CN101250429A - Pretreatment method of heavy poor oil - Google Patents
Pretreatment method of heavy poor oil Download PDFInfo
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- CN101250429A CN101250429A CNA2008100309518A CN200810030951A CN101250429A CN 101250429 A CN101250429 A CN 101250429A CN A2008100309518 A CNA2008100309518 A CN A2008100309518A CN 200810030951 A CN200810030951 A CN 200810030951A CN 101250429 A CN101250429 A CN 101250429A
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- distillate
- heavy poor
- poor oil
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Abstract
The invention discloses a preprocessing method for heavy poor quality oil, which comprises the following steps: evenly mixing heavy poor quality oil and distillate oil according to the mass ratio which is 1:0.2-1:4, heating up the mixture to 50-150 DEG C, simultaneously stirring 3-60min, stewing the mixed solution for 1-24h, extracting and separating out soluble material of the distillate oil and insoluble material of the distillate oil. The heavy poor quality oil of the invention has the advantages of high utilization ratio, excellent impurity removing effect, simple and easy technique and low energy consumption. When the heavy poor quality oil which is preprocessed is done with hydrogenation modification to produce fuel oil, coking of hydrogenation catalyst can be delayed, and cycle of operation of the device can be prolonged.
Description
One, technical field:
The present invention relates to heavy poor oil deep processing, particularly relate to a kind ofly before the heavy poor oil hydrogenation, from heavy poor oil, remove the pretreatment process of impurity.
Two, background technology:
In recent years, along with the minimizing day by day of petroleum resources, the world is to the continuous increase of petroleum demand amount, and crude oil price is also constantly soaring, and cheap heavy poor oil deep processing is oil and concern of coal chemical industry industry and attention extremely.
The heavy poor oil deep processing mainly contains hydrogenation and two kinds of methods of decarburization, and wherein producing high-grade fuel oil by hydro-upgrading is the important channel of improving the heavy poor oil added value and effectively utilizing heavy poor oil, has good economic benefits and environment-friendly advantage.But the difficult point of heavy poor oil hydrogenation is: 1. density is big, and is mobile poor, is unfavorable for hydroprocessing; 2. it has a large amount of metallic impurity and very easily makes poisoning of catalyst and inactivation; 3. carbon residue, ash oontent are high and also contain the strong polar compound of the polymer that is difficult to hydrogenation in a large number (benzene insoluble), very easily in interchanger, process furnace and the coking of beds top, pipeline and beds are stopped up, and device can't turn round.Therefore, must before the heavy poor oil hydrogenation, carry out pre-treatment, remove metal, carbon residue, ash content, reduce density, benzene insoluble content it.
The distillatory method is adopted in pre-treatment before the heavy poor oil hydrogenation mostly, and there is following deficiency in this method: only utilized the light ends of heavy poor oil, and the heavy ends of heavy poor oil wastes, the heavy poor oil utilization ratio is low, and the energy consumption height.
CN101045884, CN1237151C have introduced a kind of pretreatment process of heavy poor oil, are to utilize C earlier
3-C
8Distillates such as alkane the heavy poor oil raw material is carried out diasphaltene, obtain deasphalted oil and de-oiled asphalt, and then the former carried out shortening.This method adopts extraction to replace traditional distillation, and technology is simplified, but can not remove water and inorganic salt in the raw material, and de-oiled asphalt is as hydrogenation component, and raw material availability is low.
Three, summary of the invention:
The objective of the invention is to propose a kind of heavy poor oil utilization ratio height, effective elimination impurity, and the heavy poor oil pretreatment process simple, that energy consumption is low.
The objective of the invention is to be achieved through the following technical solutions: a kind of pretreatment process of heavy poor oil is characterized in that comprising the steps: 1. heavy poor oil and distillate being mixed by mass ratio in 1: 0.2～1: 4; 2. the gained mixed solution is heated to 50～150 ℃, stirs 3～60min simultaneously; 3. mixed solution leaves standstill 1～24h, and extracting and separating goes out distillate solvend and distillate insolubles.
Described heavy poor oil comprises the middle coalite tar heavy constituent of cutting behind the light constituent, the full cut of coal tar that the lurgi pressure gasification method generates or its heavy constituent, the full cut of liquefied coal coil without any processing, the liquefied coal coil heavy constituent behind the cutting light constituent.
Described distillate can be petroleum catalytic cracking solar oil and/or heavy gas oil cut, also can be in the hydrogenated oil that comes out of coal tar hydrogenating unit, middle oil distillate, the tail oil cut one or more.Distillate has good extracting power to the alkane in the heavy poor oil, aromatic hydrocarbons and most colloid, bituminous matter, and it need not separate when follow-up heavy poor oil hydrogenation, has played the effect that reduces heavy poor oil density, reduces the reactor bed temperature rise simultaneously.
Described extracting and separating is whole extraction system to be divided into the layering of carrying out after the immiscible liquid phase by polarity and density separate; Separating technology can be to stir to leave standstill settler layering separating technology, or the extraction tower continuous separation technology.
Described step 2. in, in the gained mixed solution, add entry, its addition is 0～30% of a heavy poor oil mass percent.
Described step 2. in, in the gained mixed solution, add emulsion splitter, emulsion splitter is one or more of polyethers, amine, phenols, its addition 0～500ppm.
Described distillate solvend comprises the component that can be used for hydrogenation in distillate and the heavy poor oil, and described distillate insolubles comprises the impurity that can not be used for hydrogenation in the heavy poor oil.
Adopt the present invention that heavy poor oil is carried out pre-treatment, following advantage arranged:
1. not only reduced heavy poor oil density, benzene insoluble content, and effective elimination impurity such as ash content, moisture, carbon residue, inorganic salt and mechanical impurity, help follow-up hydro-upgrading; 2. heavy poor oil utilization ratio height reaches 85～99%, remarkable in economical benefits; 3. simple for process, energy consumption is low.
Four, specific embodiments
The invention will be further described below in conjunction with embodiment.
Embodiment 1
800g liquefied coal coil＞360 ℃ cut and 160g hydrofining diesel oil are mixed (mass ratio 1: 0.2) be heated to 80 ℃, add 240ml (30%) water then, the 100ppm emulsion splitter changes over to behind the stirring 3min again and leaves standstill 2h, and layering gets 844g diesel oil solvend, water and diesel oil insolubles.Coal tar＞360 a ℃ cut utilization ratio is 85.5%.Liquefied coal coil character sees Table 1 after liquefied coal coil＞360 ℃ cut and the pre-treatment.
Liquefied coal coil character after table 1 liquefied coal coil＞360 ℃ cut and the pre-treatment
Embodiment 2
800g liquefied coal coil and 3200g catalysis solar oil are mixed (mass ratio 1: 4) be heated to 50 ℃, add 80ml (10%) water then, the 500ppm emulsion splitter leaves standstill 24h after stirring 60min again, and layering gets 3992g diesel oil solvend, water and diesel oil insolubles.The liquefied coal coil utilization ratio is 99%.Liquefied coal coil character sees Table 2 after liquefied coal coil and the pre-treatment.
Liquefied coal coil character after table 2 liquefied coal coil and the pre-treatment
Embodiment 3
Coalite tar heavy oil mixes (mass ratio 1: 0.8) with the 160g FCC heavy diesel oil and is heated to 150 ℃ in carrying 200g behind the phenol, and stirring 15min leaves standstill 1h, and layering gets diesel oil solvend 350g, diesel oil insolubles.Coalite tar heavy oil utilization ratio is 95% in carrying behind the phenol.In carrying behind the phenol after coalite tar heavy oil and the pre-treatment coal tar heavy duty oil nature see Table 3
Coal tar heavy duty oil nature after coalite tar heavy oil and the pre-treatment during table 3 is carried behind the phenol
Embodiment 4
1000g Shandong strange evaporating method coal tar heavy duty oil distillate and 2000g coal tar hydrogenating are generated oil to mix (mass ratio 1: 2) and is heated to 80 ℃, add 50ml (5%) water then, the 10ppm emulsion splitter, leave standstill 24h again after stirring 30min, layering gets 2876g hydrogenated oil solvend, water and hydrogenated oil insolubles.Coal tar heavy duty oil distillate utilization ratio is 87.6%.The coal tar heavy duty oil nature sees Table 4 after coal tar heavy duty oil distillate and the pre-treatment
Coal tar character after table 4 Shandong strange evaporating method coal tar heavy duty oil distillate and the pre-treatment
From example 1,2,3,4 as can be seen, coal tar through mobile after the pre-treatment and density be improved significantly; Carbon residue, ash content, metal, benzene insoluble content significantly reduce, for next step hydro-upgrading has been created advantageous conditions.
Claims (6)
1. the pretreatment process of a heavy poor oil is characterized in that: include following steps: 1. heavy poor oil and distillate were mixed by mass ratio in 1: 0.2～1: 4; 2. the gained mixed solution is heated to 50～150 ℃, stirs 3～60min simultaneously; 3. mixed solution leaves standstill 1～24h, and extracting and separating goes out distillate solvend and distillate insolubles.
2. according to the pretreatment process of the described heavy poor oil of claim 1, it is characterized in that: the full cut of coal tar that described heavy poor oil can be the middle coalite tar heavy constituent of cutting behind the light constituent, the lurgi pressure gasification method generates or its heavy constituent, without in the full cut of liquefied coal coil of any processing, the liquefied coal coil heavy constituent behind the cutting light constituent one or more.
3. according to the pretreatment process of the described heavy poor oil of claim 1, it is characterized in that: described distillate is petroleum catalytic cracking solar oil and/or petroleum catalytic cracking heavy gas oil.
4. according to the pretreatment process of claim 1,3 described heavy poor oils, it is characterized in that: described distillate is one or more in the hydrogenated oil that comes out of coal tar hydrogenating unit, middle oil distillate, the tail oil cut.
5. according to the pretreatment process of the described heavy poor oil of claim 1, it is characterized in that: described step 2. in, in the gained mixed solution, add entry, its addition is 0～30% of a heavy poor oil mass percent.
6. according to the pretreatment process of the described heavy poor oil of claim 1, it is characterized in that: described step 2. in, in the gained mixed solution, add emulsion splitter, emulsion splitter is one or more of polyethers, amine, phenols, its addition 0～500ppm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008100309518A CN101250429A (en) | 2008-03-28 | 2008-03-28 | Pretreatment method of heavy poor oil |
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| CNA2008100309518A CN101250429A (en) | 2008-03-28 | 2008-03-28 | Pretreatment method of heavy poor oil |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102492451A (en) * | 2011-12-13 | 2012-06-13 | 中国矿业大学 | Extracting and separating method of high-temperature coal tar |
| WO2012120537A2 (en) * | 2011-02-11 | 2012-09-13 | Reliance Industries Ltd. | A process for improving aromaticity of heavy aromatic hydrocarbons |
-
2008
- 2008-03-28 CN CNA2008100309518A patent/CN101250429A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2012120537A2 (en) * | 2011-02-11 | 2012-09-13 | Reliance Industries Ltd. | A process for improving aromaticity of heavy aromatic hydrocarbons |
| WO2012120537A3 (en) * | 2011-02-11 | 2012-12-06 | Reliance Industries Ltd. | Process for improving aromaticity of heavy aromatic hydrocarbons |
| CN102492451A (en) * | 2011-12-13 | 2012-06-13 | 中国矿业大学 | Extracting and separating method of high-temperature coal tar |
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Application publication date: 20080827 |