CN1325938A - Process for preparing acicular petroleum coke from S-contained ordinary-pressure residual oil - Google Patents
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Abstract
A process for preparing acicular petroleum coke from sulfur-contained ordinary-pressure residual oil includes such steps as hydrorefining, hydrodemetalating, hydrodesulfurizing, separating, hydrogenating to generate hydrogenated heavy fraction oil, and delay coking in a certain condition. Its advantages are low CTE (less than 2.6X10 to the power -6/deg.C, low sulfur content (less than 0.7 wt.%) and high quality.
Description
The invention belongs to a kind of under the situation that does not have hydrogen the thermal non-catalytic cracking method of hydrocarbon ils, more particularly, be a kind of method of producing acicular petroleum coke from residual oil.
Acicular petroleum coke (being called for short pin Jiao) has advantages such as thermal expansivity (hereinafter to be referred as CTE) is low, graphitization characteristic is good, broken back outward appearance is needle-like, have tangible filamentary structure and higher anisotropy at microscopically, be the framework material of making the superpower electrode, therefore be widely used on the Steel industry.
In the superpower steel-smelting electric furnace, must adopt superpower or ultra-high power graphite electrode, this electrode can stand the impact of severe condition jumpy at short notice.Burst for electrode being unlikely produce bigger thermal stresses when rapid heating or the chilling, require the CTE of electrode little, and the CTE of electrode depends primarily on pin Jiao's CTE, so CTE becomes the critical index of the burnt quality of expression pin.
The sulphur content that is used for superpower electrode needle Jiao of Graphite Electrodes manufacturing must be low, because the service temperature of greying stove is high, about 2800 ℃ of typical graphitization temperature, so sulphur can not appear in the final Graphite Electrodes, in graphitizing process, be accompanied by the effusion of sulphur, puffing takes place.After sulphur at high temperature gasifies, in coke granule, overflow, make hole wall deliquescing when greying, produce single group and expand through hole.Finally make Graphite Electrodes intensity be subjected to grievous injury.
The index of the burnt quality of pin is as follows:
True density, gram per centimeter
3＞2.12
CTE, * 10
-6/ ℃ 2.35～2.60 (1000 ℃ of carbon rod sample preparation methods)
Sulphur content, heavy % ≯ 0.7
Ash, heavy % ≯ 0.15
The burnt production technology of pin is a theoretical basis with the mesophasespherule formation mechanism, the general raw material that adopts is rich in aromatic hydrocarbons such as fluid catalytic cracking decant oil, thermal cracking residue, lube oil furfural refining extraction oil or preparing ethylene by steam cracking residual oil etc., though more than these raw materials can produce pin Jiao through different raw material pretreatment process, but because therefore resource-constrained is difficult to organize more massive industrial production.
Compare with above-mentioned raw materials, the residual oil wide material sources are heavy oil residues that crude oil obtains through atmospheric and vacuum distillation, general raw material as common coker.In order to enlarge pin Jiao's raw material sources, people are that raw material carries out having carried out number of research projects aspect the burnt production of pin particularly contain sulfur resid with residual oil.
USP4,235,703 disclose a kind of method from residual oil production high-quality Jiao, and this method will be produced superpower electrode refinery coke through delay coking process after the hydrodemetallation (HDM) again from the straight run vacuum residuum of naphthenic base crude or long residuum through hydrogenating desulfurization earlier.This method limits the scope of crude oil, and the characterization factor K value of crude oil must be lower than 11.4, so the source of raw material has been subjected to constraint.
USP4,894,144 disclose a kind of method for preparing low-sulfur Jiao and high-sulfur Jiao simultaneously, this method adopts hydroprocessing technique that straight run residue is carried out pre-treatment, the residual oil that hydrogenation is crossed is divided into two partly, and a part of lightweight residual oil is suitable as produces Graphite Electrodes refinery coke raw material, and another part heavy oil residue only is suitable as production aluminium metallurgy electrode refinery coke raw material, the material yield that is suitable as the burnt raw material of superpower electrode needle is low, also must go out a part of ordinary electrode refinery coke raw material.
USP5,286,371 disclose a kind of method of producing pin Jiao, and this method adopts hydroprocessing technique processing straight run residue earlier, the mink cell focus of hydrotreatment partly is mixed into solvent deasphalting unit with fluid catalytic cracking decant oil, removes logistics after the bituminous matter as the raw material of producing pin Jiao.This method can not also must be handled the purpose that just can reach refining raw material through solvent extraction the straight run residue of hydrotreatment directly as the raw material of superpower electrode refinery coke.
The objective of the invention is to provide on the basis of existing technology a kind of method of producing acicular petroleum coke from sulfur containing atmospheric.
Method provided by the invention is: after sulfur containing atmospheric was passed through hydrofining, hydrodemetallation (HDM), hydrogenating desulfurization successively, the hydrogenation heavy distillate that the separation hydrogenated oil obtains entered delayed coking unit, obtains pin Jiao under the condition of producing pin Jiao.
Method detail operations process provided by the invention is:
(1), the sulfur containing atmospheric after the preheating enters protectant hydrofining reactor is housed, at 350 ℃～420 ℃ of temperature of reaction, hydrogen dividing potential drop 5.0～22.0MPa, volume space velocity 0.5～10h
-1, hydrogen-oil ratio 500～1200Nm
3/ m
3Condition under react;
(2), the logistics handled through hydrofining enters the hydrodemetallation (HDM) reactor that Hydrodemetalation catalyst is housed, at 350 ℃～420 ℃ of temperature of reaction, hydrogen dividing potential drop 5.0～22.0MPa, volume space velocity 0.5～5.0h
-1, hydrogen-oil ratio 500～1500Nm
3/ m
3Condition under react;
(3), the logistics handled through hydrodemetallation (HDM) enters the hydrodesulphurisatioreactors reactors that Hydrobon catalyst is housed, at 350 ℃～420 ℃ of temperature of reaction, hydrogen dividing potential drop 5.0～22.0MPa, volume space velocity 0.5～5.0h
-1, hydrogen-oil ratio 500～2000Nm
3/ m
3Condition under react;
(4), enter vacuum distillation apparatus, fractionate out the hydrogenation heavy distillate through the logistics of hydrogenating desulfurization;
(5), the hydrogenation heavy distillate enters the delayed coking unit with conventional coking different operating mode separately, also can be mixed into the preheating of process furnace convection zone with other conventional raw material of producing pin Jiao, entering separation column and turning oil then is mixed into the process furnace radiation section and operates through alternating temperature, the scope of alternating temperature is 430～520 ℃, recycle ratio 0.2～1.2;
(6), the logistics that will heat enters coke drum, its operational condition is: the coke tower top pressure is 0.10～3.0MPa, 380 ℃～460 ℃ of coke tower top temperatures, pin Jiao stays in the coke drum;
(7), thermal response produced oil gas ejects from coke drum and enters separation column, fractionates out gas, gasoline, diesel oil and gas oil, turning oil mixes the charging as the process furnace radiation section with the hydrogenation heavy distillate.
The described sulfur containing atmospheric of step (1) is the long residuum of any high-sulfur crude oil, and with arbitrary proportion blended sulfur containing atmospheric.
It is mechanical impurity, metallic iron, the calcium that removes in the residual oil that the described hydrofining of step (1) mainly acts on, and used protective material is made up of the gamma-aluminium oxide carrier with diplopore distribution of 1.0～5.0 heavy % nickel oxide, 5.5～10.0 heavy % molybdenum oxides and surplus.This protectant specific surface ≮ 180 meter
2/ gram, pore volume ≮ 0.6 milliliter/gram, crushing strength ≮ 12 ton/millimeter.
The gama-alumina precursor that has the diplopore distribution in the above-mentioned protective material is hydrated aluminum oxide A and the hydrated aluminum oxide B that is made by alkyl aluminum hydrolysis method and Tai-Ace S 150 method, and by 0.7～1.2: 1 weight ratio mixes, and their pore size distribution is respectively:
Hydrated aluminum oxide A hydrated aluminum oxide B
＜50 dusts 95～96% 35～60%
50～100 dusts 2.0～3.0% 21～25%
100～250 dusts 0.5～1.0% 13～15%
250～500 dusts 0.2～0.5% 5.0～6.0%
Described gamma-aluminium oxide carrier be by the hydrated aluminum oxide mixture of above-mentioned two kinds of different pore size distributions and carbon powder, tensio-active agent, peptizing agent by weight 1: 0.05～0.1: 0.05～0.1: 0.02～0.05 and the suitable quantity of water mixing moulding, drying, roasting are made.
The described hydrodemetallation (HDM) of step (2) mainly removes heavy metal nickel in the residual oil, vanadium etc., and used catalyzer is to be made of nickel or nickel-molybdenum isoreactivity component and alumina supporter.
The described hydrogenating desulfurization of step (3) mainly removes heteroatomss such as sulphur in the residual oil, nitrogen, and used catalyzer is to be made of nickel-tungsten, nickel-molybdenum or cobalt-molybdenum isoreactivity component and alumina supporter.
The described underpressure distillation effect of step (4) is that excision is unfavorable for the light constituent that mesophasespherule is grown up, the decompression cutting temperature is 400 ℃～520 ℃, the cut that boiling point is higher than cutting temperature is the hydrogenation heavy constituent, the cut that boiling point is lower than cutting temperature is the hydrogenation light constituent, wherein the hydrogenation heavy constituent are as the raw material of producing pin Jiao, and the separation column that the hydrogenation light constituent enters in the step (7) separates.
Described pin Jiao's of step (5) raw material is 100% hydrogenation heavy constituent, perhaps hydrogenation heavy constituent and other are produced the mixture of pin Jiao's conventional raw material, and other conventional raw material of producing pin Jiao is selected from fluid catalytic cracking decant oil, thermal cracking residue, lube oil furfural refining and extracts among the residual oil (abbreviation ethylene residue) of oil, preparing ethylene by steam cracking one or more mixture out.
Below in conjunction with accompanying drawing method provided by the present invention is given further instruction.
The method flow from sulfur containing atmospheric production acicular petroleum coke that accompanying drawing illustrates, the shape and size of equipment and pipeline are not subjected to the restriction of accompanying drawing, but determine as the case may be.
Sulfur containing atmospheric enters hydrofining reactor 2 reactions through pipeline 1 earlier, logistics after refining enters HDM reactor 4 through pipeline 3 again, logistics after the demetalization enters hydrodesulphurisatioreactors reactors 6 through pipeline 5 then, logistics after the desulfurization enters vacuum distillation apparatus 8 through pipeline 7, isolated hydrogenation light fraction enters fractionating column 17 through pipeline 10, and the hydrogenation heavy distillate is successively through pipeline 9, surge tank 11, pipeline 12, pump 13 mixes separately or with other conventional raw material of producing pin Jiao from pipeline 25, enter the convection section of heating furnace 15 through pipeline 14, then after pipeline 16 enters fractionating column 17 and recycle oil mixes, successively through pipeline 18, pump 19, pipeline 20 enters the radiant section of heating furnace 15, be the alternating temperature operation this moment, and then enter coke drum 22 or 23 through pipeline 21, the oil gas that generates enters fractionating column 17 through pipeline 24 and obtains gas with the hydrogenation light fraction fractionation from pipeline 10, gasoline, diesel oil and gas oil, recycle oil mix the charging as heating furnace 15 radiant sections with logistics from pipeline 16 in fractionating column bottom.
The invention has the advantages that:
(1), the heavy distillate of the present invention after with hydrogenation be raw material, the burnt CTE of the pin of production is less than 2.6 * 10-6/ ℃, sulfur content is lower than 0.7 heavy %, and its quality reaches the requirement of high power electrodes;
(2), as the sulfur containing atmospheric wide material sources of producing the burnt raw material of pin, can form the production capacity of economic scale, avoided device because of insufficient raw material shutting down continually;
(3), sulfur containing atmospheric is before entering hydrodesulphurisatioreactors reactors and HDM reactor, earlier through protectant hydrofining reactor is housed, most mechanical admixture and metallic iron have been removed, thereby prolonged the life-span of Hydrodemetalation catalyst and Hydrobon catalyst, reduced simultaneously pin Jiao's impurity content;
(4), the shared fractionating column of hydrogenation light fraction and coking oil gas can be reduced investment outlay.
The following examples will give further instruction to method provided by the invention, but not thereby limiting the invention.
Testing used raw material is long residuum, and its character is listed in table 1; Catalyst system therefor comprises hydrogenation protecting agent RG-1 (being produced by China Petrochemical Corporation's Chang Ling catalyst plant), HDM catalyzer RF-220 (being produced by Dutch Aksu chemical company), HDS catalyzer RF-1000 (being produced by Dutch Aksu chemical company).Testing apparatus is medium-sized residual hydrogenation testing apparatus, medium-sized vacuum distillation apparatus and medium-sized delayed coking testing apparatus.Medium-sized residual hydrogenation testing apparatus comprises three placed in-line reactors, and each reactor catalyst design loadings is 500 milliliters, and these three reactors load RG-1, RF-220, RF-1000 respectively; The major equipment of medium-sized delayed coking unit has process furnace, coke drum and separation column, and wherein the coke drum capacity is the 50kg/ tower.
Embodiment 1
After sulfur containing atmospheric A passed through hydrofining, hydrodemetallation (HDM), hydrogenating desulfurization successively, hydrogenated oil separated the hydrogenation heavy distillate (＞460 ℃) that obtains through underpressure distillation and enters delayed coking unit, obtains pin Jiao under the condition of producing pin Jiao.Its processing condition and material balance see Table 2 and table 3 respectively, and the character of hydrogenation heavy distillate and coke chemicals sees Table 4 and table 5 respectively.
As can be seen from Table 1, long residuum A sulphur content reaches 3.4 heavy %, belongs to high-sulfur residual oil, and metallic nickel and content of vanadium sum are 48.6ppm, and metallic iron and calcium contents sum reach 39.4ppm.Long residuum A by hydrotreatment after, hydrogenation heavy distillate (＞460 ℃) character that generates is as shown in table 4, as can be seen from Table 4, hydrogenation heavy distillate sulphur content is reduced to 0.65 heavy %, vanadium metal content is reduced to 0.1ppm, metallic nickel content is reduced to 6.1ppm, and metallic iron and calcium contents sum are reduced to 14ppm.The burnt CTE of pin that is raw material production with this hydrogenation heavy distillate is 2.52 * 10
-6/ ℃, sulphur content is 0.68 heavy % (seeing Table 5), meets the specification of quality of superpower electrode refinery coke.
Embodiment 2
After sulfur containing atmospheric B passed through hydrofining, hydrodemetallation (HDM), hydrogenating desulfurization successively, hydrogenated oil separated the hydrogenation heavy distillate (＞460 ℃) that obtains through underpressure distillation and enters delayed coking unit, obtains pin Jiao under the condition of producing pin Jiao.Its processing condition and material balance see Table 2 and table 3 respectively, and the character of hydrogenation heavy distillate and coke chemicals sees Table 4 and table 5 respectively.
As can be seen from Table 1, long residuum B sulphur content reaches 2.9 heavy %, belongs to high-sulfur residual oil, and metallic nickel and content of vanadium sum are 130.4ppm, and metallic iron and calcium contents sum reach 8.8ppm.Long residuum B by hydrotreatment after, hydrogenation heavy distillate (＞460 ℃) character that generates is as shown in table 4, as can be seen from Table 4, hydrogenation heavy distillate sulphur content is reduced to 0.57 heavy %, vanadium metal content is reduced to 0.29ppm, metallic nickel content is reduced to 16.0ppm, and metallic iron and calcium contents sum are reduced to 7ppm.The burnt CTE of pin that is raw material production with this hydrogenation heavy distillate is 2.56 * 10
-6/ ℃, sulphur content is 0.63 heavy % (seeing Table 5), meets the specification of quality of superpower electrode refinery coke.
Table 1
| Stock oil | ??????A | ??????B |
| Density (20 ℃), gram per centimeter 3Viscosity (100 ℃), millimeter 2/ second carbon residue; Heavy % constituent content; The group composition of the hydrocarbon sulphur nitrogen of heavy %; Heavy % saturated hydrocarbons aromatic hydrocarbons gum asphalt tenor, ppm nickel vanadium iron calcium | ???0.9679 ????54.44 ?????9.68 ????85.30 ????11.05 ?????3.4 ?????0.17 ?????29.2 ?????52.0 ?????15.3 ?????3.5 ?????11.2 ?????37.4 ?????27.0 ?????12.4 | ???0.9660 ????47.59 ?????9.58 ????85.37 ????11.27 ?????2.9 ?????0.5 ?????30.7 ?????42.5 ?????23.7 ?????3.1 ?????30.4 ?????100 ?????6.6 ?????2.2 |
Table 2
Table 3
| The embodiment numbering | ?????1 | ?????2 |
| Stock oil | ?????A | ?????B |
| Operational condition | ||
| Hydrofining, HDM, HDS | ||
| The hydrogen dividing potential drop, MPa | ????13.0 | ????14.0 |
| Temperature of reaction, ℃ | ????385 | ????380 |
| Volume space velocity, h -1 | ????0.24 | ????0.35 |
| Hydrogen to oil volume ratio, Nm 3/m 3 | ????650 | ????800 |
| Delayed coking | ||
| The furnace outlet temperature, ℃ | ??440～500 | ??440～500 |
| The coke tower top pressure, MPa | ????0.30 | ????0.30 |
| Recycle ratio | ????0.75 | ????0.75 |
| The embodiment numbering | ??????1 | ??????2 |
| Hydrogenated products distribute, heavy % | ||
| Gas | ????3.82 | ????3.90 |
| Petroleum naphtha | ????0.56 | ????1.49 |
| Diesel oil | ????6.33 | ????13.94 |
| Hydrogenation heavy gas oil (350 ℃～460 ℃) | ????22.66 | ????17.95 |
| Hydrogenation heavy distillate (＞460 ℃) | ????67.97 | ????63.64 |
| Add up to | ???101.34 | ???100.92 |
| The product of delayed coking distributes, heavy % | ||
| The coking dry gas | ?????6.1 | ?????9.5 |
| Coker gasoline | ????21.7 | ????16.9 |
| Coker gas oil | ????32.3 | ????23.1 |
| Coker gas oil | ????10.8 | ????7.6 |
| Needle coke | ????29.1 | ????42.9 |
| Add up to | ???100.0 | ???100.0 |
Table 4
| The embodiment numbering | ?????1 | ??????2 |
| Hydrogenation heavy distillate density (20 ℃), gram per centimeter 3Viscosity (100 ℃), millimeter 2/ second carbon residue, heavy % ash, heavy % constituent content, the hydrocarbon sulfur family of heavy % is formed, heavy % stable hydrocarbon aromatic hydrocarbons gum asphalt metal content, ppm nickel vanadium iron and calcium | ???0.9511 ???142.9 ????10.5 ????0.02 ????87.48 ????11.71 ????0.65 ????31.6 ????51.4 ????14.2 ????2.8 ????6.1 ????0.1 ????14 | ????0.9614 ????118.7 ????11.18 ?????0.03 ????87.55 ????11.43 ????0.57 ????34.7 ????48.8 ????16.4 ????0.1 ????16.0 ????0.29 ??????7 |
Table 5
| The embodiment numbering | ??????1 | ??????2 |
| Coker gasoline density (20 ℃), gram per centimeter 3The bromine valency, gBr/100g sulphur, ppm | ???0.7312 ?????40 ?????213 | ???0.7346 ?????49 ?????207 |
| Coker gas oil density (20 ℃), gram per centimeter 3The bromine valency, the gBr/100g condensation point, ℃ aniline point, ℃ 10% carbon residue, heavy % sulphur, ppm | ???0.8282 ?????18 ????-22 ????59.6 ????0.07 ????0.10 | ???0.8373 ?????22 ????-22 ????60.4 ????0.06 ????0.13 |
| Coker gas oil density (20 ℃), gram per centimeter 3Viscosity (100 ℃), millimeter 2/ second carbon residue, heavy % basic nitrogen, ppm sulphur, heavy % nitrogen, heavy % nickel, heavy % vanadium, heavy % | ???0.8877 ????3.41 ????0.09 ?????656 ????0.48 ????0.19 ????0.24 ???＜0.01 | ???0.8971 ????5.53 ????0.13 ?????687 ????0.52 ????0.20 ????0.27 ???＜0.01 |
| Pin charred ashes part, heavy % fugitive constituent, heavy % sulphur content, heavy % true density, gram per centimeter 3CTE,×10 -6/℃ | ????0.04 ?????6.5 ????0.68 ????2.215 ????2.52 | ????0.04 ?????8.1 ????0.63 ????2.129 ????2.56 |
Claims (5)
1, a kind of method of producing acicular petroleum coke from sulfur containing atmospheric, operation steps is followed successively by:
(1), the sulfur containing atmospheric after the preheating enters protectant hydrofining reactor is housed, at 350 ℃～420 ℃ of temperature of reaction, hydrogen dividing potential drop 5.0～22.0MPa, volume space velocity 0.5～10h
-1, hydrogen-oil ratio 500～1200Nm
3/ m
3Condition under react;
(2), the logistics handled through hydrofining enters the hydrodemetallation (HDM) reactor that Hydrodemetalation catalyst is housed, at 350 ℃～420 ℃ of temperature of reaction, hydrogen dividing potential drop 5.0～22.0MPa, volume space velocity 0.5～5.0h
-1, hydrogen-oil ratio 500～1500Nm
3/ m
3Condition under react;
(3), the logistics handled through hydrodemetallation (HDM) enters the hydrodesulphurisatioreactors reactors that Hydrobon catalyst is housed, at 350～420 ℃ of temperature of reaction, hydrogen dividing potential drop 5.0～22.0MPa, volume space velocity 0.5～5.0h
-1, hydrogen-oil ratio 500～2000Nm
3/ m
3Condition under react;
(4), enter vacuum distillation apparatus, fractionate out the hydrogenation heavy distillate through the logistics of hydrogenating desulfurization;
(5), the hydrogenation heavy distillate enters the delayed coking unit with conventional coking different operating mode separately, also can be mixed into the preheating of process furnace convection zone with other conventional raw material of producing pin Jiao, entering separation column and turning oil then is mixed into the process furnace radiation section and operates through alternating temperature, the scope of alternating temperature is 430～520 ℃, recycle ratio 0.2～1.2;
(6), the logistics that will heat enters coke drum, its operational condition is: the coke tower top pressure is 0.10～3.0MPa, 380 ℃～460 ℃ of coke tower top temperatures, pin Jiao stays in the coke drum;
(7), thermal response produced oil gas ejects from coke drum and enters separation column, fractionates out gas, gasoline, diesel oil and gas oil, turning oil mixes the charging as the process furnace radiation section with the hydrogenation heavy distillate.
2, according to the method for claim 1, it is characterized in that the described sulfur containing atmospheric of step (1) is the long residuum of any high-sulfur crude oil, and with arbitrary proportion blended sulfur containing atmospheric.
3,, it is characterized in that the described protective material of step (1) is made up of the gamma-aluminium oxide carrier that diplopore distributes that has of 1.0～5.0 heavy % nickel oxide, 5.5～10.0 heavy % molybdenum oxides and surplus according to the method for claim 1.
4,, it is characterized in that the described decompression cutting temperature of step (4) is 400 ℃～520 ℃ according to the method for claim 1.
5,, it is characterized in that the described conventional raw material that other produces pin Jiao of step (5) is selected from fluid catalytic cracking decant oil, thermal cracking residue, lube oil furfural refining and extracts among the residual oil of oil, preparing ethylene by steam cracking one or more mixture out according to the method for claim 1.
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|---|---|---|---|
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| CNB001093738A CN1191321C (en) | 2000-05-31 | 2000-05-31 | Process for preparing acicular petroleum coke from S-contained ordinary-pressure residual oil |
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