CN111925821B - Separation method of high-solid-content heavy sump oil - Google Patents
Separation method of high-solid-content heavy sump oil Download PDFInfo
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- CN111925821B CN111925821B CN202010703203.2A CN202010703203A CN111925821B CN 111925821 B CN111925821 B CN 111925821B CN 202010703203 A CN202010703203 A CN 202010703203A CN 111925821 B CN111925821 B CN 111925821B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/10—Vacuum distillation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/42—Regulation; Control
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/74—Recovery of fats, fatty oils, fatty acids or other fatty substances, e.g. lanolin or waxes
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a separation method of high solid content heavy sump oil, which comprises the following steps that firstly, a raw material A of high solid content heavy sump oil enters a reduced pressure distillation tower for distillation treatment, solid sump oil B is obtained at the lower tower section, and solid sump oil C is obtained at the upper tower section; step two, separating the solid dirty oil B by oil residue to obtain solid residue and separated solid dirty oil D, heating the solid dirty oil D by a heating furnace, and returning the heated solid dirty oil D to the upper tower section of the reduced pressure distillation tower; and step three, separating light sump oil E at the top of the upper tower, first side line oil F, second side line oil G and residue oil H at the bottom of the upper tower from the upper tower section of the vacuum distillation tower according to different boiling points of the components without containing the solid sump oil D and the solid sump oil C. The separation method can separate and recover liquid components such as residual oil, heavy wax oil, light wax oil and the like in the heavy dirty oil with high solid content to the maximum extent, and can reduce the number of equipment to the maximum extent and reduce the abrasion of the equipment and pipelines when the separation effect is achieved.
Description
Technical Field
The invention belongs to the field of petrochemical industry or coal chemical industry, and particularly relates to a method for separating heavy dirty oil with high solid content.
Background
The heavy dirty oil with high solid content (more than 5 percent of solid content) has large viscosity, poor fluidity, easy coking, easy blockage and abrasion of equipment and pipelines and extremely difficult separation.
The heavy dirty oil has high viscosity and is difficult to separate by adopting a standing sedimentation method, and the separated product is a mixture of various oil products.
The prior art generally employs the following methods for separation:
1. when the filtering method is adopted for separation, due to the fact that the viscosity of the dirty oil is large, the solid particles in the dirty oil are different in size, equipment needed is too large when the filtering precision is too high, and the recovery rate of liquid components is low. If the filtration accuracy is too low, the recovered oil contains solid particles. The separated product is a mixture of various oil products.
2. The method adopts a general distillation method to separate the solid heavy dirty oil, but has the following defects:
1) the heating furnace is used for heating heavy dirty oil with high solid content or solid oil residue at the bottom of the heating tower is used for providing heat for the distillation tower, and the defects that the furnace tube of the heating furnace is easy to wear and the furnace tube of the heating furnace is easy to coke and block exist.
2) The feeding material is not blended and does not contain solid side line oil, and the feeding property is not improved.
3) The method adopts a plurality of towers to separate the solid heavy dirty oil, and has complex flow and large investment.
4) The residual oil of the tower bottom material (oil residue) after oil residue separation needs to be treated by an additional separation tower.
Disclosure of Invention
The invention aims to provide a method for separating high-solid-content heavy sump oil, which can separate and recover liquid components such as residual oil, heavy wax oil, light wax oil and the like in the high-solid-content heavy sump oil to the maximum extent.
In order to achieve the purpose, the invention adopts the following technical scheme:
a method for separating high solid content heavy sump oil comprises the following steps:
step one, feeding a raw material A with high solid content and heavy sump oil into a reduced pressure distillation tower for distillation treatment, obtaining solid sump oil B at a lower tower section, and obtaining solid sump oil C at an upper tower section;
step two, separating the solid dirty oil B by oil residue to obtain solid residue and separated solid dirty oil D, heating the solid dirty oil D by a heating furnace, and returning the heated solid dirty oil D to the upper tower section of the reduced pressure distillation tower;
and step three, separating light sump oil E at the top of the upper tower, first side line oil F, second side line oil G and residue oil H at the bottom of the upper tower from the upper tower section of the vacuum distillation tower according to different boiling points of the components without containing the solid sump oil D and the solid sump oil C.
Furthermore, any side line or multi-measuring line is provided with a branch which is communicated with the heating furnace, and any side line oil or multi-side line mixed oil is heated by the heating furnace and then returns to the feeding line of the vacuum distillation tower to be mixed with the high solid heavy dirty oil raw material A.
Furthermore, a spraying device is arranged at the lower tower top of the reduced pressure distillation tower, the raw material A with high solid content and heavy sump oil is separated into solid sump oil B and solid sump oil C after being washed, and the spraying washing oil adopts line oil on any side of the upper tower section.
Furthermore, in the first step, the temperature of the feeding line of the reduced pressure distillation tower is 350-; in the second step, the temperature of the lower tower section of the reduced pressure distillation tower is 300-350 ℃; in the third step, the temperature of the bottom of the upper tower of the reduced pressure distillation tower is 330-370 ℃, the temperature of the second side line is 300-350 ℃, the temperature of the first side line is 240-260 ℃, and the temperature of the top of the upper tower is 60-90 ℃.
Furthermore, in the second step, the oil D without solid sump is heated to 380-400 ℃ and then returned to the upper tower section of the vacuum distillation tower.
Furthermore, any side line oil or multi-side line mixed oil is heated to 400-450 ℃ and then returned to a feeding line of the vacuum distillation tower.
Furthermore, in the second step, the heating furnace does not contain the steam injected from the solid dirty oil D inlet.
Further, the pressure of the reduced pressure distillation tower is 5-10 kPaA.
The invention has the beneficial effects that:
1. the separation method is utilized to separate the high solid content heavy dirty oil, the heating furnace is arranged behind the reduced pressure distillation tower, materials (containing oil and solid residues) at the bottom of the tower below the reduced pressure distillation tower are subjected to oil residue separation treatment by the oil residue separation device and then are introduced into the heating furnace for heating, the heating furnace does not directly heat the high solid content heavy dirty oil, but heats the heavy oil without solid, and the equipment is prevented from being worn, coked and blocked.
2. Materials (containing oil and solid residues) at the bottom of the lower tower are subjected to oil residue separation treatment, the separated heavy oil is heated by a heating furnace and then used as the feeding material of the upper tower, and then deep separation is carried out.
3. The side line oil (side line oil or multi-measuring line mixed oil) on the upper tower section of the reduced pressure distillation tower is heated by a heating furnace and then returns to the tower feeding line to be mixed with the high-solid-content feeding material, so that the solid content of the mixed material can be reduced, the pipeline abrasion and the solid deposition can be reduced, and the viscosity of the mixed material can be reduced to improve the fluidity of the mixed material. Meanwhile, heat is brought to the feeding of the reduced pressure distillation tower, so that the heat required by the reduced pressure distillation is ensured, the feeding temperature of the reduced pressure distillation tower can be reduced as far as possible while the separation effect is ensured, and coking is prevented.
4. One tower achieves the separation function and effect of two towers. The vacuum distillation tower is divided into an upper tower and a lower tower. The upper tower is a separation tower without solid materials and is provided with separation internals (a packing layer or a tray), and the lower tower is a separation tower with solid materials.
5. The spraying device is arranged on the lower tower top of the reduced pressure distillation tower, so that solids are prevented from being brought into the upper tower, and meanwhile, the quality index of bottom oil of the lower tower can be flexibly adjusted.
Drawings
FIG. 1 is a schematic illustration of the separation process of the present invention;
wherein: 1. a reduced pressure distillation column; 2. a heating furnace; 3. a spraying device; 4. the system is evacuated under reduced pressure.
Detailed Description
To better illustrate the objects, aspects and advantages of the present invention, the present invention will be further described with reference to specific embodiments. This invention may be embodied in many different forms and should not be construed as limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete and will fully convey the concept of the invention to those skilled in the art, and the present invention will only be defined by the appended claims.
As shown in fig. 1, a method for separating high solid content heavy dirty oil comprises the following steps:
step one, feeding a raw material A with high solid content and heavy sump oil into a reduced pressure distillation tower 1 for distillation treatment, obtaining solid sump oil B at a lower tower section, and obtaining solid sump oil C at an upper tower section;
step two, separating solid dirty oil B from oil residue to obtain solid residue and separated solid dirty oil D, heating the solid dirty oil D by a heating furnace 2, and returning the heated solid dirty oil D to the upper tower section of a reduced pressure distillation tower 1;
and step three, separating light sump oil E at the top of the upper tower, first side line oil F, second side line oil G and residue oil H at the bottom of the upper tower from the upper tower section of the vacuum distillation tower 1 without the solid sump oil D and the solid sump oil C according to different boiling points of the components.
Specifically, the vacuum distillation column 1 is divided into an upper column section and a lower column section. And (3) feeding the high solid heavy sump oil raw material A into a reduced pressure distillation tower 1 for distillation, obtaining solid sump oil B at the lower tower section, and obtaining solid sump oil C at the upper tower section. One tower achieves the separation function and effect of two towers. The upper tower is a separation tower without solid materials, further separates the oil C without solid dirty oil, and is provided with a separation internal part (a packing layer or a tray); the lower tower is a solid material-containing separation tower for further separating solid dirty oil B.
The bottom of the upper tower segment is used for separating the residual oil H at the bottom, such as asphalt or residual oil, and comprises a drawing pump, a heat exchanger and a drawing device which are connected with the outlet at the bottom of the upper tower segment of the vacuum distillation tower 1.
The second side line is used for separating second side line oil G, such as wax oil, and comprises a drawing pump, a heat exchanger and a drawing device which are connected with a middle section outlet of the upper tower section of the reduced pressure distillation tower 1.
The first side line is used for separating first side line oil F, such as diesel oil, and comprises a suction pump, a heat exchanger and a suction device which are connected with an outlet of the upper section of the upper tower section of the vacuum distillation tower 1.
According to different boiling points of the components, the top of the upper tower section is used for separating light dirty oil E, the top of the upper tower section is connected with a heat exchanger and a pressure reduction evacuation system 4, and the pressure reduction evacuation system 4 is provided with an outlet for the light dirty oil E and an outlet for oily sewage.
The lower tower section contains solid sump oil B, the solid sump oil B is communicated with an oil residue separation device through a sump oil outlet through a tower bottom pump to obtain solid residues and separated solid sump oil D, the solid residues enter a residue removal treatment system, the sump oil outlet of the oil residue separation device is communicated with a heating furnace 2, the solid sump oil D is heated and then flows into an upper tower section of a reduced pressure distillation tower 1, and deep separation is carried out.
The heating furnace 2 is arranged behind the reduced pressure distillation tower 1, materials (containing oil and solid residues) at the bottom of the lower tower of the reduced pressure distillation tower 1 are subjected to oil residue separation treatment by the oil residue separation device and then enter the heating furnace 2 for heating, and the high-solid heavy sump oil is not directly heated by the heating furnace 2, so that the equipment of the heating furnace 2 can be prevented from being worn, coked and blocked.
Furthermore, any side line or multi-measuring line is provided with a branch communicated with the heating furnace 2, and any side line oil or multi-side line mixed oil is heated by the heating furnace 2 and then returns to the feeding line of the vacuum distillation tower 1 to be mixed with the high solid heavy dirty oil raw material A.
The side line oil (side line oil or multi-measuring line mixed oil) on the upper tower section of the reduced pressure distillation tower 1 is heated by the heating furnace 2 and then returns to the tower feeding line to be mixed with the high solid content feeding material, so that the solid content of the mixed material can be reduced, the pipeline abrasion can be reduced, and the viscosity of the mixed material can be reduced to improve the fluidity of the mixed material. Meanwhile, heat is brought to the feeding of the reduced pressure distillation tower 1, so that the heat required by reduced pressure distillation is ensured, the feeding temperature of the reduced pressure distillation tower can be reduced as far as possible while the separation effect is ensured, and coking is prevented.
Furthermore, a spraying device 3 is arranged at the lower tower top of the reduced pressure distillation tower 1, the raw material A with high solid content and heavy sump oil is separated into solid sump oil B and solid sump oil C after being washed, and the spraying and washing oil adopts line oil on any side of the upper tower section.
The spraying device 3 can prevent solids from being brought into the upper tower, and can adjust the quality index of the tower bottom oil of the lower tower. The spraying device 3 can be a spraying washing pipe or a spray head, the spraying washing oil adopts upper tower side line oil, oil of any measuring line (preferably the lowest measuring line) is used for washing solid oil gas, and the height from the lower part of the lower tower top spraying washing pipe or the spray head to the top of the feeding pipe opening is not less than 3 m.
Preferably, in the first step, the temperature of the feeding line of the reduced pressure distillation tower 1 is 350-400 ℃; in the second step, the temperature of the lower tower section of the reduced pressure distillation tower 1 is 300-350 ℃.
In the third step, the temperature of the bottom of the upper tower of the reduced pressure distillation tower 1 is 330-370 ℃, and the residue oil H at the bottom of the upper tower is cooled to 180-250 ℃ through heat exchange of a heat exchanger and enters a collecting device;
the temperature of the second side line is 300-350 ℃, the oil G on the second side line is subjected to heat exchange by a heat exchanger and is cooled to 90-120 ℃ and enters a collecting device;
the temperature of the first side line is 240-260 ℃, the oil F at the first side line is subjected to heat exchange by a heat exchanger and is cooled to 90-120 ℃ and enters a collecting device;
the temperature of the top of the upper tower is 60-90 ℃, and the light sump oil E at the top of the upper tower is cooled to 40-60 ℃ through heat exchange of a heat exchanger and enters a collecting device.
Preferably, in the second step, the oil D without solid sump is heated to 380-400 ℃ and then returned to the upper tower section of the vacuum distillation tower 1.
Preferably, the oil on any side line or the mixed oil on multiple side lines is returned to the feeding line of the vacuum distillation tower 1 after being heated to 400-450 ℃.
Preferably, in the second step, the heating furnace 2 does not contain steam injected from the inlet of the solid dirty oil D, so that the coking of the heating furnace tube can be prevented.
Preferably, the reduced pressure distillation tower 1 is connected with a reduced pressure evacuation system 4, and the pressure of the reduced pressure distillation tower 1 is 5-10 kPaA.
It should be understood that the above examples are only for clarity of illustration and are not intended to limit the embodiments. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. And are neither required nor exhaustive of all embodiments. And obvious variations or modifications therefrom are within the scope of the invention.
Claims (5)
1. A method for separating high solid content heavy sump oil is characterized in that: the content of the solid in the high solid content heavy dirty oil is more than 5 percent, and the method comprises the following steps:
step one, a raw material A with high solid content and heavy sump oil enters a reduced pressure distillation tower (1) without being heated by a heating furnace or a heat exchanger for distillation treatment, solid sump oil B is obtained at the lower tower section, and solid sump oil C is obtained at the upper tower section;
step two, separating the solid dirty oil B by oil residue to obtain solid residue and separated solid dirty oil D, and returning the solid dirty oil D to the upper tower section of the reduced pressure distillation tower (1) after being heated by the heating furnace (2);
step three, separating light dirty oil E at the top of the upper tower, first side line oil F, second side line oil G and residue oil H at the bottom of the upper tower from the oil C without solid dirty oil D and the oil C without solid dirty oil C at the upper tower section of the vacuum distillation tower (1) according to different boiling points of the components,
any side line or multiple side lines are provided with branches which are communicated with the heating furnace (2), and any side line oil or multiple side line mixed oil is heated by the heating furnace (2) and then returns to the feeding line of the reduced pressure distillation tower (1) to be mixed with the high solid heavy sump oil raw material A;
in the first step, the temperature of a feeding line of the reduced pressure distillation tower (1) is 350-400 ℃;
in the second step, the temperature of the lower section of the reduced pressure distillation tower (1) is 300-;
in the third step, the temperature of the bottom of the upper tower of the reduced pressure distillation tower (1) is 330-.
2. The method for separating the high solid content heavy dirty oil according to claim 1, characterized in that: the spray device (3) is arranged on the lower tower top of the reduced pressure distillation tower (1), the raw material A with high solid content and heavy sump oil is separated into solid sump oil B and solid sump oil C after being washed, and spray washing oil adopts line oil on any side of the upper tower section.
3. The method for separating the high solid content heavy dirty oil according to claim 1, characterized in that: the oil on either side or the mixed oil on multiple sides is returned to the feeding line of the vacuum distillation tower (1) after being heated to the temperature of 400-450 ℃.
4. The method for separating the high solid content heavy dirty oil according to claim 1, characterized in that: in the second step, steam is injected into the inlet of the heating furnace (2) without the solid dirty oil D.
5. The method for separating the high solid content heavy dirty oil according to claim 1, characterized in that: the pressure of the reduced pressure distillation tower (1) is 5-10 kPaA.
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| CN202010703203.2A CN111925821B (en) | 2020-07-21 | 2020-07-21 | Separation method of high-solid-content heavy sump oil |
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| CN202010703203.2A CN111925821B (en) | 2020-07-21 | 2020-07-21 | Separation method of high-solid-content heavy sump oil |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN205152158U (en) * | 2015-11-13 | 2016-04-13 | 中石化洛阳工程有限公司 | Coal tar suspension bed hydrocracking unit |
| CN106701178A (en) * | 2015-11-13 | 2017-05-24 | 中石化洛阳工程有限公司 | Coal tar suspended bed hydrocracking method |
| CN110229689A (en) * | 2019-04-21 | 2019-09-13 | 宁波市化工研究设计院有限公司 | Distilling apparatus and method containing solid feedstock oil |
| CN212548352U (en) * | 2020-05-06 | 2021-02-19 | 武汉金中石化工程有限公司 | High-solid-content heavy dirty oil separation system |
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2020
- 2020-07-21 CN CN202010703203.2A patent/CN111925821B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN205152158U (en) * | 2015-11-13 | 2016-04-13 | 中石化洛阳工程有限公司 | Coal tar suspension bed hydrocracking unit |
| CN106701178A (en) * | 2015-11-13 | 2017-05-24 | 中石化洛阳工程有限公司 | Coal tar suspended bed hydrocracking method |
| CN110229689A (en) * | 2019-04-21 | 2019-09-13 | 宁波市化工研究设计院有限公司 | Distilling apparatus and method containing solid feedstock oil |
| CN212548352U (en) * | 2020-05-06 | 2021-02-19 | 武汉金中石化工程有限公司 | High-solid-content heavy dirty oil separation system |
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