CN101463267B - Viscosity breaking method - Google Patents
Viscosity breaking method Download PDFInfo
- Publication number
- CN101463267B CN101463267B CN 200710303928 CN200710303928A CN101463267B CN 101463267 B CN101463267 B CN 101463267B CN 200710303928 CN200710303928 CN 200710303928 CN 200710303928 A CN200710303928 A CN 200710303928A CN 101463267 B CN101463267 B CN 101463267B
- Authority
- CN
- China
- Prior art keywords
- viscosity breaking
- viscosity
- vacuum
- breaking
- temperature
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a visbreaking method, comprising the steps of: under the condition of reduced pressure distillation, distilling the visbreaking raw materials under the reduced pressure to acquire a reduced distillate oil and vacuum residue having cutting temperature not less than 540 DEG C; subjecting visbreaking the reduced distillate oil under the condition of the visbreaking, mixing the product of the reduced distillate oil experiencing the visbreaking with the vacuum residue to acquire a mixed oil; visbreaking the mixed oil at the bottom of a visbreaking fractionating tower and acquiring gas, naphtha and visbreaking residue by means of fractionation; and causing the temperature of the reduced distillate oil for the visbreaking to be higher than that of the mixed oil for the visbreaking. By applying the visbreaking method provided by the invention, visbreaking conversion rate can be enhanced; meanwhile the visbreaking residue can be reduced in viscosity and is excellent in stability.
Description
Technical field
The present invention relates to a kind of viscosity breaking method.
Background technology
Viscosity breaking is a heavy oil mild heat conversion process, and its purpose mainly is to reduce the viscosity and the pour point of heavy oil, makes it to mix less or does not mix lightweight oil and obtain proper fuel oil, or supply raw materials for the further lighting of heavy oil.Viscosity breaking is because technology is simple, less investment, profitable, and existing still is one of important means of heavy oil upgrading.The raw material of viscosity breaking mainly is a vacuum residuum, and also available topped crude, long residuum and heavy crude are as raw material.The viscosity breaking product mainly is viscosity breaking gas, petroleum naphtha and residual oil, and visbreaking residue further underpressure distillation goes out viscosity breaking vacuum distillate and viscosity breaking vacuum residuum.
Usually between 380-490 ℃, pressure is 0.3-1.0MPa to the temperature of reaction of viscosity breaking, and the reaction times is that several minutes is to dozens of minutes.According to the difference of viscosity breaking adopting process, be divided into boiler tube formula viscosity breaking (Furnace Tube Visbreaking) and the cracking of reaction tower visbreaking (Furnace ColumnVisbreaking).
The pyrolytic cracking of boiler tube formula viscosity breaking conversion process is reflected in the reaction boiler tube of process furnace and carries out, and heater outlet temperature maintains about 485 ℃, and temperature of reaction is high, the residence time short (about 1-3min).Boiler tube formula viscosity breaking flow process is made up of a process furnace and a separation column basically.When raw material passes through process furnace, cracking reaction takes place in boiler tube, effusive liquid stream is fractionated into various distillate products, like gas, petroleum naphtha, gas oil and visbroken resids then through chilling in separation column from boiler tube.
The reaction soaker visbreaking is that the furnace outlet material is introduced reaction tower, in reaction tower, stops tens to dozens of minutes, most viscosity breakings is reflected in the visbreaking reaction tower carries out.Though the reaction soaker visbreaking also has certain cracking reaction in furnace tubing, most of cracking reaction is carried out in reaction tower.Compare with the viscosity breaking of boiler tube formula, reaction soaker visbreaking temperature of reaction is low, the residence time is long, but resulting each product yield and character and the viscosity breaking of process furnace formula are basic identical under same conversion.
Early stage reaction tower designs for downflow system, and on-stream time is short, and the interior coking of reaction tower is comparatively serious, and the coke cleaning of reaction tower then needs artificial decoking, takes very much manpower and time.Particularly when handling heavy, vacuum residuum feed inferior, operation easier is big.Therefore reacting soaker visbreaking is restricted.For addressing the above problem, shell (Shell) company has developed upflowing reaction tower viscosity breaking SSV (Shell SoakerVisbreaking) technology.Because the viscosity breaking of upflowing reaction tower has reduced furnace temperature, has prolonged the reaction times, thereby has reached under the situation of same depth of conversion, coking phenomenon greatly reduces in boiler tube and the reaction tower, and the operational cycle prolongs greatly, has improved the drawback of downflow system reaction tower.But for certain raw material, the depth of conversion of viscosity breaking has certain limit; Surpass this limit, visbreaking residue can satisfy not the requirement of visbroken resids stability owing to sediment appears in phase-splitting; If further deepen again to transform, just can cause coking, device can not be run well.
The viscosity breaking degree of depth is represented that by the viscosity breaking transformation efficiency viscosity breaking transformation efficiency equals viscosity breaking gas weight yield and adds less than 165 ℃ of viscosity breaking petroleum naphtha weight yields.The viscosity breaking transformation efficiency is high more, and the viscosity breaking degree of depth is dark more, and visbroken resids viscosity is more little, but the visbroken resids stability is poor more.The visbreaking residue stability can be measured by ASTM D4740 residual fuel oil detergency and consistency spot test method.This method is measured the result stability is divided into 5 numbers; No. 1 expression detergency and consistency are fine, and No. 2 expression detergency and consistency are better, represent that detergency and consistency are relatively poor for No. 3; No. 4 expression detergency and consistency are poor, represent that detergency and consistency are very poor for No. 5.When producing oil fuel, control stability and be not more than No. 2.Therefore the viscosity breaking operation will improve the viscosity breaking degree of depth as far as possible under the prerequisite that guarantees visbroken resids stability qualified (stability is not more than No. 2), reduces the viscosity of visbreaking residue.
In order to improve the stability that the viscosity breaking degree of depth can guarantee visbroken resids again, the someone does a lot of work.
CN1038120A discloses a kind of method that makes thickness raw material upgrading, and this method comprises: producing under the degree of depth of shell (oil company) heat filtering value greater than 0.25 viscosity breaking product, carry out viscosity breaking to a kind of sticky material; At least handle a part of viscosity breaking product; With isolate be no more than 650
that are processedheavy phase of (being roughly equal to 343 ℃) above viscosity breaking product weight 15%; Handling separation viscosity breaking product is in order to reduce shell (oil company) heat filtering value, to be at least 0.25 so that separate shell (oil company) the heat filtering value of back remainder; At least be recycled to viscosity breaking to this remainder of a part.This method is owing to looping back viscosity breaking plant after 15% heavies removal in the viscosity breaking product, therefore can improve the viscosity breaking degree of depth under the prerequisite that guarantees non-scaling and coking.But this method need be built SX and retrieving arrangement, needs bigger investment and process cost.
US4454023 discloses a kind of improving one's methods heavy viscous hydrocarbon upgrading; This method is included in the viscosity breaking process furnace that has or do not have soaking drum the viscosity breaking of heavy viscous hydrocarbon; The product that fractionation is come out from the viscosity breaking process furnace in distilation steps; And in solvent extraction with solvent treatment from the last running of distilation steps forming two kinds or more kinds of cut, these two kinds or more kinds of cut comprise and contain most of bitum last running and contain most of colloid and one or more lighting ends of oil; This improvement comprises at least a portion that contains the colloid lighting end from the solvent extraction step and the heavy viscous hydrocarbon bonded step of carrying out viscosity breaking, has increased gum level thus, and from this process, reclaims lighting end to form one or more upgraded products may.In the method, owing to, therefore can under the prerequisite that guarantees non-scaling and noncoking, improve the viscosity breaking degree of depth with looping back viscosity breaking plant after the viscosity breaking product asphaltene removal.But should invention need to build SX and retrieving arrangement, need bigger investment and process cost.
US4428824 discloses and has a kind ofly produced improving one's methods of oil fuel by residual oil raw material, and this method is made up of following steps: solvent deasphalting is carried out with said residual oil raw material in (1), with production deasphalted oil and de-oiled asphalt; (2) the said deasphalted oil of viscosity breaking; (3) said pitch remix is gone into the deasphalted oil after the said viscosity breaking; And mix the product of step (3) (4) again with distillate.But adopt the visbroken resids of the method production good security that this invention provides, but de-oiled asphalt is not through viscosity breaking, so the viscosity of viscosity breaking product is still higher.
Summary of the invention
The objective of the invention is to overcome the higher defective of viscosity of viscosity breaking product in the above-mentioned prior art, a kind of viscosity breaking method than LV viscosity breaking product is provided.
The invention provides a kind of viscosity breaking method, this method is included under the condition of underpressure distillation, and the viscosity breaking raw material is carried out underpressure distillation, obtains the vacuum residuum that vacuum distillate and cutting temperature are not less than 540 ℃; Said vacuum distillate is carried out viscosity breaking under the condition of viscosity breaking; Product after the vacuum distillate viscosity breaking is mixed with said vacuum residuum; Obtain mixing oil; Said mixing oil is carried out viscosity breaking at the bottom of viscosity breaking fractionation Tata, and fractionation obtains gas, petroleum naphtha and visbreaking residue, the temperature of said vacuum distillate being carried out viscosity breaking is higher than the temperature of said mixing oil being carried out viscosity breaking.
According to viscosity breaking method provided by the invention, can reduce the viscosity of viscosity breaking product effectively, therefore for given raw material, the viscosity of the resulting viscosity breaking product of employing the present invention can be lower than the viscosity of conventional viscosity breaking product.Thereby when producing oil fuel, can mix or not mix lightweight oil less, practice thrift the cost of producing oil fuel.
In addition; Adopt method provided by the invention can improve the degree of depth of viscosity breaking; I.e. under the prerequisite that allows the visbroken resids stability (ASTM D4740 measures the result and is not higher than No. 2), viscosity breaking gas and viscosity breaking naphtha yield increase, and visbroken resids viscosity reduces.Simultaneously; In the method for the invention; The viscosity breaking raw material is carried out underpressure distillation earlier, and vacuum distillate carries out the high temperature viscosity breaking earlier in the viscosity breaking boiler tube, and the vacuum residuum that after distillation, obtains again then carries out the low temperature viscosity breaking at the bottom of separation column; Only carry out a low temperature viscosity breaking and contain higher bitum vacuum residuum; Therefore the viscosity breaking transformation efficiency is than the height of conventional viscosity breaking, and the visbroken resids stability is better than conventional visbroken resids, can not cause the delay coking heating furnace tube coking when being used for the raw material of delayed coking unit.
For the high raw material of asphalt content, adopt method of the present invention can improve the viscosity breaking degree of depth, obtain the lower and better visbroken resids of stability of viscosity, produce the HFO that satisfies the oil fuel standard.In addition, surging along with crude oil price, the exploitation of heavy inferior crude oil more and more comes into one's own in the world wide, but heavy crude density is big, viscosity is high, is difficult to carry after exploitation is come out.Adopt viscosity breaking technology of the present invention, can reduce the viscosity of heavy crude significantly, reach the requirement of crude oil exporting, can guarantee that again the synthetic crude of producing after the viscosity breaking has stability preferably.
Description of drawings
Fig. 1 is the schema of viscosity breaking method of the present invention.
Embodiment
Viscosity breaking method provided by the invention comprises, under the condition of underpressure distillation, the viscosity breaking raw material is carried out underpressure distillation, obtains the vacuum residuum that vacuum distillate and cutting temperature are not less than 540 ℃; Said vacuum distillate is carried out viscosity breaking under the condition of viscosity breaking; Product after the vacuum distillate viscosity breaking is mixed with said vacuum residuum; Obtain mixing oil; Said mixing oil is carried out viscosity breaking at the bottom of viscosity breaking fractionation Tata, and fractionation obtains gas, petroleum naphtha and visbreaking residue, the temperature of said vacuum distillate being carried out viscosity breaking is higher than the temperature of said mixing oil being carried out viscosity breaking.
According to method provided by the invention, under preferable case, the temperature that said vacuum distillate is carried out viscosity breaking is than said mixing oil being carried out the high 30-120 of temperature ℃ of viscosity breaking, preferred 45-100 ℃.
In the present invention, for the viscosity breaking of boiler tube formula, when promptly in process furnace, carrying out viscosity breaking, the viscosity breaking temperature is meant the temperature of viscosity breaking material at furnace outlet; For the viscosity breaking of carrying out at the bottom of the fractionation Tata, the viscosity breaking temperature is meant the temperature of viscosity breaking material at the bottom of the fractionation Tata.
Viscosity breaking product of the present invention can be directly be in harmonious proportion as HFO or with a spot of lightweight oil produces oil fuel, perhaps as the raw material of technological processs such as delayed coking.
The principal element that influences the visbroken resids stability is that the bituminous matter in the residual oil is carried out dehydrogenation, taken off alkyl and condensation reaction in the viscosity breaking process; Generation is difficult for being dispersed in the bituminous matter in the viscosity breaking product; Even burnt grain, cause visbroken resids stability variation.The bituminous matter overwhelming majority in the viscosity breaking raw material is distributed in more than 540 ℃ in the vacuum residuum of (or even＞550 ℃).Therefore adopt method of the present invention; The viscosity breaking raw material is carried out deep drawing through underpressure distillation earlier; Basically the vacuum distillate of asphaltenes does not carry out the boiler tube formula viscosity breaking of the high relatively degree of depth earlier, and then it is carried out viscosity breaking with the high deep drawing vacuum residuum of asphalt content at the bottom of separation column.Like this, viscosity breaking reaction times that bituminous matter experienced is short, and temperature is relatively low, and promptly reaction depth is low, the bituminous matter dehydrogenation, takes off alkyl and condensation level is low, therefore makes the visbroken resids good security of acquisition.
According to method provided by the invention, under preferable case, said underpressure distillation is carried out in vacuum still, and the absolute pressure of said underpressure distillation column overhead is 1.3-8.3kPa, is preferably 1.8-5.3kPa.
According to method provided by the invention; Under preferable case, said vacuum distillate to be carried out the process of viscosity breaking and in the viscosity breaking process furnace, carry out, the condition of said viscosity breaking reaction comprises; The temperature out of viscosity breaking process furnace is 480-520 ℃; Be preferably 485-510 ℃, the absolute pressure of viscosity breaking furnace outlet is 0.2-1MPa, is preferably 0.3-0.6MPa that the residence time of vacuum distillate in the viscosity breaking process furnace is 0.5-4 minute, is preferably 1-2 minute.
The reaction conditions that said mixing oil is carried out viscosity breaking at the bottom of viscosity breaking fractionation Tata comprises; Temperature at the bottom of the fractionation Tata is 400-450 ℃, is preferably 415-435 ℃ that the residence time of said mixing oil at the bottom of the fractionation Tata is 10-60 minute, is preferably 20-50 minute.
For the viscosity breaking of routine, the residence time of visbroken resids at the bottom of the fractionation Tata is 10-30 minute, and column bottom temperature is 330-360 ℃, and therefore the viscosity breaking reaction can not take place with this understanding.Adopt viscosity breaking method of the present invention, because the residence time of mixing oil at the bottom of the fractionation Tata is 10-60 minute, column bottom temperature is 400-450 ℃, and therefore the viscosity breaking reaction can take place with this understanding.In the present invention; Mixing oil can be realized through the liquid level at the bottom of improving the viscosity breaking separation column in the residence time at the bottom of the viscosity breaking fractionation Tata, perhaps improved the residence time of mixing oil at the bottom of viscosity breaking fractionation Tata through diameter and volume at the bottom of the increase viscosity breaking fractionation Tata.
According to method provided by the invention, said viscosity breaking raw material can be the various raw materials that carry out viscosity breaking usually, and for example this viscosity breaking raw material can be in crude oil, topped crude, long residuum and the long vacuum residuum one or more.
Specifically describe viscosity breaking method of the present invention with reference to Fig. 1 below.
(1) underpressure distillation
Viscosity breaking raw material 1 gets in the underpressure distillation process furnace 2 and is heated to 380-420 ℃; Getting into absolute pressure of top of the tower through pipeline 3 then is that the vacuum still 4 of 1.3-8.3kPa carries out underpressure distillation; Underpressure distillation overhead 5 is gone pumped vacuum systems; On the vacuum still, in and side line 6-1, side line 6-2 and the side line 6-3 of bottom distillate vacuum distillate, mix the raw material of back as viscosity breaking, the underpressure distillation tower bottom is extracted out and is not less than 540 ℃ vacuum residuum.
(2) viscosity breaking
The vacuum distillate of decompression side line 6-1,6-2 and 6-3 is mixed after pipeline 7 entering viscosity breaking process furnace 8 carry out the viscosity breaking of boiler tube formula; Wherein, The temperature out of viscosity breaking process furnace is 480-520 ℃; The absolute pressure of viscosity breaking furnace outlet is 0.2-1.0MPa, and the residence time of vacuum distillate in the viscosity breaking process furnace is 0.5-4 minute.
The vacuum residuum of extracting out at the bottom of the vacuum still injects viscosity breaking furnace outlet pipeline 10 as quenching oil through pipeline 9; Crackate to boiler tube formula viscosity breaking outlet of still carries out chilling; Crackate after the viscosity breaking of boiler tube formula and vacuum residuum together get into viscosity breaking separation column 11 bottoms through pipeline 10 and carry out viscosity breaking; Temperature at the bottom of the fractionation Tata is 400-450 ℃; Separation column is an atmospheric operation, and the residence time of said mixing oil at the bottom of the fractionation Tata is 10-60 minute, and resulting viscosity breaking product obtains viscosity breaking gas 12, petroleum naphtha 13 and visbroken resids 14 through fractionation.
Adopt the mode of embodiment that method of the present invention is described in further detail below.
Embodiment 1
The viscosity breaking raw material is a long residuum, and promptly the density 20 ℃ the time is 0.9914g/cm
3, the kinematic viscosity in the time of 100 ℃ is 304.5mm
2/ s, carbon residue are 16.6 weight %, and condensation point is 25 ℃, and sulphur content is 2.51 weight %, and asphalt content is 10.9 weight %.
Carry out viscosity breaking according to flow process shown in Figure 1.
(1) underpressure distillation
Long residuum 1 is heated to 390 ℃ in underpressure distillation process furnace 2; Getting into absolute pressure of top of the tower through pipeline 3 then is that the vacuum still 4 of 1.8kPa carries out underpressure distillation; Respectively on vacuum still, in and side line 6-1, side line 6-2 and the side line 6-3 of bottom distillate vacuum distillate; The boiling range of three side line distilled reduced pressure distillate oil mixts is 335-598 ℃, extracts the vacuum residuum greater than 560 ℃ out in the bottom of vacuum still.Vacuum still overhead line 5 is gone pumped vacuum systems.
(2) viscosity breaking
The vacuum distillate of vacuum still side line 6-1,6-2 and 6-3 is mixed after pipeline 7 entering viscosity breaking process furnace 8 carry out the viscosity breaking of boiler tube formula; The temperature out of viscosity breaking process furnace is 490 ℃; The absolute pressure of viscosity breaking furnace outlet is 0.3MPa, and the residence time of vacuum distillate in the viscosity breaking process furnace is 2 minutes.
That extracts out at the bottom of the vacuum still injects viscosity breaking furnace outlet pipeline 10 as quenching oil greater than 560 ℃ of vacuum residuum through pipeline 9; Crackate to boiler tube formula viscosity breaking outlet of still carries out chilling; Crackate after the viscosity breaking of boiler tube formula and vacuum residuum together get into viscosity breaking separation column 11 bottoms through pipeline 10 and carry out viscosity breaking; Temperature at the bottom of the fractionation Tata is 434 ℃, and separation column is an atmospheric operation, and the residence time of said mixing oil at the bottom of the fractionation Tata is 23 minutes; Resulting viscosity breaking product obtains viscosity breaking gas 12, petroleum naphtha 13 and visbroken resids 14 through the separation column fractionation.
Long residuum 1 is after viscosity breaking, and the viscosity breaking transformation efficiency is that the kinematic viscosity of the yield of 7.44%,＞165 ℃ visbroken resids when being 92.56%, 100 ℃ is 37.20mm
2/ s, stability is No. 2.
Comparative Examples 1
Adopt the long residuum identical as the viscosity breaking raw material with embodiment 1.Carry out viscosity breaking with conventional viscosity breaking technology.
Long residuum directly advances the viscosity breaking process furnace and carries out viscosity breaking, and the temperature of furnace outlet is 490 ℃, 2 minutes residence time in the viscosity breaking process furnace of the absolute pressure 0.3MPa of viscosity breaking furnace outlet, long residuum.The viscosity breaking furnace outlet injects quenching oil, and the viscosity breaking oil behind the chilling gets into separation column, 350 ℃ of fractionator bottom temperatures.Viscosity breaking oil obtains gas, petroleum naphtha and visbroken resids through the separation column fractionation.
After viscosity breaking, the viscosity breaking transformation efficiency is that the kinematic viscosity of the yield of 6.22%,＞165 ℃ visbroken resids when being 93.78%, 100 ℃ is 64.23mm
2/ s, stability is No. 3.
Comparative Examples 2
Adopt the long residuum identical as the viscosity breaking raw material with embodiment 1.
Under 60 ℃ temperature, adopt propane long residuum to be carried out diasphaltene as solvent, the volume ratio of solvent propane and long residuum is 8: 1.Resulting diasphaltene oil properties does, over point is 345 ℃, and the kinematic viscosity of deasphalted oil under 100 ℃ is 20.53mm
2/ s, de-oiled asphalt productive rate are 30 weight %.
Deasphalted oil is got into the viscosity breaking process furnace carry out viscosity breaking, the temperature out of process furnace is 490 ℃, 2 minutes residence time in the viscosity breaking process furnace of the absolute pressure 0.3MPa of viscosity breaking furnace outlet, long residuum.The viscosity breaking furnace outlet injects quenching oil, and the viscosity breaking oil behind the chilling gets into separation column, 350 ℃ of fractionator bottom temperatures.Viscosity breaking oil obtains gas, petroleum naphtha and visbroken resids through the separation column fractionation.Visbroken resids at the bottom of the separation column mixed with de-oiled asphalt obtain mixing oil.
After viscosity breaking, the viscosity breaking transformation efficiency is that the kinematic viscosity of the yield of 4.44%,＞165 ℃ visbroken resids when being 95.56%, 100 ℃ is 98.64mm
2/ s, stability is No. 2.
Adopt the long residuum identical as the viscosity breaking raw material with embodiment 1.Carry out viscosity breaking according to flow process shown in Figure 1.
(1) underpressure distillation
Long residuum 1 is heated to 420 ℃ in underpressure distillation process furnace 2; Getting into absolute pressure of top of the tower through pipeline 3 then is that the vacuum still 4 of 5.3kPa carries out underpressure distillation; Respectively on vacuum still, in and side line 6-1, side line 6-2 and the side line 6-3 of bottom distillate vacuum distillate; The boiling range of three side line distilled reduced pressure distillate oil mixts is 318-567 ℃, extracts the vacuum residuum greater than 540 ℃ out in the bottom of vacuum still.Vacuum still overhead line 5 is gone pumped vacuum systems.
(2) viscosity breaking
The vacuum distillate of decompression side line 6-1,6-2 and 6-3 is mixed after pipeline 7 entering viscosity breaking process furnace 8 carry out the viscosity breaking of boiler tube formula; The temperature out of viscosity breaking process furnace is 510 ℃; The absolute pressure of viscosity breaking furnace outlet is 0.6MPa, and the residence time of vacuum distillate in the viscosity breaking process furnace is 1 minute.
That extracts out at the bottom of the vacuum still injects viscosity breaking furnace outlet pipeline 10 as quenching oil greater than 540 ℃ of vacuum residuum through pipeline 9; Crackate to boiler tube formula viscosity breaking outlet of still carries out chilling; Crackate after the viscosity breaking of boiler tube formula and vacuum residuum together get into viscosity breaking separation column 11 bottoms through pipeline 10 and carry out viscosity breaking; Temperature at the bottom of the fractionation Tata is 418 ℃, and separation column is an atmospheric operation, and the residence time of said mixing oil at the bottom of the fractionation Tata is 50 minutes; Resulting viscosity breaking product obtains viscosity breaking gas 12, petroleum naphtha 13 and visbroken resids 14 through the separation column fractionation.
Long residuum 1 is after viscosity breaking, and the viscosity breaking transformation efficiency is that the kinematic viscosity of the yield of 7.92%,＞165 ℃ visbroken resids when being 92.08%, 100 ℃ is 34.22mm
2/ s, stability is No. 2.
Adopt the long residuum identical as the viscosity breaking raw material with embodiment 1.Carry out viscosity breaking according to flow process shown in Figure 1.
(1) underpressure distillation
Long residuum 1 is heated to 410 ℃ in underpressure distillation process furnace 2; Getting into absolute pressure of top of the tower through pipeline 3 then is that the vacuum still 4 of 3.0kPa carries out underpressure distillation; Respectively on vacuum still, in and side line 6-1, side line 6-2 and the side line 6-3 of bottom distillate vacuum distillate; The boiling range of three side line distilled reduced pressure distillate oil mixts is 331-588 ℃, extracts the vacuum residuum greater than 550 ℃ out in the bottom of vacuum still.Vacuum still overhead line 5 is gone pumped vacuum systems.
(2) viscosity breaking
The vacuum distillate of vacuum still side line 6-1,6-2 and 6-3 is mixed after pipeline 7 entering viscosity breaking process furnace 8 carry out the viscosity breaking of boiler tube formula; The temperature out of viscosity breaking process furnace is 500 ℃; The absolute pressure of viscosity breaking furnace outlet is 0.5MPa, and the residence time of vacuum distillate in the viscosity breaking process furnace is 1.5 minutes.
That extracts out at the bottom of the vacuum still injects viscosity breaking furnace outlet pipeline 10 as quenching oil greater than 550 ℃ of vacuum residuum through pipeline 9; Crackate to boiler tube formula viscosity breaking outlet of still carries out chilling; Crackate after the viscosity breaking of boiler tube formula and vacuum residuum together get into viscosity breaking separation column 11 bottoms through pipeline 10 and carry out viscosity breaking; Temperature at the bottom of the fractionation Tata is 425 ℃, and separation column is an atmospheric operation, and the residence time of said mixing oil at the bottom of the fractionation Tata is 35 minutes; Resulting viscosity breaking product obtains viscosity breaking gas 12, petroleum naphtha 13 and visbroken resids 14 through the separation column fractionation.
Long residuum 1 is after viscosity breaking, and the viscosity breaking transformation efficiency is that the kinematic viscosity of the yield of 7.62%,＞165 ℃ visbroken resids when being 92.38%, 100 ℃ is 35.83mm
2/ s, stability is No. 2.
Product to resulting viscosity breaking among embodiment 1-3 and the Comparative Examples 1-2 carries out performance test, and gained is the result list in the table 1.
Table 1
| Embodiment 1 | Comparative Examples 1 | Comparative Examples 2 | |
|
|
| Viscosity breaking furnace outlet temperature (℃) | 490 | 490 | 490 | 510 | 500 |
| Viscosity breaking furnace outlet absolute pressure (MPa) | 0.3 | 0.3 | 0.3 | 0.6 | 0.5 |
| Material is the residence time (min) in the viscosity |
2 | 2 | 2 | 1 | 1.5 |
| Fractionator bottom temperature (℃) | 434 | - | - | 418 | 425 |
| The residence time (min) of material at the bottom of separation column | 23 | - | - | 50 | 35 |
| Viscosity breaking gas recovery ratio (weight %) | 1.80 | 1.67 | 1.21 | 1.87 | 1.84 |
| Viscosity breaking naphtha yield (weight %) | 5.64 | 4.55 | 3.23 | 6.05 | 5.78 |
| ＞165 ℃ of visbroken resids yields (weight %) | 92.56 | 93.78 | 95.56 | 92.08 | 92.38 |
| Transformation efficiency (weight %) | 7.44 | 6.22 | 4.44 | 7.92 | 7.62 |
| ＞165 ℃ of visbreaking residue character | |||||
| ASTM D4940 stability (number) | 2 | 3 | 2 | 2 | 2 |
| Condensation point (℃) | 17 | 18 | 19 | 17 | 17 |
| Sulphur (weight %) | 2.41 | 2.40 | 2.41 | 2.40 | 2.40 |
| Density (20 ℃) (g/cm 3) | 0.9770 | 0.9810 | 0.9882 | 0.9761 | 0.9766 |
| Viscosity (100 ℃) (mm 2/s) | 37.20 | 64.23 | 98.64 | 34.22 | 35.83 |
| Bituminous matter (weight %) | 12.2 | 13.7 | 11.5 | 11.9 | 12.0 |
Visible from last table 1, adopt method of the present invention, can improve the viscosity breaking transformation efficiency, promptly can improve the viscosity breaking degree of depth, can reduce the viscosity of visbroken resids simultaneously, and the good security of visbroken resids.
Claims (8)
1. a viscosity breaking method is characterized in that, this method is included under the condition of underpressure distillation, and the viscosity breaking raw material is carried out underpressure distillation, obtains the vacuum residuum that vacuum distillate and cutting temperature are not less than 540 ℃; Said vacuum distillate is carried out viscosity breaking under the condition of viscosity breaking; Product after the vacuum distillate viscosity breaking is mixed with said vacuum residuum; Obtain mixing oil; Said mixing oil is carried out viscosity breaking at the bottom of viscosity breaking fractionation Tata, and fractionation obtains gas, petroleum naphtha and visbreaking residue, the temperature of said vacuum distillate being carried out viscosity breaking is higher than the temperature of said mixing oil being carried out viscosity breaking.
2. method according to claim 1, wherein, the temperature that said vacuum distillate is carried out viscosity breaking is than said mixing oil being carried out the high 30-120 of temperature ℃ of viscosity breaking.
3. method according to claim 1, wherein, said underpressure distillation is carried out in vacuum still, and the absolute pressure of said underpressure distillation column overhead is 1.3-8.3kPa.
4. method according to claim 1 and 2; Wherein, Said vacuum distillate is carried out the process of viscosity breaking and in the viscosity breaking process furnace, carry out, the condition of said viscosity breaking reaction comprises that the temperature out of viscosity breaking process furnace is 480-520 ℃; The absolute pressure of viscosity breaking furnace outlet is 0.2-1MPa, and the residence time of vacuum distillate in the viscosity breaking process furnace is 0.5-4 minute.
5. method according to claim 4; Wherein, The condition of said viscosity breaking reaction comprises; The temperature out of viscosity breaking process furnace is 485-510 ℃, and the absolute pressure of viscosity breaking furnace outlet is 0.3-0.6MPa, and the residence time of vacuum distillate in the viscosity breaking process furnace is 1-2 minute.
6. method according to claim 1; Wherein, The condition of said mixing oil being carried out the viscosity breaking reaction at the bottom of viscosity breaking fractionation Tata comprises that the temperature at the bottom of the fractionation Tata is 400-450 ℃, and the residence time of said mixing oil at the bottom of the fractionation Tata is 10-60 minute.
7. method according to claim 6; Wherein, The condition of said mixing oil being carried out the viscosity breaking reaction at the bottom of viscosity breaking fractionation Tata comprises that the temperature at the bottom of the fractionation Tata is 415-435 ℃, and the residence time of said mixing oil at the bottom of the fractionation Tata is 20-50 minute.
8. method according to claim 1, wherein, said viscosity breaking raw material is one or more in crude oil, topped crude, long residuum and the long vacuum residuum.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200710303928 CN101463267B (en) | 2007-12-21 | 2007-12-21 | Viscosity breaking method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200710303928 CN101463267B (en) | 2007-12-21 | 2007-12-21 | Viscosity breaking method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101463267A CN101463267A (en) | 2009-06-24 |
| CN101463267B true CN101463267B (en) | 2012-12-12 |
Family
ID=40804061
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200710303928 Active CN101463267B (en) | 2007-12-21 | 2007-12-21 | Viscosity breaking method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101463267B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114958418B (en) * | 2021-02-18 | 2023-08-08 | 中国石油化工股份有限公司 | Method for producing residual oil by heating furnace |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2041916C1 (en) * | 1993-08-25 | 1995-08-20 | Институт проблем нефтепереработки АН Башкортостана | Method for production of boiler fuel |
| RU2213763C2 (en) * | 2001-05-31 | 2003-10-10 | Королева Наталия Владиславовна | Residual petroleum product processing method |
| CN1454965A (en) * | 2003-05-08 | 2003-11-12 | 中国石化集团洛阳石油化工工程公司 | Petroleum atmospheric vacuum distillation process and unit |
| CN1710027A (en) * | 2005-06-06 | 2005-12-21 | 周衍亮 | Crude oil full-fraction one-stage reduced pressure distillation process |
-
2007
- 2007-12-21 CN CN 200710303928 patent/CN101463267B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2041916C1 (en) * | 1993-08-25 | 1995-08-20 | Институт проблем нефтепереработки АН Башкортостана | Method for production of boiler fuel |
| RU2213763C2 (en) * | 2001-05-31 | 2003-10-10 | Королева Наталия Владиславовна | Residual petroleum product processing method |
| CN1454965A (en) * | 2003-05-08 | 2003-11-12 | 中国石化集团洛阳石油化工工程公司 | Petroleum atmospheric vacuum distillation process and unit |
| CN1710027A (en) * | 2005-06-06 | 2005-12-21 | 周衍亮 | Crude oil full-fraction one-stage reduced pressure distillation process |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101463267A (en) | 2009-06-24 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US8709233B2 (en) | Disposition of steam cracked tar | |
| KR101712238B1 (en) | Process for delayed coking of whole crude oil | |
| RU2673803C1 (en) | Method for upgrading partially converted vacuum residue | |
| US8535516B2 (en) | Efficient method for improved coker gas oil quality | |
| RU2634721C2 (en) | Combining deaspaltization stages and hydraulic processing of resin and slow coking in one process | |
| JP6464199B2 (en) | Sequential decomposition method | |
| TWI571508B (en) | Hydroprocessing thermally cracked products | |
| MX2007009259A (en) | Bitumen production-upgrade with common or different solvents. | |
| US6048448A (en) | Delayed coking process and method of formulating delayed coking feed charge | |
| CN111465675B (en) | Process and apparatus for recovering products of slurry hydrocracking | |
| CN101463266B (en) | Viscosity breaking method | |
| CN102899076A (en) | Delayed coking method | |
| CN1200082C (en) | Combined technologic process for manufacturing petroleum residue | |
| CN101463267B (en) | Viscosity breaking method | |
| WO2009014303A1 (en) | Method for producing feedstocks of high quality lube base oil from coking gas oil | |
| US9856421B2 (en) | Process for upgrading a heavy hydrocarbon feedstock | |
| CN103305249A (en) | Method for producing bitumen | |
| CN102899077A (en) | Coking method | |
| JPS6249917B2 (en) | ||
| CN1382766A (en) | Process for viscosity breaking of deoiled asphalt | |
| CN1448466A (en) | Method for raising production efficiency of delayed coking liquid product | |
| NO173610B (en) | PROCEDURE FOR THE PREPARATION OF KEROSEN AND / OR GAS OIL | |
| US2049000A (en) | Manufacture of asphalt and lubricating oils | |
| TWI757337B (en) | A kind of modification method and modification system of low-quality oil | |
| CN205933759U (en) | Delayed coking device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |