CN104962314A - System and method for producing raw material of needle coke by oil slurry - Google Patents
System and method for producing raw material of needle coke by oil slurry Download PDFInfo
- Publication number
- CN104962314A CN104962314A CN201510340928.9A CN201510340928A CN104962314A CN 104962314 A CN104962314 A CN 104962314A CN 201510340928 A CN201510340928 A CN 201510340928A CN 104962314 A CN104962314 A CN 104962314A
- Authority
- CN
- China
- Prior art keywords
- unit
- liquid separation
- raw material
- needle
- electrostatic solid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Coke Industry (AREA)
Abstract
The invention discloses a system for producing a raw material of needle coke by oil slurry. The system comprises a vacuum distillation unit, an electrostatic solid-liquid separation unit and an extraction unit. The vacuum distillation unit is connected with the electrostatic solid-liquid separation unit through a pipeline, and the extraction unit is connected with the electrostatic solid-liquid separation unit or the vacuum distillation unit through a pipeline. Solid particles are removed by process combination of vacuum distillation and electrostatic solid-liquid separators; effective components of the raw material for producing the needle coke are obtained by process combination of vacuum distillation and extraction; catalyst particles, especially catalyst particles with diameters smaller than 5 micrometers, in oil slurry can be removed effectively, and solid content in the oil slurry after processing is lower than 10 ppm.
Description
Technical field
The present invention relates to petrochemical complex, carbon material technical field, particularly relate to the system and method that a kind of slurry oil produces needle-shape coke raw material.
Background technology
Needle coke is a fine quality in carbon material, and be the main raw material producing superpower and smelting steel in ultrahigh-power electric furnace Graphite Electrodes, its greying goods are widely used in Electric furnace steel making electrode, nuclear reactor decelerating material and rocketry.According to the difference of raw materials for production, needle coke can be divided into oil system needle coke and coal-based needle coke two kinds.Take petroleum heavy oil as the needle coke of raw material production be oil system, the needle coke being raw material production with coal-tar pitch and cut thereof is for coal measures.
The problem of producing needle coke most critical is selection and the pre-treatment of raw material.The ingredient requirement short-side chain polycyclic aromatic hydrocarbon content of production needle coke is high, colloidal bitumen content is low.Catalytic slurry is rich in short-side chain condensed-nuclei aromatics, removes its undesirable components by certain treatment process, thus meets the component requirements producing needle coke, is the Major Fine raw material of oil system needle coke.
Catalytic slurry is usually containing a certain amount of solid particulate, and concentration is usually at about 1000 ~ 3500ppm, and be mainly catalyst fines and a certain amount of coke powder, what have a strong impact on slurry oil utilizes scope.Solia particle in raw material almost 100% is trapped in needle coke product, directly affects the ash content of needle coke.Solia particle content also can affect formation and the growth of mesophasespherule, finally affects the quality of needle coke.The slurry oil that solia particle content is high can only be used as the raw material of usual production, and in slurry oil during solid load <100ppm, can be used to produce needle coke, therefore, the solid particulate removed in catalytically cracked oil is very necessary.
In slurry oil, the median size of contained catalyzer is about 10-20 μm, and wherein about 20% is the fine particles of less than 5 μm.The sedimentation that current industrial production is conventional and filtration unit, cannot remove these fine particles by continuous print in a large number, and particularly the fine particles of less than 5 μm is difficult to remove especially.Filtration method needs the screen cloth fine and closely woven on an equal basis with particle in theory, is easy to blocking.Electrostatic solid-liquid separator, tiny particulate more easily adsorbs, and the solid load after process can be made to reach below 10ppm, even lower.
Existing catalytic slurry treatment system, be the combined system adopting " underpressure distillation+extracting ", its method adopts the combination process of extracting+underpressure distillation, makes slurry oil purifying, produces needle-shape coke raw material.Slurry oil, after vacuum distillation apparatus removing bituminous matter and partially catalyzed agent, extracts aromatic component, as the raw material producing needle coke.
Needle-shape coke raw material solid content after the process of existing slurry oil refining system is unstable, can affect the quality index such as the intensity of needle coke product in follow-up system, and underproof raw material can only be done over again or demote the raw material processed as usual production.Like this, for guaranteeing the needle-shape coke raw material that production department is qualified, during buying raw material slurry oil, the slurry oil that solid content is low can only be selected, comparatively tight to solid load index request, limit the source of raw material slurry oil, thus add production cost, have influence on the economic benefit of enterprise.
Particles contained average about 10-20 micron in slurry oil, wherein about 20% is the fine particle of less than 5 microns; Adopt traditional filtering type equipment cannot remove these particulates continuously in a large number, existing slurry oil pretreatment system is in operation and can removes greater particle size catalyst particles, but effectively can not remove the catalyst particles of less than 5 microns tiny.Especially, the colloid in slurry oil, bituminous matter to be competed adsorption phenomena in electrostatic separation process and catalyst particles, affect solia particle removal effect.
Summary of the invention
For solving the technical problem of existing existence, the invention provides the system and method that a kind of slurry oil produces needle-shape coke raw material.
For achieving the above object, technical scheme of the present invention is achieved in that
Slurry oil produces a system for needle-shape coke raw material, and described system comprises: underpressure distillation unit, electrostatic solid-liquid separation unit, extraction unit; Wherein, described underpressure distillation unit is connected with described electrostatic solid-liquid separation unit by pipeline; Described extraction unit is connected with described electrostatic solid-liquid separation unit or described underpressure distillation unit by pipeline.
Wherein, described electrostatic solid-liquid separation unit comprises electrostatic solid-liquid separator, described electrostatic solid-liquid separator comprises direct supply, programmable logic controller and multiple electrostatic solid-liquid separation module, described direct supply connects described multiple electrostatic solid-liquid separation module, for described multiple electrostatic solid-liquid separation module produces electric field; Described programmable logic controller connects described multiple electrostatic solid-liquid separation module, controls the running status of electrostatic solid-liquid separation module described in each; In parallel between electrostatic solid-liquid separation module described in each.
Wherein, described system comprises a described electrostatic solid-liquid separation unit; Or described system comprises electrostatic solid-liquid separation unit described in two or more, between each described electrostatic solid-liquid separation unit, series system is adopted to connect.
Wherein, described underpressure distillation unit comprises interchanger, process furnace and vacuum still; Described interchanger is connected by the import of pipeline with described process furnace, the outlet of described process furnace is connected by the entrance of pipeline with described vacuum still, and the outlet of described vacuum still is connected by the electrostatic solid-liquid separator of pipeline with described electrostatic solid-liquid separation unit.
Wherein, described extraction unit comprises extraction plant and solvent recovery unit; Outlet, the entrance of described extraction plant are connected with described solvent recovery unit respectively by pipeline; The entrance of described extraction plant connects the outlet of described electrostatic solid-liquid separation unit, and outlet exports needle-shape coke raw material; Or the entrance input slurry oil raw material of described extraction plant, outlet connects the entrance of described underpressure distillation unit.
Wherein, described system also comprises: hydrofining unit; If described extraction unit is connected with described electrostatic solid-liquid separation unit by pipeline, then described hydrofining unit connects the outlet of described extraction unit; If described extraction unit is connected with described underpressure distillation unit by pipeline, then described hydrofining unit connects the outlet of described electrostatic solid-liquid separation unit.
Slurry oil produces a method for needle-shape coke raw material, and described method comprises:
Raw material slurry oil enters underpressure distillation unit and carries out underpressure distillation, isolates lightweight oil component, stage casing oil ingredient and tail oil component;
Described stage casing oil ingredient enters electrostatic solid-liquid separation unit and carries out electrostatic solid-liquid separation, the solia particle that removing is remaining, obtains refining stage casing oil;
Described refining stage casing oil enters extraction unit and carries out solvent extraction, obtains needle-shape coke raw material.
Wherein, after obtaining needle-shape coke raw material, described method also comprises: described needle-shape coke raw material enters the hydrotreatment of hydrofining unit, to adjust the component concentration in described needle-shape coke raw material.
Slurry oil produces a method for needle-shape coke raw material, and described method comprises: raw material slurry oil enters extraction unit and carries out solvent extraction, extracts heavy aromatics component; Extract the raw material slurry oil after heavy aromatics component to enter underpressure distillation unit and carry out underpressure distillation, isolate the stage casing oil ingredient being applicable to produce needle-shape coke raw material; Described stage casing oil ingredient enters electrostatic solid-liquid separation unit and carries out electrostatic solid-liquid separation, the solia particle that removing is remaining, obtains needle-shape coke raw material.
Wherein, after obtaining needle-shape coke raw material, described method also comprises: described needle-shape coke raw material enters the hydrotreatment of hydrofining unit, to adjust the component concentration in described needle-shape coke raw material.
The present invention adopts electrostatic solid-liquid separation to remove except the catalyst particles in slurry oil, and advantage is that the temperature be separated is low, and resistance is little, and separation efficiency is higher, particularly thinner powder, is more easily adsorbed.By " underpressure distillation+electrostatic divides solid-liquid from device " process combination removing solia particle, the active principle producing needle-shape coke raw material is obtained by " underpressure distillation+extracting " process combination, effectively can remove the catalyst particles in slurry oil, the particularly catalyst particles of less than 5 microns tiny, makes the solid load after process reach below 10ppm.
First the solia particles such as most of catalyzer are excised through underpressure distillation in the present invention, effectively can alleviate the load of electrostatic separation, resin and asphalt etc. has also been excised in underpressure distillation simultaneously, eliminates the competitive adsorption phenomenon of electrostatic separation process, improves solia particle removal effect.
Accompanying drawing explanation
In accompanying drawing (it is not necessarily drawn in proportion), similar Reference numeral can describe similar parts in different views.The similar reference numerals with different letter suffix can represent the different examples of similar parts.Accompanying drawing generally shows each embodiment discussed herein by way of example and not limitation.
Fig. 1 is the composition structural representation that a kind of slurry oil of the embodiment of the present invention produces the system of needle-shape coke raw material;
Fig. 2 is the composition structural representation of the electrostatic solid-liquid separator of the embodiment of the present invention;
Fig. 3 is the composition structural representation of embodiment of the present invention hydrofining unit;
Fig. 4 is the schematic flow sheet that a kind of slurry oil of the embodiment of the present invention produces needle-shape coke raw material method;
Fig. 5 is the schematic flow sheet that the another kind of slurry oil of the embodiment of the present invention produces needle-shape coke raw material method;
Wherein, 1, interchanger, 2, process furnace, 3, vacuum still, 4, electrostatic solid-liquid separator, 5, extraction plant, 6, solvent recovery unit, 7, underpressure distillation unit, 8, electrostatic solid-liquid separation unit, 9, extraction unit, 10, hydrofining unit, 11, reaction unit, 12, gas-liquid separation device, 13, desulfurizer, 14, recycle hydrogen compression set.
Embodiment
For the deficiencies in the prior art, on the basis of existing technology, provide a kind of slurry oil to produce the system of needle-shape coke raw material, this system is particularly suited for the catalytic slurry of high solids content to produce needle-shape coke raw material in the present invention.
Embodiment one
As shown in Figure 1, a kind of slurry oil of the embodiment of the present invention produces the system of needle-shape coke raw material, comprises underpressure distillation unit 7, electrostatic solid-liquid separation unit 8, extraction unit 9; Wherein, underpressure distillation unit 7 is connected with electrostatic solid-liquid separation unit 8 by pipeline; Electrostatic solid-liquid separation unit 8 is connected with extraction unit 9 by pipeline.
Particularly, in the present embodiment, underpressure distillation unit 7 being placed on the first paragraph of whole system, is then electrostatic solid-liquid separation unit 8, is extraction unit 9 after electrostatic solid-liquid separation unit 8.That is, the outlet of underpressure distillation unit 7 is connected with the entrance of electrostatic solid-liquid separation unit 8, and the outlet of electrostatic solid-liquid separation unit 8 is connected with the entrance of extraction unit 9, and the outlet of extraction unit 9 obtains needle-shape coke raw material.
Particularly, as shown in Figure 1, underpressure distillation unit 7 comprises interchanger 1, process furnace 2, vacuum still 3, and wherein, the entrance of vacuum still 3 connects process furnace 2 by pipeline.Interchanger 1 is connected by the import of pipeline with process furnace 2; The outlet of process furnace 2 is connected by the entrance of pipeline with vacuum still 3, and the outlet of vacuum still 3 is connected with the electrostatic solid-liquid separator 4 of electrostatic solid-liquid separation unit 8 by pipeline.As shown in Figure 1, raw material, after interchanger 1 heat exchange, enters process furnace 2, and after this in technical process, temperature progressively reduces, and Appropriate application heat energy, reduces the wastage.
As shown in Figure 1, electrostatic solid-liquid separation unit 8 adopts electrostatic solid-liquid separator 4, and the entrance of electrostatic solid-liquid separator 4 connects the vacuum still 3 of underpressure distillation unit 7 by pipeline, export the extraction plant 5 being connected extraction unit 9 by pipeline.Here, the application of electrostatic solid-liquid separator 4, effectively can remove the catalyst particles in slurry oil, particularly the catalyst particles of less than 5 microns tiny, makes the solid load after process reach below 10ppm, can process the slurry oil raw material of high solids content.
Electrostatic solid-liquid separation unit 8 adopts electrostatic solid-liquid separator 4.Except electrostatic solid-liquid separator, traditional technology has the modes such as mechanical type separation, filtering type separation, but effect is bad.As shown in Figure 2, electrostatic solid-liquid separator 4 mainly comprises direct supply 41, multiple electrostatic solid-liquid separation module 42 and programmable logic controller (PLC) 43 etc.Described direct supply connects described multiple electrostatic solid-liquid separation module, for described multiple electrostatic solid-liquid separation module produces electric field; Described programmable logic controller connects described multiple electrostatic solid-liquid separation module, controls the running status of each described electrostatic solid-liquid separation module.The core texture of electrostatic solid-liquid separator is electrostatic solid-liquid separation module 42, and other structures are served for electrostatic solid-liquid separation module 42.The effect of direct supply 41 produces electric field, is not pump power current, neither electric consumption on lighting.The effect of programmable logic controller 43 is the valves controlling each electrostatic solid-liquid separation module 42, and each electrostatic solid-liquid separation module 42 is run automatically.After running for some time, the solia particle of absorption increases, and needs back flushing, has rinsed follow-up reforwarding row.Be in parallel between each electrostatic solid-liquid separation module 42, what have carries out back flushing, and namely some work carry out electrostatic separation process, and these processes automatically control.That is, the running status of each electrostatic solid-liquid separation module 42 is controlled automatically by programmable logic controller 43.In practical application, electrostatic solid-liquid separator 4 is modular organization, and improve treatment capacity by increasing number of modules, the quantity namely by increasing electrostatic solid-liquid separation module 42 improves the treatment capacity of electrostatic solid-liquid separator 4.
In practical application, electrostatic solid-liquid separation unit 8 can adopt the mode of two-stage tandem to dispose.That is, two electrostatic solid-liquid separation units 8 can be set in the system of the present invention, series system is adopted to connect between two described electrostatic solid-liquid separation units, the entrance of a described electrostatic solid-liquid separation unit connects described underpressure distillation unit, and the entrance of another electrostatic solid-liquid separation unit connects the outlet of this electrostatic solid-liquid separation unit.Through twice electrostatic separation, separating effect can be improved, but can cost be increased, can arrange as required like this.
Particularly, as shown in Figure 1, extraction unit 9 comprises extraction plant 5, solvent recovery unit 6.Extraction plant 5 is connected with solvent recovery unit 6 by pipeline.Outlet, the entrance of extraction plant 5 are connected with solvent recovery unit 6 respectively by pipeline.In practical application, the circulating solvent of solvent recovery unit 6 preferably uses wet furfural, and wet furfural has no significant effect quality of raffinating oil, and also simplify the technical process of Solvent recovery portion simultaneously, decreases equipment, saved investment.In practical application, extraction plant 5 is preferably extraction tower.
In addition, slurry oil of the present invention is produced in the system of needle-shape coke raw material can also increase a set of hydrofining unit again.In practical application, hydrofining unit is arranged on the final stage of system of the present invention, its sulphur content can be reduced by the hydrotreatment of hydrofining unit when needle-shape coke raw material sulphur content is high, and make the aromatic nucleus hydrotreated lube base oil that wherein part is connected with sulphur, component concentration in adjustment needle-shape coke raw material, remove the nonideal chemical composition of some trace, make the needle-shape coke raw material adaptability that obtains stronger, better quality, but cost also can corresponding increase many, can generate according to reality and need to arrange.Particularly, in the present embodiment, described hydrofining unit connects described extraction unit, specifically the entrance of described hydrofining unit is connected the outlet of extraction plant in described extraction unit, and the outlet of described hydrofining unit exports needle-shape coke raw material.
As shown in Figure 3, be the composition structural representation of hydrofining unit.Hydrofining unit 10 comprises: reaction unit 11, gas-liquid separation device 12, desulfurizer 13 and recycle hydrogen compression set 14.Wherein, reaction unit 11 adopts fixed-bed reactor, and catalyst for demetalation and desulfurization catalyst are housed in reactor, and hydrofining main chemical reactions has hydrogenating desulfurization, hydrodemetallation (HDM) etc.Demetalization, can prevent Hydrobon catalyst poisoning.Hydrodesulfurization reaction mainly contains two paths, and one is direct hydrogenation desulfurization, and two is the first hydrogenation of aromatic nucleus be connected with sulphur, then desulfurization.Needle-shape coke raw material after reaction unit 11 processes is separated through gas-liquid separation device 12 needle-shape coke raw material exporting high-quality after unreacted hydrogen.Adopt methyldiethanolamine to remove hydrogen sulfide by the isolated unreacting hydrogen of gas-liquid separation device 12 through desulfurizer 13, enter recycle hydrogen compression set 14 after compressing together with hydrogen make-up and carry out recycle.General needle-shape coke raw material requires that sulphur content is less than 0.5%, is less than 0.3%, can be used as the raw material of production high-quality needle coke by the product sulphur content after the hydrofining of hydrofining unit.
The system of being produced needle-shape coke raw material by the above-mentioned slurry oil of the present embodiment can realize the method that slurry oil refines production needle-shape coke raw material, the method comprises slurry oil underpressure distillation, solid-liquid separation, extractive process, the order of " underpressure distillation-electrostatic solid-liquid separation-extracting " is adopted to perform, particularly, as shown in Figure 4, key step is as follows:
Step 301, slurry oil underpressure distillation: that is, raw material slurry oil enters underpressure distillation unit and carries out underpressure distillation, isolates lightweight oil component, stage casing oil ingredient and tail oil component;
Particularly, from the raw material slurry oil of raw material tank field after interchanger 1 heat exchange, enter process furnace 2 again and be heated to 360-380 DEG C, enter vacuum still 3, vacuum still 3 therefrom isolates lightweight oil component, stage casing oil ingredient and tail oil component, and the colloid in slurry oil, bituminous matter and solia particle major part enter tail oil component.
Like this, resin and asphalt etc. has also been excised in underpressure distillation, eliminates the competitive adsorption phenomenon of electrostatic separation process, improves solia particle removal effect.
Step 302, electrostatic solid-liquid separation: that is, described stage casing oil ingredient enters electrostatic solid-liquid separation unit and carries out electrostatic solid-liquid separation, the solia particle that removing is remaining, obtains refining stage casing oil;
Particularly, stage casing oil ingredient step 301 obtained and raw material slurry oil carry out heat exchange, temperature is down to 160-200 DEG C, enter the electrostatic solid-liquid separation module 42 of electrostatic solid-liquid separator 4, produce high-voltage electric field by direct supply 41 in electrostatic solid-liquid separation module 42, solia particle generation galvanic couple polarization under the high-voltage electric field effect of electrostatic solid-liquid separation module 42, thus adsorbed, the solia particles such as the catalyzer that removing is remaining, obtain refining stage casing oil.
Here, electrostatic solid-liquid separator 4 effectively can remove the catalyst particles in slurry oil, particularly the catalyst particles of less than 5 microns tiny, makes the solid load after process reach below 10ppm.
Step 303, extractive process: that is, described refining stage casing oil enters extraction unit and carries out solvent extraction, obtains needle-shape coke raw material.
Particularly, after the refining stage casing oil that step 302 is obtained and the heat exchange of raw material slurry oil, be cooled to 40-50 DEG C, enter extraction tower and extraction plant 5 carries out solvent extraction, after extracting recovery of oil solvent out, obtain needle-shape coke raw material, after extraction plant 5 extracting, recovered solvent sends into solvent recovery unit 6 by its outlet, and solvent recovery unit 6 is sent extraction plant 5 back to by the entrance of extraction plant 5 after being refined by solvent dehydration and reused.
Here, in step 303 of the present invention, extraction plant 5 extracting adopts furfural to make solvent, agent-oil ratio 1:1, column bottom temperature 35-45 DEG C, tower top temperature 60-65 DEG C.
Here, in step 301 of the present invention, 302, by adjusting the operating parameters of vacuum still 3 and extraction plant 5, the active principle producing needle-shape coke raw material can be obtained.Slurry oil can remove bituminous matter, colloid and partially catalyzed agent through vacuum still 3, and removing bituminous matter and colloid can eliminate the competitive adsorption phenomenon of electrostatic separation process, improves solia particle removal effect.
If increase hydrofining unit in system, in correlation method, finally can also increase the step of a hydrotreatment, to reduce the sulphur content in needle-shape coke raw material, remove the nonideal chemical composition of some trace, make the needle-shape coke raw material adaptability that obtains stronger, better quality, but cost also can corresponding increase many, can generate according to reality and need to arrange.
In the present embodiment, adopt the order of " underpressure distillation-electrostatic solid-liquid separation-extracting " to process, temperature is reduced from high to low successively, makes full use of heat energy, can save energy.
Embodiment two
The slurry oil that the present embodiment provides produces the system of needle-shape coke raw material, and its composition is identical with embodiment one, unlike the annexation of underpressure distillation unit, electrostatic solid-liquid separation unit and extraction unit.In the present embodiment, extraction unit being placed on the first paragraph of whole system, is then underpressure distillation unit, is electrostatic solid-liquid separation unit after underpressure distillation unit.That is, the outlet of extraction unit is connected with the entrance of underpressure distillation unit, and the outlet of underpressure distillation unit is connected with the entrance of electrostatic solid-liquid separation unit, and the outlet of electrostatic solid-liquid separation unit exports needle-shape coke raw material.
Particularly, in extraction unit, outlet, the entrance of extraction plant are connected with solvent recovery unit respectively by pipeline.Raw material slurry oil is entered by the entrance of extraction plant, and the outlet of extraction plant connects the entrance of interchanger in underpressure distillation unit.
In underpressure distillation unit, the entrance of interchanger connects the outlet of extraction plant, exports and is connected with the import of process furnace by pipeline; The outlet of process furnace is connected with the entrance of vacuum still by pipeline, and the outlet of vacuum still is connected by the entrance of pipeline with solid-liquid separator 4 electrostatic in electrostatic solid-liquid separation unit.
In electrostatic solid-liquid separation unit, the entrance of electrostatic solid-liquid separator 4 connects the outlet of vacuum still in underpressure distillation unit by pipeline, outlet exports needle-shape coke raw material.
In the present embodiment, underpressure distillation unit, electrostatic solid-liquid separation unit are identical with embodiment one with the composition structure in extraction unit, also can adopt mode described in embodiment one, repeat no more in actual deployment and application.
The system of being produced needle-shape coke raw material by the above-mentioned slurry oil of the present embodiment can realize the method that slurry oil refines production needle-shape coke raw material, the method comprises slurry oil underpressure distillation, solid-liquid separation, extractive process, substantially identical with method described in embodiment one, difference is processing sequence.In the present embodiment, first extracting, again solid-liquid separation, last underpressure distillation, i.e. " extracting-underpressure distillation-electrostatic solid-liquid separation ".Particularly, as shown in Figure 5, the method comprises the steps:
Step 401, extractive process: raw material slurry oil, first through extraction plant, extracts heavy aromatics component;
Namely, raw material slurry oil enters extraction unit and carries out solvent extraction, extracts heavy aromatics component.
Step 402, vacuum distillation process: again through vacuum distillation apparatus, cuts out the component being applicable to produce needle coke;
Here, extract the raw material slurry oil after heavy aromatics component and enter underpressure distillation unit and carry out underpressure distillation, isolate the stage casing oil ingredient being applicable to produce needle-shape coke raw material.
Step 403, solid-liquid separation process: carry out solid-liquid separation, removing solia particle wherein, reaches needle-shape coke raw material standard.
Here, the described stage casing oil ingredient of step 402 enters electrostatic solid-liquid separation unit and carries out electrostatic solid-liquid separation, the solia particle that removing is remaining, obtains needle-shape coke raw material.
In the present embodiment, the specific implementation process of each step of aforesaid method is identical with embodiment one, repeats no more.
If increase hydrofining unit in the present embodiment, hydrofining unit can be connected to the outlet of described electrostatic solid-liquid separation unit, namely the entrance of hydrofining unit is connected to the outlet of electrostatic solid-liquid separator in electrostatic solid-liquid separation unit, exports needle-shape coke raw material by the outlet of hydrofining unit.If increase hydrofining unit in system, in correlation method, finally can also increase the step of a hydrotreatment, namely after obtaining needle-shape coke raw material, described needle-shape coke raw material is sent into the hydrotreatment of hydrofining unit, to reduce the sulphur content in needle-shape coke raw material, adjustment component concentration, component concentration in adjustment needle-shape coke raw material, remove the nonideal chemical composition of some trace, make the needle-shape coke raw material adaptability that obtains stronger, better quality, but cost also can corresponding increase many, can generate according to reality and need to arrange.
Slurry oil provided by the invention produces the system of needle-shape coke raw material, adopt underpressure distillation+extraction process, producible needle-shape coke raw material product has heavy aromatics, light aromatic hydrocarbons, wax oil, pitch, BTX aromatics etc., and heavy aromatics is mainly used in Rubber Softener, modifying asphalt, PDC softening agent, needle coke etc.
Present system adopts electrostatic solid-liquid separator to remove except the catalyst particles in slurry oil, and advantage is that the temperature be separated is low, and resistance is little, and separation efficiency is higher, particularly thinner powder, is more easily adsorbed.By " underpressure distillation+electrostatic divides solid-liquid from device " process combination removing solia particle, the active principle producing needle-shape coke raw material is obtained by " underpressure distillation+extracting " process combination, effectively can remove the catalyst particles in slurry oil, the particularly catalyst particles of less than 5 microns tiny, makes the solid load after process reach below 10ppm.First excise the solia particles such as most of catalyzer through underpressure distillation in the present invention, then the load of static separator can be alleviated through static separator, improve particulate removal effect.Through underpressure distillation excision resin and asphalt, eliminate the competitive adsorption phenomenon of electrostatic separation process, improve solia particle removal effect.
The above, be only preferred embodiment of the present invention, be not intended to limit protection scope of the present invention.
Claims (10)
1. slurry oil produces a system for needle-shape coke raw material, and it is characterized in that, described system comprises: underpressure distillation unit, electrostatic solid-liquid separation unit, extraction unit; Wherein, described underpressure distillation unit is connected with described electrostatic solid-liquid separation unit by pipeline; Described extraction unit is connected with described electrostatic solid-liquid separation unit or described underpressure distillation unit by pipeline.
2. system according to claim 1, is characterized in that, described electrostatic solid-liquid separation unit comprises electrostatic solid-liquid separator;
Described electrostatic solid-liquid separator comprises direct supply, programmable logic controller and multiple electrostatic solid-liquid separation module, and described direct supply connects described multiple electrostatic solid-liquid separation module, for described multiple electrostatic solid-liquid separation module produces electric field; Described programmable logic controller connects described multiple electrostatic solid-liquid separation module, controls the running status of electrostatic solid-liquid separation module described in each; In parallel between electrostatic solid-liquid separation module described in each.
3. system according to claim 2, is characterized in that,
Described system comprises a described electrostatic solid-liquid separation unit;
Or described system comprises electrostatic solid-liquid separation unit described in two or more, between each described electrostatic solid-liquid separation unit, series system is adopted to connect.
4. system according to claim 2, is characterized in that,
Described underpressure distillation unit comprises interchanger, process furnace and vacuum still; Described interchanger is connected by the import of pipeline with described process furnace, the outlet of described process furnace is connected by the entrance of pipeline with described vacuum still, and the outlet of described vacuum still is connected by the electrostatic solid-liquid separator of pipeline with described electrostatic solid-liquid separation unit.
5. system according to claim 1, is characterized in that,
Described extraction unit comprises extraction plant and solvent recovery unit; Outlet, the entrance of described extraction plant are connected with described solvent recovery unit respectively by pipeline;
The entrance of described extraction plant connects the outlet of described electrostatic solid-liquid separation unit, and outlet exports needle-shape coke raw material; Or the entrance input slurry oil raw material of described extraction plant, outlet connects the entrance of described underpressure distillation unit.
6. system according to claim 1, is characterized in that, described system also comprises: hydrofining unit;
If described extraction unit is connected with described electrostatic solid-liquid separation unit by pipeline, then described hydrofining unit connects the outlet of described extraction unit;
If described extraction unit is connected with described underpressure distillation unit by pipeline, then described hydrofining unit connects the outlet of described electrostatic solid-liquid separation unit.
7. slurry oil produces a method for needle-shape coke raw material, and it is characterized in that, described method comprises:
Raw material slurry oil enters underpressure distillation unit and carries out underpressure distillation, isolates lightweight oil component, stage casing oil ingredient and tail oil component;
Described stage casing oil ingredient enters electrostatic solid-liquid separation unit and carries out electrostatic solid-liquid separation, the solia particle that removing is remaining, obtains refining stage casing oil;
Described refining stage casing oil enters extraction unit and carries out solvent extraction, obtains needle-shape coke raw material.
8. method according to claim 7, is characterized in that, after obtaining needle-shape coke raw material, described method also comprises:
Described needle-shape coke raw material enters the hydrotreatment of hydrofining unit, to adjust the component concentration in described needle-shape coke raw material.
9. slurry oil produces a method for needle-shape coke raw material, and it is characterized in that, described method comprises:
Raw material slurry oil enters extraction unit and carries out solvent extraction, extracts heavy aromatics component;
Extract the raw material slurry oil after heavy aromatics component to enter underpressure distillation unit and carry out underpressure distillation, isolate the stage casing oil ingredient being applicable to produce needle-shape coke raw material;
Described stage casing oil ingredient enters electrostatic solid-liquid separation unit and carries out electrostatic solid-liquid separation, the solia particle that removing is remaining, obtains needle-shape coke raw material.
10. method according to claim 9, is characterized in that, after obtaining needle-shape coke raw material, described method also comprises: described needle-shape coke raw material enters the hydrotreatment of hydrofining unit, to adjust the component concentration in described needle-shape coke raw material.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510340928.9A CN104962314B (en) | 2015-06-18 | 2015-06-18 | Slurry oil produces the system and method for needle-shape coke raw material |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510340928.9A CN104962314B (en) | 2015-06-18 | 2015-06-18 | Slurry oil produces the system and method for needle-shape coke raw material |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104962314A true CN104962314A (en) | 2015-10-07 |
| CN104962314B CN104962314B (en) | 2017-10-03 |
Family
ID=54216414
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510340928.9A Expired - Fee Related CN104962314B (en) | 2015-06-18 | 2015-06-18 | Slurry oil produces the system and method for needle-shape coke raw material |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104962314B (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105482850A (en) * | 2016-01-12 | 2016-04-13 | 广西泓达生物能源科技有限公司 | System device for producing needle coke crude oil through catalytic slurry oil |
| CN108219839A (en) * | 2018-01-02 | 2018-06-29 | 中和亚通能源科技有限公司 | A kind of needle coke production method and device |
| CN110628447A (en) * | 2019-09-30 | 2019-12-31 | 鞍山开炭热能新材料有限公司 | Pretreatment early-stage process for coal-based needle coke raw material |
| CN111303939A (en) * | 2019-09-10 | 2020-06-19 | 武汉兰兆科技有限公司 | Method and system for producing needle coke raw oil by performing reduced pressure distillation on catalytic slurry oil and performing aromatic oil de-solidification |
| CN113817497A (en) * | 2021-09-26 | 2021-12-21 | 辽宁宝来生物能源有限公司 | Deep decompression pretreatment system for oil-based needle coke raw material |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5460713A (en) * | 1992-10-02 | 1995-10-24 | Mitsubishi Oil Co., Ltd. | Process for producing low viscosity lubricating base oil having high viscosity index |
| CN103484148A (en) * | 2013-09-29 | 2014-01-01 | 中国石油大学(华东) | Purifying equipment and purifying method for purifying catalytic cracking slurry oil |
| CN103497779A (en) * | 2013-08-15 | 2014-01-08 | 中国石油集团东北炼化工程有限公司葫芦岛设计院 | Pretreatment method for catalytic oil slurry for needle coke production |
| CN103666556A (en) * | 2012-09-03 | 2014-03-26 | 中国石油化工股份有限公司 | Preparation method of petroleum coke |
| CN104004540A (en) * | 2014-05-29 | 2014-08-27 | 嘉诚(福建)石油化工有限公司 | Method and device for separating heavy aromatics from catalytic cracking oil slurry |
| CN204824748U (en) * | 2015-06-18 | 2015-12-02 | 山东菏泽德泰化工有限公司 | System for slurry oil production needle coke raw materials |
-
2015
- 2015-06-18 CN CN201510340928.9A patent/CN104962314B/en not_active Expired - Fee Related
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5460713A (en) * | 1992-10-02 | 1995-10-24 | Mitsubishi Oil Co., Ltd. | Process for producing low viscosity lubricating base oil having high viscosity index |
| CN103666556A (en) * | 2012-09-03 | 2014-03-26 | 中国石油化工股份有限公司 | Preparation method of petroleum coke |
| CN103497779A (en) * | 2013-08-15 | 2014-01-08 | 中国石油集团东北炼化工程有限公司葫芦岛设计院 | Pretreatment method for catalytic oil slurry for needle coke production |
| CN103484148A (en) * | 2013-09-29 | 2014-01-01 | 中国石油大学(华东) | Purifying equipment and purifying method for purifying catalytic cracking slurry oil |
| CN104004540A (en) * | 2014-05-29 | 2014-08-27 | 嘉诚(福建)石油化工有限公司 | Method and device for separating heavy aromatics from catalytic cracking oil slurry |
| CN204824748U (en) * | 2015-06-18 | 2015-12-02 | 山东菏泽德泰化工有限公司 | System for slurry oil production needle coke raw materials |
Non-Patent Citations (1)
| Title |
|---|
| 白雪梅等: "浅谈催化裂化油浆的综合利用", 《内蒙古石油化工》 * |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105482850A (en) * | 2016-01-12 | 2016-04-13 | 广西泓达生物能源科技有限公司 | System device for producing needle coke crude oil through catalytic slurry oil |
| CN108219839A (en) * | 2018-01-02 | 2018-06-29 | 中和亚通能源科技有限公司 | A kind of needle coke production method and device |
| CN108219839B (en) * | 2018-01-02 | 2024-04-09 | 亚通石化集团有限公司 | Needle coke production method and device |
| CN111303939A (en) * | 2019-09-10 | 2020-06-19 | 武汉兰兆科技有限公司 | Method and system for producing needle coke raw oil by performing reduced pressure distillation on catalytic slurry oil and performing aromatic oil de-solidification |
| CN110628447A (en) * | 2019-09-30 | 2019-12-31 | 鞍山开炭热能新材料有限公司 | Pretreatment early-stage process for coal-based needle coke raw material |
| CN113817497A (en) * | 2021-09-26 | 2021-12-21 | 辽宁宝来生物能源有限公司 | Deep decompression pretreatment system for oil-based needle coke raw material |
| CN113817497B (en) * | 2021-09-26 | 2022-12-09 | 辽宁宝来生物能源有限公司 | Deep decompression pretreatment system for oil-based needle coke raw material |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104962314B (en) | 2017-10-03 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN204824748U (en) | System for slurry oil production needle coke raw materials | |
| CN103897731B (en) | A kind of catalytic cracking diesel oil and C 10+the method of distillate mixture manufacturing light aromatics | |
| CN102796559B (en) | Method and the device of oil fuel are produced in hydrocracking | |
| CN104962314A (en) | System and method for producing raw material of needle coke by oil slurry | |
| CN100558863C (en) | A kind of combined method of producing cleaning oil from coal-tar oil | |
| JP2018521162A (en) | Feedstock conversion method for producing fuel oil comprising a hydrotreating step, a hydrocracking step, a precipitation step, and a precipitate separation step | |
| WO2014183429A1 (en) | Heterogeneous suspension-bed hydrogenation method for coal-based oil product | |
| CN101445420B (en) | Process for preparing benzene aromatic hydrocarbon by crude benzene | |
| CN103540349A (en) | Low-quality heavy oil and residual oil hydrotreatment combined process capable of prolonging service life of catalyst | |
| CN102977916B (en) | Catalytic hydrogenation method and catalytic hydrogenation apparatus for coal tar | |
| CN102051221B (en) | Method for more producing light oil by using hydrocarbon oil | |
| CN105505550B (en) | A kind of method of waste lubricant oil regeneration processing | |
| CN103540353A (en) | Combined hydrogenation process method for treating coal tar and residual oil | |
| CN103305269B (en) | Method for producing gasoline and diesel by directly hydrogenating medium and low temperature coal tar | |
| CN112592736A (en) | Online solid removing method and system for catalytic slurry oil filler high-gradient electric field separation and adsorption | |
| CN104277879B (en) | A kind of two-stage slurry bed system hydrogenation technique of middle coalite tar | |
| CN104277876B (en) | A kind of two-stage slurry bed system hydrogenation technique of poor quality oil | |
| CN103540351A (en) | Combined technique for processing full fraction of coal tar | |
| CN102911721B (en) | Method for removing olefins from reformate through liquid phase circulation selective hydrogenation | |
| CN104449836A (en) | Trans-hydrocracking process of whole fractions of coal tar | |
| CN102533324A (en) | Hydrogenation combined process | |
| CN101434867A (en) | Suspension bed residual oil hydrogenation-catalytic cracking combined technological process | |
| CN103834438B (en) | A kind of processing method of hydrogenating desulfurization | |
| CN103059944B (en) | Hydrocracking technological method for processing inferior raw material | |
| CN114456842B (en) | Production system and production method of high-quality distillate oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| PP01 | Preservation of patent right |
Effective date of registration: 20180530 Granted publication date: 20171003 |
|
| PP01 | Preservation of patent right | ||
| PD01 | Discharge of preservation of patent |
Date of cancellation: 20210530 Granted publication date: 20171003 |
|
| PD01 | Discharge of preservation of patent | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20171003 Termination date: 20190618 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |