CN1262306A - Hydrogenation and catalystic cracking combined process for residual oil - Google Patents
Hydrogenation and catalystic cracking combined process for residual oil Download PDFInfo
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- CN1262306A CN1262306A CN 99100399 CN99100399A CN1262306A CN 1262306 A CN1262306 A CN 1262306A CN 99100399 CN99100399 CN 99100399 CN 99100399 A CN99100399 A CN 99100399A CN 1262306 A CN1262306 A CN 1262306A
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Abstract
A hydrogenation and catalytic cracking combined process for residual oil includes such steps as introducing residual oil and clarified oil into hydrogenation equipment, hydrogenation reaction under the existance of hydrogen and hydrogenation catalyst, loading the hydrogenated residual oil into catalytic cracking eqipment, cracking reaction under the existance of cracking catalyst, separating to obtain clarified oil, and returning it back to hydrogenation equipment. Said process can increase the output rate of gasoline and diesel oil.
Description
The invention belongs to the combined technical method of handling hydrocarbon ils with other step of converting of a hydroprocessing technique process and, more particularly, is a kind of combined technical method that residual hydrocracking and two kinds of processing methodes of catalytic cracking are organically combined.
Catalytic cracking is one of most important crude oil secondary processing processing method, according to the difference of raw material, generally is divided into two types of wax catalysis cracking and heavy oil fluid catalytic cracking.The recycle stock catalytic cracking is the catalytic cracking new process that the seventies grows up, and is raw material with recycle stock or residual oil.Industrial have full long residuum cracking and fraction oil to mix types such as long residuum or vacuum residuum cracking.Owing to generally contain heavy metal and bituminous matters such as nickel, vanadium in the residual oil, so cracking catalyst is produced the generation of polluting and rolling up coke, thereby this processing method has certain restriction to raw materials quality, particularly requires sulphur, nitrogen, metal impurities content and carbon residue in the raw material lower.For sulphur, nitrogen, metal impurities content and the higher poor residuum of carbon residue, must be through pre-treatment, reduce wherein sulphur, nitrogen, metal impurities content and carbon residue, could be as suitable recycle stock catalytically cracked material, and residual hydrocracking is a kind of practicable preprocessing means.
The purpose of the initial exploitation of residual hydrocracking is from doctor positive crude production low sulphur fuel oil, but along with to the reduction of oil fuel demand and to the vehicle fuel growth of requirement, residual hydrogenation turns to devices such as being mainly recycle stock catalytic cracking or coking to supply raw materials gradually.By hydrotreatment, sulphur, nitrogen, metal impurities content and carbon residue in the poor residuum are obviously reduced, thereby obtain the charging that the recycle stock catalytic cracking unit can be accepted.The improvement of charging quality, recycle stock catalytic cracking unit coke output reduces, and the catalyst consumption amount reduces, and transformation efficiency improves, and then the total process cost of recycle stock catalytic cracking unit is reduced.Need higher investment although build residual hydrogenation equipment, can be used for compensating by higher product quality and lower recycle stock catalytic cracking unit operational cost.The research of Reynolds and Silverman (Hydrocarbon Processing, April 1993) show, when processing Arabic lightweight long residuum, adopt residual hydrogenation/recycle stock catalytic cracking combination, the net profit of every barrel of raw material improves 1.45 dollars than independent recycle stock catalytic cracking.Thereby residual hydrocracking is supplied raw materials for the recycle stock catalytic cracking, has become the processing route that the refinery accepts extensively.
USP4,713,221 disclose on the residual hydrogenation of routine and catalytic cracking combined basis, and the heavy cycle oil of catalytic cracking (comprising wax catalysis cracking and recycle stock catalytic cracking) is circulated to residual hydrogenation equipment, with carry out hydrogenation after residual oil mixes, enter catalytic cracking unit again.And for the residual hydrogenation and the catalytic cracking combined processing scheme of routine, the heavy cycle oil of catalytic cracking is to carry out round-robin in catalytic cracking unit inside.The change that this is little can make the benefit of every barrel of crude oil of refinery's processing have a net increase of 0.29 dollar.
Slurry oil is the residual oil of extracting out at the bottom of the catalytic cracking fractionating tower that has catalyst fines.Generally the reactor freshening can be sent back to, but the coke growing amount can be increased.When the revivifier amount of burnt reaches capacity, when not wanting to reduce device raw material treatment capacity again, often unnecessary slurry oil discharger is removed to do oil fuel, being commonly called as is " getting rid of slurry oil operates ".Slurry oil is called clarified oil through the last oil of settlement separate catalyst powder.It is many that clarified oil contains aromatic hydrocarbons, is not suitable for doing catalytic cracking turning oil, and is used to produce acicular petroleum coke as coking raw material oil.For the refinery that does not have coker, clarified oil mostly can only be used for blendedfuel oil, and oil fuel is a kind of product of low value.
The objective of the invention is to provide on the basis of existing technology a kind of and can process catalytically cracked oil, residual hydrogenation-recycle stock catalytic cracking combination process that the light-end products yield is higher.
Processing method provided by the invention may further comprise the steps:
A, residual oil and clarified oil enter hydrogenation unit together, carry out hydrogenation reaction in the presence of hydrogen and catalyzer, and reaction product isolated obtains gas, petroleum naphtha, hydrogenated diesel oil and hydrogenated residue;
B, hydrogenated residue enter catalytic cracking unit, carry out cracking reaction in the presence of catalyzer, and reaction product isolated obtains dry gas, liquefied gas, gasoline, diesel oil, recycle stock and slurry oil, and wherein recycle stock is back to catalytic cracking unit;
C, slurry oil obtain clarified oil after separator is isolated the cracking catalyst powder, be back to hydrogenation unit.
Residual oil in the steps A both can be long residuum, also can be vacuum residuum.Typical hydrogenation method condition is: hydrogen dividing potential drop 5.0～22.0 MPas, 330～450 ℃ of temperature of reaction, volume space velocity 0.1～3.0 hour
-1, hydrogen and stock oil volume ratio (hereinafter to be referred as hydrogen-oil ratio) 350～2000, the stock oil here is meant the mixture of residual oil and clarified oil.Described catalyzer can be various hydrogenation catalysts, and its active metal component is nickel-tungsten, nickel-tungsten-cobalt, nickel-molybdenum or cobalt-molybdenum, and carrier is aluminum oxide, silicon-dioxide or amorphous aluminum silicide, and wherein aluminum oxide is the most frequently used carrier.
The residual hydrogenation type of reactor can be fixed bed, moving-bed or ebullated bed, and residual hydrogenation equipment comprises a reactor and a separation column at least.
Gas in the hydrotreatment products can be sneaked in the refinery gas, and petroleum naphtha can be used as the charging of reformer, and hydrogenated diesel oil is an ideal diesel product blending component, hydrogenated residue can be all as the charging of heavy oil catalytically cracking equipment.
Catalytic cracking unit can be that every covering device should comprise a reactor, a revivifier and a separation column at least more than a cover or overlapped.The employed catalyzer of catalytic cracking is REY, REHY, ZSM-5 equimolecular sieve catalyst or its composition, the processing method condition is: the weight ratio (hereinafter to be referred as agent-oil ratio) 3～10 of 470～570 ℃ of temperature of reaction, 1～5 second reaction times, catalyzer and stock oil, 650～750 ℃ of regeneration temperatures, the stock oil here is meant hydrogenated residue.
Gasoline in the catalytic cracking production is ideal high octane gasoline products blending component; If diesel-fuel cetane number is enough high, can directly mixes in the diesel product, otherwise need through hydrotreatment to improve its cetane value; Recycle stock returns catalyst cracker and further transforms; A small amount of slurry oil " gets rid of outward " and goes out device, and most of slurry oil obtains clarified oil after separator is isolated the cracking catalyst powder, be back to hydrogenation unit.
Below in conjunction with accompanying drawing processing method provided by the present invention is given further instruction.
Fig. 1 is residual hydrogenation provided by the present invention-catalytic cracking combination process schematic flow sheet.
Fig. 2 is conventional residual hydrogenation-catalytic cracking combined device schematic flow sheet.
Residual hydrogenation shown in Figure 1-catalytic cracking combination process flow process is as follows:
The residual oil, clarified oil and the hydrogen that come from pipeline 1,13 and 2 respectively enter residual hydrogenation equipment 14, in the presence of hydrogenation catalyst, react, the reaction product of separating residual hydrogenation, obtain gas, petroleum naphtha, hydrogenated diesel oil and hydrogenated residue, wherein through pipeline 3,4,5 caterpillars, hydrogenated residue then enters catalytic cracking unit 15 through pipeline 6 respectively for gas, petroleum naphtha and diesel oil.
Hydrogenated residue from pipeline 6 enters catalytic cracking unit 15, in the presence of cracking catalyst, react, the reaction product of separating heavy oil fluid catalytic cracking, obtain dry gas, liquefied gas, gasoline, diesel oil, recycle stock and slurry oil, dry gas wherein, liquefied gas, gasoline and diesel oil are respectively through pipeline 7,8,9,10 caterpillars, recycle stock is back to catalytic cracking unit through pipeline 11 and continues reaction, a small amount of slurry oil is through pipeline 18 caterpillars, most of slurry oil enters separator 16 through pipeline 12, removing the last slurry oil of catalyst powder is that clarified oil enters residual hydrogenation equipment 14 through pipeline 13, and the catalyst fines that removes is through pipeline 17 caterpillars.
The residual hydrogenation of routine shown in Figure 2-catalytic cracking combined device, compare with combined technical method provided by the present invention, slurry oil removes to produce oil fuel through pipeline 14, perhaps entering separator 16 through pipeline 12, to remove catalyst powder last, clarified oil is as the raw material of producing acicular petroleum coke or carbon black, rather than as the raw material of residual hydrogenation equipment.
More than the present invention has been made specific descriptions, but the present invention is not limited thereto with processing method flow process illustrated in figures 1 and 2.
The invention has the advantages that: adopt processing method flow process provided by the present invention, catalytic cracking unit freshening or the slurry oil that gets rid of outward are circulated in the raw material of residual hydrogenation equipment after separating, make catalytically cracked oil be converted into the higher light-end products of added value, improve the yield of gasoline and diesel oil, reduced the yield of heavy oil.
The following examples will give further instruction to processing method provided by the invention, but not thereby limiting the invention.Employed stock oil is long residuum in embodiment and the Comparative Examples, and its character is listed in table 1.Embodiment is identical with employed hydrogenation catalyst in the Comparative Examples, being Dutch Aksu chemical company produces, trade names are RF-220 (Hydrodemetalation catalyst), RF-1000 (Hydrobon catalyst), two kinds of catalyzer of RF-220, RF-1000 are seated in reactor epimere and hypomere respectively, and the filling ratio is 40: 60 (volume ratio); Embodiment is identical with employed cracking catalyst in the Comparative Examples, is the catalyst plant production of Qilu Petrochemical company, and trade names are MLC-500.Processing method condition and test-results are listed in table 2, the calculating benchmark is a long residuum, wherein heavy oil refers to slurry oil and part recycle stock, and the yield of gasoline was hydrotreated naphtha and catalytically cracked gasoline yield sum during product amounted to, and the yield of diesel oil is hydrogenated diesel oil and catalytic cracking diesel oil yield sum.
Comparative Examples
Test is to carry out on the machinery of a conventional residual hydrogenation shown in Figure 2 and a cover heavy oil fluid catalytic cracking.
Long residuum enters hydrogenation unit, carries out hydrogenation reaction in the presence of hydrogen and hydrogenation catalyst, and reaction product isolated obtains gas, petroleum naphtha, hydrogenated diesel oil and hydrogenated residue; Hydrogenated residue enters heavy oil catalytically cracking equipment, carries out cracking reaction in the presence of catalyzer, and reaction product isolated obtains dry gas, liquefied gas, gasoline, diesel oil, recycle stock and slurry oil, and wherein recycle stock is back to catalytic cracking unit; Catalytically cracked oil is drawn from device, as producing oil fuel, acicular petroleum coke or sooty raw material.
Embodiment
Test is to carry out on residual hydrogenation shown in Figure 1-catalytic cracking combination process device.
Long residuum and clarified oil enter hydrogenation unit together, carry out hydrogenation reaction in the presence of hydrogen and hydrogenation catalyst, and reaction product isolated obtains gas, petroleum naphtha, hydrogenated diesel oil and hydrogenated residue; Hydrogenated residue enters heavy oil catalytically cracking equipment, carries out cracking reaction in the presence of catalyzer, and reaction product isolated obtains dry gas, liquefied gas, gasoline, diesel oil, recycle stock and slurry oil, and wherein recycle stock is back to catalytic cracking unit; A small amount of slurry oil " gets rid of outward " and goes out device, and most of slurry oil obtains clarified oil after separator is isolated the cracking catalyst powder, be back to hydrogenation unit.
The result shows, processing method scheme of the present invention compares with the processing method scheme of routine, dry gas and liquefied gas yield descend to some extent, and the gasoline of high value and diesel yield have increased by 1.20 and 4.73 percentage points respectively, and the heavy oil of low value has reduced by 5.22 percentage points.
Table 1
| The stock oil title | Long residuum | Clarified oil | Mixing oil * |
| Density (20 ℃), gram per centimeter 3 | ??0.9580 | ???1.018 | ?0.9622 |
| Viscosity (100 ℃), millimeter 2/ second | ????47.6 | ????20.1 | ???46.2 |
| Carbon residue, heavy % | ?????9.6 | ?????8.6 | ????9.6 |
| Carbon, heavy % | ???85.37 | ???90.16 | ??85.98 |
| Hydrogen, heavy % | ???11.27 | ????8.93 | ??11.03 |
| Sulphur, heavy % | ????2.90 | ????0.56 | ???2.60 |
| Nitrogen, heavy % | ????0.50 | ????0.35 | ???0.39 |
| Nickel, ppm | ????34.0 | ?????1.8 | ???33.6 |
| Vanadium, ppm | ???110.0 | ?????0.2 | ???99.8 |
| Iron, ppm | ?????6.7 | ?????0.8 | ????6.4 |
| Stable hydrocarbon, heavy % | ????30.7 | ????20.2 | ???30.3 |
| Aromatic hydrocarbons, heavy % | ????42.5 | ????57.0 | ???43.4 |
| Colloid, heavy % | ????23.7 | ????16.0 | ???23.0 |
| Bituminous matter (C 7Insolubles), heavy % | ?????3.1 | ?????6.8 | ????3.4 |
*: to be long residuum with clarified oil mixed by weight 10: 1 mixing oil obtains.
Table 2
| Embodiment | Comparative Examples | |
| Residual hydrocracking | ||
| Raw material is formed, heavy % | ||
| Long residuum | ????100 | ????100 |
| Clarified oil | ????10 | ????0 |
| The processing method condition | ||
| The hydrogen dividing potential drop, MPa | ????13.0 | ????13.0 |
| Temperature of reaction, ℃ | ????384.5 | ????384.5 |
| Volume space velocity, hour -1 | ????0.259 | ????0.235 |
| Hydrogen-oil ratio | ????800 | ????800 |
| Product distributes, heavy % | ||
| Gas | ????4.32 | ????3.99 |
| Petroleum naphtha | ????2.51 | ????1.54 |
| Hydrogenated diesel oil | ????16.10 | ????13.20 |
| Hydrogenated residue | ????88.22 | ????82.30 |
| Heavy oil fluid catalytic cracking | ||
| The processing method condition | ||
| Temperature of reaction, ℃ | ????515 | ????515 |
| Agent-oil ratio | ????5 | ????5 |
| Regeneration temperature, ℃ | ????680 | ????680 |
| Product distributes, heavy % | ||
| Dry gas | ????2.17 | ????2.31 |
| Liquefied gas | ????11.91 | ????12.56 |
| Gasoline | ????33.28 | ????33.04 |
| Diesel oil | ????13.07 | ????11.24 |
| Heavy oil | ????18.98 | ????14.20 |
| Coke | ????8.82 | ????8.95 |
| Product amounts to, heavy % | ||
| Dry gas | ????2.17 | ????2.31 |
| Liquefied gas | ????11.91 | ????12.56 |
| Gasoline | ????35.78 | ????34.58 |
| Diesel oil | ????29.17 | ????24.44 |
| Heavy oil | ????8.98 | ????14.20 |
Claims (6)
1, a kind of residual hydrocracking-catalytic cracking combination process comprises:
A, residual oil and clarified oil enter hydrotreater together, carry out hydrogenation reaction in the presence of hydrogen and hydrogenation catalyst;
B, gained hydrogenated residue enter catalytic cracking unit, carry out cracking reaction in the presence of cracking catalyst;
C, the clarified oil that is obtained by the separation of gained slurry oil return hydrogenation unit.
2,, it is characterized in that the residual oil described in the steps A is long residuum and/or vacuum residuum according to the processing method of claim 1.
3, according to the processing method of claim 1, it is characterized in that the catalyzer described in the steps A is a hydrogenation catalyst, its active metal component is selected from nickel-tungsten, nickel-tungsten-cobalt, nickel-molybdenum or cobalt-molybdenum, and carrier is selected from aluminum oxide, silicon-dioxide or amorphous aluminum silicide.
4, according to the processing method of claim 1, it is characterized in that the hydrogenation conditions described in the steps A is: hydrogen dividing potential drop 5.0～22.0 MPas, 330～450 ℃ of temperature of reaction, volume space velocity 0.1～3.0 hour
-1, hydrogen and stock oil volume ratio 350～2000.
5, according to the processing method of claim 4, it is characterized in that described stock oil is the mixture of residual oil and clarified oil, clarified oil accounts for 3～20 heavy % of residual oil.
6,, it is characterized in that the catalytic cracking unit described in the step B can be more than a cover or overlaps according to the processing method of claim 1.
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| CN 99100399 CN1119397C (en) | 1999-01-28 | 1999-01-28 | Hydrogenation and catalystic cracking combined process for residual oil |
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- 1999-01-28 CN CN 99100399 patent/CN1119397C/en not_active Expired - Lifetime
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