CN208362256U - The system of coal tar dehydration - Google Patents
The system of coal tar dehydration Download PDFInfo
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- CN208362256U CN208362256U CN201820864538.0U CN201820864538U CN208362256U CN 208362256 U CN208362256 U CN 208362256U CN 201820864538 U CN201820864538 U CN 201820864538U CN 208362256 U CN208362256 U CN 208362256U
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Abstract
The utility model discloses the systems of coal tar dehydration.It include: to include at least sequentially connected mixed cell, first order water-oil separating unit and second level water-oil separating unit；Wherein, water-soluble demulsifier, water and coal tar to be processed are mixed by the mixed cell, obtain mixed material；The mixed material carries out separating treatment by the first order water-oil separating unit, obtains aqueous phase；The aqueous phase carries out separating treatment by the second level water-oil separating unit, to deviate from water.The system of coal tar dehydration provided by the utility model, can be improved the dehydrating effect to coal tar, while can take into account the effect for improving dechlorination, de- slag.
Description
Technical field
The utility model relates to the systems that coal tar dehydration technique field more particularly to a kind of coal tar are dehydrated.
Background technique
The viscous liquid of a kind of black or dark brown that coal tar is coal to be obtained through destructive distillation.The composition of coal tar is very rich
Richness, wherein the type of hydrocarbon is up to up to ten thousand kinds, therefore becomes a kind of important source material of coal chemical industry.
A large amount of water is usually contained in coal tar, this, which utilizes the following process of coal tar, has very detrimental effect.
Therefore it before coal tar carries out following process, needs to remove in water therein.The dehydration of existing coal tar dewatering system is imitated
Fruit is undesirable, therefore, it is necessary to provide a kind of system of New type coal dehydration of tar.
Utility model content
The utility model embodiment provides a kind of system of coal tar dehydration, can be improved the dehydrating effect of coal tar.
The utility model embodiment provides a kind of system of coal tar dehydration, which includes at least sequentially connected mixed
Close unit, first order water-oil separating unit and second level water-oil separating unit；Wherein, water-soluble demulsifier, water and coal to be processed
Tar is mixed by mixed cell, obtains mixed material, and mixed material is separated by first order water-oil separating unit
Processing obtains aqueous phase, and aqueous phase carries out separating treatment by second level water-oil separating unit, to deviate from water.
One aspect according to the present utility model, first order water-oil separating unit include three-phase centrifuge, three-phase centrifuge
Import and mixed cell outlet connect, for by mixed material carry out three phase separation processing with obtain aqueous phase, residual oil and
Heavy oil；
Second level water-oil separating unit includes light oil device for phase saparation, the import of light oil device for phase saparation and three-phase centrifuge
Aqueous phase export connection, for by aqueous phase carry out separating treatment to deviate from water, obtain light oil.
One aspect according to the present utility model, first order water-oil separating unit include standing tank, stand the import of tank with
The outlet of mixed cell connects, for mixed material to be carried out two-phase laminated flow processing to obtain the first aqueous phase and second aqueous
Phase；
Second level water-oil separating unit includes three-phase centrifuge and light oil device for phase saparation, wherein three-phase centrifuge into
Mouth is exported with the first aqueous phase for standing tank and is connected, for the first aqueous phase to be carried out separating treatment to deviate from water and residual oil, obtain
To heavy oil, the import of light oil device for phase saparation and the second aqueous phase for standing tank are exported and are connected, for carrying out the second aqueous phase
Separating treatment is to deviate from water, obtain light oil.
One aspect according to the present utility model, first order water-oil separating unit include the first two-phase centrifuge, first liang
The import of phase centrifuge and the outlet of mixed cell connect, for mixed material to be carried out two-phase laminated flow processing to obtain aqueous phase
With heavy oil phase；
Second level water-oil separating unit include the second two-phase centrifuge and light oil device for phase saparation, wherein the second two-phase from
The import of scheming is mutually exported with the heavy oil of the first two-phase centrifuge and is connect, for heavy oil mutually to be carried out to separating treatment to deviate from slag
Oil obtains heavy oil, and the import of light oil device for phase saparation and the aqueous phase outlet of the first two-phase centrifuge are connected, be used for aqueous phase
Separating treatment is carried out to deviate from water, obtain light oil.
One aspect according to the present utility model, light oil device for phase saparation are settle and separate tank or two-phase centrifuge.
One aspect according to the present utility model, mixed cell include mixing apparatus, and mixing apparatus is blending tank, static state is mixed
Clutch or online mixer.
One aspect according to the present utility model, mixed cell further include solution dosing apparatus, and solution dosing apparatus goes out
Mouth is connect with the demulsifier aqueous solution import of mixing apparatus, water-soluble to obtain demulsifier for mixing water-soluble demulsifier with water
Liquid.
The water out of one aspect according to the present utility model, second level water-oil separating unit is connected to mixing list through pipeline
The water inlet of member.
One aspect according to the present utility model, the water out of second level water-oil separating unit and the water inlet of mixed cell
Between be additionally provided with demineralization plant.
One aspect according to the present utility model, system further include heating module, for coal tar to be processed to be heated to
50 DEG C~90 DEG C.
The system of coal tar dehydration provided by the embodiment of the utility model, can be improved the dehydrating effect to coal tar, together
When also take into account the effect improved to coal tar dechlorination, de- slag.
Detailed description of the invention
It, below will be in the utility model embodiment in order to illustrate more clearly of the technical solution of the utility model embodiment
Required attached drawing is briefly described, for those of ordinary skill in the art, what is do not made the creative labor
Under the premise of, it is also possible to obtain other drawings based on these drawings.
Fig. 1 shows the system flow chart of the coal tar dehydration of the utility model one embodiment.
Fig. 2 shows the system flow charts of the coal tar of second embodiment of the utility model dehydration.
Fig. 3 shows the system flow chart of the coal tar dehydration of the utility model third embodiment.
Fig. 4 shows the system flow chart of the coal tar dehydration of the 4th embodiment of the utility model.
Fig. 5 shows the system flow chart of the coal tar dehydration of the 5th embodiment of the utility model.
Fig. 6 shows the system flow chart of the coal tar dehydration of the 6th embodiment of the utility model.
Fig. 7 shows the system flow chart of the coal tar dehydration of the 7th embodiment of the utility model.
Fig. 8 shows the system flow chart of the coal tar dehydration of the 8th embodiment of the utility model.
Fig. 9 shows the system flow chart of the coal tar dehydration of the 9th embodiment of the utility model.
In these flow charts, identical label represents identical meaning.Label declaration is as follows:
10, mixed cell；
11, solution dosing apparatus；12, mixing apparatus；
20, first order water-oil separating unit；
21, three-phase centrifuge；22, tank is stood；23, the first two-phase centrifuge；
30, second level water-oil separating unit；
31, light oil device for phase saparation；32, three-phase centrifuge；33, the second two-phase centrifuge；
111, demulsifier original agent tank；112, solution preparing tank；121, pipeline online mixer；113, demulsifier metering pump；
114, coal tar raw material tank；115, coal tar raw material pumps；201, mixed material surge tank；211, three-phase centrifuge；310, light oil
Phase surge tank；311, two-phase centrifuge；401, residual oil slot；402, heavy oil tank；403, light oil tank；404, Water Tank；405, sewage
Pump；
A, water；B, water-soluble demulsifier；C, coal tar to be processed；D1, heavy oil；D2, light oil；E, residual oil；F, deviate from water；
F1, the first abjection water；F2, the second abjection water；G, light oil phase；H, heavy oil phase.
Specific embodiment
The feature and exemplary embodiment of the various aspects of the utility model is described more fully below, in order to keep this practical new
The objects, technical solutions and advantages of type are more clearly understood, and with reference to the accompanying drawings and embodiments, carry out the utility model into one
Step detailed description.It should be understood that specific embodiment described herein is only configured to explain the utility model, it is not configured as
Limit the utility model.To those skilled in the art, the utility model can be in not needing these details
Implement in the case where some details.Below the description of embodiment is used for the purpose of mentioning by showing the example of the utility model
For being better understood to the utility model.
It should be noted that, in this document, relational terms such as first and second and the like are used merely to a reality
Body or operation are distinguished with another entity or operation, are deposited without necessarily requiring or implying between these entities or operation
In any actual relationship or order or sequence.Moreover, the terms "include", "comprise" or its any other variant are intended to
Non-exclusive inclusion, so that the process, method, article or equipment including a series of elements is not only wanted including those
Element, but also including other elements that are not explicitly listed, or further include for this process, method, article or equipment
Intrinsic element.In the absence of more restrictions, the element limited by sentence " including ... ", it is not excluded that including
There is also other identical elements in the process, method, article or equipment of the element.
For simplicity, some numberical ranges are only expressly disclosed herein.However, any lower limit can be with any upper limit group
Close the range for being formed and being not known and recording；And any lower limit can form the range for being not known and recording with other lower values, together
Any upper limit of sample can combine the range to be formed and not yet explicitly be recorded with any other upper limit.In addition, recorded although being not known,
Each point or single number between endpoints of ranges are included within the scope of this.Thus, each point or single number can be used as certainly
The lower limit or the upper limit of body, which combine with any other point or single number or combine to be formed with other lower limits or the upper limit, not yet explicitly to be recorded
Range.
In description herein, unless otherwise indicated, " more than ", it is " following " for comprising this number, it is " several in " one or more "
Kind " it is meant that two or more.
The above-mentioned utility model content of the utility model is not intended to the disclosed implementation of each of description the utility model
Mode or every kind of implementation.Illustrative embodiments are more particularly exemplified described below.Many places in entire chapter application,
Guidance is provided by a series of embodiments, these embodiments can use in a variety of combinations.In various embodiments, it enumerates
Only as representative group, exhaustion should not be construed as.
It is described in detail below in conjunction with Fig. 1 to Fig. 9 system being dehydrated to coal tar provided by the embodiment of the utility model.
Fig. 1 schematically shows the system flow chart of the coal tar dehydration of the utility model one embodiment.It please join
According to Fig. 1, the system for the coal tar dehydration that the utility model one embodiment provides includes sequentially connected mixed cell 10, the
Level-one water-oil separating unit 20 and second level water-oil separating unit 30.
Water-soluble demulsifier b, water a and coal tar c to be processed are respectively fed in mixed cell 10, it is single by mixing
Member 10 carries out uniformly mixed, obtains mixed material.In the mixed material, the concentration of demulsifier be 400 μ of μ g/g~2000 g/g and
The mass ratio of demulsifier and water is 1~15:100.Mixed cell 10 can be using well known to a person skilled in the art mixing to set
Standby 12, for example, water-soluble demulsifier b, water a and coal tar c to be processed are added in blending tank, keep it mixed by standing or stirring
It closes uniform.For another example carrying out water-soluble demulsifier, water using mixing apparatus such as static mixer, online mixers and wait locate
Manage the mixing of coal tar.
Referring to figure 2., mixed cell 10 optionally includes solution dosing apparatus 11, the outlet of solution dosing apparatus 11 and mixed
The demulsifier aqueous solution import connection of equipment 12 is closed, it is water-soluble to obtain demulsifier for being mixed with water a water-soluble demulsifier b
Liquid.Wherein in demulsifier aqueous solution, the mass ratio of demulsifier and water is 1~15:100.Preferably, every 100ml demulsifier water
Contain 1.0g~10.0g demulsifier in solution.Solution dosing apparatus 11 can be using well known to a person skilled in the art be used for
The equipment that solution is prepared.For example, water-soluble demulsifier b and water a is added in solution preparing tank, keep it mixed by standing or stirring
It closes uniform.For another example carrying out the mixed of water-soluble demulsifier b and water a using mixers such as static mixer, online mixers
It closes.Water a and water-soluble demulsifier b are sent in solution dosing apparatus 11, is uniformly mixed, obtains demulsifier aqueous solution.Then
Demulsifier aqueous solution is sent into mixing apparatus 12 and is mixed with coal tar to be processed, mixed material is obtained.In mixed material
The concentration of demulsifier is 400 μ of μ g/g~2000 g/g.The demulsification of demulsifier can be further increased in this way and shortens demulsification
Time further increases the dehydrating effect of coal tar.
Coal tar to be processed is heated to 50 DEG C~90 DEG C by heating module, such as 50 DEG C~80 DEG C, can further be mentioned
Height demulsification efficiency and oil-water separation, while improving the yield and purity of dehydrated coal tar.Heating module can be such as heating
Component or heat exchanger.Such as can be and be provided with heating component, such as steam pipe coil on the head tank of coal tar c to be processed, it uses
In before mixing water-soluble demulsifier b, water a with coal tar c to be processed, coal tar c to be processed is heated to 50 DEG C~90
℃.It is of course also possible to be that heat exchanger is arranged between the head tank and mixing apparatus 12 of coal tar c to be processed, treated to realize
Handle the heating of coal tar c.Aforesaid heat exchangers can be the equipment as known in the art for heat exchange, as fountain exchanges heat
Device, plate heat exchanger, shell-and-tube heat exchanger etc..It can also be and be provided with heating component on mixing apparatus 12, it is water-soluble for making
Property demulsifier b, water a and coal tar c to be processed 50 DEG C~90 DEG C at a temperature of mixed, or water-soluble demulsifier b,
After water a is mixed with coal tar c to be processed, mixed material is heated to 50 DEG C~90 DEG C.Be also possible to mixing apparatus 12 it
After heat exchanger is set, mixed material is heated to 50 DEG C~90 DEG C.Those skilled in the art can select according to the actual situation
It selects.
Further, mixed material is sent into first order water-oil separating unit 20, passes through first order water-oil separating unit 20
Separating treatment is carried out, aqueous phase is obtained.First order water-oil separating unit 20 can be using separation equipments such as standing tank, centrifuges.
Aqueous phase is sent into second level water-oil separating unit 30, is carried out at separation by second level water-oil separating unit 30
Reason, to deviate from water.Second level water-oil separating unit 30 can be using separation equipments such as settle and separate tank, centrifuges.
Carrying out two-stage water-oil separating processing by two-stage water-oil separating unit can be improved dehydrating effect, while improve dehydration
The yield and purity of coal tar, and take into account and improve dechlorination, de- slag effect.
As an example, referring to figure 3., in first order water-oil separating unit 20 use three-phase centrifuge 21, three-phase from
The import of scheming 21 is connect with the outlet of mixed cell 10.
Three-phase centrifuge 21 can be triphase horizontal screw centrifuge or three-phase butterfly centrifugal machine.Mixed material is sent into three
Processing is centrifuged in phase centrifuge 21, and by centrifugal force, light oil phase, heavy oil and the residual oil in mixed material are due to specific gravity
It is different and reach separation, light oil phase g, heavy oil d1 and residual oil e are obtained, separating effect is more excellent and the rate of departure greatly improves.Wherein
Contain light oil and water, as above-mentioned aqueous phase in light oil phase g.
The revolving speed that three-phase centrifuge 26 carries out separating treatment can be 2000r/min~5000r/min, such as 3000r/min
~4000r/min, the time can be 10s~5min, such as 10s~3min.
In order to improve separating effect, in three phase centrifugation separation process, the temperature of mixed material can be 50 DEG C~90
DEG C, such as 50 DEG C~80 DEG C.
Optionally, first order water-oil separating unit 20 can also include buffering equipment, setting three-phase centrifuge 21 with
Between mixed cell 10, for caching mixed material.Buffering equipment optionally includes heating and heat insulation module, to make mixture
Material is maintained at predetermined temperature.
In second level water-oil separating unit 30 use light oil device for phase saparation 31, the import of light oil device for phase saparation 31 with
The light oil of three-phase centrifuge 21 mutually exports connection.
Light oil device for phase saparation 31 can be settle and separate tank or two-phase centrifuge.Light oil phase g is sent into light separation of oil
Equipment 31 carries out separating treatment, to isolate abjection water f, obtain light oil d2.
When using settle and separate tank, can be will carry out standing time enough in light oil phase g feeding settle and separate tank,
Time of repose can be 5min~48h, such as 1h~for 24 hours, water and light oil due to density difference and be layered, obtained gently by upper layer
Oily d2, lower layer obtain abjection water f.
In order to improve separating effect, during settle and separate, the temperature of light oil phase g is 30 DEG C~60 DEG C, such as 40 DEG C~
60℃。
When using two-phase centrifuge, two-phase horizontal spiral seperator can be.Light oil phase g is sent into two-phase centrifuge
Processing is centrifuged, by centrifugal force, water and light oil due to specific gravity difference and reach separation, isolate abjection water f,
To light oil d2, separating effect is more excellent and the rate of departure greatly improves.Two-phase centrifuge carry out separating treatment revolving speed can be
2000r/min~5000r/min, such as 3000r/min~4000r/min, the time can be 10s~5min, such as 10s~3min.
In order to improve separating effect, in two-phase centrifugal separation processes, the temperature of light oil phase g can be 30 DEG C~60 DEG C,
Such as 40 DEG C~60 DEG C.
Optionally, second level water-oil separating unit 30 can also include buffering equipment, be arranged in light oil device for phase saparation
Between 31 and three-phase centrifuge 21, for caching light oil phase g.Buffering equipment optionally includes heating and heat insulation module, to make
Light oil phase g is maintained at predetermined temperature.
In some embodiments, referring to figure 4., it can be and part or all of abjection water f return be recycling in mixing
In material, to save water.Specifically, the water out of light oil device for phase saparation 31 connects through the water inlet of pipeline and mixed cell 10
It connects, to realize the reuse of abjection water f.The water out of light oil device for phase saparation 31 can also connect through pipeline and sewage treatment unit
It connects, when abjection water f return in part to be recycling in mixed material, rest part abjection water f is sent to sewage treatment unit
It is handled.
Optionally, before deviating from water f reuse, abjection water f is carried out except salt treatment.It can be in light oil device for phase saparation
Demineralization plant is set between 31 water out and the water inlet of mixed cell 10, to realize to abjection water f desalination.Aforementioned desalination is set
It is standby to can be using demineralizer known in the art, such as vaporising device, electric demineralizer etc..
As another example, referring to figure 5., tank 22 is stood using tank 22 is stood in first order water-oil separating unit 20
Import connect with the outlet of mixed cell 10.
Standing tank 22 can be the container known in the art for settle and separate.Mixed material is sent into and is stood in tank 22
Time enough is stood, time of repose can be 5min~48h, and such as 1h~for 24 hours, heavy oil phase and light oil are mutually due to the difference of density
And be layered, light oil phase g is obtained by upper layer, lower layer obtains heavy oil phase h.Wherein contain heavy oil, residual oil and water in heavy oil phase h, is upper
The aqueous phase stated, as the first aqueous phase；Contain light oil and water in light oil phase g, is also above-mentioned aqueous phase, it is aqueous as second
Phase.
In order to improve separating effect, during settle and separate, the temperature of mixed material can be 50 DEG C~90 DEG C, such as
50 DEG C~80 DEG C.
Optionally, first order water-oil separating unit 20 can also include buffering equipment, setting stand tank 22 with mix
Between unit 10, for caching mixed material.Buffering equipment optionally includes heating and heat insulation module, protect mixed material
It holds in predetermined temperature.
In second level water-oil separating unit 30 use three-phase centrifuge 32 and light oil device for phase saparation 31, wherein three-phase from
The import of scheming 32 is mutually exported with the heavy oil for standing tank 22 and is connect, the import of light oil device for phase saparation 31 and the light oil for standing tank 22
Mutually outlet connection.
Three-phase centrifuge 32 can be triphase horizontal screw centrifuge or three-phase butterfly centrifugal machine.Heavy oil phase h is sent into three
Processing is centrifuged in phase centrifuge 32, by centrifugal force, water, heavy oil and residual oil in heavy oil phase h due to specific gravity not
With and reach separation, isolate the first abjection water f1 and residual oil e, obtain heavy oil d1, separating effect is more excellent and the rate of departure greatly
It improves.
The revolving speed that three-phase centrifuge 32 carries out separating treatment can be 2000r/min~5000r/min, such as 3000r/min
~4000r/min, the time can be 10s~5min, such as 10s~3min.
In order to improve separating effect, in three phase centrifugation separation process, the temperature of heavy oil phase h can be 50 DEG C~90 DEG C,
Such as 50 DEG C~80 DEG C.
Optionally, second level water-oil separating unit 30 can also include setting in three-phase centrifuge 32 and stand between tank 22
Buffering equipment, for caching heavy oil phase h.Buffering equipment optionally includes heating and heat insulation module, keep heavy oil phase h
In predetermined temperature.
Light oil device for phase saparation 31 can be settle and separate tank or two-phase centrifuge.Light oil phase g is sent into light separation of oil
Equipment 31 carries out separating treatment, to isolate the second abjection water f2 in light oil phase g, obtain light oil d2.Light oil device for phase saparation
31 and its to light oil phase g carry out separating treatment detail as it was noted above, details are not described herein.
Optionally, second level water-oil separating unit 30 can also include setting in light oil device for phase saparation 31 and stand tank
Buffering equipment between 22, for caching light oil phase g.Buffering equipment optionally includes heating and heat insulation module, to make light oil
Phase g is maintained at predetermined temperature.
First abjection water f1 and the second abjection water f2 constitute total abjection water f.In some embodiments, Fig. 6 is please referred to, it can
To be that part or all of abjection water f return is recycling in mixed material, to save water.Specifically, three-phase centrifuge
32 water out and/or the water out of light oil device for phase saparation 31 are connect through pipeline with the water inlet of mixed cell 10, to realize
Deviate from the reuse of water f.The water out of the water out of three-phase centrifuge 32 and/or light oil device for phase saparation 31 can also through pipeline with
Sewage treatment unit connection, when abjection water f return in part to be recycling in mixed material, rest part abjection water f is sent
It is handled to sewage treatment unit.
It is understood that when three-phase centrifuge 32 water out and light oil device for phase saparation 31 water out with mix
When the water inlet of unit 10 is connected, the water out of three-phase centrifuge 32 and the water out point of light oil device for phase saparation 31 can be
It is not connected to the water inlet of mixed cell 10, is also possible to the water out of three-phase centrifuge 32 and the water of light oil device for phase saparation 31
Outlet is connect after pipeline remittance is all the way with the water inlet of mixed cell 10.
Optionally, before deviating from water f reuse, abjection water f is carried out except salt treatment.It can be in three-phase centrifuge 32
And/or light oil device for phase saparation 31 water out and mixed cell 10 water inlet between demineralization plant is set, to realize to de-
It is discharged f desalination.Aforementioned demineralization plant can be using demineralizer known in the art, such as vaporising device, electric demineralizer
Deng.
As another example, Fig. 7 is please referred to, uses the first two-phase centrifuge 23 in first order water-oil separating unit 20,
The import of first two-phase centrifuge 23 is connect with the outlet of mixed cell 10.
First two-phase centrifuge 23 can be two-phase horizontal spiral seperator.Mixed material is sent into the first two-phase centrifuge
Processing is centrifuged in 23, by centrifugal force, heavy oil phase and light oil mutually reach separation due to the difference of specific gravity, obtain weight
Oily phase h and light oil phase g, separating effect is more excellent and the rate of departure greatly improves.Wherein, light oil and water are contained in light oil phase g, as
Above-mentioned aqueous phase contains heavy oil and residual oil in heavy oil phase h.
The revolving speed that processing is centrifuged in first two-phase centrifuge 23 can be 2000r/min~5000r/min, such as
3000r/min~4000r/min, the time can be 10s~5min, such as 10s~3min.
In order to improve separating effect, in the two-phase centrifugal separation processes of mixed material, the temperature of mixed material can be
50 DEG C~90 DEG C, such as 50 DEG C~80 DEG C.
Optionally, first order water-oil separating unit 20 can also include buffering equipment, be arranged in the first two-phase centrifuge
Between 23 and mixed cell 10, for caching mixed material.Buffering equipment optionally includes heating and heat insulation module, mixes to make
It closes material and is maintained at predetermined temperature.
The second two-phase centrifuge 33 and light oil device for phase saparation 31 are used in second level water-oil separating unit 30, wherein the
The import of two two-phase centrifuges 33 is mutually exported with the heavy oil of the first two-phase centrifuge 23 and is connect, the import of light oil device for phase saparation 31
It mutually exports and connect with the light oil of the first two-phase centrifuge 23.
Second two-phase centrifuge 33 can be two-phase horizontal spiral seperator.Heavy oil phase h is sent into the second two-phase centrifuge
Processing is centrifuged in 33, by centrifugal force, heavy oil and residual oil due to specific gravity difference and reach separation, to deviate from slag
Oily e, heavy oil d1 is obtained, separating effect is more excellent and the rate of departure greatly improves.
The revolving speed that processing is centrifuged in second two-phase centrifuge 33 can be 2000r/min~5000r/min, such as
3000r/min~4000r/min, the time can be 10s~5min, such as 10s~3min.
In order to improve separating effect, in the two-phase centrifugal separation processes of heavy oil phase h, the temperature of heavy oil phase h can be 50
DEG C~90 DEG C, such as 50 DEG C~80 DEG C.
Optionally, second level water-oil separating unit 30 can also include being arranged in the second two-phase centrifuge 33 and first liang
Buffering equipment between phase centrifuge 23, for caching heavy oil phase h.Buffering equipment optionally includes heating and heat insulation module, uses
So that heavy oil phase h is maintained at predetermined temperature.
Light oil device for phase saparation 31 can be settle and separate tank or two-phase centrifuge.Light oil phase g is sent into light separation of oil
Equipment 31 carries out separating treatment, to deviate from the water in light oil phase g, obtains abjection water f and light oil d2.Light oil device for phase saparation 31 and
It carries out the detail of separating treatment as it was noted above, details are not described herein to light oil phase g.
Optionally, second level water-oil separating unit 30 can also include being arranged in light oil device for phase saparation 31 and first liang
Buffering equipment between phase centrifuge 23, for caching light oil phase g.Buffering equipment optionally includes heating and heat insulation module, uses
So that light oil phase g is maintained at predetermined temperature.
In some embodiments, Fig. 8 is please referred to, can be and part or all of abjection water f return is recycling in mixing
In material, to save water.Specifically, the water out of light oil device for phase saparation 31 connects through the water inlet of pipeline and mixed cell 10
It connects, to realize the reuse of abjection water f.The water out of light oil device for phase saparation 31 can also connect through pipeline and sewage treatment unit
It connects, when abjection water f return in part to be recycling in mixed material, rest part abjection water f is sent to sewage treatment unit
It is handled.
Optionally, before deviating from water f reuse, abjection water f is carried out except salt treatment.It can be in light oil device for phase saparation
Demineralization plant is set between 31 water out and the water inlet of mixed cell 10, to realize to abjection water f desalination.Aforementioned desalination is set
It is standby to can be using demineralizer known in the art, such as vaporising device, electric demineralizer etc..
In the system that the coal tar of the utility model is dehydrated, heavy oil outlet be can connect to first order water-oil separating unit
20 import returns to first order water-oil separating unit 20 and carries out circular treatment when heavy oil detection is unqualified, and, light oil goes out
Mouth also can connect to the import of first order water-oil separating unit 20, when light oil detection is unqualified, return to first order grease point
Circular treatment is carried out from unit 20.
As a specific example, as shown in figure 9, the system of coal tar dehydration includes sequentially connected mixed cell
10, first order water-oil separating unit 20 and second level water-oil separating unit 30.
Wherein, mixed cell 10 includes demulsifier original agent tank 111 and solution preparing tank 112, and demulsifier original agent tank 111 goes out
Mouth is connect with the demulsifier import of solution preparing tank 112, and water supply interface is connect with the water inlet of solution preparing tank 112.Passing through will
The water-soluble demulsifier being stored in demulsifier original agent tank 111 and the water from water supply interface are sent into solution preparing tank 112, are made
It is uniformly mixed, obtains demulsifier aqueous solution.
Mixed cell 10 further includes pipeline online mixer 121, and the outlet of solution preparing tank 112 is through demulsifier metering pump
113 connect with the demulsifier import of pipeline online mixer 121, and the outlet of coal tar raw material tank 114 is pumped through coal tar raw material
115 connect with the coal tar oil inlet of pipeline online mixer 121.By will be from the demulsifier aqueous solution of solution preparing tank 112
It is uniform with the coal tar to be processed feeding progress of pipeline online mixer 121 on-line mixing from coal tar raw material tank 114, it send
Mixed material out.Wherein, the feeding amount of demulsifier aqueous solution is measured by demulsifier metering pump 113, and coal tar to be processed is sent
Enter amount and passes through 115 regulation of coal tar raw material pump.
First order water-oil separating unit 20 includes three-phase centrifuge 211, and three-phase centrifuge 211 can be triphase horizontal spiral
Centrifuge or three-phase butterfly centrifugal machine.The import of three-phase centrifuge 311 is connect with the outlet of pipeline online mixer 121.First
Include still optionally further mixed material surge tank 201 in grade water-oil separating unit 20, is set to three-phase centrifuge 311 and pipeline
Between online mixer 121, to cache mixed material, and it is optionally provided with heating and heat insulation module, for making mixed material
Temperature is 50 DEG C~90 DEG C, such as 50 DEG C~80 DEG C.The residual oil outlet of three-phase centrifuge 311 is connect with residual oil slot 401, heavy oil goes out
Mouth is connect with heavy oil tank 402.
Second level water-oil separating unit 30 includes two-phase centrifuge 311, and two-phase centrifuge 311 can be two-phase horizontal spiral
Centrifuge.The light oil of three-phase centrifuge 211 is mutually exported to be connect with the import of two-phase centrifuge 311, wherein optionally, three phase centrifugation
The light oil of machine 211, which is mutually exported, to be connect through light oil phase surge tank 310 with the import of two-phase centrifuge 311, to cache light oil phase, and
It is optionally provided with heating and heat insulation module, for making 30 DEG C~60 DEG C of temperature of light oil phase, such as 40 DEG C~60 DEG C.Two-phase centrifugation
The light oil outlet of machine 311 is connect with light oil tank 403, water out and Water Tank 404 connect.
Optionally, the outlet of heavy oil tank 402 and the outlet of light oil tank 403 are respectively connected to qualified tank (not shown)
Or subsequent processing.
Optionally, the outlet of heavy oil tank 402 is connect with the import of three-phase centrifuge 211.When first order water-oil separating unit
20 include mixed material surge tank 201 when, the outlet of heavy oil tank 402 can also be and the import of mixed material surge tank 201 company
It connects.
Optionally, the outlet of light oil tank 403 is connect with the import of three-phase centrifuge 211.When first order water-oil separating unit
20 include mixed material surge tank 201 when, the outlet of light oil tank 322 can also be and the import of mixed material surge tank 201 company
It connects.
Optionally, the outlet of Water Tank 404 is divided into two branches after sewage pump 405, and one of branch is matched with solution
The water inlet of tank 112 processed connects, another branch is connected to sewage treatment unit.
Mixed material be first fed into three-phase centrifuge 211 carry out three phase centrifugation separating treatment, send out light oil phase g, residual oil e and
Heavy oil d1.Residual oil e is sent into residual oil slot 401, and heavy oil d1 is sent into heavy oil tank 402, is sent into qualified tank or next work after detection is qualified
Sequence, underproof 211 circular treatment of return three-phase centrifuge.Light oil phase g is sent into two-phase centrifuge 311 and carries out two-phase centrifugation point
From processing, abjection water f and light oil d2 is sent out.Light oil d2 is sent into light oil tank 403, is sent into qualified tank or next work after detection is qualified
Sequence, underproof 211 circular treatment of return three-phase centrifuge.Deviating from water f points is two-way, wherein rework solution preparing tank all the way
121 are recycled, and another way is sent into sewage treatment unit and discharge after purified treatment is qualified.
Optionally, it is provided with demineralization plant between Water Tank 404 and solution preparing tank 121, to remove to abjection water f
Then salt treatment carries out reuse again.Aforementioned demineralizer can be using device known in the art, such as vaporising device, electricity
Demineralizer etc..
The system of coal tar dehydration shown in Fig. 9, is optionally connected to middle control unit for each equipment, realizes the automatic of system
Change control, high degree of automation simplifies operation and monitoring.
The technical solution of the system of aforementioned coal tar dehydration and technical characteristic are readily applicable to shown in Fig. 9 herein
In the system of coal tar dehydration, details are not described herein.
Using coal tar provided by the embodiment of the utility model be dehydrated system, can by emulsification system water, Cl salt,
Mechanical admixture etc. is sufficiently released from emulsification system, and heavy oil d1 and light oil d2 constitute total dehydrated coal tar d, through detecting
Its dehydrating effect is significantly improved, while the effect of dechlorination, de- slag is also significantly improved.
In obtained dehydrated coal tar d water content reduce, be reduced to 2.5 weight % hereinafter, even 0.5 weight % hereinafter,
More even 0.3 weight % is hereinafter, such as 0.1 weight % or less.Deviate from water f in oil content reduce, be reduced to 5.0 weight % with
Under in addition 1.0 weight % hereinafter, more even 0.1 weight % hereinafter, such as 0.05 weight % hereinafter, such as 0.01 weight again
Measure % or less.
Chlorinty reduces in obtained dehydrated coal tar d, is reduced to 40 μ g/g hereinafter, even 25 μ g/g are hereinafter, more very
To being 10 μ g/g hereinafter, such as 5 μ g/g are hereinafter, can reduce chloride ion in coal tar to the interference of subsequent technique and to subsequent
The corrosion of production equipment.The content of mechanical admixture reduces in obtained dehydrated coal tar d, is reduced to 0.1 weight % hereinafter, very
To being 0.05 weight % hereinafter, more even 0.01 weight % is hereinafter, for example 0.005 weight % is hereinafter, can reduce coal tar
In interference of the mechanical admixture to subsequent technique and the abrasion to remaining production equipment.
The system of coal tar provided by the embodiment of the utility model dehydration, simple process, operation are convenient, construction investment is low,
Maintenance cost is low, reduces to coal tar dehydration, dechlorination, the effect height of de- slag and effect stability, the usage amount of demulsifier.
The system of coal tar provided by the embodiment of the utility model dehydration, be particularly suitable for middle coalite tar (600 DEG C~
800 DEG C of fractions).If the system of coal tar provided by the embodiment of the utility model dehydration is applied to the dehydration of middle coalite tar,
Water content is the 5 weight % of weight %~35 in coalite tar in this, also containing largely with the higher group for helping emulsification
Point, such as the 20 weight % of weight %~30 of phenols, the 25 weight % of weight %~40 of gum asphalt, 0.5 weight of content of impurities
The weight % of %~4 is measured, 0.5 weight % of water content is hereinafter, even 0.3 weight in the dehydrated coal tar obtained after dehydration
% is measured hereinafter, more even 0.1 weight % or less；Chlorinty is reduced to 25 μ g/g hereinafter, even 10 μ g/g are hereinafter, more even
It is 5 μ g/g or less；The content of mechanical admixture is reduced to 0.1 weight % hereinafter, even 0.05 weight % is hereinafter, more even
0.01 weight % or less.
Further the utility model is illustrated below with reference to embodiment.The utility model is not limited to implementation hereafter
Example.
Test method
Water content GB/T 2288-2008 " coke chemicals aquametry " method three according to national standards: karl Fischer
Method is measured.Wherein using ten thousand water flowing of Switzerland point (volumetric method) instrument 915, plum Teller electronic balance (sensibility reciprocal 0.02g).
Chlorinity is measured referring to international standard ASTM D4929, ASTM D5808, SH/T 1757.Wherein using beauty
The total chlorine analyzers ECS3000 of state thermoelectricity ThermoFischer, plum Teller electronic balance (sensibility reciprocal 0.1mg).
Content of impurities is surveyed referring to GB/T 511 " petroleum and oil product and additive mechanical admixture measuring method "
It is fixed.Wherein use plum Teller electronic balance (sensibility reciprocal 0.1mg).
Embodiment 1
According to Fig. 5, embodiment 1 is carried out.
(600 DEG C~800 DEG C fractions, water content are 20.36 weight % to middle coalite tar to be processed, and chlorinity is
486.37 μ g/g, content of impurities be 0.80 weight %) in coal tar raw material tank by steam-coil-heater to 70 DEG C, through coal
Tar stock is pumped to pipeline online mixer, mixes with the demulsifier aqueous solution sent from solution preparing tank, obtains mixture
Material.Wherein, demulsifier is water-soluble demulsifier phenolic resin polyethers, contains demulsifier 10g in every 100ml demulsifier aqueous solution,
Demulsifier concentration is 1000 μ g/g in mixed material.
Mixed material is by standing tank, under the conditions of 70 DEG C, carries out settle and separate processing for 24 hours, obtains light oil phase g, heavy oil
Phase h two-phase.Light oil phase g enters light oil phase surge tank caching, and wherein light oil phase surge tank internal temperature control is at 50 DEG C.Heavy oil phase
H is sent into heavy oil phase surge tank caching, and wherein heavy oil phase surge tank internal temperature control is at 70 DEG C.
Further, heavy oil phase h passes through three-phase butterfly centrifugal machine, carries out three phase centrifugation under the conditions of 3500r/min, 70 DEG C
Separating treatment 30s obtains the first abjection water f1, heavy oil d1 and residual oil e three-phase.
And light oil phase g passes through two-phase horizontal spiral centrifuge, and two-phase centrifugation is carried out under the conditions of 3500r/min, 50 DEG C
Separating treatment 20s obtains the abjection of light oil d2 and second water f2.
Heavy oil d1 and light oil d2 are mixed to get dehydrated coal tar, and wherein water content is 0.5 weight %, chlorinity is 10 μ g/
G, content of impurities is 0.01 weight %.First abjection water f1 and the second abjection water f2 are mixed into total abjection water, wherein oil
Content is 0.01 weight %.
Embodiment 2
According to Fig. 9, embodiment 2 is carried out.
(600 DEG C~800 DEG C fractions, water content are 25.27 weight % to middle coalite tar to be processed, and chlorinity is
527.16 μ g/g, content of impurities be 0.90 weight %) in coal tar raw material tank 114 by steam-coil-heater to 70 DEG C,
It send through coal tar raw material pump 115 to pipeline online mixer 121, is mixed with the demulsifier aqueous solution sent from solution preparing tank 112
It closes uniformly, obtains mixed material.Wherein, demulsifier is water-soluble demulsifier phenolic resin polyethers, every 100ml demulsifier aqueous solution
In contain demulsifier 2.5g, demulsifier concentration is 500 μ g/g in mixed material.Mixed material is sent into mixed material surge tank 201
Caching, wherein 201 internal temperature control of mixed material surge tank is at 70 DEG C.
Mixed material passes through three-phase butterfly centrifugal machine, and three phase centrifugation separating treatment is carried out under the conditions of 3000r/min, 70 DEG C
30s obtains light oil phase g, heavy oil d1, residual oil e three-phase.
Residual oil e is sent into residual oil slot 401.
Heavy oil d1 be sent into heavy oil tank 402, through detecting, in heavy oil d1 water content be 0.50 weight %, chlorinity be 12 μ g/g,
Content of impurities is 0.01 weight %, detects the qualified tank of qualified feeding.
Light oil phase g enters two-phase horizontal spiral centrifuge by light oil phase surge tank 310, wherein light oil phase surge tank 310
Internal temperature control is at 50 DEG C.In two-phase horizontal spiral centrifuge, under the conditions of 3000 r/min, 50 DEG C, to light oil phase g into
Row two-phase centrifuging treatment 20s obtains light oil d2 and abjection water f.Light oil d2 enters light oil tank 403, through detecting, light oil d2
Middle water content is 0.10 weight %, chlorinity is 5 μ g/g, content of impurities 0, detects the qualified tank of qualified feeding.Deviate from water
Oil content is 0.01 weight % in f, abjection water f is sent into Water Tank 404, abjection water f a part in Water Tank 404 returns molten
Liquid preparing tank 112 is used for the preparation of demulsifier aqueous solution, and another part discharges after sending to sewage treatment unit purified treatment.
Heavy oil d1 and light oil d2 are mixed to get dehydrated coal tar, and wherein water content is about 0.3 weight %, chlorinity is about
8.5 μ g/g, content of impurities are about 0.005 weight %.
Comparative example 1
It is similar to Example 2, unlike, (600 DEG C~800 DEG C evaporate middle coalite tar to be processed in comparative example 1
Point, water content is 20.36 weight %, and chlorinity is 486.37 μ g/g, and content of impurities is 0.80 weight %), and, comparison
Solution preparing tank is not provided in example 1, water-soluble demulsifier is directly mixed with middle coalite tar, in obtained mixed material
Demulsifier concentration is 3000 μ g/g, and, time of three phase centrifugation separating treatment is 10min, since demulsification is poor, water with
Oil base is originally not separated by, and is only obtained the 5% light oil phase for being equivalent to coal tar weight to be processed, therefore is not carried out two-phase centrifuge separation
Treatment process.
Water content is 22 weight % in the isolated heavy oil of mixed material three phase centrifugation, and wherein water content is 8 weight %.
Above description is only a specific implementation of the present invention, but the protection scope of the utility model is not limited to
In this, anyone skilled in the art within the technical scope disclosed by the utility model, can be readily occurred in various
Equivalent modifications or substitutions, these modifications or substitutions should be covered within the scope of the utility model.Therefore, this is practical
Novel protection scope should be subject to the protection scope in claims.
Claims (10)
1. a kind of system of coal tar dehydration, which is characterized in that the system includes at least sequentially connected mixed cell, first
Grade water-oil separating unit and second level water-oil separating unit；Wherein,
Water-soluble demulsifier, water and coal tar to be processed are mixed by the mixed cell, obtain mixed material；
The mixed material carries out separating treatment by the first order water-oil separating unit, obtains aqueous phase；
The aqueous phase carries out separating treatment by the second level water-oil separating unit, to deviate from water.
2. system according to claim 1, which is characterized in that the first order water-oil separating unit includes three phase centrifugation
Machine, the import of the three-phase centrifuge are connect with the outlet of the mixed cell, for the mixed material to be carried out three-phase separate
From processing to obtain aqueous phase, residual oil and heavy oil；
The second level water-oil separating unit includes light oil device for phase saparation, the import of the light oil device for phase saparation and described three
The aqueous phase of phase centrifuge exports connection, for the aqueous phase to be carried out separating treatment to deviate from water, obtain light oil.
3. system according to claim 1, which is characterized in that the first order water-oil separating unit includes standing tank, institute
The import for stating standing tank is connect with the outlet of the mixed cell, for the mixed material to be carried out two-phase laminated flow processing to obtain
To the first aqueous phase and the second aqueous phase；
The second level water-oil separating unit includes three-phase centrifuge and light oil device for phase saparation, wherein the three-phase centrifuge
Import and it is described stand tank the first aqueous phase export connect, for by first aqueous phase carry out separating treatment to deviate from
Water and residual oil obtain heavy oil, and the import of the light oil device for phase saparation and second aqueous phase for standing tank are exported and connected, use
In by second aqueous phase carry out separating treatment to deviate from water, obtain light oil.
4. system according to claim 1, which is characterized in that the first order water-oil separating unit include the first two-phase from
The import of scheming, the first two-phase centrifuge is connect with the outlet of the mixed cell, for carrying out the mixed material
Two-phase laminated flow processing is to obtain aqueous phase and heavy oil phase；
The second level water-oil separating unit includes the second two-phase centrifuge and light oil device for phase saparation, wherein described second liang
The import of phase centrifuge is mutually exported with the heavy oil of the first two-phase centrifuge and is connect, for mutually carrying out at separation the heavy oil
To deviate from residual oil, obtain heavy oil, the import of the light oil device for phase saparation and the aqueous phase of the first two-phase centrifuge go out reason
Mouth connection, for the aqueous phase to be carried out separating treatment to deviate from water, obtain light oil.
5. according to the described in any item systems of claim 2 to 4, which is characterized in that the light oil device for phase saparation is to stand to divide
From tank or two-phase centrifuge.
6. system according to any one of claims 1 to 4, which is characterized in that the mixed cell includes mixing apparatus, institute
Stating mixing apparatus is blending tank, static mixer or online mixer.
7. system according to claim 6, which is characterized in that the mixed cell further includes solution dosing apparatus, described
The outlet of solution dosing apparatus is connect with the demulsifier aqueous solution import of the mixing apparatus, is used for water-soluble demulsifier and water
Mixing is to obtain demulsifier aqueous solution.
8. system according to any one of claims 1 to 4, which is characterized in that the water of the second level water-oil separating unit
Outlet is connected to the water inlet of the mixed cell through pipeline.
9. system according to claim 8, which is characterized in that the water out of the second level water-oil separating unit with it is described
Demineralization plant is additionally provided between the water inlet of mixed cell.
10. system according to any one of claims 1 to 4, which is characterized in that the system also includes heating modules, use
In the coal tar to be processed is heated to 50 DEG C~90 DEG C.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108611112A (en) * | 2018-06-05 | 2018-10-02 | 陕西煤业化工集团神木天元化工有限公司 | The method and system of coal tar dehydration |
| CN111676044A (en) * | 2019-11-06 | 2020-09-18 | 宁夏银海鸿兴煤化工有限公司 | Coal tar dehydration process |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108611112A (en) * | 2018-06-05 | 2018-10-02 | 陕西煤业化工集团神木天元化工有限公司 | The method and system of coal tar dehydration |
| CN111676044A (en) * | 2019-11-06 | 2020-09-18 | 宁夏银海鸿兴煤化工有限公司 | Coal tar dehydration process |
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