CN103374394B - Grading loading method of catalyst and application of grading loading method, and hydrogenation treatment method of heavy oils - Google Patents
Grading loading method of catalyst and application of grading loading method, and hydrogenation treatment method of heavy oils Download PDFInfo
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Abstract
The invention discloses a grading loading method of a catalyst. The method comprises the following step of: orderly arranging a first hydrogenation guard catalyst bed, a hydrodemetallization catalyst bed and a hydrodesulfurization catalyst bed in a plurality of reactors connected in series. The method is characterized by also comprising the step of adding a second hydrogenation guard catalyst bed between the hydrodemetallization catalyst bed and the hydrodesulfurization catalyst bed. Besides, the invention also provides an application of the grading loading method in hydrogenation treatment of heavy oils, and particularly provides a hydrogenation treatment method of the heavy oils. The hydrogenation treatment method disclosed by the invention is used for hydrogenation treatment of the heavy oils and has the advantages of delaying inactivation of a hydrodesulfurization catalyst, a hydrogenating residual carbon removal catalyst or a hydrodenitrogenation catalyst.
Description
Technical field
The present invention relates to a kind of grading loading method and application thereof of catalyzer, and be specifically related to a kind of hydroprocessing process of heavy oil product.
Background technology
Heavy oil product hydrogenation technique is a kind of heavy oil product deep processing technology, this technique is under the existence of hydrogen and catalyzer, carry out hydrogenating desulfurization, hydrodenitrification, hydrodemetallation (HDM) and carbon residue to residual oil to transform and hydrocracking reaction, residual oil after the hydrogenation obtained can be used as the charging of fine quality catalytic cracking to produce light-end products, to reach residual oil lighting to greatest extent, realize sludgeless oil refinery.
In heavy oil product hydrogenation process, the main reaction occurred has hydrodemetallation (HDM), hydrogenating desulfurization, hydrodenitrification reaction and carbon residue conversion and bitum hydrocracking reaction etc.Heavy oil product is as in all components of residual oil, and bituminous matter is the most unmanageable component.Bitum molecular weight is very large, and containing sulphur, nitrogen, heavy metal and multinuclear aromatic compound.
" heavy oil product " refers to the hydro carbons of the high asphalt content obtained by topped crude, petroleum residual oil, oil-sand, pitch, shale oil, liquefaction coal or recovered oil.Heavy oil product contains various pollutent usually, the residual matter of such as carbon containing, sulphur, nitrogen and metal.Current fixed bed hydrogenation process application is comparatively extensive; generally adopt catalyzer grading loading technology; generally in processing heavy oil product reactor sequences, load hydrogenation protecting agent successively; hydrodemetallation (HDM) agent, hydrodemetallation (HDM) sweetening agent, hydrogen desulfurization agent, hydrodenitrification agent, removal of ccr by hydrotreating agent; remove the metal in heavy oil product, sulphur, nitrogen and carbon residue, produce qualified catalytically cracked material.But because different crude oils has difference, therefore need develop different catalyst grades for different oil product and join filling method, to extend the work-ing life of heavy oil product hydrotreatment catalyst series.As CN1133722C proposes a kind of layering filling method processing the catalyzer of high nitrogen-containing poor-quality heavy residuum, in fixed-bed reactor, load hydrogenation protecting agent bed, hydrodemetallation (HDM) agent bed, the hydrodenitrification agent bed of transition, hydrogen desulfurization agent bed and hydrodenitrification agent bed successively.
Along with the minimizing day by day of crude oil, the lighting of heavy oil requires more and more higher, has some crude oil calcium contentss higher, for the heavy oil product that calcium contents is higher, realize hydrocracking to reach higher light oil yield, the importance improving the processing method of the transformation efficiency of residual oil manifests day by day.In general, calcium containing compound in crude oil is divided into inorganic calcium compound and organocalcium compound, inorganic calcium can remove completely in technology of electric de-salting process, organic calcium is then needed to add special decalcifying agent remove, nonetheless, for this crude oil, the calcium contents in its heavy oil product hydrogenating materials also can be greater than 10ug/g.
Therefore, a kind of grading loading method that can be effective to the catalyzer of High calcium containing crudes hydrotreatment of exploitation is needed badly.
Reason bad to the hydrogenation crude treatment effect of high calcium content in prior art is that the organocalcium compound in heavy oil product is easier in catalyst external surface generation hydrogenation decalcification reaction, and the CaS of generation is deposited on granules of catalyst outside surface with the form of crystallization.In addition, calcium very easily penetrates catalyst for demetalation bed and deposits to hydrogenating desulfurization and follow-up hydrogenation takes off on carbon residue or hydrodenitrogenation catalyst, causes catalyst deactivation.Therefore, if on the basis of existing technology, after Hydrodemetalation catalyst bed, the calcium in oil product can be removed further, then can improve the hydrotreatment effect of the crude oil of high calcium content.The present inventor completes the present invention on this basis.
The invention provides a kind of grading loading method of catalyzer; the method comprises; the first hydrogenation protecting catalyst bed, Hydrodemetalation catalyst bed and Hydrobon catalyst bed is set gradually in multiple reactors of series connection; it is characterized in that, the method is also included between described Hydrodemetalation catalyst bed and Hydrobon catalyst bed and sets up the second hydrogenation protecting catalyst bed.
The present invention also provides the application of grading loading method in the hydrotreatment of heavy oil product of above-mentioned catalyzer.And a kind of hydroprocessing process of heavy oil product is specifically provided, it is characterized in that, the method comprises, at hydrotreating reaction conditions, heavy oil product and hydrogen are introduced in multiple hydrogenators of connecting successively, and with the catalyst exposure in the plurality of hydrogenator, described catalyzer loads according to the grading loading method of above-mentioned catalyzer.
Utilize method of the present invention to carry out hydrotreatment to heavy oil product, the inactivation of Hydrobon catalyst, removal of ccr by hydrotreating catalyzer or hydrodenitrogenation catalyst can be delayed.Particularly for the heavy oil product of high calcium content, utilize method of the present invention, at continuous seepage after 3000 hours, in hydrogenated oil, the content of calcium still can control within 9 μ g/g, and utilize the method for prior art, at continuous seepage after 3000 hours, in hydrogenated oil, the content of calcium is 13 μ g/g.
Summary of the invention
The object of this invention is to provide a kind of catalyst grade and join filling method and application thereof, and a kind of hydroprocessing process utilizing this grading loading method is specifically provided.
Accompanying drawing explanation
Accompanying drawing is used to provide a further understanding of the present invention, and forms a part for specification sheets, is used from explanation the present invention, but is not construed as limiting the invention with embodiment one below.In the accompanying drawings:
Fig. 1 is the process flow sheet of one embodiment of the present invention;
Fig. 2 is the process flow sheet of prior art.
Embodiment
The invention provides a kind of grading loading method of catalyzer; the method comprises; the first hydrogenation protecting catalyst bed, Hydrodemetalation catalyst bed and Hydrobon catalyst bed is set gradually in multiple reactors of series connection; it is characterized in that, the method is also included between described Hydrodemetalation catalyst bed and Hydrobon catalyst bed and sets up the second hydrogenation protecting catalyst bed.
According to the present invention; the object of setting up the second hydrogenation protecting catalyst bed is the calcium removed further in oil product; therefore; the loadings of above-mentioned catalyzer can be selected according to the calcium contents in pending oil product; consider and remove the effect of calcium and the effect of desulfurization; preferably; with the total fill able volume of described multiple catalyst reactor for benchmark; the loadings of the catalyzer in the second hydrogenation protecting catalyst bed is 1-30 volume %; more preferably 2-20 volume %; be more preferably 2-15 volume %, most preferably be 2-10 volume %.
Preferably; this grading loading method arranges removal of ccr by hydrotreating denitrification catalyst bed after being also included in Hydrobon catalyst bed; removal of ccr by hydrotreating catalyzer and/or hydrodenitrogenation catalyst is filled with in described removal of ccr by hydrotreating denitrification catalyst bed; further preferably, this grading loading method is also included between described Hydrobon catalyst bed and removal of ccr by hydrotreating denitrification catalyst bed and sets up the 3rd hydrogenation protecting catalyst bed.
Similar to the abovely; consider and remove the effect of calcium and the effect of de-carbon residue denitrogenation; preferably; with the total fill able volume of described multiple catalyst reactor for benchmark; the loadings of the catalyzer in the 3rd hydrogenation protecting catalyst bed is 1-20 volume %, more preferably 2-10 volume %.
Preferably, the volume ratio of the loadings of the catalyzer in the loadings of the catalyzer in described second hydrogenation protecting catalyst bed and described 3rd hydrogenation protecting catalyst bed is 1: 0.2-1.The present inventor finds, loads, can be processed the effect of the oil product of high calcium content better according to the ratio in above-mentioned preferable range.
Catalyzer in described first hydrogenation protecting catalyst bed, the second hydrogenation protecting catalyst bed and the 3rd hydrogenation protecting catalyst bed can be identical or different, can be all conventional various hydrogenation protecting catalysts.As the RG series hydrogenation protecting catalyst produced purchased from catalyzer Chang Ling branch office.
According to the present invention, the relative loadings of described first hydrogenation protecting catalyst bed, Hydrodemetalation catalyst bed, Hydrobon catalyst bed and the catalyzer in removal of ccr by hydrotreating denitrification catalyst bed can with this area routine use identical.Such as; with the total fill able volume of described multiple catalyst reactor for benchmark; the loadings of the catalyzer in described first hydrogenation protecting catalyst bed can be 1-20 volume %; the loadings of the catalyzer in described Hydrodemetalation catalyst bed can be 5-70 volume %; the loadings of the catalyzer in described Hydrobon catalyst bed can be 15-70 volume %, and the loadings of the catalyzer in described removal of ccr by hydrotreating denitrification catalyst bed is preferably 5-70 volume %.
The grading loading method of catalyzer of the present invention can be used for the hydrotreatment of heavy oil product.Preferably, in described heavy oil product, the content of calcium is more than 10ppm, is more preferably 15-30ppm.Particularly, the invention provides a kind of hydroprocessing process of heavy oil product, it is characterized in that, the method comprises, at hydrotreating reaction conditions, heavy oil product and hydrogen are introduced in multiple hydrogenators of connecting successively, and with the catalyst exposure in the plurality of hydrogenator, described catalyzer loads according to the grading loading method of above-mentioned catalyzer.
Method of the present invention can be used for the hydrogenator of different structure, and each hydrogenator can adopt upflowing charging, also can adopt downflow system charging, and preferably, each hydrogenator is upflow fixed bed reactor.
According to the present invention, the number of described multiple hydrogenator is preferably 2-6; The number of the beds in each hydrogenator is preferably 2-6, more preferably 2-4.The number of the hydrogenation catalyst bed in the number of described hydrogenator and each hydrogenator can carry out suitable adjustment as required.As, in heavy oil product, metal content is very high, then can arrange the Hydrodemetalation catalyst bed of multiple number.Similarly, in each beds, the loadings of catalyzer also can adjust as required.
In the present invention, described heavy oil product can be crude oil, the long residuum obtained by crude oil and vacuum residuum, the various oil obtained by coal, tar sand, resinous shale and pitch, and their mixture.Sulphur content in these residual oil raw materials, nitrogen content, asphalt content, beavy metal impurity content and carbon residue content are higher all to some extent.
In the present invention, described heavy oil product refers in particular to long residuum or the vacuum residuum of asphaltenes.The boiling range of long residuum is more than about 345 DEG C.The boiling range of vacuum residuum is more than about 500 DEG C, and usually has higher viscosity than long residuum.Preferably, in described heavy oil product, the content of calcium is more than 10ppm, is more preferably 15-30ppm.
According to the present invention, described hydrogenation protecting catalyst, Hydrodemetalation catalyst, Hydrobon catalyst and removal of ccr by hydrotreating catalyzer can be the catalyzer with these functions of this area routine.Carbon residue, nitrogen and sulphur exist in residual oil usually used as pollutent, although these pollutents may exist as relatively simple molecule, they are remained in hydrocarbon molecules more firmly by chemical bond usually.So and remove metallographic phase ratio, removing carbon residue, sulphur and nitrogen needs more highly active hydrogenation catalyst usually.Usually, above-mentioned catalyzer be all with heat-resisting porous inorganic oxide as aluminum oxide be carrier, with group vib and/or group VIII metal as the oxide compound of one or more in W, Mo, Co and Ni is active ingredient, optionally adds other various auxiliary agent as one or more catalyzer in P, Si, F and B.Combinationally use after can being purchased separately various catalyzer during use; also the complete series catalyst for hydrotreatment of residual oil comprising above-mentioned various catalyzer can be directly purchased, as RG, RDM, RMS and RCS series weight, hydrotreating guard catalyst for residual oil, Hydrodemetalation catalyst, Hydrobon catalyst and removal of ccr by hydrotreating catalyzer purchased from catalyzer Chang Ling branch office.
According to the present invention, described hydrotreatment reaction conditions can be the hydrotreatment reaction conditions of this area routine, and preferably, temperature is 300-420 DEG C, more preferably 360-420 DEG C; Pressure is 10-17MPa, more preferably 13-16MPa; Hydrogen to oil volume ratio is 200-2000, more preferably 420-1500; During the liquid of heavy oil product, volume space velocity is 0.10-0.45h
-1, more preferably 0.14-0.30h
-1.
In the present invention, in described multiple reactor, the setting of multiple beds can adjust according to practical situation, as the height of each bed, number and position, preferably, can arrange as shown in Figure 1.
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described in detail.Should be understood that, embodiment described herein, only for instruction and explanation of the present invention, is not limited to the present invention.
As shown in Figure 1, this device adopts 4 reactors in series, the top-down technical process of stock oil, stock oil and hydrogen enter a, b, c and d reactor of series connection from 101 pipelines successively, wherein, be disposed with 4 beds in a reactor, comprise RG-10E (hydrogenation protecting catalyst) bed, RG-20A (hydrogenation protecting catalyst) bed, RG-20B (hydrogenation protecting catalyst) bed and RDM-2B (Hydrodemetalation catalyst) bed; Be disposed with two beds in b reactor, comprise RDM-2B bed and RDM-3B (Hydrodemetalation catalyst) bed; Be disposed with 4 beds in c reactor, comprise RG-10E bed, RG-20A bed, RG-20B bed and RMS-1B (Hydrobon catalyst) bed; Be disposed with 4 beds in d reactor, comprise RG-10E bed, RG-20A bed, RG-20B bed and RCS-1 (removal of ccr by hydrotreating catalyzer) bed.
And in the method for prior art, as shown in Figure 2, the catalyzer in a reactor is from top to bottom: RG-10E, RG-20A, RG-20B and RDM-2B; RDM-2B and RDM-3B is loaded successively in b reactor; All RMS-1B is loaded in c reactor; All RCS-1 is loaded in d reactor.
Below, by embodiment, method of the present invention is described in detail.
In the embodiment of the present invention, equipment therefor is fixed bed hydrogenation process testing apparatus as shown in Figure 1, and this device adopts 4 volumes to be reactors in series, the top-down technical process of stock oil of 1 liter.
RG, RDM and RMS used, RCS series weight, hydrotreating guard catalyst for residual oil, Hydrodemetalation catalyst and Hydrobon catalyst are that China Petrochemical Industry's catalyzer Chang Ling branch office produces.
Embodiment 1
Adopt device as shown in Figure 1, the filling situation of each catalyst reactor is:
Catalyzer in a reactor is RG-10E, RG-20A, RG-20B, RDM-2B catalyzer from top to bottom, and the ratio of each catalyst loading volume is 10: 15: 20: 55;
Filling RDM-2B and RDM-3B catalyzer in b reactor, the ratio of each catalyst loading volume is 55: 45;
In c reactor, the catalyzer of filling is RG-10E, RG-20A, RG-20B and RMS-1B catalyzer from top to bottom, and the ratio of admission space is 5: 7.5: 10: 77.5;
In d reactor, the catalyzer of filling is RG-10E, RG-20A, RG-20B and RCS-1 catalyzer from top to bottom, and the ratio of admission space is 2.5: 3.5: 5: 89;
The flow process of residual hydrogenation reaction is be 14.7MPa in reaction pressure, and hydrogen-oil ratio is 600 (v/v), and during liquid, volume space velocity is 0.22h
-1operational condition under, the residual oil raw material M of high calcium content and hydrogen are mixed into a reactor, and enter b, c, d reactor successively subsequently, and the temperature of reaction of a reactor is 370 DEG C, and the temperature of reaction of b, c and d reactor is 380 DEG C.The main character of this residual oil raw material M is listed in table 1.The character of the hydrogenated oil product obtained when the steady running 1000,2000 and 3000 hours of slag input oil is in table 2.
Table 1
| Project | Chang Ling mixing raw material (residual oil raw material M) |
| Density (20 DEG C), g/cm 3 | 0.960 |
| Viscosity (80 DEG C), mm 2/s | 117.7 |
| MCR (% by weight) | 9.81 |
| Sulphur content (% by weight) | 0.89 |
| Heavy metal content (μ g/g) | |
| Ni+V | 47 |
| Ca | 21 |
| Four composition (% by weight) | |
| Stable hydrocarbon | 30.6 |
| Aromatic hydrocarbons | 40.0 |
| Colloid | 28.2 |
| Bituminous matter (C 7Insolubles) | 1.2 |
Table 2
Comparative example 1
4 volumes are adopted to be reactors in series, the top-down technical process of stock oil of 1 liter, as shown in Figure 2.According to the flow direction of stock oil, four reactors are followed successively by a, b, c and d.
The complete series s-generation catalyst for hydrotreatment of residual oil that the catalyzer adopted is Research Institute of Petro-Chemical Engineering's exploitation, catalyzer Chang Ling branch office produces, comprises RG, RDM, RMS and RCS series weight, hydrotreating guard catalyst for residual oil, Hydrodemetalation catalyst, hydrogenating desulfurization and hydrogenation and takes off carbon residue catalyzer.
The filling situation of each catalyst reactor is:
Catalyzer in a reactor is RG-10E, RG-20A, RG-20B, RDM-2B catalyzer from top to bottom, and the ratio of each catalyst loading volume is 10: 15: 20: 55;
Filling RDM-2B and RDM-3B catalyzer in b reactor, the ratio of each catalyst loading volume is 55: 45; In c reactor, the catalyzer of filling is all RMS-1B catalyzer; In d reactor, the catalyzer of filling is all RCS-1 catalyzer;
The flow process of residual hydrogenation reaction is be 14.7MPa in reaction pressure, and hydrogen-oil ratio is 600 (v/v), and during liquid, volume space velocity is 0.22h
-1operational condition under, residual oil raw material M and hydrogen are mixed into a reactor, and enter b, c, d reactor successively subsequently, and the temperature of reaction of a reactor is 370 DEG C, and the temperature of reaction of b, c, d and e reactor is 380 DEG C.The character of the hydrogenated oil product obtained when steady running 1000,2000 and 3000 hours is in table 3.
Table 3
Embodiment 2
Adopt device as shown in Figure 1, the filling situation of each catalyst reactor is:
Catalyzer in a reactor is RG-10E, RG-20A, RG-20B, RDM-2B catalyzer from top to bottom, and the ratio of each catalyst loading volume is 10: 10: 20: 60;
Filling RDM-2B and RDM-3B catalyzer in b reactor, the ratio of each catalyst loading volume is 50: 50;
In c reactor, the catalyzer of filling is RG-10E, RG-20A, RG-20B and RMS-1B catalyzer from top to bottom, and the ratio of admission space is 5: 5: 10: 80;
In d reactor, the catalyzer of filling is RG-10E, RG-20A, RG-20B and RCS-1 catalyzer from top to bottom, and the ratio of admission space is 2.5: 2: 5.5: 90;
The flow process of residual hydrogenation reaction is be 400 DEG C in temperature of reaction, and reaction pressure is 13.2MPa, and hydrogen-oil ratio is 1000 (v/v), and during liquid, volume space velocity is 0.28h
-1operational condition under, residual oil raw material M and hydrogen are mixed into a reactor, and enter b, c, d reactor successively subsequently.The character of the hydrogenated oil product obtained when the steady running 1000,2000 and 3000 hours of slag input oil is in table 4.
Table 4
Embodiment 3
Adopt device as shown in Figure 1, the filling situation of each catalyst reactor is:
Catalyzer in a reactor is RG-10E, RG-20A, RG-20B, RDM-2B catalyzer from top to bottom, and the ratio of each catalyst loading volume is 15: 15: 30: 40;
Filling RDM-2B and RDM-3B catalyzer in b reactor, the ratio of each catalyst loading volume is 70: 30;
In c reactor, the catalyzer of filling is RG-10E, RG-20A, RG-20B and RMS-1B catalyzer from top to bottom, and the ratio of admission space is 10: 10: 20: 60;
In d reactor, the catalyzer of filling is RG-10E, RG-20A, RG-20B and RCS-1 catalyzer from top to bottom, and the ratio of admission space is 5: 5: 10: 80;
The flow process of residual hydrogenation reaction is be 415 DEG C in temperature of reaction, and reaction pressure is 15.6MPa, and hydrogen-oil ratio is 1400 (v/v), and during liquid, volume space velocity is 0.15h
-1operational condition under, residual oil raw material M and hydrogen are mixed into a reactor, and enter b, c, d reactor successively subsequently.The character of the hydrogenated oil product obtained when the steady running 1000,2000 and 3000 hours of slag input oil is in table 5.
Table 5
Embodiment 4
Method according to embodiment 1 carries out residual hydrocracking, unlike, all load RCS-1 catalyzer in d reactor.
The character of the hydrogenated oil product obtained when the steady running 1000,2000 and 3000 hours of slag input oil is in table 6.
Table 6
As can be seen from the result of embodiment 1-3 and comparative example 1, catalyst according to the invention grading loading method carries out hydrotreatment to heavy oil product, can delay the inactivation of Hydrobon catalyst, removal of ccr by hydrotreating catalyzer or hydrodenitrogenation catalyst.Particularly for the heavy oil product of high calcium content, utilize method of the present invention, at continuous seepage after 3000 hours, in hydrogenated oil, the content of calcium still can control within 9 μ g/g, and utilize the method for prior art, at continuous seepage after 3000 hours, in hydrogenated oil, the content of calcium is 13 μ g/g.
The difference of embodiment 4 and embodiment 1 is only not arrange hydrogenation protecting catalyst between Hydrobon catalyst and removal of ccr by hydrotreating denitrification catalyst in embodiment 4; as can be seen from the result of embodiment 4 and embodiment 1; set up the second hydrogenation protecting catalyst bed between described Hydrodemetalation catalyst bed and Hydrobon catalyst bed while, between described Hydrobon catalyst bed and removal of ccr by hydrotreating denitrification catalyst bed, set up the 3rd hydrogenation protecting catalyst bed is the preferred embodiment of the present invention.
In addition, also can carry out arbitrary combination between various different embodiment of the present invention, as long as it is without prejudice to thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (12)
1. the grading loading method of a catalyzer; the method comprises; the first hydrogenation protecting catalyst bed, Hydrodemetalation catalyst bed and Hydrobon catalyst bed is set gradually in multiple reactors of series connection; it is characterized in that, the method is also included between described Hydrodemetalation catalyst bed and Hydrobon catalyst bed and sets up the second hydrogenation protecting catalyst bed.
2. method according to claim 1, wherein, with the total fill able volume of described multiple catalyst reactor for benchmark, the loadings of the catalyzer in the second hydrogenation protecting catalyst bed is 1-30 volume %.
3. method according to claim 1, wherein, this grading loading method arranges removal of ccr by hydrotreating denitrification catalyst bed after being also included in Hydrobon catalyst bed, is filled with removal of ccr by hydrotreating catalyzer and/or hydrodenitrogenation catalyst in described removal of ccr by hydrotreating denitrification catalyst bed.
4. method according to claim 3, wherein, this grading loading method is also included between described Hydrobon catalyst bed and removal of ccr by hydrotreating denitrification catalyst bed and sets up the 3rd hydrogenation protecting catalyst bed.
5. method according to claim 4, wherein, with the total fill able volume of described multiple catalyst reactor for benchmark, the loadings of the catalyzer in the 3rd hydrogenation protecting catalyst bed is 1-20 volume %.
6. according to the method in claim 1-5 described in any one; wherein; with the total fill able volume of described multiple catalyst reactor for benchmark; the loadings of the catalyzer in described first hydrogenation protecting catalyst bed is 1-20 volume %; the loadings of the catalyzer in described Hydrodemetalation catalyst bed is 5-70 volume %, and the loadings of the catalyzer in described Hydrobon catalyst bed is 15-70 volume %.
7., according to the method in claim 3-5 described in any one, wherein, with the total fill able volume of described multiple catalyst reactor for benchmark, the loadings of the catalyzer in described removal of ccr by hydrotreating denitrification catalyst bed is 5-70 volume %.
8. the application of grading loading method in the hydrotreatment of heavy oil product of the catalyzer in claim 1-7 described in any one, wherein, in described heavy oil product, the content of calcium is more than 10ppm.
9. the hydroprocessing process of a heavy oil product, it is characterized in that, the method comprises, at hydrotreating reaction conditions, heavy oil product and hydrogen are introduced in multiple hydrogenators of connecting successively, and with the catalyst exposure in the plurality of hydrogenator, described catalyzer loads according to the grading loading method of the catalyzer in claim 1-7 described in any one.
10. method according to claim 9, wherein, the number of described multiple hydrogenator is 2-6, and the number of the beds in each hydrogenator is 2-6.
11. methods according to claim 9, wherein, in described heavy oil product, the content of calcium is more than 10ppm.
12. according to the method in claim 9-11 described in any one, and wherein, described hydrotreatment reaction conditions comprises, and temperature is 300-420 DEG C, and pressure is 10-17MPa, and hydrogen to oil volume ratio is 200-2000, and during the liquid of heavy oil product, volume space velocity is 0.10-0.45h
-1.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1362481A (en) * | 2001-01-05 | 2002-08-07 | 中国石油化工股份有限公司 | Catalyst sorting and loading method |
| CN1597856A (en) * | 2003-09-15 | 2005-03-23 | 中国石油化工股份有限公司 | Heavy slag oil fixed bed hydrogenating treatment process |
| US7476309B2 (en) * | 2001-06-08 | 2009-01-13 | Albemarle Netherlands B.V. | Two-stage heavy feed hpc process |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1362481A (en) * | 2001-01-05 | 2002-08-07 | 中国石油化工股份有限公司 | Catalyst sorting and loading method |
| US7476309B2 (en) * | 2001-06-08 | 2009-01-13 | Albemarle Netherlands B.V. | Two-stage heavy feed hpc process |
| CN1597856A (en) * | 2003-09-15 | 2005-03-23 | 中国石油化工股份有限公司 | Heavy slag oil fixed bed hydrogenating treatment process |
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