CN1076749C - Composite process for modulation thermal conversion and solvent deasphalting - Google Patents
Composite process for modulation thermal conversion and solvent deasphalting Download PDFInfo
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Abstract
The present invention relates to combination technology for modulation thermal conversion and solvent deasphalting. The directly distilled vacuum residue is moderated and thermally converted, reaction products are distilled and separated to prepare atmospheric residue of thermal conversion, and the atmospheric residue of thermal conversion and catalytic cracking slurry oil are mixed according to the weight ratio of 0 to 0.33: 1 to be used as solvent deasphalting raw oil. Paraffinic solvent with low molecules and the solvent deasphalting raw oil enter an extraction tower after being mixed according to the volume ratio of 3 to 12: 1, and carry out two sections or one section of solvent deasphalting under the subcritical condition or the supercritical condition of the solvent, and the solvent is circularly used after being recovered. Compared with the solvent deasphalting technology of the conventional vacuum residue, the combination technology has the advantages that the modified oil yield is increased by 10%.
Description
The present invention relates to a kind of combination process of heavy oil deep processing, more particularly, is to relax the combination process that these two kinds of heavy oil deep complete processings of thermal transition and solvent deasphalting organically combine.
The seventies rises, and solvent deasphalting has obtained to use more widely as a kind of processing means that catalytically cracked material is provided.But this technology because its heavy metal removing rate is lower, further develops it and is restricted when some poor residuums of processing (as triumph vacuum residuum).Solvent deasphalting only is a physical separating process, can't change the original distribution of residual oil heavy metal.Therefore,, can only take to reduce the approach of deasphalted oil yield, obtaining the low deasphalted oil of nickel content, thereby satisfy the specification of quality of downstream catalytic conversion process charging for the vacuum residuum that has contained a large amount of nickel compounds in the sort of soluble constituent.
Thermally splitting is a kind of important on-catalytic, the heavy oil upgrading technology of non-hydrogenation.Wherein the transformation efficiency of viscosity breaking is minimum, and yield of light oil is lower; The transformation efficiency of delayed coking is the highest, and yield of light oil is the highest, but a large amount of coke of while by-product.
Introduced the combined modifying process of a kind of HSC-ROSE (High conversion Soaker Cracking-Residue Oil Supercritical Extraction) of Japanese Toyo Engineering Corp. exploitation among the CN86102643A.This technology is at first carried out thermal transition with residual oil in the bottom is connected with the Soaker type reactor of overheated steam, invert point is between viscosity breaking and delayed coking, the thermal transition residual oil carries out solvent deasphalting again, the deasphalted oil of thermally splitting distillate and thermal transition residual oil is mixed into upgrading oil, as the raw material of downstream catalytic hydrocracking.The total liquid of this technology upgrading oil is received and is higher than delayed coking, accepts at identical liquid with the direct solvent diasphaltene and compares, and the heavy metal content of upgrading oil is lower.But a newly-built cover HSC plant investment is very big.
Introduced a kind of heavy oil lighting technology of Dutch Shell Internationale Research Maatschappij B.V exploitation among the CN1044116A.This technology is with after residual oil (＞520 ℃ of cuts the are at least 25%) preheating, carries out thermally splitting, and transformation efficiency (in＞520 ℃ of cuts) is at least 35%, and thermal cracking residue obtains deasphalted oil and pitch through solvent deasphalting.This method transformation efficiency improves, and does not also produce the problem of unsettled residual oil and periodical operation.But this method does not relate to the problem that removes of heavy metal, and the thermally splitting transformation efficiency improves, and causes the deasphalted oil degradation.
The objective of the invention is to provide on the basis of existing technology a kind of and can improve mitigation thermal transition-solvent deasphalting combination process that yield of light oil can improve the lightweight oil quality again.
Combination process provided by the invention is: straight run vacuum residuum is entered from thermal conversion reaction device bottom, is that 380～450 ℃, pressure are 0～0.5MPa, the residence time to be to relax thermal transition under the condition of 10～120min in temperature.Reacted logistics enters atmospheric distillation tower after extracting out from thermal conversion reaction device top, separates the thermal transition long residuum that obtains and mixes the stock oil of back as solvent deasphalting with catalytically cracked oil by weight 1: 0～0.33; The stock oil of low molecule alkane solvent and solvent deasphalting (hereinafter to be referred as agent-oil ratio) 3～12: 1 by volume enters extraction tower after mixing by static mixer, under the subcritical or super critical condition of solvent, carry out two sections solvent deasphaltings or one section solvent deasphalting, recycle after the solvent recuperation.
Combination process provided by the invention is so concrete enforcement: straight run vacuum residuum is entered from thermal conversion reaction device bottom, in temperature is 380～450 ℃, being preferably 385～430 ℃, pressure is 0～0.5MPa, being preferably 0.3～0.4MPa, the residence time is 10～120min, is preferably under the condition of 20～40min to relax thermal transition.Reacted logistics enters atmospheric distillation tower after extracting out from thermal conversion reaction device top, separates obtaining reacted gas, raw gasline, gas oil and thermal transition long residuum.The thermal transition long residuum mixes the stock oil of back as solvent deasphalting with catalytically cracked oil by weight 1: 0～0.33.The stock oil of low molecule alkane solvent and solvent deasphalting by volume 3～12: 1, be preferably 6～8: 1 by entering extraction tower after the static mixer mixing, under the subcritical or super critical condition of solvent, carry out two sections solvent deasphaltings or one section solvent deasphalting, recycle after the solvent recuperation.
The content of nickel and vanadium is higher than 30ppm in the straight run vacuum residuum heavy metal used in the present invention.Raw gasline, gas oil that thermal transition obtains go hydrofining.
The employed low molecule alkane solvent of extracting part is selected from a kind of or two or more mixture wherein among propane, Trimethylmethane, normal butane, the Skellysolve A in the solvent deasphalting technology.
Under the undercritical conditions of solvent, carry out extracting, be meant that service temperature and pressure are lower than the critical temperature and the emergent pressure of solvent respectively.Under the super critical condition of solvent, carry out extracting, be meant that service temperature and pressure are higher than the critical temperature and the emergent pressure of solvent respectively.
Two sections solvent deasphaltings are meant that ejecting the light phase solution of solvent that contains that comes from extraction tower enters the sedimentation tower, after deasphalted oil solution is extracted out from the sedimentation top of tower, by entering the deasphalted oil recovery tower behind the topping-up pump, operate under the critical or super critical condition of solvent, the deasphalted oil solution that contains a small amount of solvent at the bottom of the tower passes through and obtains deasphalted oil after the flash distillation stripping further reclaims solvent; The de-oiled asphalt solution that comes out from extraction tower, sedimentation tower bottom, hydrosol obtain de-oiled asphalt, colloid respectively after reclaiming solvent through the flash distillation stripping respectively; Solvent cycle is used.In two sections solvent deasphaltings, the working pressure of sedimentation tower is identical with the working pressure of extraction tower, and the service temperature of sedimentation tower is higher 5～20 ℃ than the service temperature of extraction tower.
One section solvent deasphalting is meant that ejecting the solvent deasphalting oil solution that contains that comes from extraction tower enters the deasphalted oil recovery tower after by topping-up pump, operate under the critical or super critical condition of solvent, the deasphalted oil solution that contains a small amount of solvent at the bottom of the tower passes through and obtains deasphalted oil after the flash distillation stripping further reclaims solvent; The de-oiled asphalt solution that comes out from the extraction tower bottom passes through and obtains de-oiled asphalt after the flash distillation stripping reclaims solvent; Solvent cycle is used.
Deasphalted oil solution among the present invention can carry out solvent recuperation under the critical condition of solvent, promptly the service temperature of deasphalted oil recovery tower and pressure equal the critical temperature and the emergent pressure of solvent respectively; Deasphalted oil solution also can carry out solvent recuperation under the super critical condition of solvent, promptly the service temperature of deasphalted oil recovery tower and pressure are higher than the critical temperature and the emergent pressure of solvent respectively.
Below in conjunction with accompanying drawing combination process provided by the present invention is given further instruction.
Accompanying drawing 1 illustrates the flow process of mitigation thermal transition-two section solvent deasphalting combination process.
Straight run vacuum residuum enters through the bottom of pipeline [1] from thermal conversion reaction device [2], and reacted logistics enters atmospheric distillation tower [4] after extracting out from thermal conversion reaction device [2] top, separates obtaining reacted gas, raw gasline, gas oil and thermal transition long residuum.The thermal transition long residuum of atmospheric distillation tower [4] bottom through pipeline [5] with after catalytically cracked oil from pipeline [6] mixes by a certain percentage, enter static mixer [8] by raw oil pump [7] together, low molecule alkane solvent from recovery system enters static mixer [8] through pipeline [26] simultaneously, the two enters extraction tower [9] after according to certain mixed, under the subcritical or super critical condition of solvent, carry out extracting, the light phase solution of solvent that contains of cat head enters sedimentation tower [12] through pipeline [10], after the deasphalted oil solution that obtains after the sedimentation is extracted out from sedimentation tower [12] top, enter deasphalted oil recovery tower [14] by topping-up pump [13], under the critical or super critical condition of solvent, operate, the solvent of cat head is through pipeline [17], [26] turn back to static mixer [8], the deasphalted oil solution that contains a small amount of solvent at the bottom of the tower enters deasphalted oil flash steam stripper [16] through pipeline [15], obtains deasphalted oil at the bottom of the tower behind the recovery solvent.The hydrosol that obtains after the sedimentation enters colloid flash steam stripper [20] through pipeline [19] after extracting out from sedimentation tower [12] bottom, obtains colloid at the bottom of the tower behind the recovery solvent.The de-oiled asphalt heavy phase solution of extraction tower [9] bottom enters de-oiled asphalt flash steam stripper [23] through pipeline [22], obtains de-oiled asphalt at the bottom of the tower behind the recovery solvent.The solvent at deasphalted oil flash steam stripper [16], colloid flash steam stripper [20] and de-oiled asphalt flash steam stripper [23] top boosts by solvent pump [25] together after pipeline [26] turns back to static mixer [8] recycles respectively after pipeline [18], [21] and [24] are converged.
Accompanying drawing 2 illustrates the flow process of mitigation thermal transition-section solvent deasphalting combination process.
Straight run vacuum residuum enters through the bottom of pipeline [1] from thermal conversion reaction device [2], and reacted logistics enters atmospheric distillation tower [4] after extracting out from thermal conversion reaction device [2] top, separates obtaining reacted gas, raw gasline, gas oil and thermal transition long residuum.The thermal transition long residuum of atmospheric distillation tower [4] bottom through pipeline [5] with after catalytically cracked oil from pipeline [6] mixes by a certain percentage, enter static mixer [8] by raw oil pump [7] together, low molecule alkane solvent from recovery system enters static mixer [8] through pipeline [26] simultaneously, the two enters extraction tower [9] after according to certain mixed, under the subcritical or super critical condition of solvent, carry out extracting, the solvent-laden deasphalted oil solution of cat head enters deasphalted oil recovery tower [14] through pipeline [10] by topping-up pump [13], under the critical or super critical condition of solvent, operate, the solvent of cat head is through pipeline [17], [26] turn back to static mixer [8], the deasphalted oil solution that contains a small amount of solvent at the bottom of the tower enters deasphalted oil flash steam stripper [16] through pipeline [15], obtains deasphalted oil at the bottom of the tower behind the recovery solvent.The de-oiled asphalt solution of extraction tower [9] bottom enters de-oiled asphalt flash steam stripper [23] through pipeline [22], obtains de-oiled asphalt at the bottom of the tower behind the recovery solvent.The solvent at deasphalted oil flash steam stripper [16] and de-oiled asphalt flash steam stripper [23] top boosts by solvent pump [25] together after pipeline [26] turns back to static mixer [8] recycles respectively after pipeline [18] and pipeline [24] converge.
The difference of two sections solvent deasphaltings and one section solvent deasphalting is that extraction tower and sedimentation tower two towers are partly used in the extracting of two sections flow processs, and the many colloid flash steam strippers of recovery part obtain deasphalted oil, colloid and three kinds of products of de-oiled asphalt; And the extracting of one section flow process part is only used tower of extraction tower, obtains two kinds of products of deasphalted oil and de-oiled asphalt.
Major advantage of the present invention is: straight run vacuum residuum is after relaxing thermal transition, the thermal transition long residuum is when solvent deasphalting, its deasphalted oil yield is apparently higher than independent vacuum residuum solvent deasphalting, add thermal transition distillate part, total upgrading oil yield increases about 10 percentage points.The nickel content of deasphalted oil all is lower than 10ppm.This process makes full use refinery conventional device is optimized combination, does not need to increase big equipment, invests lessly, and smooth operation is adjusted processing ease.Deasphalted oil both can be used as catalytically cracked material, also can be used as the raw material of hydrocracking, can also be as the thermally splitting raw material of lube stock or various severities.De-oiled asphalt both can be used as the raw material of road bitumen, also can be used as the raw material of emulsion fuel, can also produce synthetic gas as gasified raw material.Colloid can be used for blendedfuel oil, also can be used as the blending component of road bitumen.
Accompanying drawing is the schematic flow sheet that relaxes thermal transition one solvent deasphalting combination process.
Accompanying drawing 1 illustrates the flow process of mitigation thermal transition-two section solvent deasphalting combination process.
Accompanying drawing 2 illustrates the flow process of mitigation thermal transition-section solvent deasphalting combination process.
Each numbering is described as follows in accompanying drawing 1 and the accompanying drawing 2:
[1], pipeline is all represented in [3], [5], [6], [10], [11], [15], [17], [18], [19], [21], [22], [24], [26]; [7] represent raw oil pump, [13] represent topping-up pump, and [25] represent solvent pump; [2] represent the thermal conversion reaction device; [4] represent atmospheric distillation tower; [8] represent static mixer; [9] represent extraction tower; [12] represent the sedimentation tower; [14] represent the deasphalted oil recovery tower; [16] represent deasphalted oil flash steam stripper; [20] represent colloid flash steam stripper; [23] represent de-oiled asphalt flash steam stripper.
Below in conjunction with embodiment the present invention is given further instruction, but not thereby limiting the invention.
The used straight run vacuum residuum and the main character of catalytically cracked oil are listed in table 1 in embodiment and the Comparative Examples, and propane and butane solvent all are taken from full scale plant.Data in embodiment and the Comparative Examples are listed in table 2, table 3 and table 4.
Nickel content is that the vacuum residuum A of 100ppm enters from thermal conversion reaction device bottom, is that 405 ℃, pressure are 0.38MPa, the residence time to be to relax thermal transition under the condition of 25min in temperature.Reacted logistics enters atmospheric distillation tower after extracting out from thermal conversion reaction device top, separates obtaining reacted gas, raw gasline, gas oil and thermal transition long residuum.From the propane solvent of recovery system with mix by static mixer from the thermal transition long residuum of air distillation tower bottom 8: 1 by volume after enter extraction tower, in the extraction tower temperature is that 68/46 ℃ (at the bottom of cat head/tower), pressure are extracting under the 4.0MPa condition, obtain solvent-laden light phase solution and heavy phase solution, light phase solution obtains solvent-laden deasphalted oil solution and hydrosol after separating through the sedimentation tower, and the service temperature of sedimentation tower is that 86/51 ℃ (at the bottom of cat head/tower), pressure are 4.0MPa.Deasphalted oil solution obtains deasphalted oil through critical recovery, flash distillation stripping after reclaiming solvent, and hydrosol, de-oiled asphalt heavy phase solution obtain colloid, de-oiled asphalt after reclaiming solvent through the flash distillation stripping respectively, recycle after the solvent recuperation.The deasphalted oil yield that obtains accounts for the 30m% of diasphaltene raw material, and its carbon residue is 1.2m%, and nickel content is 0.6ppm.The total recovery of upgrading oil, i.e. the raw gasline of deasphalted oil and thermal transition, gas oil yield sum account for the 32m% of vacuum residuum A.
Comparative Examples 1
As different from Example 1, vacuum residuum A is without relaxing thermal transition, but only carries out solvent deasphalting.Propane solvent and vacuum residuum A 8: 1 by volume enter extraction tower after mixing by static mixer, are that 67/45 ℃ (at the bottom of cat head/tower), sedimentation tower temperature are that 85/50 ℃ (at the bottom of cat head/tower), pressure are 4.0MPa in the extraction tower temperature.Pressure is extracting under the 4.0MPa condition, and the solvent in the deasphalted oil solution recycles after the solvent recuperation by critical recovery.The deasphalted oil yield that obtains accounts for the 19m% of diasphaltene raw material, and its carbon residue is 1.1m%, and nickel content is 0.9ppm.The deasphalted oil yield is than low 13 percentage points of upgrading oil total recovery among the embodiment 1.
Nickel content is that the vacuum residuum B of 46.7ppm enters from thermal conversion reaction device bottom, is that 425 ℃, pressure are 0.4MPa, the residence time to be to relax thermal transition under the condition of 30min in temperature.Reacted logistics enters atmospheric distillation tower after extracting out from thermal conversion reaction device top, separates obtaining reacted gas, raw gasline, gas oil and thermal transition long residuum.Butane solvent (normal butane and Trimethylmethane mol ratio are 1: 1) with from the thermal transition long residuum of air distillation tower bottom 5: 1 by volume, by entering extraction tower after the static mixer mixing, in the extraction tower temperature is that 145/125 ℃ (at the bottom of cat head/tower), pressure are extracting under the 4.0MPa condition, obtain solvent-laden deasphalted oil solution and de-oiled asphalt solution, the solvent in the deasphalted oil solution is by supercritical recovery.The deasphalted oil yield that obtains accounts for the 66m% of diasphaltene raw material, and its carbon residue is 3.7m%, and nickel content is 7.4ppm.The total recovery of upgrading oil, i.e. the raw gasline of deasphalted oil and thermal transition, gas oil yield sum account for the 70m% of vacuum residuum B.
Comparative Examples 2
As different from Example 2, vacuum residuum B is without relaxing thermal transition, but only carries out solvent deasphalting.Butane solvent (normal butane and Trimethylmethane mol ratio are 1: 1) and vacuum residuum B 8: 1 by volume, by entering extraction tower after the static mixer mixing, in the extraction tower temperature is that 145/125 ℃ (at the bottom of cat head/tower), pressure are extracting under the 4.0MPa condition, what obtain contains light phase solution of solvent and heavy phase solution, obtain deasphalted oil and de-oiled asphalt through solvent recuperation respectively, recycle after the solvent recuperation.The deasphalted oil yield that obtains accounts for the 60m% of diasphaltene raw material, and its carbon residue is 3.2m%, and nickel content is 7.2ppm.The deasphalted oil yield is than low 9 percentage points of upgrading oil total recovery among the embodiment 2.
Nickel content is that the vacuum residuum A of 100ppm enters from thermal conversion reaction device bottom, is that 410 ℃, pressure are 0.38MPa, the residence time to be to relax thermal transition under the condition of 25min in temperature.Reacted logistics enters atmospheric distillation tower after extracting out from thermal conversion reaction device top, separates obtaining reacted gas, raw gasline, gas oil and thermal transition long residuum.Catalytically cracked oil mixes the stock oil of back as solvent deasphalting with the thermal transition long residuum with weight ratio at 0.25: 1, from the stock oil of the propane solvent of recovery system and solvent deasphalting 8: 1 by volume, by entering extraction tower after the static mixer mixing, in the extraction tower temperature is that 60/45 ℃ (at the bottom of cat head/tower), pressure are extracting under the 4.0MPa condition, what obtain contains light phase solution of solvent and heavy phase solution, obtain deasphalted oil and de-oiled asphalt through solvent recuperation respectively, recycle after the solvent recuperation.The deasphalted oil yield that obtains accounts for the 45m% of straight run vacuum residuum and catalytically cracked oil sum, and its carbon residue is 2.2m%, and nickel content is 6.6ppm.The total recovery of upgrading oil, i.e. the raw gasline of deasphalted oil and thermal transition, gas oil yield sum account for the 50m% of vacuum residuum A and catalytically cracked oil sum.
Comparative Examples 3
Vacuum residuum A and catalytically cracked oil mix stock oil as solvent deasphalting with weight ratio at 4: 1, the stock oil of propane solvent and solvent deasphalting 8: 1 by volume, by entering extraction tower after the static mixer mixing, in the extraction tower temperature is that 57/42 ℃ (at the bottom of cat head/tower), pressure are extracting under the 4.0MPa condition, what obtain contains light phase solution of solvent and heavy phase solution, obtain deasphalted oil and de-oiled asphalt through solvent recuperation respectively, recycle after the solvent recuperation.The deasphalted oil yield that obtains accounts for the 40m% of vacuum residuum A and catalytically cracked oil sum, and its carbon residue is 2.5m%, and nickel content is 9.0ppm.The deasphalted oil yield is than low 10 percentage points of upgrading oil total recovery among the embodiment 3.
Table 1
| Material name | Vacuum residuum A | Catalytically cracked oil | Vacuum residuum B |
| Density (20 ℃), g/cm 3Viscosity (100 ℃), mm 2Carbon residue; The m% heavy metal; Ppm Ni V Fe Cu element; M% C H S N H/C (atomic ratio) four components, saturated part of fragrance part gum asphalt of m% | 0.9881 2396.0 18.46 100 1.5 25.6 ＜0.1 86.82 11.79 0.43 0.76 1.63 19.2 34.2 44.3 2.3 | 1.0019 17.61 3.27 0.2 ＜0.1 3.6 ＜0.1 88.59 10.00 0.30 0.20 1.35 48.5 40.4 11.1 - | 0.9679 44.48 14.31 46.7 2.7 19.1 ＜0.1 86.72 11.47 1.08 0.83 1.59 28.8 34.5 35.2 1.5 |
Table 2
| Relax thermal transition part operation conditional operation temperature, ℃ working pressure, the MPa residence time, the min product distributes, the normal slag propane deasphalting part of m% reacted gas raw gasline and gas oil thermal transition (two sections flow processs) operational condition agent-oil ratio, v/v extraction temperature (at the bottom of cat head/tower), ℃ extracting pressure, MPa settling temperature (at the bottom of cat head/tower), ℃ deasphalted oil recovery tower temperature, ℃ deasphalted oil recovery tower pressure, MPa product yield and character deasphalted oil yield, m% colloid yield, m% de-oiled asphalt yield, m% deasphalted oil carbon residue, m% deasphalted oil nickel content, total (accounting for raw material), the m% of receiving of ppm upgrading | Embodiment | 1 405 0.38 25 14 95 8: 1 68,/46 4.0 86,/51 96 4.2 30 10 60 1.2 0.6 32 | Comparative Examples 1------8: 1 67,/45 4.0 85,/50 96 4.2 19 15 66 1.1 0.9 19 |
Table 3
| Relax thermal transition part operation conditional operation temperature, ℃ working pressure, the MPa residence time, the min product distributes, the normal slag butane deasphalting part of m% reacted gas raw gasline and gas oil thermal transition (one section flow process) operational condition agent-oil ratio, v/v extraction temperature (at the bottom of cat head/tower), ℃ extracting pressure, MPa deasphalted oil recovery tower temperature, ℃ deasphalted oil recovery tower pressure, MPa product yield and character deasphalted oil yield, m% de-oiled asphalt yield, m% deasphalted oil carbon residue, m% deasphalted oil nickel content, total (accounting for raw material), the m% of receiving of ppm upgrading | Embodiment | 2 425 0.40 30 2 13 85 5: 1 1,45/,125 4.0 180 5.0 66 34 3.7 7.4 69 | Comparative Examples 2------5: 1 1,45/,125 4.0 180 5.0 60 40 3.2 7.2 60 |
Table 4
| Relax thermal transition part operation conditional operation temperature, ℃ working pressure, the MPa residence time, min product distribution (accounting for straight run vacuum residuum), the normal slag propane deasphalting part of m% reacted gas raw gasline and gas oil thermal transition (one section flow process) operational condition agent-oil ratio, v/v extraction temperature (at the bottom of cat head/tower), ℃ extracting pressure, MPa deasphalted oil recovery tower temperature, ℃ deasphalted oil recovery tower pressure, the MPa product yield, m% (accounting for straight run vacuum residuum and catalytically cracked oil sum) deasphalted oil de-oiled asphalt deasphalted oil carbon residue, m% deasphalted oil nickel content, ppm upgrading oil is total receives m% (accounting for straight run vacuum residuum and catalytically cracked oil sum) | | Comparative Examples 3------8: 1 57,/42 4.0 96 4.2 40 60 2.5 9.0 40 |
Claims (9)
1, a kind of mitigation thermal transition-solvent deasphalting combination process, it is characterized in that making straight run vacuum residuum to enter from thermal conversion reaction device bottom, is that 380～450 ℃, pressure are 0～0.5MPa, the residence time to be to relax thermal transition under the condition of 10～120min in temperature; Reacted logistics enters atmospheric distillation tower after extracting out from thermal conversion reaction device top, separates the thermal transition long residuum that obtains and mixes the stock oil of back as solvent deasphalting with catalytically cracked oil by weight 1: 0～0.33; Be selected among propane, Trimethylmethane, normal butane, the Skellysolve A a kind of or wherein two or more mixture by static mixer mix after enter extraction tower at 3～12: 1 by volume as the stock oil of solvent and solvent deasphalting, under the subcritical or super critical condition of solvent, carry out two sections solvent deasphaltings or one section solvent deasphalting, recycle after the solvent recuperation.
2,, it is characterized in that the content of nickel and vanadium is higher than 30ppm in the straight run vacuum residuum heavy metal by the described combination process of claim 1.
3, by the described combination process of claim 1, it is characterized in that relaxing thermal transition temperature and be 385～430 ℃, pressure is that 0.3～0.4MPa, the residence time are 20～40min.
4,, it is characterized in that the volume ratio of the raw material of low molecule alkane solvent and solvent deasphalting is 6～8: 1 by the described combination process of claim 1.
5, by the described combination process of claim 1, the undercritical conditions that it is characterized in that solvent is meant that service temperature and pressure are lower than the critical temperature and the emergent pressure of solvent respectively, and the super critical condition of solvent is meant that service temperature and pressure are higher than the critical temperature and the emergent pressure of solvent respectively.
6, by the described combination process of claim 1, it is characterized in that two sections solvent deasphaltings are meant that ejecting the light phase solution of solvent that contains that comes from extraction tower enters the sedimentation tower, after deasphalted oil solution is extracted out from the sedimentation top of tower, by entering the deasphalted oil recovery tower behind the topping-up pump, operate under the critical or super critical condition of solvent, the deasphalted oil solution that contains a small amount of solvent at the bottom of the tower passes through and obtains deasphalted oil after the flash distillation stripping further reclaims solvent; The de-oiled asphalt solution that comes out from extraction tower, sedimentation tower bottom, hydrosol obtain de-oiled asphalt, colloid respectively after reclaiming solvent through the flash distillation stripping respectively.
7, by the described combination process of claim 6, it is characterized in that the working pressure of sedimentation tower is identical with the working pressure of extraction tower, the service temperature of sedimentation tower is higher 5～20 ℃ than the service temperature of extraction tower.
8, by the described combination process of claim 1, it is characterized in that one section solvent deasphalting is meant that ejecting the solvent deasphalting oil solution that contains that comes from extraction tower enters the deasphalted oil recovery tower after by topping-up pump, operate under the critical or super critical condition of solvent, the deasphalted oil solution that contains a small amount of solvent at the bottom of the tower passes through and obtains deasphalted oil after the flash distillation stripping further reclaims solvent; The de-oiled asphalt solution that comes out from the extraction tower bottom passes through and obtains de-oiled asphalt after the flash distillation stripping reclaims solvent.
9, by claim 6 or 8 described combination procesies, it is characterized in that deasphalted oil solution can carry out solvent recuperation under the critical condition of solvent, promptly the service temperature of deasphalted oil recovery tower and pressure equal the critical temperature and the emergent pressure of solvent respectively; Deasphalted oil solution also can carry out solvent recuperation under the super critical condition of solvent, promptly the service temperature of deasphalted oil recovery tower and pressure are higher than the critical temperature and the emergent pressure of solvent respectively.
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| US8152994B2 (en) * | 2007-12-27 | 2012-04-10 | Kellogg Brown & Root Llc | Process for upgrading atmospheric residues |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN86102643A (en) * | 1985-05-13 | 1986-11-12 | 东洋工程株式会社 | The treating processes of heavy oil residue |
| CN1044116A (en) * | 1988-12-05 | 1990-07-25 | 国际壳牌研究有限公司 | The method of conversion of heavy hydrocar-bonaccous feedstock |
-
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN86102643A (en) * | 1985-05-13 | 1986-11-12 | 东洋工程株式会社 | The treating processes of heavy oil residue |
| CN1044116A (en) * | 1988-12-05 | 1990-07-25 | 国际壳牌研究有限公司 | The method of conversion of heavy hydrocar-bonaccous feedstock |
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| CN1233644A (en) | 1999-11-03 |
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