CN101747926A - Method for coking heavy oil of coal tar - Google Patents
Method for coking heavy oil of coal tar Download PDFInfo
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- CN101747926A CN101747926A CN200910215113A CN200910215113A CN101747926A CN 101747926 A CN101747926 A CN 101747926A CN 200910215113 A CN200910215113 A CN 200910215113A CN 200910215113 A CN200910215113 A CN 200910215113A CN 101747926 A CN101747926 A CN 101747926A
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Abstract
A method for coking heavy oil of coal tar comprises the following steps: the heavy oil of coal tar is preheated to the temperature T1 in a heavy oil heating furnace (HF) to become logistics HFE; heat removal oil (LRO) is heated to the temperature T2 in a heat removal oil heating furnace (LF) to become logistics LFE, wherein T2 is higher than T1; and After being mixed and reaching the coking reaction temperature of the heavy oil of coal tar, the logistics HFE and the logistics LFE enter a coking reactor (CR) to complete coking reaction. Wax oil, the product from coking, can be used as the LRO. The heavy oil, the product from coking, cycles to the entrance of the HF to realize partial or complete thermal cracking. The method is especially suitable for the coking process of the medium-low temperature heavy oil of coal tar, can effectively reduce the temperature T1 at the exit of the HF, slow down coking of the HF tube and lengthen the operation cycle. When the hydrofined wax oil generated by a coal tar light distillate hydrofining unit (PH) is used as the LRO, and light oil, the product from coking, enters a hydrogenation reactor of PH, the combined process of cracking of the heavy oil of coal tar is formed.
Description
Technical field
The present invention relates to a kind of method for coking heavy oil of coal tar; Say the coking method that the present invention relates to a kind of coal-tar middle oil heavy oil or coalite tar heavy oil especially; More particularly the present invention relates to a kind of raising heat medium oil furnace outlet temperature, effectively reduce the coking method of coal tar heavy oil furnace outlet temperature.
Background technology
As everyone knows, delayed coking is a kind of sophisticated heavy oil heating pyrolyze technology, and mink cell focus is warming up to coking temperature through process furnace, enters coke drum then, finishes thermo-cracking and pyrogenic reaction in coke drum, is converted into gas, gasoline, diesel oil, wax oil and coke.Usually coke drum is provided with two at least, by the serialization of blocked operation implement device production.
Known coalite tar or coal-tar middle oil coking process are as the coking reactor charging with full cut coalite tar or coal-tar middle oil.
Yet above-mentioned technology is directly used in inferior heavy oil such as coalite tar, there is following shortcoming in coal-tar middle oil coking:
1. coalite tar last running or coal-tar middle oil last running (such as atmospheric boiling point 〉=510 ℃ cut) asphalt content height, coking starting temperature are low, as make it reach suitable pyrogenic reaction temperature with the process furnace direct heating, usually very easily high temperature section coking in furnace tubing of above-mentioned coal tar heavy fractioning under this temperature causes device shut-down etc.; Therefore, simply transplant the black petroleum products delay coking process, have above-mentioned shortcoming.
2. coalite tar or coal-tar middle oil, hydrocarbon component mainly is polycyclic aromatic hydrocarbons, colloid, bituminous matter, sulphur, nitrogen, metal content height in the molecule.The dominant characteristics of its pyrogenic reaction is pyrolysis chain rupture, disconnected side chain, produces micro-molecular gas, and polycyclic aromatic hydrocarbons transforms to colloid, and colloid is to asphaltenes conversion, bituminous matter condensation green coke, and ash content enters in the coke simultaneously.Directly use initial full cut coalite tar or coal-tar middle oil as the coking reactor charging, its consequence is that light constituent (atmospheric boiling point the is lower than 500 ℃) cracking in the coal tar produces a large amount of carburet hydrogens, from improving the liquid product yield angle, be disadvantageous, the macromolecular cleavage of considerable part go out become behind the carburet hydrogen than the more newborn unsaturated link(age)s of small molecules, keep the higher aromatic base main body of degree of unsaturation or be condensed into bigger aromatic hydrocarbons to a certain extent, in hydroconversion process, also will increase the hydrogen consumption, increase reaction heat; Charging is uneconomic as coking reactor for therefore full cut coalite tar or coal-tar middle oil.
Therefore, the present invention proposes a kind of raising heat medium oil furnace outlet temperature, effectively reduces the coking method of coal tar heavy oil furnace outlet temperature, and this method is not appeared in the newspapers.
For having any low coking raw material oil of coking starting temperature, the present invention is suitable for.
The heavy oil heat processing technique similar to technical solution of the present invention is black petroleum products twin furnace selectivity thermocracking process.Twin furnace selectivity thermocracking process, two stoves are set with the weight charging of reacting by heating tower respectively, stock oil directly enters the separation column bottom during operation, steam the gasoline in the contained a small amount of lightweight oil and reaction product in the raw material with the heat exchange of tower charging oil gas, heavy cycle oil at the bottom of the formation tower behind the diesel oil, extract light cycle oil out at the tower middle part, both are sent to the light oil process furnace respectively, heavy oil heater is (for avoiding coking in boiler tube, so will be light, heavy cycle oil is heated to differing temps respectively in two stoves), enter reaction tower then and carry out heat cracking reaction, temperature of reaction is 485～500 ℃, pressure 1.8～2.0MPa; Reaction product enters the separation column fractionation after flashing tower is told cracking-residuum, gasoline and diesel oil overall yield are about 60～65%, and gasoline octane rating lower (motor-method octane number about 55～60) and stability are poor; Condensation point of diesel oil-20 ℃ is so that-30 ℃, cetane value about 60; Thermal cracking residue is a good raw material of producing needle coke.This technology does not produce coke, and it is very big that its product property, operational condition and coking differ.
Therefore, the object of the present invention is to provide a kind of raising heat medium oil furnace outlet temperature, effectively reduce the coking method of coal tar heavy oil furnace outlet temperature.
Summary of the invention
A kind of method for coking heavy oil of coal tar of the present invention is characterized in that comprising following steps:
1. described coal tar heavy oil is preheated to temperature T 1 at heavy oil heater HF becomes logistics HFE;
2. heat medium oil LRO is heated to temperature T 2 at heat medium oil process furnace LF becomes logistics LFE, and T2 is higher than T1;
3. reach the coking heavy oil of coal tar temperature of reaction after logistics HFE and logistics LFE mix and enter coking reactor CR generation pyrogenic reaction;
4. the oily vapour of coking reactor CR discharge enters coking product oil vapour Separation and Recovery part RR.
Feature of the present invention further is: 5. at least a portion coking product wax oil uses as heat medium oil.
Feature of the present invention further is: 6. at least a portion coking product heavy oil enters coking reactor CR after being circulated to heavy oil heater HF heating.
Feature of the present invention further is: 6. at least a portion coking product heavy oil is circulated to heavy oil heater HF inlet and mixes with coal tar heavy oil.
Feature of the present invention further is: temperature T 2 is higher at least 10 ℃ than temperature T 1.
Feature of the present invention further is: 1. logistics HFE temperature T 1 is 375～515 ℃, and pressure is 0.15～1.0MPa; 2. logistics LFE temperature T 2 is 425～600 ℃, and pressure is 0.15～2.0MPa; Temperature T 2 is higher at least 10 ℃ than temperature T 1; 3. the pyrogenic reaction temperature that reaches after logistics HFE and the logistics LFE mixing is 425～520 ℃, and pyrogenic reaction pressure is 0.15～1.0MPa.
Feature of the present invention further is: 4. at Separation and Recovery part RR, pyrogenic reaction generates oily vapour and enters separation column.
Feature of the present invention further is: 4. at Separation and Recovery part RR, it is gas and oil through the condensation refrigerated separation that pyrogenic reaction generates oily vapour;
Feature of the present invention further is: 4. at Separation and Recovery part RR, pyrogenic reaction generates oily vapour and is separated into deep fat vapour and deep fat at the high temperature separate part; Deep fat vapour is separated into normal temperature oil gas and normal temperature oil at the normal temperature separate part.
Feature of the present invention further is: 4. at Separation and Recovery part RR, pyrogenic reaction generates oily vapour and is separated into one-level deep fat vapour and one-level deep fat at one-level high temperature separate part; The one-level deep fat is separated into secondary deep fat vapour and secondary deep fat at secondary high temperature separate part; Secondary deep fat vapour is separated into normal temperature oil gas and normal temperature oil at the normal temperature separate part.
Feature of the present invention further is: 3. pyrogenic reaction partly is provided with two coking reactor blocked operations, the complete operation cycle of coking reactor comprises a green coke stage, a decoking stage, and the decoking stage comprises to vacuumize reclaims oily vapour step in the coking reactor.
Feature of the present invention further is: original coal tar obtains mainly being lower than the coal tar benzoline that 510 ℃ of components form and mainly being higher than the coal tar heavy oil that 510 ℃ of components are formed by atmospheric boiling point by atmospheric boiling point at the coal tar separate part, and at least a portion hydrogenation wax oil that the hydro-refining unit PH of described coal tar benzoline obtains is used as heat medium oil.
Feature of the present invention further is: the hydrogenator that coking product lightweight oil enters the hydro-refining unit PH of coal tar benzoline contacts with catalyzer.
Feature of the present invention is that further the preferable operational condition of each step is: 1. logistics HFE temperature T 1 is 400～460 ℃, and pressure is 0.15～0.8MPa; 3. the pyrogenic reaction temperature that reaches after logistics HFE and the logistics LFE mixing is 450～520 ℃, and pyrogenic reaction pressure is 0.15～0.8MPa.
Feature of the present invention is that further the operational condition of optimization is: 1. logistics HFE temperature T 1 is 400～460 ℃, and pressure is 0.15～0.25MPa; 3. the pyrogenic reaction temperature that reaches after logistics HFE and the logistics LFE mixing is 460～495 ℃, and pyrogenic reaction pressure is 0.15～0.25MPa.
Embodiment
Below describe the present invention in detail.
Pressure of the present invention is absolute pressure.
Conventional boiling point of the present invention refers to the vapor-liquid equilibrium temperature of material under a barometric point.
Conventional gas hydrocarbon of the present invention refers to and is the gasiform hydro carbons under the normal condition, comprises methane, ethane, propane, butane.
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.
Petroleum naphtha of the present invention refers to conventional boiling point and is lower than 200 ℃ conventional liq hydrocarbon.
It is 200～375 ℃ hydro carbons that diesel component of the present invention refers to conventional boiling point.
It is 375～530 ℃ hydro carbons that wax oil component of the present invention refers to conventional boiling point.
It is hydro carbons more than 530 ℃ that residue fraction of the present invention refers to conventional boiling point.
It is hydro carbons more than 510 ℃ that heavy oil component of the present invention refers to conventional boiling point.
The composition of component of the present invention or concentration or content or yield value unless stated otherwise, are the weight basis value.
Original coal tar separation device obtains mainly being lower than coal tar benzoline that 510 ℃ of components form and mainly being higher than the coal tar heavy oil that 510 ℃ of components are formed by atmospheric boiling point by atmospheric boiling point.
Coal tar benzoline of the present invention contains petroleum naphtha component, diesel component, wax oil component, one or several component in the heavy constituent more usually.Coal tar benzoline of the present invention can be a product, also can be two or more narrow fraction products, also can be the product in a plurality of narrow fraction products or the mixture of several products.
Coal tar heavy oil of the present invention, refer to mainly and be higher than the coal tar heavy oil that 510 ℃ of components are formed by atmospheric boiling point, usually mainly refer to coal-tar middle oil heavy oil or coalite tar heavy oil, contain a large amount of polycyclic aromatic hydrocarbonss, colloid, bituminous matter, ash content, metal.
Heat medium oil LRO of the present invention refers to the coking temperature than the high oil product of coking temperature that cooperates the coal tar heavy oil that uses, and this coking temperature difference is the bigger the better.Simultaneously, heat medium oil LRO preferably treats cracked wax oil or heavy oil, the hydrogenation wax oil that obtains such as the hydro-refining unit PH of coal tar benzoline.
The typical coal-tar middle oil heavy oil of table 1 analytical results
| Project | The result |
| Sulphur, % | ????0.43 |
| Project | The result |
| Nitrogen, % | ????0.86 |
| C/H，％ | ????89.2/5.90 |
| Carbon residue, % | ????38 |
| Softening temperature (ring and ball method), ℃ | ????104 |
| Ductility (25 ℃), cm | ????0 |
| Penetration degree (25 ℃) | ????3 |
| Four components, % | |
| Bituminous matter | ????44 |
| Fragrance divides | ????7 |
| Saturated branch | ????0.7 |
| Colloid | ????14.8 |
| Total recovery, % | ????66.5 |
| Impurity, % | ????33.5 |
Coking heavy oil of coal tar of the present invention generates oil, refers to the conventional liq hydrocarbon that coal tar heavy oil raw material coking generates, and it contains petroleum naphtha component, diesel component, wax oil component and more heavy constituent usually.Coking heavy oil of coal tar of the present invention generates oil, can be a product, also can be two or more narrow fraction products, also can be the product in a plurality of narrow fraction products or the mixture of several products.
Coking heavy oil of coal tar product lightweight oil of the present invention refers to the lightweight conventional liq hydrocarbon that coal tar heavy oil raw material coking generates, and it contains petroleum naphtha component, diesel component, wax oil component usually.Coking heavy oil of coal tar product lightweight oil of the present invention can be a product, also can be two or more narrow fraction products, also can be the product in a plurality of narrow fraction products or the mixture of several products.
According to method for coking heavy oil of coal tar of the present invention, comprise following steps:
1. described coal tar heavy oil is preheated to temperature T 1 at heavy oil heater HF becomes logistics HFE;
2. heat medium oil LRO is heated to temperature T 2 at heat medium oil process furnace LF becomes logistics LFE, and T2 is higher than T1;
3. reach the coking heavy oil of coal tar temperature of reaction after logistics HFE and logistics LFE mix and enter coking reactor CR generation pyrogenic reaction;
4. the oily vapour of coking reactor CR discharge enters coking product oil vapour Separation and Recovery part RR.
At least a portion coking product wax oil can be used as heat medium oil.
Enter coking reactor CR after at least a portion coking product heavy oil can being circulated to heavy oil heater HF heating.
At least a portion coking product heavy oil can be circulated to heavy oil heater HF inlet mixes with coal tar heavy oil.
Temperature T 2 of the present invention is higher at least 10 ℃ than temperature T 1.
Each step operational condition of the present invention is: 1. logistics HFE temperature T 1 is 375～515 ℃, and pressure is 0.15～1.0MPa; 2. logistics LFE temperature T 2 is 425～600 ℃, and pressure is 0.15～2.0MPa; Temperature T 2 is higher at least 10 ℃ than temperature T 1; 3. the coking heavy oil of coal tar temperature of reaction that reaches after logistics HFE and the logistics LFE mixing is 425～520 ℃, and pyrogenic reaction pressure is 0.15～1.0MPa.
The preferable operational condition of each step is: 1. logistics HFE temperature T 1 is 400～460 ℃, and pressure is 0.15～0.8MPa; 3. the pyrogenic reaction temperature that reaches after logistics HFE and the logistics LFE mixing is 450～520 ℃, and pyrogenic reaction pressure is 0.15～0.8MPa.
Optimize operational condition be: 1. logistics HFE temperature T 1 is 400～460 ℃, and pressure is 0.15～0.25MPa; 3. the pyrogenic reaction temperature that reaches after logistics HFE and the logistics LFE mixing is 460～495 ℃, and pyrogenic reaction pressure is 0.15～0.25MPa.
A kind of operating method of separate part is: 4. at Separation and Recovery part RR, pyrogenic reaction generates oily vapour and enters separation column.Pyrogenic reaction generates oily vapour and is separated into gas, petroleum naphtha, diesel oil, wax oil, residual oil etc. at separation column.
A kind of operating method of separate part is: 4. at Separation and Recovery part RR, it is gas and oil (containing components such as petroleum naphtha, diesel oil, wax oil, residual oil) through the condensation refrigerated separation that pyrogenic reaction generates oily vapour.
A kind of operating method of separate part is: 4. at Separation and Recovery part RR, pyrogenic reaction generates oily vapour and is separated into deep fat vapour and deep fat at the high temperature separate part; Deep fat vapour is separated into normal temperature oil gas and normal temperature oil at the normal temperature separate part.Pyrogenic reaction generates oily vapour and is separated into gas, lower boiling oil (normal temperature oil), high boiling point oil (deep fat).
A kind of operating method of separate part is: 4. at Separation and Recovery part RR, pyrogenic reaction generates oily vapour and is separated into one-level deep fat vapour and one-level deep fat at one-level high temperature separate part; One-level deep fat vapour is separated into secondary deep fat vapour and secondary deep fat at secondary high temperature separate part; Secondary deep fat vapour is separated into normal temperature oil gas and normal temperature oil at the normal temperature separate part.Pyrogenic reaction generates oily vapour and is separated into gas, lower boiling oil (normal temperature oil), mid-boiling point oil (secondary deep fat), high boiling point oil (one-level deep fat).
Pyrogenic reaction of the present invention partly is provided with two coking reactor blocked operations, and the complete operation cycle of coking reactor comprises a green coke stage, a decoking stage, and the decoking stage comprises to vacuumize reclaims oily vapour step in the coking reactor.
According to the present invention, original coal tar obtains mainly being lower than coal tar benzoline that 510 ℃ of components form and mainly being higher than the coal tar heavy oil that 510 ℃ of components are formed by atmospheric boiling point by atmospheric boiling point at the coal tar separate part, at least a portion hydrofining wax oil that the hydro-refining unit PH of described coal tar benzoline obtains coker heat medium oil of the present invention, the combination thermal cracking of realization hydrogenation wax oil.
Feature of the present invention further is: the hydrogenator that coking product lightweight oil enters the hydro-refining unit PH of coal tar benzoline contacts with catalyzer.
The hydrogenation wax oil that generates as coal tar light distillate hydrogenation refining plant PH is used as heat medium oil, when coking product lightweight oil removes the PH hydrogenator, has formed coal tar heavy oil cracking combination process.
Heavy oil heater HF of the present invention and heat medium oil process furnace LF can be two-in-one process furnace, to reduce investment.
In order to bring into play the advantage of the inventive method, known suitable various coking technologies all can be used or applied in any combination, such as slowing down technology such as heating furnace tube coking.
Compare with known coal tar coking process, the invention has the advantages that:
1. reduce heavy oil heater HF tapping temperature, the significant prolongation coker cycle of operation;
2. the hydrofining tail oil can be realized its thermally splitting as heat medium oil;
3. the coking product lightweight oil hydrogenator that enters the hydro-refining unit PH of coal tar benzoline contacts with catalyzer, with easy flow process, finishes hydro-upgrading;
4. can constitute " coal tar separates--hydrofining of coal tar benzoline+coking product lightweight oil--coking heavy oil of coal tar and hydrofining tail oil thermo-cracking " combination process, compare with the hydroeracking unit that the hydrofining tail oil is set, have reduced investment, energy consumption is low, easy and simple to handle, the coal tar utilization ratio is high overall merit.
Embodiment
Obtain yield behind the coal-tar middle oil underpressure distillation separation light constituent (atmospheric boiling point is lower than 510 ℃) of character such as table 2 and be about 12.0% coal tar heavy oil, character such as table 1.
The separating obtained light constituent of coal-tar middle oil underpressure distillation (atmospheric boiling point is lower than 510 ℃) yield is about 84%, finish hydrofining through coal tar light constituent hydro-upgrading unit, the yield that obtains is about the hydrofining tail oil of 18.4% (with respect to full cut coal-tar middle oil), character such as table 3.
Hydrofining tail oil quantity is 1.53: 1 with the ratio of coal tar heavy duty weight of oil.
At the coal tar separate part, service temperature be 295 ℃ VACUUM TOWER BOTTOM oil as coal tar heavy oil, being preheated to temperature T 1 (about 430 ℃, pyrogenic reaction pressure be 0.2MPa) by heavy oil heater HF becomes coal tar heavy oil logistics HFE behind the stove; The hydrofining tail oil is heated to temperature T 2 (about 553 ℃, pressure be 0.5MPa) as heat medium oil LRO by heat medium oil process furnace LF becomes heat medium oil logistics LFE, and the temperature difference that T2 is higher than T1 is 123 ℃; It is about 495 ℃ (exceeding about 65 ℃ of T1) that logistics HFE and heat medium oil logistics LFE mix the back temperature, enters coking reactor CR then pyrogenic reaction takes place; Two serializations that the coking reactor blocked operation is realized producing, the oily vapour that coking reactor is discharged enters the separate part Separation and Recovery, and separation and recovery method can be any scheme of the present invention.
Coal tar heavy oil mixes the back temperature value by the temperature T 1 after the heavy oil heater HF preheating, hydrofining tail oil LRO by heat medium oil process furnace LF heated temperatures T2, logistics HFE and heat medium oil logistics LFE, product distribution according to expection is definite, can be preferred within the specific limits.If the expression of present embodiment data owner effectively reduces heavy oil heater HF tapping temperature.
Compare with known coal tar coking process, the present invention has significantly reduced heavy oil heater HF tapping temperature, but the significant prolongation coker cycle of operation.
As can be seen, alkane accounts for 71.7% in the hydrofining tail oil, and aromatic hydrocarbons accounts for 28.3%, and the thermal cracking process primary product is petroleum naphtha, diesel oil, light wax oil, and gas yield can be very low, because three rings, Fourth Ring aromaticity content only 3.1%, the condensation reaction ratio is very low.A large amount of free radicals and small quantity of hydrogen that hydrofining tail oil thermal cracking process produces distribute to the speed of response of coking heavy oil of coal tar process and product and will bring favourable influence.
The hydrogenator that coking product lightweight oil enters the hydro-refining unit PH of coal tar benzoline contacts with catalyzer.
Coking product heavy oil is circulated to heavy oil heater HF inlet to be mixed with coal tar heavy oil.
Present embodiment has totally formed coal tar heavy oil cracking combination process.Compare with hydrofining tail oil hydroeracking unit is set, have reduced investment, energy consumption is low, easy and simple to handle, the coal tar utilization ratio is high overall merit.
The full cut analytical results of temperature tar in the table 2
| Project | Numerical value | Remarks |
| Cut | Full cut | |
| Density (20 ℃), kg/m 3 | 1.0981 | |
| C/H，％ | 84.86/9.07 | |
| Carbon residue, % | 5.11 | |
| Heavy metal, ppm | 67 |
Table 3 hydrofining tail oil
| Project | The result |
| The cut scope, ℃ | ????＞330 |
| Density (20 ℃), g.cm -3 | ????0.8991 |
| Boiling range, ℃ | |
| IBP/10％/30％/50％ | ????247/329/356/379 |
| 70％/90％/95％/EBP | ????403/43?5/457/529 |
| Sulphur, μ g.g -1 | ????12.9 |
| Nitrogen, μ g.g -1 | ????14.5 |
| Condensation point, ℃ | ????28 |
| Aromatic hydrocarbons, % | ????28.3 |
| Monocycle | ????13.5 |
| Dicyclo | ????8.5 |
| Three rings | ????2.1 |
| Project | The result |
| The Fourth Ring | ????1.0 |
Claims (15)
1. method for coking heavy oil of coal tar is characterized in that comprising following steps:
1. described coal tar heavy oil is preheated to temperature T 1 at heavy oil heater HF becomes logistics HFE;
2. heat medium oil LRO is heated to temperature T 2 at heat medium oil process furnace LF becomes logistics LFE, and T2 is higher than T1;
3. reach the coking heavy oil of coal tar temperature of reaction after logistics HFE and logistics LFE mix and enter coking reactor CR generation pyrogenic reaction;
4. the oily vapour of coking reactor CR discharge enters coking product oil vapour Separation and Recovery part RR.
2. method according to claim 1 is characterized in that:
5. at least a portion coking product wax oil uses as heat medium oil.
3. method according to claim 1 is characterized in that:
6. at least a portion coking product heavy oil enters coking reactor CR after being circulated to heavy oil heater HF heating.
4. method according to claim 3 is characterized in that:
6. at least a portion coking product heavy oil is circulated to heavy oil heater HF inlet and mixes with coal tar heavy oil.
5. according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that:
Temperature T 2 is higher at least 10 ℃ than temperature T 1.
6. according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that:
1. logistics HFE temperature T 1 is 375～515 ℃, and pressure is 0.15～1.0MPa;
2. logistics LFE temperature T 2 is 425～600 ℃, and pressure is 0.15～2.0MPa; Temperature T 2 is higher at least 10 ℃ than temperature T 1;
3. the coking heavy oil of coal tar temperature of reaction that reaches after logistics HFE and the logistics LFE mixing is 425～520 ℃, and pyrogenic reaction pressure is 0.15～1.0MPa.
7. according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that:
4. at Separation and Recovery part RR, pyrogenic reaction generates oily vapour and enters separation column.
8. according to claim 1 or 2 or 3 or 4 described methods, it is characterized in that:
4. at Separation and Recovery part RR, it is gas and oil through the condensation refrigerated separation that pyrogenic reaction generates oily vapour.
9. method according to claim 8 is characterized in that:
4. at Separation and Recovery part RR, pyrogenic reaction generates oily vapour and is separated into deep fat vapour and deep fat at the high temperature separate part; Deep fat vapour is separated into normal temperature oil gas and normal temperature oil at the normal temperature separate part.
10. method according to claim 9 is characterized in that:
4. at Separation and Recovery part RR, pyrogenic reaction generates oily vapour and is separated into one-level deep fat vapour and one-level deep fat at one-level high temperature separate part; One-level deep fat vapour is separated into secondary deep fat vapour and secondary deep fat at secondary high temperature separate part; Secondary deep fat vapour is separated into normal temperature oil gas and normal temperature oil at the normal temperature separate part.
11., it is characterized in that according to claim 1 or 2 or 3 or 4 described methods:
3. pyrogenic reaction partly is provided with two coking reactor blocked operations, and the complete operation cycle of coking reactor comprises a green coke stage, a decoking stage, and the decoking stage comprises to vacuumize reclaims oily vapour step in the coking reactor.
12., it is characterized in that according to claim 1 or 2 or 3 or 4 described methods:
The coal tar separate part obtains mainly being lower than the coal tar benzoline that 510 ℃ of components form and mainly being higher than the coal tar heavy oil that 510 ℃ of components are formed by atmospheric boiling point by atmospheric boiling point, and at least a portion hydrofining wax oil that the hydro-refining unit PH of described coal tar benzoline obtains is used as heat medium oil.
13. method according to claim 12 is characterized in that:
The hydrogenator that coking product lightweight oil enters the hydro-refining unit PH of coal tar benzoline contacts with catalyzer.
14. method according to claim 6 is characterized in that:
1. logistics HFE temperature T 1 is 400～460 ℃, and pressure is 0.15～0.8MPa;
3. the pyrogenic reaction temperature that reaches after logistics HFE and the logistics LFE mixing is 450～520 ℃, and pyrogenic reaction pressure is 0.15～0.8MPa.
15. method according to claim 14 is characterized in that:
1. logistics HFE temperature T 1 is 400～460 ℃, and pressure is 0.15～0.25MPa;
3. the pyrogenic reaction temperature that reaches after logistics HFE and the logistics LFE mixing is 460～495 ℃, and pyrogenic reaction pressure is 0.15～0.25MPa.
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| CN200910215113A CN101747926A (en) | 2009-12-26 | 2009-12-26 | Method for coking heavy oil of coal tar |
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Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5645712A (en) * | 1996-03-20 | 1997-07-08 | Conoco Inc. | Method for increasing yield of liquid products in a delayed coking process |
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2009
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Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5645712A (en) * | 1996-03-20 | 1997-07-08 | Conoco Inc. | Method for increasing yield of liquid products in a delayed coking process |
Non-Patent Citations (1)
| Title |
|---|
| 刘建明等: ""中、低温煤焦油延迟焦化的工艺研究"", 《燃料与化工》 * |
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Application publication date: 20100623 |