temperature
Degree is 114-118 DEG C, and tower side produces S150# aromatic solvent naphthas；
It is described to add hydrogen Residual oil from first using two rectifying column, that is, first rectifying columns and Second distillation column
The middle part of rectifying column is fed, and the temperature of the tower reactor reboiler of the first rectifying column is 105-110 DEG C, tower top temperature 52-60
DEG C, tower top pressure 15-25kPa, reflux ratio 0.5-5.0, number of plates 50-60, overhead extraction S100# aromatic solvent naphthas,
Tower kettle product is pumped up into Second distillation column；The temperature of the tower reactor reboiler of the Second distillation column is 119-121 DEG C, tower top temperature
Degree be 77-83 DEG C, tower top pressure 15-25kPa, reflux ratio 1.0-3.0, number of plates 55-65, overhead extraction naphthane or
S150# aromatic solvent naphthas, tower kettle product are pumped up into de- naphthalene tower；Or
Use two rectifying columns in another situation, i.e. third distillation column and when four rectifying columns, described plus hydrogen Residual oil from
The middle part of third distillation column is fed, and the temperature of the tower reactor reboiler of the third distillation column is 105-115 DEG C, and tower top temperature is
36-39 DEG C, tower top pressure 15-25kPa, reflux ratio 1.0-5.0, number of plates 75-80, overhead extraction Mixed XYLENE, tower
It is 57-63 DEG C that side, which produces temperature, and tower side produces S100# aromatic solvent naphthas, and tower kettle product is pumped up into the 4th rectifying column；It is described
The temperature of the tower reactor reboiler of 4th rectifying column is 118-124 DEG C, and tower top temperature is 79-84 DEG C, tower top pressure 15-25kPa,
Reflux ratio is 1.0-5.0, number of plates 55-65, overhead extraction naphthane or S150# aromatic solvent naphthas, and tower kettle product is through pump
It is sent into and takes off naphthalene tower；
Preferably, in step b), finally obtained tower kettle product in step a) is fed in the middle part of de- naphthalene tower, it is described de-
The temperature of the tower reactor reboiler of naphthalene tower is 152-158 DEG C, and tower top temperature is 100-105 DEG C, tower top pressure 25-35kPa, reflux
Than for 1-8.0, number of plates 45-50, tower reactor obtains tower kettle product, main component is S180# aromatic solvent naphthas；
Preferably, in step c), the liquid product of the overhead extraction of the de- naphthalene tower in step b) is being protected under normal pressure
Hold temperature in the case of 90-95 DEG C or more by high-temperature resistant pump be delivered directly to crystallization case in, in crystallizing case, normal pressure,
It at a temperature of 82-90 DEG C, is crystallized under 2.5-6.0m/h flow velocitys, to obtain the naphthalene product of the solid of 95% or more purity.
Description of the drawings
Fig. 1 is the figure according to the separator of an embodiment of the utility model；
Fig. 2 is the figure according to the separator of the another embodiment of the utility model；
Fig. 3 is the figure according to the separator of the another embodiment of the utility model.
Specific implementation mode
The utility model will be described below by specific implementation mode, but following embodiment is only used for describing this practicality newly
Type, rather than limit the scope of the utility model.
Fig. 1 shows the schematic diagram of the device of an embodiment of the utility model.In Fig. 1, hydrogen Residual oil is added to detach
Device includes that 1 lightness-removing column of tower (i.e. first rectifying column), 2 naphthane tower (i.e. Second distillation column) of tower, tower 3 take off naphthalene tower, 4 bleaching tower of tower
With crystallization case.1 lightness-removing column of the tower is fed from middle part, and bottom of tower discharge port is connected with feed inlet in the middle part of naphthane tower；Naphthane tower
Bottom discharge mouth is connected with feed inlet in the middle part of de- naphthalene tower；De- naphthalene tower bottom discharge port is connected with feed inlet in the middle part of bleaching tower.Each tower
Bottom of tower be connected to respectively with reboiler, the tower top of above-mentioned tower 1, tower 2 and tower 4 is connected to condenser respectively, and the tower 3 takes off naphthalene tower
Tower top is connect with crystallization case.
Fig. 2 shows the schematic diagrames of the device of the another embodiment of the utility model.In fig. 2, separator master
To include aromatic solvent naphtha tower I (i.e. rectifying column), aromatic solvent naphtha tower II (i.e. de- naphthalene tower), crystallization case；Wherein aromatic solvent naphtha
The bottom of tower extraction mouth of tower I is connect with aromatic solvent naphtha tower II；The overhead extraction mouth of the aromatic solvent naphtha tower II connects with crystallization case
It connects, the bottom of tower extraction mouth of the aromatic solvent naphtha tower II is connect with product storage tank (not shown).The bottom of tower of each tower respectively with boil again
Device is connected to, and the tower top of each tower is connected to condenser respectively.
Fig. 3 shows the schematic diagram of the device of the another embodiment of the utility model.In figure 3, add hydrogen Residual oil point
Include lightness-removing column (i.e. third distillation column), naphthane tower (i.e. the 4th rectifying column), de- naphthalene tower, decoloration kettle and crystallization case from device.
The lightness-removing column of Fig. 3 is fed from middle part, and bottom of tower discharge port is connected with feed inlet in the middle part of naphthane tower；Naphthane tower bottom goes out
Material mouth is connected with feed inlet in the middle part of de- naphthalene tower；De- naphthalene tower bottom discharge port is connected with decoloration kettle feed inlet.The bottom of tower of above-mentioned each tower
It is connected to respectively with reboiler, the top of lightness-removing column, naphthane tower and the kettle that decolourizes is connected to condenser respectively, the tower of the de- naphthalene tower
Top is connect with crystallization case.
Embodiment 1
As shown in Figure 1, plus hydrogen separator for residual oil includes 1 lightness-removing column of tower, 2 naphthane tower of tower, tower 3 takes off naphthalene tower and tower 4 is de-
Color tower.1 lightness-removing column of the tower is fed from middle part, and bottom of tower discharge port is connected with feed inlet in the middle part of naphthane tower；Naphthane tower bottom
Discharge port is connected with feed inlet in the middle part of de- naphthalene tower；De- naphthalene tower bottom discharge port is connected with feed inlet in the middle part of bleaching tower.It is above-mentioned all kinds of
Bottom of tower is connected to reboiler respectively, and the tower top of each tower is connected to condenser respectively in addition to tower 3, the condenser and vacuum system
Connection.Major product 1-5 is respectively S100#, naphthane (or S150#), crude naphthalene (or refined naphthalene), S180# solvent naphthas and tail
Oil.S100# solvent naphtha water white transparencies, density 0.86-0.87 boiling ranges are 155 DEG C -180 DEG C；S150# solvent naphthas are water white transparency liquid
Body main component is naphthane, and density 0.875-0.910, boiling range is 180-210 DEG C；S180# yellowish transparency liquids, it is close
0.915-0.935 is spent, boiling range is 195-245 DEG C.Specific separation scheme includes the following steps：
1. hydrogen C9+ will be added to enter in tower in the middle part of lightness-removing column, lightness-removing column top operating pressure (10~30Kpa), reflux ratio
(0.5-5.0), tower top temperature (50~62 DEG C), bottom temperature (100~115 DEG C), it is low boiling point solvent oil that tower top, which obtains product,
Fraction A, mainly S100# solvent naphthas.Kettle material is mainly methyl indan, naphthane, naphthalene and heavy oil etc..
2. by the tower reactor material of 1 step by being sent into the middle part of naphthane tower, naphthane knockout tower operating pressure (10~15KPa) is returned
Stream is naphthalene, first than (1.0-3.0) tower top temperature (80~85 DEG C), bottom temperature (118~122 DEG C), kettle material key component
Base naphthalene etc.
3. the tower reactor material of 2 steps is transported to feed inlet in the middle part of de- naphthalene tower.This tower top operating pressure (50~60Kpa), tower top
Temperature (130~135 DEG C), bottom temperature (130~140 DEG C) are the high boiling fraction of C11 or more in tower reactor at this time.Tower top obtains
Be main fractions to naphthalene, crude naphthalene or refined naphthalene can be produced according to market situation by entering back into crystallization case, isolate in addition to naphthalene
Component enter in head tank.
4. the tower reactor material of 3 steps is transported to feed inlet in the middle part of bleaching tower.This tower top operating pressure (10~20Kpa), tower top
Temperature (90~110 DEG C), it is main fractions that bottom temperature (160~180 DEG C) tower top, which obtains S180# solvent naphthas, and secondary fraction also may be used
To produce the high boiling aromatic hydrocarbon solvent oil of different boiling range sections according to the requirement of different clients.Tower reactor product is the very deep tail of color
Oil.
In the present embodiment 1, hydrogen Residual oil is added to mainly contain Mixed XYLENE 0.2%-30.2%, 1,3,5- trimethylbenzene 2.30%-
3.5%, 1,2,4- trimethylbenzene 3.32%-3.6%, indane 18.0%-41.52%, naphthane 10.0%-14.0%, naphthalene
6.03%-14.92%, 1- methyl naphthalene 0.59%-1.18%, 2- methyl naphthalene 1.56%-3.30%, other impurity 15.0%-
17.8% etc..The utility model takes off four rectifying columns of naphthalene tower and bleaching tower and carries out separating-purifying by lightness-removing column, naphthane tower,
Isolated naphthane and naphthalene purity respectively reach 95% or more, and other products are as high boiling aromatic hydrocarbon solvent oil product, finally
Tail oil product can be used for pitch and pitch extension product.The advantageous effect of this programme is：The utility model has operation letter
Just, the features such as investment poor benefit is high, product purity height and high process brakingization degree.Separation process operation temperature is relatively low,
Low energy consumption, has preferable economic benefit and social benefit.
Embodiment 2
As shown in Fig. 2, separator includes mainly aromatic solvent naphtha I towers, aromatic solvent naphtha II towers (de- naphthalene tower), crystallization
Case；The equal output addition product of aromatic solvent naphtha I column overheads, side line, tower reactor material enter aromatic solvent naphtha II towers through pump；Aromatic solvent
Oily II column overheads produce the crystallized case output high-purity naphthalene product of product, and tower reactor material is delivered to product storage tank through pump；Aromatic solvent
Oily I towers, aromatic solvent naphtha II towers operate under negative pressure；Product extraction is connected with cooler.
Raw material C9 is through being pumped into aromatic solvent naphtha I towers, 10~20Kpa of operating pressure of tower top, tower top temperature 48~52
DEG C, reflux ratio is 0.5~3.0, and overhead extraction product is solvent naphtha 100# aromatic solvent naphthas, and key component is dimethylbenzene, front three
Benzene and indane etc.；For tower side take-off controlled at 112~120 DEG C, extraction product is solvent naphtha S150# aromatic solvent naphthas, main
Will group be divided into methyl indan and naphthane etc.；Bottom temperature is 135~155 DEG C, and material group becomes naphthalene and methyl naphthalene etc., tower reactor master
Heat source is provided by conduction oil, exchanged heat in tower reactor reboiler.Material enters aromatic solvent naphtha II towers through pump.
Enter aromatic solvent naphtha II towers through pump from aromatic solvent naphtha I tower tower reactor material, the operating pressure 40Kpa of tower top~
50Kpa, 130~140 DEG C of tower top temperature, reflux ratio be 0.5~5.0, overhead extraction material enter crystallization case obtain crude naphthalene or
Refined naphthalene；Bottom temperature is 155~180 DEG C, and material composition is mainly the S180# high boiling aromatic hydrocarbon solvent oil of C14+, is conveyed through pump
To product storage tank.
In example 2, the composition of crude benzole hydrogenation by-product C9+ raw materials is as shown in table 1 below.
Table 1
| Serial number | Substance | Accounting % | Serial number | Substance | Accounting % |
| 1 | Benzene | 0 | 7 | Indane | 27.705 |
| 2 | Toluene | 0.01 | 8 | Naphthane | 19.38 |
| 3 | Ethylbenzene | 0.02 | 9 | Naphthalene | 15.392 |
| 4 | Mixed XYLENE | 0.04 | 10 | 1- methyl naphthalenes | 2.21 |
| 5 | 1.3.5 trimethylbenzene | 2.64 | 11 | 2- methyl naphthalenes | 1.92 |
| 6 | 1.2.4 trimethylbenzene | 3.47 | 12 | Other | 27.203 |
The step of by embodiment 2, the composition of the major product of acquisition is as shown in table 2.
Table 2
| Serial number | Name of product | Accounting |
| 1 | S100# aromatic solvent naphthas | 56.06% |
| 2 | S150# aromatic solvent naphthas | 11.14% |
| 3 | Crude naphthalene | 16.15% |
| 5 | S180 aromatic solvent naphthas | 16.65% |
| It amounts to | 100% |
Embodiment 3
As shown in figure 3, the separator includes lightness-removing column, naphthane tower takes off naphthalene tower and bleaching tower.In embodiment 3,
Lightness-removing column can detach dimethylbenzene, and Mixed XYLENE, 80% or more Mixed XYLENE accounting are obtained from overhead extraction.And naphthane tower
The content that naphthane can be changed by adjusting operating parameter, to obtain whether naphthane or S150 solvent naphthas (have specific
Which kind of experimental data such as obtain naphthane under the conditions of, which kind of is obtained S150 solvent naphthas under the conditions of).De- naphthalene tower can also lead to
It overregulates relevant parameter and obtains crude naphthalene or refined naphthalene.Decoloration kettle then deviates from S180 solvent naphthas macromolecular chain similar to the object of pitch
Matter improves solvent oil quality.
The specific separation method of embodiment 3 is as follows：
Raw material adds hydrogen Residual oil to enter in the middle part of lightness-removing column, and top of tower temperature is 35~40 DEG C, and pressure is 10KPa~20KPa.
Between reflux ratio is 1.0~5.0.Overhead product is mainly Mixed XYLENE, and product boiling range is mainly controlled at 120~140 DEG C, wherein
Mixed XYLENE accounting is 80 or more, as market plus hydrogen Mixed XYLENE quality.Side take-off temperature is controlled at 55-65 DEG C, production
Product are S100# aromatic solvent naphthas.Lightness-removing column tower reactor is heated using conduction oil, and tower bottom reboiler is main heating equipment.Tower
Kettle temperature degree is controlled at 100~115 DEG C.Lightness-removing column product is mixture, and product is obtained by way of side take-off can be significantly
Reduce equipment investment and energy consumption.Kettle material is pumped by conveying in the middle part of naphthane tower again.
Naphthane column overhead operation temperature be 75-88 DEG C, pressure be 10KPa~20Kpa, reflux ratio be 1.0-5.0 it
Between.Major product is naphthane.This tower naphthane purity can reach 95% or more, and reflux ratio can be reduced according to market situation and is carried
To rise tower top temperature reduce naphthane purity, to produce S150# solvent naphthas.Tower reactor is also to be heated by reboiler, conduction oil
Improve heat source.Bottom temperature is controlled at 112~130 DEG C.
Naphthane tower reactor material is transported to feed inlet in the middle part of de- naphthalene tower.This tower top operating pressure (50~60Kpa), tower top temperature
(130~135 DEG C), bottom temperature (130~150 DEG C) are the high boiling fraction of C11 or more in tower reactor at this time.Tower top obtains naphthalene
Main fractions, crude naphthalene or refined naphthalene, the component in addition to naphthalene isolated can be produced according to market situation by entering back into crystallization case
Into in head tank.
De- naphthalene tower tower reactor material is transported in decoloration kettle.Decoloration kettle has heating mantle, controls temperature in the kettle after being passed through conduction oil
Limpid S180# aromatic solvent naphthas are steamed at 150~180 DEG C, in kettle.The tail oil of difficult evaporation is transported to production by high-temperature resistant pump in kettle
Product tank field, tail oil can be used for pitch processing or production anti-decaying paint.Decolourizing, kettle is less with floor space, and equipment investment is few, operation
Easy feature.
Claims (5)
1. a kind of from the device for adding hydrogen Residual oil aromatics separation solvent naphtha and naphthalene Related product, which is characterized in that the device includes：
Rectifying column, wherein the rectifying column includes middle part feed inlet, tower reactor reboiler, overhead condenser, overhead extraction mouth, tower side
Mouth is produced, bottom of tower produces mouth, and the number of plates of drawdown pump, the rectifying column is 60-80,
De- naphthalene tower, the de- naphthalene tower connects with the bottom of tower of rectifying column extraction mouth, the de- naphthalene tower include take off naphthalene tower middle part into
Material mouth takes off naphthalene tower tower reactor reboiler, takes off naphthalene column overhead condenser, takes off naphthalene column overhead and produces mouth, takes off naphthalene tower bottom of tower and produces mouth, takes off naphthalene
The number of plates of tower drawdown pump, the de- naphthalene tower is 40-55；
Case is crystallized, the crystallization case is connect with the overhead extraction mouth of the de- naphthalene tower.
2. a kind of from the device for adding hydrogen Residual oil aromatics separation solvent naphtha and naphthalene Related product, which is characterized in that the device includes：
Rectifying column, wherein
The rectifying column includes first rectifying column and Second distillation column, and the first rectifying column includes charging in the middle part of first rectifying column
Mouthful, first rectifying column tower reactor reboiler, first rectifying column overhead condenser, first rectifying column overhead extraction mouth, first rectifying column
Bottom of tower produces mouth, and the number of plates of first rectifying column drawdown pump, the first rectifying column is 45-65；The Second distillation column includes the
Feed inlet in the middle part of two rectifying columns, Second distillation column tower reactor reboiler, Second distillation column overhead condenser, Second distillation column tower top are adopted
Outlet, Second distillation column bottom of tower produce mouth, and the number of plates of Second distillation column drawdown pump, the Second distillation column is 50-70；Described
The first rectifying column bottom of tower extraction mouth of one rectifying column is connect with feed inlet in the middle part of the Second distillation column of the Second distillation column；
De- naphthalene tower, the de- naphthalene tower are connect with the Second distillation column bottom of tower of Second distillation column extraction mouth, the de- naphthalene tower packet
Feed inlet in the middle part of de- naphthalene tower is included, naphthalene tower tower reactor reboiler is taken off, takes off naphthalene column overhead condenser, naphthalene column overhead is taken off and produces mouth, take off naphthalene tower
Bottom of tower produces mouth, takes off naphthalene tower drawdown pump, and the number of plates of the de- naphthalene tower is 40-55；
Case is crystallized, the crystallization case is connect with the overhead extraction mouth of the de- naphthalene tower.
3. a kind of from the device for adding hydrogen Residual oil aromatics separation solvent naphtha and naphthalene Related product, which is characterized in that the device includes：
Rectifying column, wherein
The rectifying column includes third distillation column and the 4th rectifying column, and the third distillation column includes charging in the middle part of third distillation column
Mouthful, third distillation column tower reactor reboiler, third distillation column overhead condenser, third distillation column overhead extraction mouth, third distillation column
Tower side produces mouth, and third distillation column bottom of tower produces mouth, and the number of plates of third distillation column drawdown pump, the third distillation column is 70-85；
4th rectifying column includes feed inlet in the middle part of the 4th rectifying column, and the 4th tower bottom of rectifying tower reboiler, the 4th rectifying column tower top is cold
Condenser, the 4th rectifying column tower top produce mouth, and the 4th rectifying tower bottom produces mouth, the 4th rectifying column drawdown pump, the 4th rectifying column
The number of plates of rectifying column is 50-70；Third distillation column bottom of tower extraction mouth and the 4th rectifying column of the third distillation column
Feed inlet connection in the middle part of 4th rectifying column；
De- naphthalene tower, the de- naphthalene tower are connect with the 4th rectifying tower bottom of the 4th rectifying column extraction mouth, the de- naphthalene tower packet
Feed inlet in the middle part of de- naphthalene tower is included, naphthalene tower tower reactor reboiler is taken off, takes off naphthalene column overhead condenser, naphthalene column overhead is taken off and produces mouth, take off naphthalene tower
Bottom of tower produces mouth, takes off naphthalene tower drawdown pump, and the number of plates of the de- naphthalene tower is 40-55；
Case is crystallized, the crystallization case is connect with the overhead extraction mouth of the de- naphthalene tower.
4. device according to any one of claim 1-3, which is characterized in that the device further includes：
Bleaching tower, the bleaching tower are connect with the bottom of tower of de- naphthalene tower extraction mouth, wherein
The bleaching tower includes feed inlet in the middle part of bleaching tower, bleaching tower tower reactor reboiler, bleaching tower overhead condenser, bleaching tower tower
Top extraction mouth, bleaching tower bottom of tower produce mouth, and the number of plates of bleaching tower drawdown pump, the bleaching tower is 10-25.
5. device according to any one of claim 1-3, which is characterized in that the device further includes：
Decolourize kettle, and the decoloration kettle is connect with the bottom of tower of de- naphthalene tower extraction mouth, wherein
The decoloration kettle includes heating mantle, condenser.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721652399.7U CN207958177U (en) | 2017-12-01 | 2017-12-01 | From the device for adding hydrogen Residual oil aromatics separation solvent naphtha and naphthalene Related product |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721652399.7U CN207958177U (en) | 2017-12-01 | 2017-12-01 | From the device for adding hydrogen Residual oil aromatics separation solvent naphtha and naphthalene Related product |
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| CN207958177U true CN207958177U (en) | 2018-10-12 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109867580A (en) * | 2017-12-01 | 2019-06-11 | 唐山旭阳化工有限公司 | From the method and apparatus for adding hydrogen Residual oil aromatics separation solvent naphtha and naphthalene Related product |
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2017
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109867580A (en) * | 2017-12-01 | 2019-06-11 | 唐山旭阳化工有限公司 | From the method and apparatus for adding hydrogen Residual oil aromatics separation solvent naphtha and naphthalene Related product |
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