CN101892065B - Coal tar processing method - Google Patents
Coal tar processing method Download PDFInfo
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- CN101892065B CN101892065B CN 201010003280 CN201010003280A CN101892065B CN 101892065 B CN101892065 B CN 101892065B CN 201010003280 CN201010003280 CN 201010003280 CN 201010003280 A CN201010003280 A CN 201010003280A CN 101892065 B CN101892065 B CN 101892065B
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- Prior art keywords
- coal tar
- oil
- temperature
- washing section
- tar
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- 239000011280 coal tar Substances 0.000 title claims abstract description 68
- 238000003672 processing method Methods 0.000 title abstract 3
- 238000005406 washing Methods 0.000 claims abstract description 30
- 238000004939 coking Methods 0.000 claims abstract description 24
- 238000000034 method Methods 0.000 claims description 28
- 238000000926 separation method Methods 0.000 claims description 23
- 239000011269 tar Substances 0.000 claims description 9
- 241000282326 Felis catus Species 0.000 claims 1
- 238000005194 fractionation Methods 0.000 claims 1
- 238000010438 heat treatment Methods 0.000 abstract description 4
- 239000010426 asphalt Substances 0.000 abstract description 3
- 238000007599 discharging Methods 0.000 abstract 2
- 238000009835 boiling Methods 0.000 description 9
- 239000003245 coal Substances 0.000 description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 239000007788 liquid Substances 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 239000005864 Sulphur Substances 0.000 description 3
- 239000002283 diesel fuel Substances 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 238000000197 pyrolysis Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 230000001934 delay Effects 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000013618 particulate matter Substances 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 239000011294 coal tar pitch Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000004508 fractional distillation Methods 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a coal tar processing method, which comprises the following steps of: feeding coal tar into a fractionating tower T, setting a washing section at a position above a coal tar feeding hole of the fractionating tower T, discharging washing section outside throwing oil from the washing section, and discharging residual oil from the bottom of the fractionating tower T; and further heating the washing section outside throwing oil to a temperature T1, and coking the heated washing section outside throwing oil and the residual oil at a temperature T2 together, wherein the temperature T1 is higher than the temperature T2. The coal tar processing method has the advantages of improving the flexibility of controlling the asphalt content of lightweight distillate oil and effectively reducing the exit temperature of a residual oil heating furnace.
Description
Technical field
The present invention relates to a kind of coal tar working method, in being particularly suitable for, sepn process and the coking of coalite tar.
Background technology
As everyone knows, in pyrolysis of coal or coal generating gas or other process, coalite tar contains a large amount of lightweight oil components that is suitable for hydrocracking and (is lower than 510 ℃ petroleum naphtha component such as conventional boiling point, diesel component, the wax oil component), simultaneously, contain a large amount of bituminous matters in coalite tar or its residual oil, ash content and particulate matter, production run shows, because the coal tar fractional distillation tower adopts the charging process furnace usually, liquid internal reflux amount is very little in the opening for feed upper column, when washing section is set, in tower, extract partially liq out, return tower internal upper part position then and increase this tower section liquid flow rate, ash content or particle in the washing upstream, ash content and particulate matter accumulating rate are fast, need regular break-down maintenance, change tower feed zone upper column internals, the flow passage that cleaning is stopped up.
One of purpose of the present invention is to provide a kind of coal tar separation method, produces washing section and gets rid of oil outward, reduces ash content and particle concentration in the circulation cleaning oil, improves the handiness of control light ends oily bitumen matter content.
On the other hand, the residual oil of centering, coalite tar carries out coking and adds man-hour, after washing section gets rid of oil outward and is heated to temperature T 1, with temperature be the residual oil of T2, carry out coking together, temperature T 1 can effectively reduce residual oil furnace outlet temperature than temperature T 2 height, delays the coking speed of residual oil in heating furnace tube.
Two of purpose of the present invention is to provide a kind of coal tar to separate and the residuum coking method.
Similar approach of the present invention is not appeared in the newspapers.
Summary of the invention
A kind of coal tar separation method of the present invention, use separation column that coal tar is separated into light ends oil and residual oil, it is characterized in that: coal tar enters separation column T, the above position of coal tar mouth at separation column T arranges washing section, washing section is discharged washing section and is got rid of oil outward, and separation column T discharges residual oil in the bottom.
Feature of the present invention further is: washing section gets rid of oil outward mainly to be made up of wax oil component and residue fraction, be heated to temperature T 1 after, with temperature be the residual oil of T2, carry out coking together, temperature T 1 is than temperature T 2: generally high at least 10 ℃, high at least 30 ℃ usually.
Feature of the present invention further is: the working pressure of separation column T be negative pressure, generally be lower than 0.06MPa, be usually less than 0.04MPa.
Feature of the present invention further is: coal tar can be from the coal tar of middle temperature process of coking or from coal tar or coal-tar middle oil or the coalite tar of semi-coking process.
Embodiment
Below describe the present invention in detail.
Pressure of the present invention refers to absolute pressure.
Conventional boiling point of the present invention refers to vapour, the liquid equilibrium temperature of material under a barometric point.
Conventional liq hydrocarbon of the present invention refers to the hydro carbons that is in a liquid state under the normal condition, comprises the hydro carbons that pentane and boiling point thereof are higher.
Proportion of the present invention unless stated otherwise, refers to the ratio of water-mass density under fluid density and normal pressure under normal pressure, the 15.6 ℃ of conditions, the 15.6 ℃ of conditions.
The composition of component of the present invention or concentration or content value unless stated otherwise, are the weight basis value.
Coal tar of the present invention, refer to and contain the coal tar that is suitable for the hydro-upgrading component, it is from the coal-tar products of pyrolysis of coal or coal generating gas or other process, coal tar of the present invention can be from the coal tar of middle temperature process of coking or from coal tar or coal-tar middle oil or the coalite tar of semi-coking process, coal tar of the present invention contains the residue fraction that is rich in the coal-tar pitch component.
Therefore, coal tar of the present invention, it can be the by product (coalite tar) of coal generating gas, also can be coal coking pyrolysis of coal process by product coal tar or the coal tar fraction of (comprising semi-coking, middle temperature process of coking), coal tar of the present invention can also be the mixing oil of above-mentioned coal tar.
Because raw coal character and coking or gas-making process condition all change within the specific limits, the coal tar oil properties also changes within the specific limits.Coal tar oil properties proportion of the present invention is generally 0.89～1.15, and usually metal content is that 5～80PPm, sulphur content are 0.1～0.4%, nitrogen content is 0.6～1.6%.Coal tar of the present invention, inorganic water-content is 0.2～5.0% sometimes, sometimes organic oxygen level be 2.5～11%, especially be 3.5～10%, be 5～10% more particularly.
According to the present invention, before described coal tar separates, the process of passing through the filtering solid particulate usually.
Residual oil of the present invention refers to coal tar residual oil, mainly is higher than 510 ℃ component by conventional boiling point and forms.
Coal-tar naphtha cut of the present invention refers to the coal tar fraction that conventional boiling point is generally 60～220 ℃, is generally 60～200 ℃.
Coal tar diesel oil distillate of the present invention refers to the coal tar fraction that conventional boiling point is generally 160～390 ℃, is generally 180～370 ℃.
Coal tar wax oil cut of the present invention refers to the coal tar fraction that conventional boiling point is generally 350～530 ℃, is generally 350～510 ℃.
Coal tar light ends oil of the present invention refers to the coal tar fraction that conventional boiling point is generally 60～530 ℃, is generally 60～510 ℃, and therefore, it can be coal-tar naphtha cut, coal tar diesel oil distillate, coal tar wax oil cut or its mixing oil.
A kind of coal tar working method of the present invention, use separation column that coal tar is separated into light ends oil and residual oil, coal tar enters separation column T, in the above position of coal tar mouth of separation column T washing section is set, washing section is discharged washing section and is got rid of oil outward, and separation column T discharges residual oil in the bottom.
According to the present invention, washing section gets rid of oil outward mainly to be made up of wax oil component and residue fraction, be heated to temperature T 1 after, with temperature be the residual oil of T2, carry out coking together, temperature T 1 is than temperature T 2 height.
According to the present invention, temperature T 1 is than temperature T 2: generally high at least 10 ℃, high at least 30 ℃ usually.
According to the present invention, the working pressure of separation column T be negative pressure, generally be lower than 0.06MPa, be usually less than 0.04MPa.
The invention has the advantages that:
1. produce washing section and get rid of oil outward, reduce ash content and particle concentration in the cycles of washing oil, improved the handiness of control light ends oily bitumen matter content.
2. the residual oil of centering, coalite tar carries out coking and adds man-hour, after washing section gets rid of oil outward and is heated to temperature T 1, with temperature be the residual oil of T2, carry out coking together, temperature T 1 can effectively reduce residual oil furnace outlet temperature than temperature T 2 height, delays the coking speed of residual oil in heating furnace tube.
Embodiment
Coal-tar middle oil character sees Table 1, adopts the present invention to separate, and separation column is divided into upper and lower two sections, and the separation column epimere is rectifying section, and the separation column hypomere comprises washing section, coal tar raw material flash zone and water vapor stripping stage.Fractionator overhead pressure is 0.02MPa, and all coal tar are separated into overhead oil, stage casing, tower top that return tank of top of the tower discharges and extract oil (diesel oil), stage casing, tower bottom out and extract oil (wax oil), washing section out and get rid of residual oil at the bottom of oil and the tower outward.After washing section gets rid of oil outward and is heated to temperature T 1, be that the residual oil of T2 mixes the back temperature and is with temperature, carry out coking together, temperature T 1 effectively reduces residual oil furnace outlet temperature than temperature T 2 high 50 ℃ of degree.
Table 1 dehydration back coal tar lightweight oil analytical data
| Project | Lightweight oil |
| Density (20 ℃), kg/m 3 | 0.9822 |
| Boiling range, ℃ (D2287) | |
| IBP/10％ | 165/222 |
| 30％/50％ | 289/332 |
| 70％/90％ | 366/407 |
| 95％/EBP | 430/524 |
| Sulphur, % | 0.13 |
| Nitrogen, % | 0.7659 |
| C/H | 83.37/9.16 |
| Condensation point, ℃ | 10 |
| Viscosity (100 ℃), mm/s 2 | 3.467 |
| Carbon residue, % | 0.47 |
| Acid number, mgKOH/g | 0 |
| Heavy metal, ppm | |
| Fe | 40.47 |
| Na | 0.37 |
| Ni | 0.0143 |
| V | 0.0252 |
Table 2 coal-tar residue oil analysis data
| Project | Numerical value |
| Sulphur content, % | 0.40 |
| Nitrogen content, % | 0.8519 |
| The C/H weight ratio | 89.1/5.90 |
| Carbon residue, % | 37.8 |
| Softening temperature (ring and ball method), ℃ | 106 |
| Ductility (25 ℃), cm | 0 |
Table 3 component content of coal tar
| The component title | Yield, % | Remarks |
| Water | 4.22 | |
| Lightweight oil | 83.77 | |
| Residual oil | 12.03 | |
| Add up to | 100.00 |
Table 4 embodiment operational condition table
| Sequence number | Technical scheme | Embodiment | |
| 1 | Charging furnace operation condition | ||
| 1.1 | Feed rate, kg/h | 26101 | |
| 1.2 | The furnace outlet temperature, ℃ | 360 | |
| 1.3 | Furnace outlet pressure, MPa | 0.07 | |
| 2 | The separation column operational condition | ||
| 2.1 | Total cooling load, MMkcal/h | 5.5 | |
| 2.2 | Top pressure, MPa | 0.020 | |
| 2.3 | Head temperature, ℃ | 105 | |
| 2.4 | Reflux temperature, ℃ | 40 | |
| 2.5 | First side line | ||
| Extract temperature out, ℃ | 178 | ||
| ASTMD86,5% distillates a temperature, ℃ | 249 | ||
| ASTMD86,95% distillates a temperature, ℃ | 337 | ||
| 2.6 | Second side line | ||
| ASTMD86,5% distillates a temperature, ℃ | 354 | ||
| ASTMD86,95% distillates a temperature, ℃ | ≮495 | ||
| 2.7 | Bottom temp, ℃ | 300 | |
| 2.8 | Bottom water stripping steam flow, kg/h | 2468 | |
| 2.9 | The residual oil flow, kg/h | 2794 | |
| 2.10 | The washing oil internal circulating load, kg/h | 20000 | |
| 2.11 | Washing oil is the amount of getting rid of outward, kg/h | 1062 |
Although this paper only enumerates an embodiment, be enough to show effect of the present invention.
Claims (9)
1. coal tar working method is characterized in that:
1. use separation column that coal tar is separated into light ends oil and residual oil, coal tar enters separation column T, the above position of coal tar mouth at separation column T arranges washing section, washing section is discharged washing section and is got rid of oil outward, washing section gets rid of oil outward mainly to be made up of wax oil component and residue fraction, and separation column T discharges residual oil in the bottom;
2. in the coking part, washing section gets rid of oil outward, and to be heated to temperature T 1 back be that the residual oil of T2 carries out coking with temperature, and temperature T 1 is than at least 10 ℃ of temperature T 2 height.
2. method according to claim 1 is characterized in that:
Temperature T 1 is than at least 30 ℃ of temperature T 2 height.
3. method according to claim 1 and 2 is characterized in that:
The cat head working pressure of separation column T is negative pressure.
4. method according to claim 1 and 2 is characterized in that:
The working pressure of separation column T is less than 0.06MPa.
5. method according to claim 1 and 2 is characterized in that:
The working pressure of separation column T is less than 0.04MPa.
6. method according to claim 1 and 2 is characterized in that:
Coal tar is the coal tar from middle temperature process of coking.
7. method according to claim 1 and 2 is characterized in that:
Coal tar is the coal tar from the semi-coking process.
8. method according to claim 1 and 2 is characterized in that:
Coal tar is coal-tar middle oil.
9. method according to claim 1 and 2 is characterized in that:
Coal tar is coalite tar.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010003280 CN101892065B (en) | 2010-01-10 | 2010-01-10 | Coal tar processing method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010003280 CN101892065B (en) | 2010-01-10 | 2010-01-10 | Coal tar processing method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101892065A CN101892065A (en) | 2010-11-24 |
| CN101892065B true CN101892065B (en) | 2013-08-28 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201010003280 Expired - Fee Related CN101892065B (en) | 2010-01-10 | 2010-01-10 | Coal tar processing method |
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| Country | Link |
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| CN (1) | CN101892065B (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103897727A (en) * | 2014-03-18 | 2014-07-02 | 何巨堂 | Ash-removing method for ash-containing hydrocarbon deeply-hydrogenated oil by washing |
| CN104498076B (en) * | 2014-11-06 | 2017-08-22 | 何巨堂 | A kind of method that light oil is produced in the hydrocarbon stream of self-contained heavy oil |
| CN104498077A (en) * | 2014-11-10 | 2015-04-08 | 何巨堂 | Method for preparing light oil from low-hydrogen-content oil with self-contained asphalten |
| CN104531201A (en) * | 2014-12-03 | 2015-04-22 | 何巨堂 | Method for preparing light oil from hydrocarbon material flows containing heavy oil |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1461793A (en) * | 2002-05-31 | 2003-12-17 | 中国石油化工股份有限公司 | Method of removing fine coke from coking oil gas |
| CN101575537A (en) * | 2008-05-06 | 2009-11-11 | 牟艳春 | Process for producing light and heavy fuel oil and high-quality asphalt by hydrogenating coal tar at medium and low temperature |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62192487A (en) * | 1986-02-19 | 1987-08-24 | Sumitomo Metal Ind Ltd | Method for treating coal tar |
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2010
- 2010-01-10 CN CN 201010003280 patent/CN101892065B/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1461793A (en) * | 2002-05-31 | 2003-12-17 | 中国石油化工股份有限公司 | Method of removing fine coke from coking oil gas |
| CN101575537A (en) * | 2008-05-06 | 2009-11-11 | 牟艳春 | Process for producing light and heavy fuel oil and high-quality asphalt by hydrogenating coal tar at medium and low temperature |
Non-Patent Citations (1)
| Title |
|---|
| JP昭62-192487A 1987.08.24 |
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| Publication number | Publication date |
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| CN101892065A (en) | 2010-11-24 |
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