CN1954046B - Delayed coking process for producing free-flowing coke using polymeric additives - Google Patents
Delayed coking process for producing free-flowing coke using polymeric additives Download PDFInfo
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- CN1954046B CN1954046B CN2005800154051A CN200580015405A CN1954046B CN 1954046 B CN1954046 B CN 1954046B CN 2005800154051 A CN2005800154051 A CN 2005800154051A CN 200580015405 A CN200580015405 A CN 200580015405A CN 1954046 B CN1954046 B CN 1954046B
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Abstract
A delayed coking process for making substantially free-flowing coke, preferably shot coke. A coker feedstock, such as a vacuum residuum, is heated in a heating zone to coking temperatures then conducted to a coking zone wherein volatiles are collected overhead and coke is formed. A low molecular weight additive is added to the feedstock prior to it being heated in the heating zone, prior to its being conducted to the coking zone, or both.
Description
Invention field
The present invention relates to a kind of delayed coking method that is used to produce fundamental freedom mobile coke, preferred free flowing granule shape coke (shot coke).In the heating zone, coking furnace charging (as vacuum residuum) is heated to coking temperature, imports the coking district subsequently, wherein collect volatile matter and form coke at the top.Before in the heating zone, heating, before the importing coking district or before the two, the suitable polymer blend additive is added in the charging, to strengthen the formation of free-flowing coke.
Description of Related Art
Delayed coking comprises gas, liquid stream and the coke of thermolysis to generate various boiling ranges of petroleum residue (residual oil).By part residual oil being converted into more valuable liquid and gas products, postpone to use mainly as a kind of method that is used for these low value chargings of waste treatment from the residual oil in coking heavy and heavy acid (high-sulfur) crude oil.Though the coke that obtains is considered to the by product of low value usually, it can have some value, can be used as fuel (fuel grade coke), is used to generate the electrode (anode level coke) of aluminium etc. according to its quality.
In delay coking process, rapid heating charging in fired heater or tube furnace.Subsequently the charging of heating is led to and maintain in the coking drum that produces under the pyrogenic condition, typical temperature is higher than 400 ℃ and be higher than under the atmospheric pressure.The resid feed of the heating in the coking drum also forms volatile component, and volatile component removes and lead to separation column at the top, remaining coke.When the coking drum was full of coke, the charging of heating switched in another drum, and hydrocarbon vapour blows out from the coking drum with steam.Water quenching subsequently should be roused so that temperature is reduced less than 300
(149 ℃), drainage water afterwards.When cooling and drain step end, use the high speed water injection to bore and/or cut and open drum discharge coke afterwards.
Usually use and portal from the coke beds center drill from the high-pressure water jet that is positioned at the nozzle on the drill tools.The nozzle of the head horizontal alignment of parting tool cuts out coke from this drum subsequently.Coke excision step has increased the time of passing through and the cost of whole technology considerably.Therefore, expectation can be produced free-pouring coke in the coking drum, need not and common relevant expense and the time of coke excision.
Even the coking drum can be rendered as fully and be cooled, but the subregion of this drum can thoroughly not cooled off.This phenomenon also is known as " heat drum " sometimes, and this may be the result of combination who has the coke of variform in the drum, and it can contain more than one type solid coke product combination, just needle coke, sponge coke and particulate state coke.Because the particulate state coke of reuniting can be than the faster cooling of other form coke (as bigger particulate state coke mass or sponge coke), should be desirably in the delay coking stove to produce and be mainly fundamental freedom mobile coke, preferred particulates shape coke, to avoid or minimum heat-transmission drum.
Summary of the invention
In one embodiment, provide a kind of delayed coking method, it comprises:
(a) but in first heating zone, petroleum residual oil is heated to and is lower than coking temperature but residual oil is the temperature of pumping liquid under this temperature;
(b) residual oil with described heating imports in second heating zone that is heated coking temperature;
(c) residual oil with described heating imports the coking district from described second heating zone, wherein collects vapor product at the top and forms solid coking product; With
(d) introduce at least a effective polymeric additive of formation for fundamental freedom mobile coke in described residual oil, wherein in the upstream of second heating zone selects, between described second heating zone and the described coking district one selects or two places introduce described polymeric additive in the described residual oil.
In a preferred embodiment, the coking district is in delayed coker drum, and formation fundamental freedom mobile particulate state coke produced.
In another embodiment, provide a kind of delayed coking method, it comprises:
(a) be under 70 ℃～370 ℃ in temperature, vacuum residuum is contacted with at least a polymeric additive of significant quantity to be enough to this additive is distributed to time in the charging substantially equably;
(b) vacuum residuum with contact is heated to the significant temp of the described charging of coking;
(c) vacuum residuum of described heating being loaded into pressure is 15～80psig (the significant quantity time that hot coke beds is formed, this hot coke beds unrestricted flow of at least a portion; With
(d) this hot coke beds of water quenching at least a portion.
In another embodiment, polymeric additive is selected from the ethylenediamine tetraacetic alcohol alcoxylates of polyoxyethylene, polyoxypropylene, polyoxyethylene-polyoxypropylene multipolymer, Volpo S 10, the ethylenediamine tetraacetic alcohol alcoxylates of polyoxypropylene alcohol, ethylenediamine tetraacetic alcohol alcoxylates and its mixture of polyoxyethylene-polyoxypropylene alcohol.The polymeric additive molecular weight is preferably 1,000～30, and 000, more preferably 1,000～10,000.Multipolymer is preferably segmented copolymer.In Fig. 1 and 2 of the application, provided the illustrative example of this polymkeric substance.
In another embodiment, form fundamental freedom mobile particulate state coke produced, and from the coking district, shift out.The coking district is preferably delayed coker drum.Can be incorporated into heating zone (it is coking furnace) in charging and mix with the additive introducing and with charging before, perhaps can between coking furnace and coking drum, be introduced in the charging.Within the scope of the invention, be that additive is all introduced in the charging at two places also.Can add same additives or multiple additives in each position independently; Perhaps can add different additive or multiple additives in each position.
The term " combination " that uses is got its broad sense with " contact ", just in some cases, when having additive in the charging in additive, charging or the physics and/or the chemical transformation of additive and/or charging can take place in the two.In other words, the present invention is not restricted to additive wherein and/or charging after contact and/or combination or the situation of chemistry and/or physical change do not take place during it." significant quantity " of additive will be for causing forming the additive amount of free-pouring coke, preferred fundamental freedom mobile particulate state coke in the coking district when contacting with charging.The common scope of significant quantity is 100～100,000ppm (based on the charging gross weight).Certainly, consumption depends on employed special additive kind and its chemistry and physical aspect.For the additive materials of disperseing better physics and chemical species in being in charging, to compare with more being difficult to those additive materials of dispersive, significant quantity is littler usually.Therefore, most preferably be partially dissolved at least organism, more preferably be dissolved in additive in the resid feed.
Expectation is distributed to additive in the resid feed equably, with the heterogeneous body zone of avoiding coke morphology to form.That is, do not wish in coking drum, to have such position, in the basic unrestricted flow of this coke and coke not unrestricted flow substantially in other zone.Realize the dispersion of additive by the technology of any suitable, preferably the effluent of additive is introduced in the charging by position in expectation.Can add this additive in the resid feed by additive is dissolved in.The viscosity (for example by heating, interpolation solvent etc.) that reduced residual oil before sneaking into additive will promote that additive is dissolved in the resid feed.Can utilize high energy to mix or use static mixing equipment to participate in additive, especially in incoming flow, have a dispersion of the additive of relative low solubility.
Preferably, the whole or basic whole coke that form in the methods of the invention are fundamental freedom mobile coke, fundamental freedom mobile particulate state coke more preferably.Also preferably, during coke forms and afterwards, at least a portion is present in volatile matter in the coking drum from this method, separates and derive, preferably carry out at the bulging top of this coking.
Description of drawings
The application Fig. 1 does not wherein use additive for the light micrograph of the residual oil of demonstration the embodiment of the present application.
The application Fig. 2 has wherein used polyoxyethylene-polyoxypropylene (Pluronic) additive for the light micrograph of the residual oil of demonstration the embodiment of the present application.
The application Fig. 3 is the light micrograph of the residual oil of demonstration the embodiment of the present application, has wherein used ethylenediamine tetraacetate (Tetronic) additive of Volpo S 10.
It is 170 * 136 microns cross polarization light opticmicroscope that whole Photomicrographs among these figure have used viewing area.
Detailed Description Of The Invention
The charging that is applicable to delayed coking is an oil decompression residue (" residual oil ").Such petroleum residue obtains under reduced pressure remove distillment usually from crude oil feeding after, and it is characterized in that forming by the component of macromole size and molecular weight, generally contain: (a) bituminous matter and other high molecular aromatic structure, it will suppress the speed of hydrotreatment and/or hydrocracking and cause catalyst deactivation; (b) metal pollutant naturally occurring or that from the crude oil pre-treatment, obtain in the crude oil, this pollutent tends to make hydrotreatment and/or hydrocracking catalyst inactivation and influences catalyst regeneration; (c) high-load relatively sulphur and nitrogen compound, it produces the SO of unfavorable amount when the burning petroleum residue
2, SO
3, and NO
xThe nitrogen compound that exists in the residual oil also tends to make the catalytic cracking catalyst inactivation.
In one embodiment, resid feed is including but not limited to the tar in the residue in normal pressure or underpressure distillation crude oil or normal pressure or the underpressure distillation heavy oil, visbroken resids, coal slurry, shale oil, the diasphaltene unit or the combination of these materials.Also can use normal pressure and decompression topping heavy bitumen.Usually, this charging is high boiling hydrocarbon material, and the initial boiling point that rises of demarcation is that about 538 ℃ or higher, api gravity are that 20 ° or littler, Kang Laxun carbon residue content are 0～40wt%.
Usually resid feed is carried out delayed coking.Usually, in delayed coking, it is that (in the well heater under 344.74～3792.12kPa), wherein be heated to temperature is 480 ℃～520 ℃ to 50～500psig that residue oil fraction (as the petroleum residue charging) is pumped into pressure.Subsequently its inlet by the drum end is discharged into the coking district, is generally in the adiabatic coking drum of vertical orientation.Pressure is low relatively usually in the drum, as 15～80psig (103.42～551.58kPa), remove at the top can make volatile matter.The typical operation temperature of drum is 410 ℃～475 ℃.Hot feed is thermally splitting for some time (" scorch time ") in the coking drum, discharges the volatile matter of mainly being made up of hydrocarbon product, and it rises continuously by coke mass (bed) and at the top it is collected.Volatile products are delivered to distill in the coking fractionator and reclaim coking gas, petroleum naphtha, lightweight gas oil and heavy gas oil cut.In one embodiment, small portion can be present in heavy coker gas oil in the product stream of introducing in the coking fractionator collects and circulates, and combine with fresh feed (coker feed component), form coker well heater or coking furnace charging thus.Except volatile products, delayed coking also forms the solid coke product.
Three kinds of dissimilar solid delay coking device products are arranged usually, and they have different value, outward appearance and performance, just needle coke, sponge coke and particulate state coke.Needle coke is top-quality in three types.Needle coke has high electric conductivity (with low thermal expansivity) when further thermal treatment, and is used for the production of electric arc steel.The content of its sulphur and metal is relatively low, and produces from some more high-quality coker feed usually, and this charging comprises more aromatic feed, as the tar of the slurry in the cat cracker and decanted oil and thermally splitting.Usually, can not form this product by the delayed coking resid feed.
Sponge coke (a kind of more inferior coke) forms in refinery usually.Inferior refinery coker feed has a large amount of bituminous matters, heteroatoms and metal, and it generates this more inferior coke.If the content of sulphur and metal is enough low, sponge coke can be used for producing the electrode of aluminium industry.If the content of sulphur and metal is too high, coke can be used as fuel so.Title " sponge coke " comes from the outward appearance of its porous spongy.The conventional delayed coking method of the preferred vacuum resid feed of use the present invention can generate the sponge coke of aggregation substance usually, and its intensive that need comprise brill and water-jet technology is removed process.As discussed above, make cycling time this method quite complicated owing to having increased.
The particulate state coke is considered to the coke of lowest quality.Term " particulate state coke " derives from its shape that is similar to BB size [about 1/16 inch to 3/8 inch (.16cm～.95cm)] ball.The particulate state coke is the same with other type coke to tend to be gathered into relatively large (especially with the mixture of sponge coke in), and diameter is greater than 1 foot sometimes.Can cause the problem of refinery's equipment and processing aspect like this.The particulate state coke makes from the high resin bituminous matter charging of lowest quality usually, and obtains especially for the good high-sulfur fuel of cement kiln and steel production former.Also have other coke, it is known as " transition coke (transition coke) ", and the expression form is between sponge coke and particulate state coke or owing to combine the coke of mixture composition of the particulate state coke of sponge coke.For example, mainly have the physical appearance that is similar to sponge, but have little particulate ball to begin to form the coke of the sign of discrete shape.
According to the present invention,, can make fundamental freedom mobile particulate state coke by handling resid feed with one or more polymeric additives.This additive is those that enhanced granule shape coke generates during delayed coking.Under efficient temperature, just will promote additive in charging, under the dispersive temperature, to handle resid feed with one or more additives.This temperature is generally 70 ℃～500 ℃, is preferably 150 ℃～370 ℃, more preferably 185 ℃～350 ℃.
The non-limiting example of polymeric additive of the present invention comprises those that are selected from following material: ethylenediamine tetraacetic alcohol alcoxylates and its mixture of the ethylenediamine tetraacetic alcohol alcoxylates of polyoxyethylene, polyoxypropylene, polyoxyethylene-polyoxypropylene multipolymer, Volpo S 10, the ethylenediamine tetraacetic alcohol alcoxylates of polyoxypropylene alcohol, polyoxyethylene-polyoxypropylene alcohol.
Use this polymeric additive with significant quantity.That is, consumption is at least the amount of the free-flowing coke that obtains expected degree.This consumption is generally 300～500wppm, be preferably 300～3000wppm and 300～2000wppm more preferably, based on the weight of heavy oil feed.
Within the scope of the present invention, second type additive and polymeric additive can be used in combination.This additive of second type is can be with the metallic additive of liquid or solid form use, preferred liquid form.The non-limiting example of the metallic additive that can use in the invention process comprises metal hydroxides, naphthenate and/or carboxylate salt, metal acetylacetonates, Lewis acid, metallic sulfide, metal acetate, metal carbonate, metallic high surface area solids, the salt of inorganic oxide and oxide compound.The preferable alloy of oxyhydroxide is basic metal and alkaline-earth metal, more preferably potassium and sodium.Preferred basic salt.If metallic additive and polymeric additive are used in combination, the total amount of two kinds of additives should not surpass for the given maximum consumption of polymeric additive, just is 5000wppm to the maximum.
Preferably with 900
(482.22 ℃)～1040
The cut of (560 ℃) normal pressure boiling point (AEBP) material of equal value remains under the 10wt%, will promote the coke morphology that coke morphology is got back to less combination and less self-supporting like this.
The initial liquid spheres that causes forming the particulate state coke that forms of the rapid drying/coking/division of liquid intermediate phase (mesophase) forms.Being on good terms in the middle of slowly dry scatter initial liquid intermediate phase and coking on the spot, and causes forming the extended network of sponge coke.Medium dry speed is produced as the transition coke of the mixture of spongy and particulate state coke, and wherein the particulate state coke embeds in the sponge coke.When the sealer that forms embedded particles shape coke and superheated vapo(u)r owing to sponge coke cut/bore the coking drum of delayed coking, a kind of situation in back can cause coke outburst or " heat drum ".When the bit hits sealing, it relates to steam and particulate state coke BB.Very expectation can be produced particulate or sponge coke with controllable manner, and avoids forming transition coke.Refinery can need not to bore and just cut out sponge coke or discharge the particulate state coke.Add polymeric additive of the present invention coking is carried out under higher temperature,, allow dry coke and formation particulate state coke ball quickly because its heat cross-linking that has slowed down between the intermediate phase layer reacts.Except higher temperature, operate the coking drum down at lower pressure (for example 15psi vis 45psi (103.42 vis 310.26kPa)) and can allow the volatility crackate to overflow, and make them as the residence time minimum of liquid in intermediate phase.The polyethers additive disturb the mink cell focus intermediate phase to form and crosslinked aspect also be effectively because they in the coking drum with the speed decomposition (usually 425 ℃ under) slower than coke drying rate.
Accurate condition during with the additive treating resid feed depends on charging and additive.That is the condition during, with the additive treating charging depends on composition and the performance for the treatment of pyrogenic charging and additive therefor.Can determine these conditions according to routine.For example, can pass through coking in mini-reactor (as Mirocarbon Residue Test Unit (MCRTU)), under different time and temperature, operate several times with the specific charging that contains additive.Utilize described optical crossover polarization microscope to analyze the coke that obtains subsequently herein.Preferred coke morphology (just, to generate fundamental freedom fluidic coke) for mean sizes is 0.5～10 μ m, is preferably the coke microstructure of the discrete film micro area of 1～5 μ m, be similar to the mosaic described in the application Fig. 2 and 3 (mosaic) to a certain extent.Shown the coke microstructure of representing non-free flowing powder shape coke among the application Fig. 1, the coke microstructure of demonstration mainly is made up of non-discrete or bigger basin, size up to 60 μ m or bigger, be generally 10～60 μ m.
Also can use coking processing aid commonly used in the inventive method, comprise defoamer.When by ordinary method production particulate state coke, the particulate state coke gathers usually still needs water-jet technology with its degree that shifts out.
In one embodiment of the invention, at first with promoting the polymeric additive of the present invention that forms fundamental freedom mobile coke to handle resid feed.By keeping the coking drum under low relatively pressure, can collect a large amount of volatile matters that form, the gathering of the particulate state coke that obtains that has suppressed not expect at the top.Combined feed is the volume ratio of the fresh feed of furnace charge (fresh feed+turning oil) and continuous delayed coking operation than (" CFR ").Delayed coking operation adopts the circulation of 5 volume %～25 volume % (CFR is 1.05～1.25) usually.Sometimes be 0 circulation, in application-specific, circulate sometimes up to 200%.Should reduce CFR helping forming free flowing granule shape coke, and preferably not use circulation.
Usually, with continuous mode additive is imported in the coking process.If desired, additive can be dissolved in the suitable transfering fluid or form slurry therein, this fluid is generally and additive compatible with residual oil and dissolves in wherein solvent substantially.With the speed that in charging, realizes desired additive concentration fluid mixture or shurry pump are delivered in the coking process subsequently.The introducing position of additive can be for example in the exit of stove charging charge pump or near the outlet of coker conveyer line.Can have a pair of mixing vessel, this operates in the mode that additive is incorporated in the coking process continuously mixing vessel.
Can regulate the introducing speed of additive according to the kind of resid feed in the coking furnace.Charging can be than needing less additive away from the charging in the ultimate value in the ultimate value of production particulate state coke.
For the additive that is difficult to be dissolved or dispersed in the resid feed, additive is transferred in mixing/slurry container, and mixed with the slurry medium compatible with charging.The non-limiting example of suitable slurry medium comprises coker heavy gas oil, water etc.Can for example in container, provide energy to disperse this additive by mixing tank.
For the additive that can be dissolved or dispersed in comparalive ease in the resid feed, additive is transferred in the mixing vessel, and mixed with the fluid transfer medium compatible with charging.The non-limiting example of suitable fluid transfer medium comprises warm sludge oil (temperature is 150 ℃～300 ℃), coker heavy gas oil, light cycle, heavy reformate and its mixture.Also can use catalysis slurry oil (cat slurry oil) (CSO), although it may suppressant additive generates the ability of discrete particle shape coke in some cases.Can for example in container, provide energy to disperse this additive by mixing tank.
The present invention may be better understood with reference to the following indefiniteness embodiment that provides for purposes of illustration.
Embodiment
Use is set forth the present invention from Tetronic and Pluronic polymkeric substance that BASF Corporation obtains.These polymkeric substance are the multipolymer of oxyethane and propylene oxide.The molecular-weight average of every kind of polymeric additive is 1500.
Polymeric additive shown in below using in the present embodiment.These polymkeric substance are the multipolymer and the commercially available acquisition of oxyethane and propylene oxide.Left side additive is the Tetronic multipolymer, and the right additive is the Pluronic copolymer additives, obtains from BASF Corporation.The molecular-weight average of every kind of polymeric additive is 1500.
2g Baton Rouge Refinery Vacuum Tower Bottoms is fed among the Microcarbon Reactor Test Unit (MCR).With residual oil be heated to 400 ℃ and remain on 400 ℃ following 2 hours, the gravimetric analysis residue.Add two kinds of above-mentioned polymeric additives of 3000wppm and operate residual oil once more.The polarized light optical microphotograph that carries out residue detects.Following table has shown this result.
Table
| Additive | Residual oil (g) | Additive, mg | Additive (wppm) | R.T. to 400 ℃ and kept 4 hours |
| Do not have | 4.52 | ----- | ----- | 27.38 |
| Pluronic F-108 | 4.20 | 12.80 | 3048 | 26.90 |
| ?Tetronic?1508 | 4.63 | 13.90 | 3002 | 27.39 |
The application Fig. 1,2 and 3 Photomicrograph have shown this microscopic analysis result, and it has confirmed the effect of polymeric additive of the present invention.Fig. 1 is for non-additive result and can observe the spheroid of many lights, and it shows and has a large amount of anisotropy coke.Fig. 2 represents use polyoxyethylene-polyoxypropylene (Pluronic) and the operation carried out, wherein observes with respect to Fig. 1 to have less relatively microballoon, shows the formation that has suppressed the anisotropy coke thus.The application Fig. 3 represents the ethylenediamine tetraacetic alcohol alcoxylates (Tetronic) of use polyoxyethylene-polyoxypropylene alcohol and the operation carried out, wherein observes to have isotropic phase, and it shows the formation that has suppressed the anisotropy coke substantially up hill and dale.Thus, polymeric additive of the present invention has suppressed the formation of anisotropy coke and has changed coke morphology.
Claims (6)
1. delayed coking method comprises:
(a) but in first heating zone, petroleum residual oil is heated to and is lower than coking temperature but residual oil is the temperature of pumping liquid under this temperature;
(b) residual oil with described heating imports in second heating zone that is heated coking temperature;
(c) residual oil with described heating imports the coking district from described second heating zone, wherein collects vapor product at the top and forms free-pouring coking product; With
(d) in described residual oil, introduce 300～3,000wppm is selected from polyoxyethylene, polyoxypropylene, polyoxyethylene-polyoxypropylene multipolymer, the ethylenediamine tetraacetic alcohol alcoxylates of Volpo S 10, the ethylenediamine tetraacetic alcohol alcoxylates of polyoxypropylene alcohol, pure and mild its mixture of the ethylenediamine tetraacetic alkoxylate of polyoxyethylene-polyoxypropylene alcohol and molecular weight are 1,000～30,000 at least a effective polymeric additive of formation for fundamental freedom mobile particulate state coke is wherein at the point of the upstream of second heating zone, between described second heating zone and the described coking district select or two places introduce described polymeric additive in the described residual oil.
2. the process of claim 1 wherein that resid feed is a vacuum residuum.
3. the process of claim 1 wherein that this additive of at least a portion dissolves in charging.
4. the method for claim 2, wherein this additive of at least a portion dissolves in charging.
5. each method among the claim 1-4, wherein also use second additive of significant quantity, wherein second additive is metallic additive, and it is selected from one or more metal ring alkyl salts, metal acetylacetonates, Lewis acid and inorganic oxide.
6. each method among the claim 1-4 is wherein also used second additive of significant quantity, and wherein second additive is one or more in KOH, NaOH, carboxylate salt and the metal acetylacetonates.
Applications Claiming Priority (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US10/846,034 US7303664B2 (en) | 2003-05-16 | 2004-05-14 | Delayed coking process for producing free-flowing coke using a metals-containing additive |
| USPCT/US2004/015319 | 2004-05-14 | ||
| US10/846,034 | 2004-05-14 | ||
| PCT/US2004/015319 WO2004104139A1 (en) | 2003-05-16 | 2004-05-14 | Delayed coking process for producing free-flowing shot coke |
| PCT/US2005/016714 WO2005113712A1 (en) | 2004-05-14 | 2005-05-12 | Delayed coking process for producing free-flowing coke using polymeric additives |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1954046A CN1954046A (en) | 2007-04-25 |
| CN1954046B true CN1954046B (en) | 2011-08-10 |
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ID=38059725
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200580015512 Pending CN1954048A (en) | 2004-05-14 | 2005-05-12 | Delayed coking process for producing free-flowing coke using low molecular weight aromatic additives |
| CN2005800154051A Expired - Fee Related CN1954046B (en) | 2004-05-14 | 2005-05-12 | Delayed coking process for producing free-flowing coke using polymeric additives |
| CN 200580015561 Pending CN1954051A (en) | 2004-05-14 | 2005-05-12 | Delayed coking process for producing free-flowing coke using an overbased metal detergent additive |
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| Application Number | Title | Priority Date | Filing Date |
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| CN 200580015512 Pending CN1954048A (en) | 2004-05-14 | 2005-05-12 | Delayed coking process for producing free-flowing coke using low molecular weight aromatic additives |
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| CN 200580015561 Pending CN1954051A (en) | 2004-05-14 | 2005-05-12 | Delayed coking process for producing free-flowing coke using an overbased metal detergent additive |
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| JP (3) | JP2008504376A (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112779038A (en) * | 2021-01-19 | 2021-05-11 | 山西沁新能源集团股份有限公司 | Preparation method of special coke for ceramic fiber vertical melting furnace, special coke for ceramic fiber vertical melting furnace and application of special coke |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US8496805B2 (en) * | 2009-07-10 | 2013-07-30 | Exxonmobil Research And Engineering Company | Delayed coking process |
| US9139781B2 (en) * | 2009-07-10 | 2015-09-22 | Exxonmobil Research And Engineering Company | Delayed coking process |
| DE102011082699A1 (en) * | 2011-09-14 | 2013-03-14 | Sgl Carbon Se | Production of carbon fiber reinforced coke |
| CN110734779B (en) * | 2019-10-15 | 2021-03-05 | 湖南中科星城石墨有限公司 | Isotropic coke suitable for lithium ion battery cathode raw material and preparation method thereof |
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|---|---|---|---|---|
| US4612109A (en) * | 1980-10-28 | 1986-09-16 | Nl Industries, Inc. | Method for controlling foaming in delayed coking processes |
| US5258115A (en) * | 1991-10-21 | 1993-11-02 | Mobil Oil Corporation | Delayed coking with refinery caustic |
-
2005
- 2005-05-12 JP JP2007513384A patent/JP2008504376A/en active Pending
- 2005-05-12 BR BRPI0511045-9A patent/BRPI0511045A/en not_active IP Right Cessation
- 2005-05-12 JP JP2007513383A patent/JP2008504375A/en active Pending
- 2005-05-12 CN CN 200580015512 patent/CN1954048A/en active Pending
- 2005-05-12 BR BRPI0511019-0A patent/BRPI0511019A/en not_active IP Right Cessation
- 2005-05-12 JP JP2007513385A patent/JP2008502743A/en active Pending
- 2005-05-12 BR BRPI0511023A patent/BRPI0511023B1/en not_active IP Right Cessation
- 2005-05-12 CN CN2005800154051A patent/CN1954046B/en not_active Expired - Fee Related
- 2005-05-12 CN CN 200580015561 patent/CN1954051A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4612109A (en) * | 1980-10-28 | 1986-09-16 | Nl Industries, Inc. | Method for controlling foaming in delayed coking processes |
| US5258115A (en) * | 1991-10-21 | 1993-11-02 | Mobil Oil Corporation | Delayed coking with refinery caustic |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112779038A (en) * | 2021-01-19 | 2021-05-11 | 山西沁新能源集团股份有限公司 | Preparation method of special coke for ceramic fiber vertical melting furnace, special coke for ceramic fiber vertical melting furnace and application of special coke |
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| BRPI0511023B1 (en) | 2016-03-29 |
| CN1954051A (en) | 2007-04-25 |
| BRPI0511019A (en) | 2007-11-27 |
| CN1954046A (en) | 2007-04-25 |
| BRPI0511045A (en) | 2007-11-27 |
| JP2008504375A (en) | 2008-02-14 |
| BRPI0511023A (en) | 2007-11-27 |
| JP2008504376A (en) | 2008-02-14 |
| JP2008502743A (en) | 2008-01-31 |
| CN1954048A (en) | 2007-04-25 |
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