CN105251246A - Method for removing catalyst solid powder in oil slurry - Google Patents
Method for removing catalyst solid powder in oil slurry Download PDFInfo
- Publication number
- CN105251246A CN105251246A CN201510731522.3A CN201510731522A CN105251246A CN 105251246 A CN105251246 A CN 105251246A CN 201510731522 A CN201510731522 A CN 201510731522A CN 105251246 A CN105251246 A CN 105251246A
- Authority
- CN
- China
- Prior art keywords
- slurry oil
- oil
- settling
- slurry
- catalyst solid
- 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.)
- Pending
Links
Abstract
The invention relates to a method for removing catalyst solid powder in oil slurry, and provides a technological method for scientifically and effectively using a catalytic cracking slurry oil deliming agent, and a set of complete condition requirements for using the technology. The method provided by the invention can be also used for settling separation of catalyst solid in catalytic cracking recycle oil and solid particles in other heavy oil. Through adopting the technological method and the technological conditions provided by the invention, after statically settling the catalytic cracking slurry oil and the recycle oil, the ash content can be reduced below 0.08 percent, generally, the static settling time for achieving the settling separation target cannot exceed 72 hours, and the static settling time for most industrial application cases is ranged between 0 hour and 24 hours.
Description
Technical field
The present invention relates to a kind of process of efficiency utilization slurry oil deliming agent sedimentation separation catalyst powder in catalytic cracking oil slurry.More particularly, be a kind ofly utilize the technological process of slurry oil deliming agent process slurry oil and corresponding process conditions.
Background technology
FCC slurry oil is the unconverted hydro carbons that a kind of boiling point produced in catalytic cracking process is greater than 350 DEG C, and character is very special, is wherein rich in resin and asphalt, has the advantages that viscosity is high and density is large.FCC slurry oil has good economic worth, but because FCC slurry oil contains the catalyst solid powder of 2000 ~ 9000ppm, its economic scale and increment utilization is very limited.Be in particular in the following aspects:
1. when the blend component of catalytic slurry as heavy oil, if without purification, the catalyst solid powder in slurry oil can make heating furnace nozzles wear and tear, and causes the problems such as furnace tubing surface serious dust stratification, thermal efficiency decline, energy consumption increase;
2. slurry oil is an important source material source of Carbon black production.According to statistics, the carbon black raw material oil (CBO) in the world more than 50% is FCC slurry oil.The ash content (ASTMD-482) of CBO requires that the ash content index of top grade product is then 300ppm or 200ppm for 500ppm;
3. slurry oil is the quality raw materials of delayed coking, can improve the lightweight rate of crude oil processing as coking raw material further, and what is more important slurry oil can be used for producing the needle coke making each graphite electrode.Also the ash content of slurry oil must be made to drop to below 500ppm;
4. the raw material sources of residual hydrocracking are extensive.During the raw material of catalytic slurry as residual hydrocracking process, the ash content of slurry oil also must be made to drop to below 500ppm, otherwise the catalyst fines that slurry oil is carried secretly can cause hydrogenation catalyst hole plug, pressure drop increase and catalysqt deactivation etc.;
5. catalytic slurry is rich in heavy aromatics more than 60%, and after solvent extraction, heavy arene is the desirable inserts of rubber and plastic processing.But the existence of catalyst fines makes troubles then can to the operation of extraction tower and solvent recovery.
To fully effectively utilize FCC slurry oil, the catalyst solid powder in slurry oil must be removed.
The technology of existing Removal of catalyst pressed powder comprises: natural sedimentation, auxiliary agent sedimentation separation method, filtration method, electrostatic separation method and centrifugal separation etc.Except auxiliary agent sedimentation separation method and filtration method have commercial Application case exception, additive method does not all also have commercial Application case.But auxiliary agent sedimentation separation method i.e. the slurry oil deliming agent alleged by the present invention (or claiming capturing settling agent method) at present, mostly all be only limited to the research to deliming agent (or claiming capturing settling agent) itself, nearly all not to the research of the application principle of deliming agent, technique for applying and method.Through us years of researches and commercial Application case, the process application principle of slurry oil deliming agent and method have vital effect to the results of industrial application of slurry oil deliming agent and the time of sedimentation separation.
Summary of the invention
The invention provides a kind of deviate from the method for catalyst solid powder in slurry oil, the defect that sinking speed in prior art is slow to overcome, removal efficiency is low.
Remove a method for catalyst solid powder in slurry oil, it is characterized in that: said method comprising the steps of:
The first step, obtains mixture with the Homogeneous phase mixing in dynamic mixer of the catalytic cracked oil pulp under certain temperature conditions in proportion by slurry oil deliming agent; Described ratio is weight ratio or volume ratio, and the addition of described slurry oil deliming agent accounts for 0.003 ~ 0.2% of described slurry oil; Certain temperature described is 50 DEG C ~ 360 DEG C;
Second step, mixture obtained for the first step is injected slurry oil settling tank from bottom and carries out sedimentation, settling temperature is 50 DEG C ~ 360 DEG C; Described bottom to refer at the bottom of settling tank tank having living space between 2.5 meters of cross sections more than at the bottom of cross section to tank;
Further, adopted in a first step dynamic mixer can be pipe line type high-shear dispersing emulsifying machine, mulser, homogenizer, homogeneous emulsifying machine etc.
The present invention has the remarkable results such as sinking speed is fast, removal efficiency is high.
Accompanying drawing explanation
The process chart that Fig. 1 provides for the embodiment of the present invention.
Detailed description of the invention
Below in conjunction with accompanying drawing, the embodiment of the present invention is further elaborated.
Step 1: the ratio of slurry oil deliming agent by the slurry oil next with one or more sets catalytic cracking units is extracted out from slurry oil deliming agent pans.
The ratio limiting slurry oil deliming agent and slurry oil is in step 1 0.00003 ~ 0.002, and this ratio both can be mass values, also can be volume ratio.
Step 2: the slurry oil that the slurry oil deliming agent described in step 1 and one or more sets catalytic cracking units come is mixed at a certain temperature in dynamic mixer, obtained mixture.
Limiting mixing temperature is in step 2 50 DEG C ~ 360 DEG C, and the main purpose limiting this temperature range to reduce the viscosity of slurry oil, is conducive to the diffusion of deliming agent in slurry oil and the task performance performance of blender.Slurry oil and deliming agent through the abundant shearing of blender after mixing, deliming agent and slurry oil mix evenly, " electric eliminating " and " flocculation " function of deliming agent can be given full play to like this.Dynamic mixer of the present invention, also can be referred to as pipe line type high-shear dispersing emulsifying machine, mulser, homogenizer, homogeneous emulsifying machine etc.
Step 3: the mixture that step 2 is obtained is entered slurry oil settling tank from bottom and carries out sedimentation.
Limit slurry oil deliming agent and slurry oil mixture in step 3 to enter from certain position bottom settling tank, bottom of the present invention to refer at the bottom of settling tank tank having living space between 2.5 meters of cross sections more than at the bottom of cross section to tank.This limits the main purpose that this interval enters: one is the concentration advantage giving full play to capturing settling agent and catalyst granules, form " band caught by net " or claim " close phase layer ", the catalyst molecule in slurry oil is used to grow up, for the rapid subsidence of catalyst granules creates conditions at this area coalesces or flocculation; Two is the settling heights shortening catalyst granules and agglomerate and floccule body, effectively reduces the sedimentation time.
Limiting settling temperature is in step 3 50 DEG C ~ 360 DEG C, and in this temperature range, one is be conducive to catalyst granules to show Brownian movement feature, thus accelerator activator particles collision and coalescent; Two is the viscosity that effectively can reduce continuous phase (slurry oil), reduces the resistance to catalyst granules sedimentation, and according to Stokes' law, the viscosity of continuous phase and sedimentation (or floating) speed are inversely proportional to, and which adds sinking speed; Three is the density reducing slurry oil to a certain extent, increase the density contrast between decentralized photo (catalyst granules) and continuous phase (slurry oil), according to Stokes' law, density is directly proportional to sedimentation (or floating) speed, so just accelerates the sinking speed of catalyst granules.
Should be understood that, for those of ordinary skills, can be improved according to the above description or convert, and all these improve and convert the protection domain that all should belong to claims of the present invention.
Claims (2)
1. remove a method for catalyst solid powder in slurry oil, it is characterized in that: said method comprising the steps of:
The first step, obtains mixture with the Homogeneous phase mixing in dynamic mixer of the catalytic cracked oil pulp under certain temperature conditions in proportion by slurry oil deliming agent; Described ratio is weight ratio or volume ratio, and the addition of described slurry oil deliming agent accounts for 0.003 ~ 0.2% of described slurry oil; Certain temperature described is 50 DEG C ~ 360 DEG C;
Second step, mixture obtained for the first step is injected slurry oil settling tank from bottom and carries out sedimentation, settling temperature is 50 DEG C ~ 360 DEG C; Described bottom to refer at the bottom of settling tank tank having living space between 2.5 meters of cross sections more than at the bottom of cross section to tank.
2. a kind of method removing catalyst solid powder in slurry oil according to claim 1, is characterized in that: dynamic mixer adopted in a first step can be pipe line type high-shear dispersing emulsifying machine, mulser, homogenizer, homogeneous emulsifying machine etc.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510731522.3A CN105251246A (en) | 2015-11-03 | 2015-11-03 | Method for removing catalyst solid powder in oil slurry |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510731522.3A CN105251246A (en) | 2015-11-03 | 2015-11-03 | Method for removing catalyst solid powder in oil slurry |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105251246A true CN105251246A (en) | 2016-01-20 |
Family
ID=55091346
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510731522.3A Pending CN105251246A (en) | 2015-11-03 | 2015-11-03 | Method for removing catalyst solid powder in oil slurry |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105251246A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108611117A (en) * | 2018-05-04 | 2018-10-02 | 成都合睿升石化科技有限责任公司 | A kind of catalytic cracked oil pulp processing method and system |
| CN110093176A (en) * | 2018-01-30 | 2019-08-06 | 深圳市科拉达精细化工有限公司 | A kind of method of purified treatment coal tar |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1330129A (en) * | 2001-06-25 | 2002-01-09 | 浙江江南工贸集团股份有限公司 | Settling process for separating catalyst powder from catalytically cracked oil |
| CN101670199A (en) * | 2009-09-21 | 2010-03-17 | 段华山 | Capturing settling agent and method for removing catalyst solid powder in oil slurry |
| US20100163499A1 (en) * | 2008-12-30 | 2010-07-01 | Odueyungbo Seyi A | Optimizing solid / liquid separation with solvent addition |
| CN102585895A (en) * | 2012-03-14 | 2012-07-18 | 李志英 | Separation method for solid particles in catalytic slurry oil |
| CN104046382A (en) * | 2013-03-15 | 2014-09-17 | 中国石油天然气股份有限公司 | Method for removing catalyst from catalytic cracking oil slurry |
-
2015
- 2015-11-03 CN CN201510731522.3A patent/CN105251246A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1330129A (en) * | 2001-06-25 | 2002-01-09 | 浙江江南工贸集团股份有限公司 | Settling process for separating catalyst powder from catalytically cracked oil |
| US20100163499A1 (en) * | 2008-12-30 | 2010-07-01 | Odueyungbo Seyi A | Optimizing solid / liquid separation with solvent addition |
| CN101670199A (en) * | 2009-09-21 | 2010-03-17 | 段华山 | Capturing settling agent and method for removing catalyst solid powder in oil slurry |
| CN102585895A (en) * | 2012-03-14 | 2012-07-18 | 李志英 | Separation method for solid particles in catalytic slurry oil |
| CN104046382A (en) * | 2013-03-15 | 2014-09-17 | 中国石油天然气股份有限公司 | Method for removing catalyst from catalytic cracking oil slurry |
Non-Patent Citations (1)
| Title |
|---|
| 陈俊杰: "用沉降助剂脱除催化裂化油浆中的催化剂粉末", 《石油炼制与化工》 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110093176A (en) * | 2018-01-30 | 2019-08-06 | 深圳市科拉达精细化工有限公司 | A kind of method of purified treatment coal tar |
| CN108611117A (en) * | 2018-05-04 | 2018-10-02 | 成都合睿升石化科技有限责任公司 | A kind of catalytic cracked oil pulp processing method and system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103242881B (en) | The method of separate bitumen class material from coal directly-liquefied residue | |
| CN101475820A (en) | Purification method for coal pitch | |
| CN101824329A (en) | Novel process for eliminating quinoline insoluble substances in coal tar medium temperature pitch | |
| CN103979768B (en) | Method for tempering oily sludge blended with coal water slurry | |
| CN103436280B (en) | Coal directly-liquefied residue is utilized to prepare the method for coke | |
| CN101787298A (en) | Coal art pitch purification method | |
| CN105154154A (en) | Ultrafine coal water slurry preparation method | |
| CN105251246A (en) | Method for removing catalyst solid powder in oil slurry | |
| CN103509572B (en) | A kind of technique utilizing solvent method to prepare high-quality coal-based needle coke | |
| CN106883871A (en) | A kind of production method of needle-shape coke raw material | |
| CN106318440A (en) | Catalyzing and cracking slurry oil settling agent and preparation method and application thereof | |
| CN105482850A (en) | System device for producing needle coke crude oil through catalytic slurry oil | |
| CN106281449B (en) | A kind of method and system of coal tar production light Fuel and needle coke | |
| CN102268277B (en) | Method for extracting hydrocarbon oil from oil sand and producing ceramsite | |
| CN103102932B (en) | Hydrocarbon modification separation method | |
| CN103509574B (en) | Process for preparing high-quality coal-series needle-coke | |
| CN101691427A (en) | Blending-process method for producing environment-friendly rubber oil | |
| CN103102934A (en) | Pretreatment method for inferior heavy oil | |
| CN107459825B (en) | A kind of hard grades of bitumen incremental agent and preparation method thereof | |
| CN101693772B (en) | Method for producing environment-friendly rubber oil through blending method | |
| CN108611114B (en) | Method for extracting oil residue of coal-to-liquid | |
| CN104164247A (en) | Method for separating light component oil and solid slag from medium-low temperature heavy coal tar, and application of solid slag in bonding semi-coke to prepare briquette and formcoke by | |
| CN103923688A (en) | Method for removing catalyst solid particle from catalytic oil slurry | |
| CN103881750B (en) | A kind of coal tar hydrogenation process of maximum using coal tar residue | |
| CN107916122A (en) | A kind of Biological asphalt and preparation method thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20160120 |