CN110527539A - Coal-based needle coke pretreatment unit and process - Google Patents
Coal-based needle coke pretreatment unit and process Download PDFInfo
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- CN110527539A CN110527539A CN201910940162.6A CN201910940162A CN110527539A CN 110527539 A CN110527539 A CN 110527539A CN 201910940162 A CN201910940162 A CN 201910940162A CN 110527539 A CN110527539 A CN 110527539A
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- 238000000034 method Methods 0.000 title claims abstract description 34
- 230000008569 process Effects 0.000 title claims abstract description 26
- 239000011311 coal-based needle coke Substances 0.000 title claims abstract description 21
- 239000002904 solvent Substances 0.000 claims abstract description 173
- 239000012046 mixed solvent Substances 0.000 claims abstract description 67
- 239000002994 raw material Substances 0.000 claims abstract description 28
- 238000001514 detection method Methods 0.000 claims abstract description 19
- 238000004064 recycling Methods 0.000 claims abstract description 17
- 239000000463 material Substances 0.000 claims abstract description 10
- 238000012544 monitoring process Methods 0.000 claims abstract description 10
- 238000000605 extraction Methods 0.000 claims abstract description 8
- 238000012797 qualification Methods 0.000 claims abstract description 7
- 238000002156 mixing Methods 0.000 claims description 17
- SMWDFEZZVXVKRB-UHFFFAOYSA-N Quinoline Chemical compound N1=CC=CC2=CC=CC=C21 SMWDFEZZVXVKRB-UHFFFAOYSA-N 0.000 claims description 12
- 230000008676 import Effects 0.000 claims description 12
- 238000001816 cooling Methods 0.000 claims description 10
- 125000001931 aliphatic group Chemical group 0.000 claims description 9
- 239000003849 aromatic solvent Substances 0.000 claims description 9
- 239000003795 chemical substances by application Substances 0.000 claims description 9
- 238000013461 design Methods 0.000 claims description 9
- 238000004062 sedimentation Methods 0.000 claims description 9
- 239000010426 asphalt Substances 0.000 claims description 8
- 239000011305 binder pitch Substances 0.000 claims description 8
- 238000004519 manufacturing process Methods 0.000 claims description 7
- 239000011295 pitch Substances 0.000 claims description 7
- 238000010438 heat treatment Methods 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 6
- 238000012806 monitoring device Methods 0.000 claims description 6
- 238000000746 purification Methods 0.000 claims description 6
- 238000003756 stirring Methods 0.000 claims description 6
- 238000011084 recovery Methods 0.000 claims description 5
- 229910003460 diamond Inorganic materials 0.000 claims description 4
- 239000010432 diamond Substances 0.000 claims description 4
- 230000000694 effects Effects 0.000 claims description 4
- 230000007115 recruitment Effects 0.000 claims description 4
- 238000010348 incorporation Methods 0.000 claims description 3
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 claims description 3
- 239000007921 spray Substances 0.000 claims description 3
- 230000006641 stabilisation Effects 0.000 claims description 3
- 238000011105 stabilization Methods 0.000 claims description 3
- 239000004148 curcumin Substances 0.000 claims description 2
- 239000000203 mixture Substances 0.000 abstract description 4
- 239000011294 coal tar pitch Substances 0.000 abstract description 2
- 238000002360 preparation method Methods 0.000 abstract description 2
- 239000011331 needle coke Substances 0.000 description 6
- 239000000047 product Substances 0.000 description 5
- 238000012360 testing method Methods 0.000 description 4
- 238000004364 calculation method Methods 0.000 description 3
- 239000003350 kerosene Substances 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 239000011280 coal tar Substances 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 description 1
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical group [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000010406 cathode material Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000003111 delayed effect Effects 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 229910002804 graphite Inorganic materials 0.000 description 1
- 239000010439 graphite Substances 0.000 description 1
- 238000005087 graphitization Methods 0.000 description 1
- 239000002010 green coke Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 229910052744 lithium Inorganic materials 0.000 description 1
- 239000002932 luster Substances 0.000 description 1
- 239000007773 negative electrode material Substances 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000010008 shearing Methods 0.000 description 1
- 239000004332 silver Substances 0.000 description 1
- 229910052709 silver Inorganic materials 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000005303 weighing Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
- C10C1/00—Working-up tar
- C10C1/005—Working-up tar by mixing two or more coaltar fractions
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
- C10C3/00—Working-up pitch, asphalt, bitumen
- C10C3/005—Working-up pitch, asphalt, bitumen by mixing several fractions (also coaltar fractions with petroleum fractions)
Abstract
The invention belongs to coal tar pitch continuous extractions, settle preparation technical field, more particularly, to a kind of coal-based needle coke pretreatment unit and process, it is characterized by comprising light phase solvent recovering systems for coal-based needle coke pretreatment unit, heavy phase solvent recovering system, the mixed solvent pretreatment system being connected respectively with light phase solvent recovering system and heavy phase solvent recovering system, the control system being connected with this mixed solvent pretreatment system, mixed solvent pretreatment system includes slot among mixed solvent, multidirectional premixer, pipe-line mixer, the subsider being connected with this pipe-line mixer.The present invention raw material maltha mix with qualified solvent and the allocation process of qualification solvent in, it can be by the flow monitoring value and online Density Detection result of each materials such as raw material maltha, qualified solvent, recycling mixed solvent, through computer or the artificial adjustment calculated and match when inlet amount by DCS control room direct control operation items, the simplified control of automation or semi-automation is realized.
Description
Technical field
It is pre- more particularly, to a kind of coal-based needle coke the invention belongs to coal tar pitch continuous extraction, sedimentation preparation technical field
Processing unit and process.
Background technique
Needle coke be using the catalytic slurry in coal tar asphalt or petroleum refining process as raw material, it is preprocessed to be refined
It is carried out after material asphalt prepared by delayed coking, calcining, appearance is silver gray, has metallic luster, structural porous has
Obvious flowing texture has threadiness or acicular texture trend.Needle coke is with thermal expansion coefficient is low, impurity content is low, conductive
The advantages that high-efficient and easy graphitization.Mainly for the production of high power (HP) and ultra high power (VHP) graphite electrode.It is needle-shaped at present
Coke is also widely used for the raw material of lithium cell cathode material, and negative electrode material obtained has specific capacity height, long service life, safety
The features such as, it is one of indispensable raw material of new energy field.
, raw material pretreatment process unit needle coke production technology is made of three technique units respectively: 1), 2), delay coke
Change technique unit, 3), green coke calcine technology unit.Pretreatment of raw material is very important a ring during producing needle coke
Section, process be by softening point 35 DEG C -40 DEG C coal tar soft asphalt and mixed solvent (aromatic solvent, aliphatic solvent and
Recycling design) be mixed in a certain ratio after carry out extraction sedimentation, obtain purification maltha of the quinoline insolubles less than 0.1%, as
The raw material of needle coke is produced, Reusability can be recycled in solvent.The qualified solvent configuration of raw material pretreatment process unit is basic at present
Pre-coordination is carried out using several solvent surge-tanks, wherein at least 1 surge-tank internal solvent allotment is qualified spare, and 1-2 just
Testing result is being deployed or is waiting, 1 is used, but when the adjustment of solvent composition and ratio index, cannot be switched at once new
The qualified solvent of proportion, online solvent currently in use will continue to use, at the same at once according to the proportion index of newest adjustment into
Row coordinating solvents switch the solvent that flux bath uses newest proportion again after allotment is qualified.The qualification for deploying 30-40 tons of a slot is molten
Agent the used time about 3-3.5 hours, deploys 30-40 tons of a slot after adjusting solvent burden ratio index from solvent delivery to using result to detect
Qualified solvent, from supplement be formulated to result detect about 1-2 hours sometimes, the testing result such as solvent index is unqualified, then needs
Continue to deploy, increase used time 1-2 hours every time.
It deploys qualified mixed solvent and raw material maltha and pipe-line mixer is delivered to by pump respectively, according to certain solvent ratio
(solvent ratio=solvent/pitch, generally between 0.8-1.1) mixed miscella (ρ20℃=1.051) enter subsider to be sunk
Drop separation.Upper layer light phase (ρ20℃=1.037) laggard by the heated stove heating of pump conveying from light phase medial launder is flow to by overflow port
Enter in destilling tower, refined bitumen is obtained after solvent recovery.Bottom heavy phase (ρ20℃=1.189) through adding after subsider bottom is gone out by pumping
Hot stove heating enters in destilling tower, and solvent recovery obtains heavy phase pitch.
Process above the problem is that: installation area is big, complex process, investment is big, power consumption is high, cost
Greatly, employment is more, is difficult to realize intelligent control.More importantly when product quality is unqualified or solvent burden ratio needs to adjust, no
Operation adjustment can be made online at the first time, and during new qualified solvent configuration and testing result wait, it can only
By upsetting original system material balance or continuing to produce substandard product as adjustment means, this not only gives the entirety of system flat
Weighing apparatus operation brings difficulty, returns product quality and production cost brings burden, can also be to the operation of subsequent process unit when serious
Adverse effect is caused with product quality.
Summary of the invention
The object of the present invention is to provide a kind of coal-based needle coke pretreatment unit and processes, to overcome needle coke to produce
Deficiency existing for raw material pretreatment stage in technique.
The purpose of the present invention is what is realized by following technical proposals:
Coal-based needle coke pretreatment unit of the invention, it is characterised in that including light phase solvent recovering system, heavy phase solvent recovery
System, the mixed solvent pretreatment system being connected respectively with the light phase solvent recovering system and heavy phase solvent recovering system,
The control system being connected with this mixed solvent pretreatment system,
The mixed solvent pretreatment system includes slot among mixed solvent, is mixed by multidirectional premixer feed pump with described
The multidirectional premixer that bonding solvent medial launder is connected, the pipeline being connected with the outlet of this multidirectional premixer by pipeline are mixed
Clutch, the subsider being connected with this pipe-line mixer,
The light phase solvent recovering system includes the light phase feeder trough being connected with the subsider, passes through light phase feed pump
The light phase tube furnace being connected with the light phase feeder trough, the light phase tower being connected with this light phase tube furnace, with this light phase tower bottom
The refined bitumen pump that portion is connected, the light phase solvent cooler being connected with the light phase top of tower are cooling with this light phase solvent
The light phase solvent medial launder that device is connected, this light phase solvent medial launder pass through slot among light phase solvent pump and the mixed solvent
It is connected,
The heavy phase solvent recovering system includes the heavy phase feeder trough being connected with the subsider, passes through heavy phase feed pump
The heavy phase tube furnace being connected with the heavy phase feeder trough, the heavy phase tower being connected with this heavy phase tube furnace, with this heavy phase tower bottom
The binder pitch that portion is connected produces pump, and the heavy phase solvent cooler being connected with the heavy phase top of tower is molten with this heavy phase
The heavy phase solvent medial launder that agent cooler is connected, this heavy phase solvent medial launder pass through heavy phase solvent pump and the mixed solvent
Medial launder is connected,
The control system includes computer, several flow monitoring devices for being connect with this computer by wireless signal and
Line density detection device, mixed solvent centre slot, multidirectional premixer and the pipe-line mixer are equipped with the flow
Monitoring device and online device for detecting density.
The multidirectional premixer includes mixer case, and the cyclone at the top of this mixer case is arranged in, setting
The primary raw material import A of the cyclone apex is arranged in, along the mixer in outlet F in the mixer case bottom
Vane type disperser entrance B, the vane type disperser entrance C and vane type disperser entrance D that shell circumferential side wall is uniformly arranged,
The measuring mouth E of the mixer case lower part is set, the format sieve plate of lower part is arranged in the mixer case and is located at,
The mixer case is the assembly of top cone, middle part cylindrical body and lower part cone, and the cyclone is from institute
The mixer case top cone stated runs through into the middle part cylindrical body of mixer case, and the measuring mouth E is arranged described
On the lower part centrum of mixer case.
The format sieve plate is located at the middle part cylindrical body bottom-up 1/5th of the mixer case.
Vane type disperser entrance B, vane type disperser entrance C and the vane type disperser entrance D is located at described
At the one third of the middle part cylindrical body of mixer case from up to down, the vane type disperser entrance B, vane type dispersion
Device entrance C and vane type disperser entrance D is circumferentially in 1200 Uniformly distributed, the measuring mouth E is located at the mixer case
Lower part centrum medium position.
Utilize the process of coal-based needle coke pretreatment unit, it is characterised in that include the following steps:
(1) respectively from the light phase recycling design and heavy phase recycling design of light phase tower top and heavy phase tower top, while it is molten to enter mixing
Agent medial launder；Solvent burden ratio amount is calculated by density difference, the mixed solvent density of slot is (conventional among detection mixed solvent
Density value ρ100℃=0.830-850), according to this detected value, then the standard curve of control solvent density and solvent burden ratio relationship
(before manufacture, being demarcated using two kinds of fresh solvents to solvent burden ratio, be mixed to get the standard curve by quasi-), is calculated
To fresh aromatic solvent or the magnitude of recruitment of aliphatic solvent；
(2) two kinds of mixed solvents for entering slot among mixed solvent, are extracted out by multidirectional premixer feed pump from multidirectional premixing
The primary raw material import A of device is squeezed into, and mixed solvent accounts for 90-95% in solvent burden ratio；
(3) aromatic solvent and aliphatic solvent are measured according to the ratio from side vane type disperser entrance B, vane type disperser entrance C
It squeezes into, vane type disperser entrance D is as spare mouth；
A, primary raw material import A liquid is in through A mouthfuls of cyclones under 0.01m/s-2m/s flow velocity and 0.01MPa-0.5MPa pressure
45 DEG C of rotated versions spray, and form ultromotivity Stirring ability in multidirectional premixer inner；
B, B, C, D are different solvents liquid-inlet, and B, C, D liquid are in 0.01m/s-2m/s flow velocity and 0.01MPa-0.5MPa pressure
It is lower to be sprayed in 30 DEG C of degree angles with spiral form through entry impeller formula disperser, it is generated with the main feed that main material import A enters
Collision mixes under the effect of ultromotivity Stirring；
C, incorporation time is -30 seconds 25 seconds in multidirectional premixer, then sheared through multidirectional premixer bottom format sieve plate,
It is flowed out after current stabilization by lower part outlet F；
D, it detects to obtain qualified mixed solvent (conventional density value ρ in multidirectional premixer measuring mouth E, measuring mouth E100℃=
0.830-0.850)；
(4) it is completed in multidirectional premixer when solvent sufficiently mixed in the duct by outlet F outflow and maltha after proportion mixing
It closes, then is sufficiently mixed by pipe-line mixer, and sample tap is set after pipe-line mixer and detects (the satisfaction sedimentation of mixing oil density
It is required that conventional density value ρ20℃=1.051)；
(5) enter subsider progress weight with the well-mixed solvent of maltha mutually to separate；The interface of final settlement qualification is heavy
At the thief hatch for dropping slot, pass through density (the conventional density value ρ of detection extraction light phase oil20℃=1.037) come quickly to judge light phase oil
Sedimentation is qualified, or passes through the foundation of the two density values of light phase oil and miscella changed as solvent than adjustment；
(6) light phase oil enters in light phase feeder trough after separating, and enters light phase after light phase feed is pumped into light phase diamond heating
The light phase solvent of tower, the recycling of light phase column overhead enters light phase solvent medial launder after light phase solvent cooler is cooling, enters back into mixed
Bonding solvent medial launder is recycled, and purification maltha of the light phase tower tower bottom quinoline insolubles less than 0.1% is sent to tank field medial launder；
(7) heavy phase oil enters in heavy phase feeder trough after separating, and enters heavy phase after heavy phase feed is pumped into heavy phase diamond heating
The heavy phase solvent of tower, the recycling of heavy phase column overhead enters heavy phase solvent medial launder after heavy phase solvent cooler is cooling, enters back into mixed
Bonding solvent medial launder is recycled, and heavy phase tower tower bottom pitch is sent to tank field medial launder and takes out as binder pitch.
Flow monitoring value and online Density Detection in each step is as a result, feed back to control system by signal, through counting
Calculation machine or the artificial adjustment calculated and match when inlet amount by control system direct control operation items；And in inlet amount and solvent
When the adjustment of the indexs such as proportion, by on-line checking and progress real-time monitoring is calculated.
Advantages of the present invention:
Coal-based needle coke pretreatment unit of the invention and process mixs and qualification in raw material maltha with qualified solvent
In the allocation process of solvent, can by the flow monitoring value of each materials such as raw material maltha, qualified solvent, recycling mixed solvent and
Line density testing result feeds back to computer by signal, through computer or the artificial direct control operation items that calculate with when
The simplified control of automation or semi-automation is realized in the adjustment of inlet amount；And in the adjustment of the indexs such as inlet amount and solvent burden ratio,
It by on-line checking and can calculate to be regulated and controled in time, system disorders and cost is avoided to waste.
Detailed description of the invention
Fig. 1 is process flow diagram of the invention.
Fig. 2 is the structural schematic diagram of the multidirectional premixer of the present invention.
Fig. 3 is the top view of Fig. 2 of the present invention.
Specific embodiment
A specific embodiment of the invention is further illustrated with reference to the accompanying drawing.
As shown in Figure 1-3, coal-based needle coke pretreatment unit of the invention, it is characterised in that including light phase solvent recovery system
System, heavy phase solvent recovering system, the mixing being connected respectively with the light phase solvent recovering system and heavy phase solvent recovering system
Solvent pre-treatment system, the control system being connected with this mixed solvent pretreatment system,
The mixed solvent pretreatment system includes slot 1 among mixed solvent, by multidirectional premixer feed pump 2 with it is described
The multidirectional premixer 3 that slot 1 is connected among mixed solvent, is connected with the outlet of this multidirectional premixer 3 by pipeline
Pipe-line mixer 4, the subsider 5 being connected with this pipe-line mixer 4,
The light phase solvent recovering system includes the light phase feeder trough 14 being connected with the subsider 5, is given by light phase
The light phase tube furnace 16 that material pump 15 is connected with the light phase feeder trough 14, the light phase tower being connected with this light phase tube furnace 16
17, the refined bitumen pump 21 being connected with this 17 bottom of light phase tower is cold with the light phase solvent being connected at the top of the light phase tower 17
But device 18, the light phase solvent medial launder 19 being connected with this light phase solvent cooler 18, this light phase solvent medial launder 19 pass through light
Phase solvent pump 20 is connected with slot 1 among the mixed solvent,
The heavy phase solvent recovering system includes the heavy phase feeder trough 6 being connected with the subsider 5, is fed by heavy phase
The heavy phase tube furnace 8 that pump 7 is connected with the heavy phase feeder trough 6, the heavy phase tower 9 being connected with this heavy phase tube furnace 8 are heavy with this
The binder pitch extraction pump 10 that 9 bottom of phase tower is connected, with the heavy phase solvent cooler being connected at the top of the heavy phase tower 9
11, the heavy phase solvent medial launder 12 being connected with this heavy phase solvent cooler 11, it is molten that this heavy phase solvent medial launder 12 passes through heavy phase
Agent pump 13 is connected with slot 1 among the mixed solvent,
The control system includes computer, several flow monitoring devices for being connect with this computer by wireless signal and
Line density detection device, mixed solvent centre slot 1, multidirectional premixer 3 and the pipe-line mixer 4 are equipped with the stream
Measure monitoring device and online device for detecting density.
The multidirectional premixer 3 includes mixer case 3-2, and the eddy flow at the top of this mixer case 3-2 is arranged in
The outlet F of the bottom the mixer case 3-2 is arranged in device 3-1, be arranged in primary raw material at the top of the cyclone 3-1 into
Mouth A, the vane type disperser entrance B being uniformly arranged along the mixer case 3-2 circumferential side wall, vane type disperser entrance C
With vane type disperser entrance D, the measuring mouth E3-4 of the lower part the mixer case 3-2 is set, is arranged in the mixer
Format sieve plate 3-3 in shell 3-2 and positioned at lower part,
The mixer case 3-2 is the assembly of top cone, middle part cylindrical body and lower part cone, the cyclone 3-
1 runs through from the mixer case 3-2 top cone into the middle part cylindrical body of mixer case 3-2, the measuring mouth
E3-4 is arranged on the lower part centrum of the mixer case 3-2.
The format sieve plate 3-3 is located at the middle part cylindrical body bottom-up 1/5th of the mixer case 3-2.
Vane type disperser entrance B, vane type disperser entrance C and the vane type disperser entrance D is located at described
At the one third of the middle part cylindrical body of mixer case 3-2 from up to down, the vane type disperser entrance B, vane type
Disperser entrance C and vane type disperser entrance D is circumferentially in 1200Uniformly distributed, the measuring mouth E3-4 is located at described mixed
The medium position of the lower part centrum of clutch shell 3-2.
Utilize the process of coal-based needle coke pretreatment unit, it is characterised in that include the following steps:
(1) respectively from the light phase recycling design and heavy phase recycling design of light phase tower top 17 and heavy phase tower top 9, while entering mixing
Solvent medial launder 1；Solvent burden ratio amount is calculated by density difference, the mixed solvent density of slot 1 among detection mixed solvent
(conventional density value ρ100℃=0.830-850), according to this detected value, then the standard of control solvent density and solvent burden ratio relationship
Curve (before manufacture, is demarcated solvent burden ratio using two kinds of fresh solvents, be mixed to get the standard curve by quasi-), meter
Calculation obtains the magnitude of recruitment of fresh aromatic solvent or aliphatic solvent；
(2) two kinds of mixed solvents for entering slot 1 among mixed solvent, are extracted out by multidirectional premixer feed pump 2 from multidirectional premix
The primary raw material import A of clutch 3 is squeezed into, and mixed solvent accounts for 90-95% in solvent burden ratio；
(3) aromatic solvent and aliphatic solvent are measured according to the ratio from side vane type disperser entrance B, vane type disperser entrance C
It squeezes into, vane type disperser entrance D is as spare mouth；
A, primary raw material import A liquid is in through A mouthfuls of cyclones under 0.01m/s-2m/s flow velocity and 0.01MPa-0.5MPa pressure
45 DEG C of rotated versions spray, and ultromotivity Stirring ability is formed inside multidirectional premixer 3；
B, B, C, D are different solvents liquid-inlet, and B, C, D liquid are in 0.01m/s-2m/s flow velocity and 0.01MPa-0.5MPa pressure
It is lower to be sprayed in 30 DEG C of degree angles with spiral form through entry impeller formula disperser, it is generated with the main feed that main material import A enters
Collision mixes under the effect of ultromotivity Stirring；
C, incorporation time is -30 seconds 25 seconds in multidirectional premixer 3, then through multidirectional 3 bottom format sieve plate 3-3 of premixer
It is flowed out after shearing, current stabilization by lower part outlet F；
D, it detects to obtain qualified mixed solvent (conventional density value in multidirectional 3 measuring mouth E3-4 of premixer, measuring mouth E3-4
ρ100℃=0.830-0.850)；
(4) it is completed in multidirectional premixer 3 when solvent sufficiently mixed in the duct by outlet F outflow and maltha after proportion mixing
It closes, then is sufficiently mixed by pipe-line mixer 4, and (it is heavy to meet for setting sample tap detection mixing oil density after pipe-line mixer 4
Desired conventional density value ρ drops20℃=1.051)；
(5) enter the progress of subsider 5 weight with the well-mixed solvent of maltha mutually to separate；The interface of final settlement qualification is heavy
At the thief hatch for dropping slot 5, pass through density (the conventional density value ρ of detection extraction light phase oil20℃=1.037) come quickly to judge light phase oil
Sedimentation is qualified, or passes through the foundation of the two density values of light phase oil and miscella changed as solvent than adjustment；
(6) light phase oil enters in light phase feeder trough 14 after separating, and heats through the feeding light phase tube furnace 16 of light phase feed pump 15 laggard
Enter light phase tower 17, the light phase solvent of 17 recovered overhead of light phase tower enters among light phase solvent after light phase solvent cooler 18 is cooling
Slot 19 enters back into slot 1 among mixed solvent and is recycled, purification maltha of the 17 tower bottom quinoline insolubles of light phase tower less than 0.1%
It send to tank field medial launder；
(7) heavy phase oil enters in heavy phase feeder trough 6 after separating, and is sent into after heavy phase tube furnace 8 heats through heavy phase feed pump 7 and enters weight
The heavy phase solvent of phase tower 9,9 recovered overhead of heavy phase tower enters heavy phase solvent medial launder 12 after heavy phase solvent cooler 11 is cooling,
Slot 1 among mixed solvent is entered back into be recycled, 9 tower bottom pitch of heavy phase tower be sent to tank field medial launder as binder pitch outside
It sells.
Flow monitoring value and online Density Detection in each step is as a result, feed back to control system by signal, through counting
Calculation machine or the artificial adjustment calculated and match when inlet amount by control system direct control operation items；And in inlet amount and solvent
When the adjustment of the indexs such as proportion, by on-line checking and progress real-time monitoring is calculated.
Coal-based needle coke pretreatment unit and process purpose of the invention is to provide a kind of coal-based needle coke pretreatment
Abbreviated system and method, to overcome deficiency present in raw material pretreatment process.Coal-based needle coke pretreatment of the invention is short
Flow process and method mainly pass through multidirectional premixer 3 and replace several solvent surge-tanks, calculate solvent with density difference
Blending amount realizes, the solvent burden ratio amount that directly mixes in multidirectional premixer 3, while subsider 5 can also reduce by 1/2 appearance
Product, without the buffering capacity volume for considering 5 solvent burden ratio of subsider.
The recycling design that two kinds of mixed solvents are pushed up respectively from the top of light phase tower 17 and heavy phase tower 9, recycling design enter simultaneously
Slot 1 among mixed solvent is extracted out by multidirectional premixer feed pump 2 and is beaten from the primary raw material import A of multidirectional premixer 3
Enter, mixed solvent accounts for 90-95% in solvent burden ratio, so will as main solvent return match other two fresh solvent: aromatic solvent and
Aliphatic solvent is measured squeeze into according to the ratio from side vane type disperser entrance B, vane type disperser entrance C, vane type disperser
Entrance D is flowed out and maltha after solvent completes proportion mixing in multidirectional premixer 3 by lower part outlet F as spare mouth
It mixes, then is sufficiently mixed by pipe-line mixer 4 in the duct, carry out weight subsequently into subsider 5 and mutually separate, it is light after separation
Mutually oil is into light phase tower 17, and the mixed solvent of recovered overhead enters slot 1 among mixed solvent and is recycled, and tower bottom quinoline insolubles are small
Purification maltha in 0.1% is sent to tank field medial launder；For heavy phase oil into heavy phase tower 9, it is molten that the mixed solvent of recovered overhead enters mixing
Agent medial launder 1 is recycled, and tower bottom pitch is sent to tank field medial launder and takes out as binder pitch.
The method for realizing this technique is that solvent burden ratio amount is calculated by density difference, and it is molten to first have to detection mixing
Mixed solvent density (the conventional density value ρ of agent medial launder 1100℃=0.830-850), it is close according to this detected value, then control solvent
The standard curve of degree and solvent burden ratio relationship (before manufacture, is demarcated solvent burden ratio using two kinds of fresh solvents, by quasi-
It is mixed to get the standard curve), the magnitude of recruitment of fresh aromatic solvent or aliphatic solvent is calculated, then pass through multidirectional premixing
Device 3 is pre-mixed with mixed solvent.It detects to obtain qualified mixed solvent (routine in multidirectional 3 measuring mouth E3-4 of premixer
Density value ρ100℃=0.830-0.850).Then maltha is sufficiently mixed by pipeline and mixed solvent through pipe-line mixer 4, and
Sample tap detection mixing oil density is set after pipe-line mixer 4 and (meets the conventional density value ρ of settlement request20℃=1.051), most
The qualified interface of sedimentation is at the thief hatch of subsider 5 eventually, and passes through density (the conventional density value ρ of detection extraction light phase oil20℃=
1.037) come quickly to judge that the sedimentation of light phase oil is qualified；It can also be by the variation of light phase oil and miscella the two density values as molten
Foundation of the agent than adjustment.In summary: raw material maltha mix with qualified solvent and the allocation process of qualification solvent in, can
By the flow monitoring value of each materials such as raw material maltha, qualified solvent, recycling mixed solvent and online Density Detection as a result, passing through
Signal feeds back to DCS control room, through computer or it is artificial calculate and by DCS control room direct control operation items with when feeding
The simplified control of automation or semi-automation is realized in the adjustment of amount；And in the adjustment of the indexs such as inlet amount and solvent burden ratio, it can lead to
It crosses on-line checking and calculates to be regulated and controled in time, system disorders and cost is avoided to waste.
Embodiment:
650 kgs/hour of kerosene solvents are squeezed among mixed solvent in slot 1 by light phase solvent pump 20,1000 kgs/hour of washing oil
Solvent is squeezed among mixed solvent in slot 1 by heavy phase solvent pump 13, kerosene: washing oil=0.65:1 after mixing, mixed solvent by
Multidirectional premixer feed pump 2 squeezes into 3 A mouthfuls of multidirectional premixer, kerosene and washing oil solvent, public by 72 from side B mouthfuls, C mouthfuls
Jin/hour and 111 kgs/hour are squeezed into, after solvent completes proportion mixing in multidirectional premixer 3 by F mouthful outflows and
1830 kgs/hour of malthas mix in pipe-line mixer 4, mutually separate subsequently into weight is carried out in subsider 5, after separation
2930 kgs/hour of light phase oil enter in light phase feeder trough 14, heat through the feeding light phase tube furnace 16 of light phase feed pump 15 laggard
Enter in light phase tower 17, it is molten that 879 kgs/hour of light phase solvents of recovered overhead enter light phase after light phase solvent cooler 18 is cooling
Agent medial launder 19 is recycled, and 2051 kg/hour purification malthas of the tower bottom quinoline insolubles less than 0.1% are by refined bitumen
Pump 21 is sent to tank field.733 kgs/hour of heavy phase oil are isolated in subsider 5 to enter in heavy phase oil groove 6, are sent through heavy phase feed pump 7
Enter after heavy phase tube furnace 8 heats and enter in heavy phase tower 9,183 kgs/hour of heavy phase solvents of recovered overhead are cooling through heavy phase solvent
Enter heavy phase solvent medial launder 12 after device 11 is cooling to be recycled, 550 kgs/hour of pitches of tower bottom are produced by binder pitch and pumped
10 send to tank field.
Coal-based needle coke pretreatment unit of the invention and process, mixed with qualified solvent in raw material maltha and
It, can be by the flow monitoring value of each materials such as raw material maltha, qualified solvent, recycling mixed solvent in the allocation process of qualified solvent
With online Density Detection as a result, feeding back to computer by signal, match through computer or the artificial direct control operation items that calculate
The simplified control of automation or semi-automation is realized in the when adjustment of inlet amount；And in the indexs tune such as inlet amount and solvent burden ratio
When whole, it by on-line checking and can calculate to be regulated and controled in time, system disorders and cost is avoided to waste.
Claims (6)
1. a kind of coal-based needle coke pretreatment unit, it is characterised in that including light phase solvent recovering system, heavy phase solvent recovery system
System, the mixed solvent pretreatment system being connected respectively with the light phase solvent recovering system and heavy phase solvent recovering system, with
The control system that this mixed solvent pretreatment system is connected,
The mixed solvent pretreatment system includes slot among mixed solvent, is mixed by multidirectional premixer feed pump with described
The multidirectional premixer that bonding solvent medial launder is connected, the pipeline being connected with the outlet of this multidirectional premixer by pipeline are mixed
Clutch, the subsider being connected with this pipe-line mixer,
The light phase solvent recovering system includes the light phase feeder trough being connected with the subsider, passes through light phase feed pump
The light phase tube furnace being connected with the light phase feeder trough, the light phase tower being connected with this light phase tube furnace, with this light phase tower bottom
The refined bitumen pump that portion is connected, the light phase solvent cooler being connected with the light phase top of tower are cooling with this light phase solvent
The light phase solvent medial launder that device is connected, this light phase solvent medial launder pass through slot among light phase solvent pump and the mixed solvent
It is connected,
The heavy phase solvent recovering system includes the heavy phase feeder trough being connected with the subsider, passes through heavy phase feed pump
The heavy phase tube furnace being connected with the heavy phase feeder trough, the heavy phase tower being connected with this heavy phase tube furnace, with this heavy phase tower bottom
The binder pitch that portion is connected produces pump, and the heavy phase solvent cooler being connected with the heavy phase top of tower is molten with this heavy phase
The heavy phase solvent medial launder that agent cooler is connected, this heavy phase solvent medial launder pass through heavy phase solvent pump and the mixed solvent
Medial launder is connected,
The control system includes computer, several flow monitoring devices for being connect with this computer by wireless signal and
Line density detection device, mixed solvent centre slot, multidirectional premixer and the pipe-line mixer are equipped with the flow
Monitoring device and online device for detecting density.
2. coal-based needle coke pretreatment unit according to claim 1, it is characterised in that the multidirectional premixer packet
Mixer case is included, the cyclone at the top of this mixer case is set, the outlet F of the mixer case bottom is set,
The primary raw material import A of the cyclone apex is set, the vane type being uniformly arranged along the mixer case circumferential side wall
Disperser entrance B, vane type disperser entrance C and vane type disperser entrance D, are arranged in the survey of the mixer case lower part
Mouth E is measured, the format sieve plate of lower part is arranged in the mixer case and is located at,
The mixer case is the assembly of top cone, middle part cylindrical body and lower part cone, and the cyclone is from institute
The mixer case top cone stated runs through into the middle part cylindrical body of mixer case, and the measuring mouth E is arranged described
On the lower part centrum of mixer case.
3. coal-based needle coke pretreatment unit according to claim 2, it is characterised in that the format sieve plate is located at institute
It states at the middle part cylindrical body bottom-up 1/5th of mixer case.
4. coal-based needle coke pretreatment unit according to claim 2, it is characterised in that the vane type disperser enters
Mouthful B, vane type disperser entrance C and vane type disperser entrance D be located at the middle part cylindrical body of the mixer case on to
Under one third at, vane type disperser entrance B, the vane type disperser entrance C and vane type disperser entrance D exist
It is in 120 on circumference0Uniformly distributed, the measuring mouth E is located at the medium position of the lower part centrum of the mixer case.
5. utilizing the process of coal-based needle coke pretreatment unit, it is characterised in that include the following steps:
(1) respectively from the light phase recycling design and heavy phase recycling design of light phase tower top and heavy phase tower top, while it is molten to enter mixing
Agent medial launder；Solvent burden ratio amount is calculated by density difference, the mixed solvent density of slot is (conventional among detection mixed solvent
Density value ρ100℃=0.830-850), according to this detected value, then the standard curve of control solvent density and solvent burden ratio relationship
(before manufacture, being demarcated using two kinds of fresh solvents to solvent burden ratio, be mixed to get the standard curve by quasi-), is calculated
To fresh aromatic solvent or the magnitude of recruitment of aliphatic solvent；
(2) two kinds of mixed solvents for entering slot among mixed solvent, are extracted out by multidirectional premixer feed pump from multidirectional premixing
The primary raw material import A of device is squeezed into, and mixed solvent accounts for 90-95% in solvent burden ratio；
(3) aromatic solvent and aliphatic solvent are measured according to the ratio from side vane type disperser entrance B, vane type disperser entrance C
It squeezes into, vane type disperser entrance D is as spare mouth；
A, primary raw material import A liquid is in through A mouthfuls of cyclones under 0.01m/s-2m/s flow velocity and 0.01MPa-0.5MPa pressure
45 DEG C of rotated versions spray, and form ultromotivity Stirring ability in multidirectional premixer inner；
B, B, C, D are different solvents liquid-inlet, and B, C, D liquid are in 0.01m/s-2m/s flow velocity and 0.01MPa-0.5MPa pressure
It is lower to be sprayed in 30 DEG C of degree angles with spiral form through entry impeller formula disperser, it is generated with the main feed that main material import A enters
Collision mixes under the effect of ultromotivity Stirring；
C, incorporation time is -30 seconds 25 seconds in multidirectional premixer, then sheared through multidirectional premixer bottom format sieve plate,
It is flowed out after current stabilization by lower part outlet F；
D, it detects to obtain qualified mixed solvent (conventional density value ρ in multidirectional premixer measuring mouth E, measuring mouth E100℃=
0.830-0.850)；
(4) it is completed in multidirectional premixer when solvent sufficiently mixed in the duct by outlet F outflow and maltha after proportion mixing
It closes, then is sufficiently mixed by pipe-line mixer, and sample tap is set after pipe-line mixer and detects (the satisfaction sedimentation of mixing oil density
It is required that conventional density value ρ20℃=1.051)；
(5) enter subsider progress weight with the well-mixed solvent of maltha mutually to separate；The interface of final settlement qualification is heavy
At the thief hatch for dropping slot, pass through density (the conventional density value ρ of detection extraction light phase oil20℃=1.037) come quickly to judge light phase oil
Sedimentation is qualified, or passes through the foundation of the two density values of light phase oil and miscella changed as solvent than adjustment；
(6) light phase oil enters in light phase feeder trough after separating, and enters light phase after light phase feed is pumped into light phase diamond heating
The light phase solvent of tower, the recycling of light phase column overhead enters light phase solvent medial launder after light phase solvent cooler is cooling, enters back into mixed
Bonding solvent medial launder is recycled, and purification maltha of the light phase tower tower bottom quinoline insolubles less than 0.1% is sent to tank field medial launder；
(7) heavy phase oil enters in heavy phase feeder trough after separating, and enters heavy phase after heavy phase feed is pumped into heavy phase diamond heating
The heavy phase solvent of tower, the recycling of heavy phase column overhead enters heavy phase solvent medial launder after heavy phase solvent cooler is cooling, enters back into mixed
Bonding solvent medial launder is recycled, and heavy phase tower tower bottom pitch is sent to tank field medial launder and takes out as binder pitch.
6. the process according to claim 5 using coal-based needle coke pretreatment unit, it is characterised in that Mei Gebu
Flow monitoring value and online Density Detection in rapid is as a result, feed back to control system by signal, through computer or artificial calculating
And the adjustment by control system direct control operation items with when inlet amount；And it is adjusted in the indexs such as inlet amount and solvent burden ratio
When, by on-line checking and calculate progress real-time monitoring.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115216324A (en) * | 2022-06-29 | 2022-10-21 | 鞍钢化学科技有限公司 | System and method for prolonging operation period of coal-based needle coke pretreatment settling tank |
Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0423960A1 (en) * | 1989-10-16 | 1991-04-24 | The Standard Oil Company | Heavy oil upgrating under dense fluid phase conditions utilizing emulsified feed stocks |
| CN1793287A (en) * | 2005-12-29 | 2006-06-28 | 中钢集团鞍山热能研究院 | Process for producing tar needle-shape coke raw material |
| US20100126911A1 (en) * | 2008-11-26 | 2010-05-27 | Tapantosh Chakrabarty | Method For Using Native Bitumen Markers To Improve Solvent-Assisted Bitumen Extraction |
| CN101724424A (en) * | 2008-10-21 | 2010-06-09 | 上海宝钢化工有限公司 | Method for purifying maltha by using solvent deposition method |
| CN103320151A (en) * | 2013-07-08 | 2013-09-25 | 鞍山星源达科技有限公司 | Coke oven tamping machine for tests and uniform density control method thereof |
| CN106147835A (en) * | 2015-03-30 | 2016-11-23 | 中国石油大学(北京) | A kind of combined method separating catalytic cracked oil pulp and preparing oil system needle coke |
| CA2935112A1 (en) * | 2015-07-02 | 2017-01-02 | Dan Giesbrecht | System and process for estimating solvent recovery |
| KR101832362B1 (en) * | 2016-12-06 | 2018-02-26 | 곽호준 | Apparatus for disposing waste vinyl and plastic |
| CN108587665A (en) * | 2018-05-21 | 2018-09-28 | 卢素珠 | A kind of uniformly heated melting plant of asphalt |
| CN109253943A (en) * | 2018-08-23 | 2019-01-22 | 辽宁科技大学 | The monitoring method of oil nature is mixed in a kind of coal-based needle coke production process |
| CN109935784A (en) * | 2017-12-19 | 2019-06-25 | 宁德时代新能源科技股份有限公司 | Positive plate and electrochemical cell |
| CN210683689U (en) * | 2019-09-30 | 2020-06-05 | 鞍山兴德工程技术有限公司 | Coal-based needle coke pretreatment device |
-
2019
- 2019-09-30 CN CN201910940162.6A patent/CN110527539A/en active Pending
Patent Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0423960A1 (en) * | 1989-10-16 | 1991-04-24 | The Standard Oil Company | Heavy oil upgrating under dense fluid phase conditions utilizing emulsified feed stocks |
| CN1793287A (en) * | 2005-12-29 | 2006-06-28 | 中钢集团鞍山热能研究院 | Process for producing tar needle-shape coke raw material |
| CN101724424A (en) * | 2008-10-21 | 2010-06-09 | 上海宝钢化工有限公司 | Method for purifying maltha by using solvent deposition method |
| US20100126911A1 (en) * | 2008-11-26 | 2010-05-27 | Tapantosh Chakrabarty | Method For Using Native Bitumen Markers To Improve Solvent-Assisted Bitumen Extraction |
| CN103320151A (en) * | 2013-07-08 | 2013-09-25 | 鞍山星源达科技有限公司 | Coke oven tamping machine for tests and uniform density control method thereof |
| CN106147835A (en) * | 2015-03-30 | 2016-11-23 | 中国石油大学(北京) | A kind of combined method separating catalytic cracked oil pulp and preparing oil system needle coke |
| CA2935112A1 (en) * | 2015-07-02 | 2017-01-02 | Dan Giesbrecht | System and process for estimating solvent recovery |
| KR101832362B1 (en) * | 2016-12-06 | 2018-02-26 | 곽호준 | Apparatus for disposing waste vinyl and plastic |
| CN109935784A (en) * | 2017-12-19 | 2019-06-25 | 宁德时代新能源科技股份有限公司 | Positive plate and electrochemical cell |
| CN108587665A (en) * | 2018-05-21 | 2018-09-28 | 卢素珠 | A kind of uniformly heated melting plant of asphalt |
| CN109253943A (en) * | 2018-08-23 | 2019-01-22 | 辽宁科技大学 | The monitoring method of oil nature is mixed in a kind of coal-based needle coke production process |
| CN210683689U (en) * | 2019-09-30 | 2020-06-05 | 鞍山兴德工程技术有限公司 | Coal-based needle coke pretreatment device |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115216324A (en) * | 2022-06-29 | 2022-10-21 | 鞍钢化学科技有限公司 | System and method for prolonging operation period of coal-based needle coke pretreatment settling tank |
| CN115216324B (en) * | 2022-06-29 | 2023-12-08 | 鞍钢化学科技有限公司 | System and method for prolonging operation period of coal-based needle coke pretreatment settling tank |
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