CN104164254A - Heavy oil processing process - Google Patents
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- CN104164254A CN104164254A CN201310192801.8A CN201310192801A CN104164254A CN 104164254 A CN104164254 A CN 104164254A CN 201310192801 A CN201310192801 A CN 201310192801A CN 104164254 A CN104164254 A CN 104164254A
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Abstract
The invention provides a heavy oil processing process. According to the process, a fresh fed material is heated in a convection section of a heating furnace, and is subjected to a reaction in a shallow thermal cracking reactor; a material delivered from the reactor is subjected to gas-liquid separation; separated liquid-phase material is returned to a coking heating furnace and is heated; the heated liquid-phase material is divided into two parts which enter a coke tower respectively from the upper part (including the top part) and from the bottom part of the coke tower, and is subjected to deep thermal reaction; produced oil gas leaves from the top of the coke tower, and is fractionated in a coking fractionation tower; and after fractionation, a part of coking heavy oil is returned as circulation oil and is subjected to the reaction again. With the process, yields of dry gas and coke can be reduced, liquid product yield can be improved, heating furnace coking can be retarded, and coking device operation period can be prolonged.
Description
Technical field
The present invention relates to the refining of petroleum technique in a kind of refining of petroleum field, relate in particular to a kind of heavy oil upgrading technique.
Background technology
Along with the development of global economy, to the demand of lightweight, clean fuel oil also rapid growth, and former oil quality along with the continuous increase of Oil extraction amount worse and worse, be mainly manifested in that density is large, viscosity is high, heavy metal content is high, sulphur content is high, nitrogen content is high, resin and asphalt content is high, this processing of the giving crude oil especially secondary processing of heavy oil has brought larger difficulty.
At present, the processing of heavy oil to be to take off charcoal technique as main, and the feature such as delay coking process has that de-charcoal is thorough, flow process simple, technology maturation, plant investment are low has become one of important process of heavy oil upgrading.But along with the viscosity of processing heavy oil increases, carbon residue improves and the increase of pitch value content etc. brought challenge to the operation of delayed coking unit, not only product distribution variation, and coking in heating furnace tube further aggravates, have influence on the long-term operation of device.
In order to improve the liquid product yield of delayed coking and to extend the on-stream time of delayed coking, refining of petroleum investigator has researched and developed relevant Technology, and various combination procesies are more concerned.
EP209225A2 discloses a kind of residual oil solvent deasphalting one delayed coking combined technical method, utilize the solvent not being recovered in de-oiled asphalt to vaporize in Furnace Tube of Coker Unit and improve the oil gas linear speed in boiler tube, to alleviate the Coking in boiler tube, and utilize delayed coking unit to reclaim the solvent in de-oiled asphalt, reach energy-conservation object.
CN00124904.5 discloses the combined method of a kind of shallow degree solvent deasphalting and delayed coking, and the part or all of and optional conventional coking raw material of deasphalted oil enters the process furnace of delayed coking unit, then enters coke drum and carries out pyrogenic reaction.The method, by after easily the small part bituminous matter of coking is taken off in residual oil, has been improved the feed properties of delayed coking unit, the liquid product yield of delayed coking is increased, and extended the on-stream time of delayed coking unit.
Patent US4455219, US4784744, US5006223, US4378288, US4518487, CN01143254.3, CN200410050791.5, CN99125284.5, CN03133538.1, CN02139673.6, CN02109408.X etc. are mainly to utilize lower boiling material part or all replace heavy recycle stock, or in coking charging, add the methods such as free radical material to improve the liquid yield of delayed coking, reduce the yield of coke.
US4443325 is the combination process that utilizes dehesion and coking, and by after the fractionation of dehesion distilled oil, dehesion residual oil is as the charging of delayed coking unit, and to improve the yield of liquid, this combination process flow process is longer, and not only plant investment is high, and its process cost is also high.
CN98117809.X discloses a kind of thermocracking process of heavy oil, is delayed coking is combined with mitigation thermocracking process, and wax tailings enters to relax in thermal cracking reactor and reacts, the fractionation together with coking oil gas of the oil gas of generation.Unconverted oil turns back to coker as turning oil.This technique has improved the yield of lightweight oil, can make diesel oil increase by 5～15 percentage points, but liquid receives and decrease, and the coking tendency of heating furnace tube is improved little.
CN98117811.1 discloses a kind of improved delay coking process, is that coking raw material oil is first relaxed to thermally splitting, obtains the low-boiling point material of 5V%～15V% as hydrogen supply agent and thinner, then enters coke drum and carries out degree of depth thermally splitting.Adopt this technique can alleviate the coking of Furnace Tube of Coker Unit, improve liquid product yield, but this processing method is made up of two process furnace, invest corresponding with energy consumption higher.
Summary of the invention
The technical problem that investment energy consumption is high, liquid receipts are lower existing in order to solve prior art, the invention provides a kind of heavy oil upgrading technique, this technique can reduce the productive rate of dry gas and coke, improves liquid product yield, slow down the coking of furnace tubing, extend the cycle of operation of delayed coking unit.
Heavy oil upgrading technique provided by the invention, comprises the following steps:
1) after the convection zone that the fresh feed after heat exchange enters coking heater is heated to 370 DEG C～450 DEG C, enter reactor through the material inlet of shallow degree thermal cracking reactor and carry out shallow degree heat cracking reaction, go out after the material of reactor mixes with from the turning oil of coking fractional distillation column, to enter knockout drum and carry out gas-liquid separation, isolated oil gas removes coking fractional distillation column, and isolated liquid phase material turns back to coking heater and continues heating;
2) step 1) in return to coking heater liquid phase material be heated to point two-way after 470 DEG C～520 DEG C and enter coke drum from the top (comprising top) of coke drum and bottom respectively and carry out the thermal response of the degree of depth through process furnace, the material that wherein enters tower from coke drum top along tower wall eddy flow and, the coke that thermal response generates is stayed in coke drum, and the oil gas that reaction generates leaves coking fractional distillation column fractionation from the top of coke drum;
3) from step 1) and step 2) oil gas after coking fractional distillation column fractionation, partly or entirely coking heavy oil returns to step 1 as turning oil) enter knockout drum.
In above-mentioned heavy oil upgrading technique, described turning oil is the coking heavy oil from coking fractional distillation column, turning oil also can be divided into two portions, part turning oil with go out to enter knockout drum after the mixing of materials of reactor and carry out gas-liquid separation, another part turning oil mixed before entering coking heater convection zone with fresh feed, then went process furnace heating.Now, just form the second heavy oil upgrading technique provided by the invention, comprised the steps:
1) fresh feed after heat exchange enters the heating of coking heater convection zone after mixing with a part for the turning oil from coking fractional distillation column, after being heated to 370 DEG C～450 DEG C, enter reactor through the material inlet of shallow degree thermal cracking reactor and carry out shallow degree heat cracking reaction, go out after the material of reactor mixes with another part of the turning oil from coking fractional distillation column, to enter knockout drum and carry out gas-liquid separation, isolated oil gas removes coking fractional distillation column, and isolated liquid phase material turns back to coking heater and continues heating;
2) step 1) in return to coking heater liquid phase material be heated to point two-way after 470 DEG C～520 DEG C and enter coke drum from the top of coke drum and bottom respectively and carry out the thermal response of the degree of depth through process furnace, the material that wherein enters tower from coke drum top along tower wall eddy flow and, the coke that thermal response generates is stayed in coke drum, and the oil gas that reaction generates leaves coking fractional distillation column fractionation from the top of coke drum;
3) from step 1) and step 2) oil gas after coking fractional distillation column fractionation, partly or entirely coking heavy oil is as turning oil, in turning oil, a part is returned to step 1) the convection zone heating that enters process furnace after mixing with fresh feed, another part returns to step 1) enter knockout drum.
Certainly, described turning oil also can all mix before entering coking heater convection zone with fresh feed, then went process furnace heating.Now, just form the third heavy oil upgrading technique provided by the invention, comprised the steps:
1) fresh feed after heat exchange enters the heating of coking heater convection zone after mixing with from whole turning oils of coking fractional distillation column, after being heated to 370 DEG C～450 DEG C, enter reactor through the material inlet of shallow degree thermal cracking reactor and carry out shallow degree heat cracking reaction, the material that goes out reactor enters knockout drum and carries out gas-liquid separation, isolated oil gas removes coking fractional distillation column, and isolated liquid phase material turns back to coking heater and continues heating;
2) step 1) in return to coking heater liquid phase material be heated to point two-way after 470 DEG C～520 DEG C and enter coke drum from the top of coke drum and bottom respectively and carry out the thermal response of the degree of depth through process furnace, the material that wherein enters tower from coke drum top along tower wall eddy flow and, the coke that thermal response generates is stayed in coke drum, and the oil gas that reaction generates leaves coking fractional distillation column fractionation from the top of coke drum;
3) from step 1) and step 2) oil gas after coking fractional distillation column fractionation, partly or entirely coking heavy oil is as turning oil, turning oil all returns to step 1) convection zone that enters process furnace after mixing with fresh feed heats.
In above-mentioned three kinds of heavy oil upgrading techniques provided by the invention:
Described fresh feed includes but not limited to one or more the mixture in turning oil and clarified oil, cracking of ethylene residual oil and the tar-bitumen etc. of extraction oil, catalytic cracking of vacuum residuum, long residuum, heavy crude, decompressed wax oil, de-oiled asphalt, deasphalted oil, residual hydrogenation heavy oil, thermal cracking residue, lube oil finishing.
Described turning oil includes but not limited to coking heavy oil and wax tailings, with the ratio of fresh feed be 0～1.5: 1.0.
Described is entering before coking heater heating through the isolated liquid phase material of knockout drum, can sneak into low-boiling point material or add free radical compounds to accelerate the coking of the mobile of boiler tube inner fluid or inhibition boiler tube, described low-boiling point material includes but not limited to coker gasoline, cooking gas and water vapor.
Described shallow degree thermal cracking reactor includes but not limited to tower reactor and shell-and-tube reactor.In the time adopting tower reactor, one or more series connection.
The feeding manner of described shallow degree thermal cracking reactor comprises bottom in and top out and two kinds of modes of upper entering and lower leaving.
The feeding temperature of described shallow degree thermal cracking reactor is 370 DEG C～450 DEG C, preferably 380 DEG C～410 DEG C; The residence time is 10min～180min, preferably 30min～120min.In the time that the inlet amount of reactor changes, can inject high-temperature water vapor in company with material from its material inlet and regulate the residence time, with the reactor coking that prevents that heavy oil excessive fragmentation from causing.
The described amount that enters the material of tower from coke drum top accounts for from coking heater and exports 25%～100% of total inventory, and preferably 50%～75%; In the time that whole materials enter tower from the top of coke drum, be blown into appropriate (account for the whole material feeding amounts of total coke drum 0.5%～3%) high-temperature water vapor from the bottom of coke drum to coke drum and, to retain green coke passage, be convenient to decoking.Above-mentioned per-cent is all weight percentage.
Described includes but not limited to from the side-fed of the above coke drum of foam layer in the top of coke drum, a green coke cycle from the charging of coke drum top; After entering coke drum, high-temperature oil gas mode with eddy flow below the tangent position of coke drum enters tower, makes gas-liquid sharp separation.
Technique of the present invention is to utilize a process furnace on existing delayed coking unit that thermal response (cracking+condensation) process of shallow degree thermal cracking process and the degree of depth is organically combined, and simultaneously divides two-way to enter tower from the top of coke drum and bottom respectively to process a kind of complete processing of heavy oil from the high-temperature material of coking heater outlet.This technique tool has the following advantages:
1. can reduce the productive rate of cooking gas and coke, improve the yield of liquid product.
2. can make process furnace radiation section charging lighting (viscosity reduces, and boiling range lightens), and the linear speed in boiler tube is increased, this is not only conducive to conduct heat, and has improved heat transfer efficiency; And can slow down the coking of boiler tube, be conducive to the long periods of time in order of device.
3. reduced the oil gas linear speed of coke drum green coke hole and responding layer, this is not only conducive to slow down the coke drum vibrations that processing charging inferior brings, and can reduce the height of foam layer, reduces the amount of carrying of coke powder.The following process of this cycle of operation to extension fixture and product is all very favourable.
4. compared with prior art, work flow is simple, less investment, and energy consumption is low.
5. pair adaptability to raw material is strong, can process heavy oil more inferior.
Brief description of the drawings
Fig. 1 is the schematic flow sheet of conventional delay coking process.
Fig. 2 is the schematic flow sheet of the first heavy oil upgrading technique provided by the invention.
In figure: 1-coking heater, the shallow degree thermal cracking reactor of 2-, 3-knockout drum, 4a, 4b-coke drum, 5-coking fractional distillation column, 6-coking heater convection zone feeding line, 7-process furnace convection zone outlet line, 8-reactor is to the gas pipeline of knockout drum, 9-knockout drum oil gas vent pipeline, 10-knockout drum liquid phase material outlet line, 11-process furnace radiation section outlet line, 11a-coke drum bottom feeding line, 11b-coke drum top feeding line, 12-coke drum oil gas vent pipeline, 13-coking fractional distillation column feeding line; 14-coking fractional distillation column heavy oil goes out tower pipeline, 15-turning oil transfer line.
Embodiment
Below in conjunction with drawings and Examples, the invention will be further described, but do not limit the scope of the invention, and those skilled in the art can, according to the requirement of the character of raw material, object product, be easy to select suitable operating parameters within the scope of the present invention.
As shown in Figure 2, fresh feed enters the convection zone heating of coking heater 1 through coking heater convection zone feeding line 6, when being heated to 370 DEG C～450 DEG C, after preferably 380 DEG C～410 DEG C, enter shallow degree thermal cracking reactor 2 through process furnace convection zone outlet line 7 and carry out shallow degree heat cracking reaction, be to stop 10min～180min under 0.3MPa～3.0Mpa in reactor gauge pressure, preferably 30min～120min, then leave reactor 2 and carry out gas-liquid separation to the gas pipeline 8 of knockout drum with remove knockout drum 3 (or claiming tundish) after the turning oil of turning oil transfer line 15 mixes from coking fractional distillation column 5 through reactor, oil gas goes coking fractional distillation column 5 to carry out fractionation through coking fractional distillation column feeding line 13 from separating tank deck after knockout drum oil gas vent pipeline 9 mixes with from the high-temperature oil gas of coke drum oil gas vent pipeline 12, reenter coking heater 1 radiation section from the liquid phase material of separating tank bottom through knockout drum liquid phase material outlet line 10 and continue heating, be divided into two-way when being heated to after 470 DEG C～520 DEG C through process furnace radiation section outlet line 11, one tunnel enters tower through coke drum bottom feeding line 11a from the bottom of coke drum 4a (or 4b) and carries out pyrogenic reaction, and another road enters tower from the top of coke drum 4a (or 34b) through coke drum top feeding line 11b, enter after tower along tower wall eddy flow and under, gas-liquid sharp separation, the material of staying in tower is proceeded pyrogenic reaction, the gauge pressure that said process maintains coke drum tower top is 0.103MPa～1.0Mpa, filling the burnt time is 3hr～48hr, the coke that pyrogenic reaction generates is stayed in coke drum, and the high-temperature oil gas that goes out coke column overhead by chilling after through pipeline 12 and air-fuel mixture from knockout drum 3, then go coking fractional distillation column to distill through coking fractional distillation column feeding line 13, the heavy oil that goes out coking Fractionator Bottom goes out tower pipeline 14 through coking fractional distillation column heavy oil and is divided into two portions, a part turns back to coking fractional distillation column the high-temperature oil gas from coke drum is carried out to cooling, washing, and another part removes knockout drum 3 as turning oil through turning oil transfer line 15.
Embodiment 1
Press the technical process shown in Fig. 2, the heavy oil I (listing in table 1) of 320 DEG C enters coking heater 1 convection zone and heats after pump pressurization, the steam injection amount of heating tube in section of convection chamber is 0.76% (to account for the weight of heavy oil, lower same), the temperature of charge of controlling heating tube in section of convection chamber outlet is 410 DEG C, and then entering shallow degree thermal cracking reactor 2 is the heat cracking reaction that stops 40.2min under 0.35MPa and carry out shallow degree in gauge pressure.
Go out after the mixture of shallow degree thermal cracking reactor 2 mixes with from the turning oil of coking fractional distillation column 5, to enter knockout drum 3 and carry out gas-liquid separation, oil gas goes coking fractional distillation column 5 fractionation.The radiation section that liquid phase turns back to coking heater 1 continues heating, injects 1.95% water vapor at radiant coil, and the outlet of still oil temperature of controlling radiant coil is 498 DEG C, is then divided into two-way and removes coke drum 4a or 4b.
High-temperature material one road from coking heater 1 radiation section outlet enters tower from the top of coke drum, and inlet amount accounts for 75% of coking total feed, enter after tower along tower wall eddy flow and under, realize the sharp separation of gas-liquid two-phase, liquid phase enters responding layer and continues reaction; And another road enters tower from the bottom of coke drum, inlet amount accounts for 25% of coking total feed.The coke that pyrogenic reaction generates is stayed in coke drum, and the oil gas that reaction generates leaves from the top of coke drum, enters coking fractional distillation column 5 carry out fractionation after chilling through main oil gas piping.
Comparative example 1
Press the technical process shown in Fig. 1, the heavy oil I (character is with embodiment 1) of 320 DEG C enters coking heater 1 convection zone heating after pump pressurization, after the material that goes out convection zone directly mixes with from the turning oil of coking fractional distillation column 5, enter knockout drum 3 and carry out gas-liquid separation, oil gas goes coking fractional distillation column 5 fractionation.The radiation section that liquid phase turns back to coking heater 1 continues heating, inject 1.91% water vapor to accelerate the flow velocity in boiler tube at radiant coil, controlling the outlet of still oil temperature of radiant coil is 498 DEG C, and then high-temperature material all enters tower (conventional coking process) and carries out pyrogenic reaction from the bottom of coke drum.The coke generating is stayed in coke drum, and reaction generates oil gas and leaves from the top of coke drum, enters coking fractional distillation column 5 carry out fractionation after chilling through main oil gas piping.
The radiation section charging fraction distribution of embodiment 1 and comparative example 1 is in table 2, and operational condition and product distribute and also list in table 3.
Find out from table 2 and table 3, embodiment 1 is compared with comparative example 1, and the boiling range of radiation section charging obviously lightens, thereby can accelerate the linear speed in boiler tube, in improving heat transfer coefficient, also can slow down tube coking; Aspect product distribution, liquid is received has increased by 2.46 percentage points, and wherein diesel oil distillate productive rate improves 1.43 percentage points, and wax tailings productive rate improves 1.78 percentage points, and the productive rate of gas, coke and gasoline fraction reduces.
The main character of table 1 embodiment 1 and comparative example 1 charging heavy oil I
Table 2 embodiment 1 and comparative example 1 process furnace radiation section charging boiling range contrast
The operational condition of table 3 technique of the present invention and existing technique and product distribute and contrast
Embodiment 2
The present embodiment is mainly investigated the variation of heavy oil I character before and after shallow degree thermally splitting.
Shallow degree thermally splitting condition is with embodiment 1.The mixture of heavy oil I after shallow degree thermally splitting is through cooling, point analysis of variance, and the product obtaining distributes and the main character of shallow degree thermally splitting heavy oil is listed in table 4.
Contrast table 1 and table 4 are found out, the heavy oil viscosity of shallow degree thermally splitting significantly reduces, dehesion rate at 100 DEG C is 74.13%, boiling range lightens, the productive rate of gas and 180 DEG C of gasoline fractions of < accounts for respectively 1.56% and 3.92% of fresh feed, has improved the feed properties of process furnace radiation section.
The product distribution of the shallow degree thermally splitting of table 4 heavy oil I and the main character of shallow degree thermally splitting heavy oil
Embodiment 3
Coking tendency after heavy oil and shallow degree thermally splitting thereof in heating furnace tube is investigated.
Test principle: adopt traditional heat dirt method (temperature differential method) to evaluate the coking tendency of heavy oil in heating furnace tube, its principle is to decline according to heat transfer efficiency after the dirty testing tube of Jiao (heating furnace tube) coking and fouling, thereby after making fluid by the dirty testing tube of Jiao, the coking tendency of heavy oil is investigated in the corresponding reduction of temperature.
Test method: when on-test, with pump, stock oil is extracted out from head tank, inputted burnt dirty testing tube.Control furnace temp is constant, and stock oil flow velocity and testing tube ingress stock oil temperature are remained unchanged in whole process of the test.In the time that test starts, burnt dirty testing tube is interior without incrustation, entire thermal resistance minimum, and the heat that process furnace is passed to fluid is maximum, thereby burnt dirty testing tube fluid outlet temperature is the highest.Along with the carrying out of test, burnt dirt deposition on test tube wall increases, and heat transmission resistance increases thereupon, and fluid gained heat reduces gradually.Under the certain condition of process furnace power, keep fluid inlet temperature and constant flow rate, fluid outlet temperature is inevitable to decline thereupon.So fluid outlet temperature when on-test when fluid outlet temperature and off-test has a temperature head Δ T, in the time that burnt dirt increases, T is larger for temperature head Δ.
The heavy oil II (character is in table 5) that process of the test is one: 180 DEG C enters with a certain amount of flow velocity through pump pressurization that to preheat stove (be convection zone and the radiation section of delayed coking full scale plant process furnace, lower same) heating, the temperature that control preheats outlet of still material is 406 DEG C, entering the shallow degree thermal cracking reactor of upflowing reacts, material stops 60min (the cold oil residence time) in reactor, and the temperature that goes out reactor is 395 DEG C.Then enter process furnace (radiation section, lower same) heating.The inlet temperature that this logistics enters process furnace is 390 DEG C, and the output rating of quick adjustment process furnace makes the temperature of outlet material start to be stabilized in 496 DEG C, and the output rating that then maintains process furnace is constant.
The heavy oil II that process of the test is two: 180 DEG C enters and preheats stove heating with a certain amount of flow velocity through pump pressurization, and the inlet temperature that control logistics enters process furnace is 390 DEG C, and below operation is with process of the test one.
The operational condition of above-mentioned test and test-results are in table 6.As seen from Table 6, under same coking evaluation test condition, adopt patent of the present invention, the coking tendency in its boiler tube obviously slows down.
The main character of table 5 embodiment 3 charging heavy oil II
Coking tendency test conditions and the result of table 6 embodiment 3
Embodiment 4
Test one: press technical process shown in Fig. 2, taking heavy oil III (character is in table 7) as fresh feed, after being heated to 495 DEG C by process furnace, divide two strands and enter coke drum, wherein upper feeding accounts for 75% of combined feed total feed, enter after tower along tower wall eddy flow and under, lower charging accounts for 25% of combined feed total feed, and concrete technology condition is in table 8.
Test two: press technical process shown in Fig. 1, enter tower (traditional delay coking process) from whole materials of furnace outlet from the bottom of coke drum, stock oil character and processing condition are in table 7 and table 8.
The main character of table 7 embodiment 4 charging heavy oil III
Two test operation conditions of table 8 embodiment 4 and effect comparison
Through analog calculation, in above-mentioned two test coke drums, the relative linear speed of green coke hole and foam layer is in table 8.As seen from Table 8, when upper feeding account for combined feed total feed 75% compared with traditional technology, liquid is received and is improved 0.89 percentage point; In coke drum, the linear speed in green coke hole is only 25% left and right of conventional delay coking process, after linear speed reduces, can weaken springing up of the interior soft burnt layer of coke drum, thereby can slow down the vibrations of coke drum; And the oil gas linear speed of foam layer in coke tower is only for adopting 77% left and right of conventional delay coking process, this has not only reduced the height of foam layer, reduce carrying of coke powder, simultaneously also can lower separation column and go out the coke powder amount of carrying of tower product, this is all beneficial to the refining of product and the coking that slows down furnace tubing.
Claims (15)
1. a heavy oil upgrading technique, is characterized in that comprising the following steps:
1) after the convection zone that the fresh feed after heat exchange enters coking heater is heated to 370 DEG C～450 DEG C, enter reactor through the material inlet of shallow degree thermal cracking reactor and carry out shallow degree heat cracking reaction, go out after the material of reactor mixes with from the turning oil of coking fractional distillation column, to enter knockout drum and carry out gas-liquid separation, isolated oil gas removes coking fractional distillation column, and isolated liquid phase material turns back to coking heater and continues heating;
2) step 1) in return to coking heater liquid phase material be heated to point two-way after 470 DEG C～520 DEG C and enter coke drum from the top of coke drum and bottom respectively and carry out the thermal response of the degree of depth through process furnace, the material that wherein enters tower from coke drum top along tower wall eddy flow and, the coke that thermal response generates is stayed in coke drum, and the oil gas that reaction generates leaves coking fractional distillation column fractionation from the top of coke drum;
3) from step 1) and step 2) oil gas after coking fractional distillation column fractionation, partly or entirely coking heavy oil returns to step 1 as turning oil) enter knockout drum.
2. heavy oil upgrading technique according to claim 1, is characterized in that: the feeding temperature of described shallow degree thermal cracking reactor is 370 DEG C～450 DEG C, and the residence time is 10min～180min.
3. heavy oil upgrading technique according to claim 2, is characterized in that: the feeding temperature of described shallow degree thermal cracking reactor is 380 DEG C～410 DEG C, and the residence time is 30min～120min.
4. heavy oil upgrading technique according to claim 1, is characterized in that: described turning oil and the ratio of fresh feed are 0～1.5: 1.0.
5. heavy oil upgrading technique according to claim 1, is characterized in that: the described amount that enters the material of tower from coke drum top accounts for from coking heater and exports 25%～100% of total inventory.
6. heavy oil upgrading technique according to claim 5, is characterized in that: the described amount that enters the material of tower from coke drum top accounts for from coking heater and exports 50%～75% of total inventory.
7. heavy oil upgrading technique according to claim 5, it is characterized in that: the described amount that enters the material of tower from coke drum top accounts for from coking heater and exports 100% of total inventory, be blown into from the bottom of coke drum 0.5%～3% high-temperature water vapor that accounts for the whole material feeding amounts of coke drum to coke drum.
8. heavy oil upgrading technique according to claim 1, is characterized in that: inject high-temperature water vapor from the material inlet of described shallow degree thermal cracking reactor in company with material.
9. heavy oil upgrading technique according to claim 1, is characterized in that: described sneaks into low-boiling point material or add free radical compounds to accelerate the coking of the mobile of boiler tube inner fluid or inhibition boiler tube before the isolated liquid phase material of knockout drum is entering the heating of coking heater radiation section.
10. heavy oil upgrading technique according to claim 9, is characterized in that: described low-boiling point material is coker gasoline, cooking gas and water vapor.
11. heavy oil upgrading techniques according to claim 1, is characterized in that: the feeding manner of described shallow degree thermal cracking reactor is bottom in and top out or upper entering and lower leaving.
12. heavy oil upgrading techniques according to claim 1, is characterized in that: described shallow degree thermal cracking reactor is tower reactor or shell-and-tube reactor.
13. heavy oil upgrading techniques according to claim 12, is characterized in that: described tower reactor is one or more series connection.
14. 1 kinds of heavy oil upgrading techniques, is characterized in that comprising the following steps:
1) fresh feed after heat exchange enters the heating of coking heater convection zone after mixing with a part for the turning oil from coking fractional distillation column, after being heated to 370 DEG C～450 DEG C, enter reactor through the material inlet of shallow degree thermal cracking reactor and carry out shallow degree heat cracking reaction, go out after the material of reactor mixes with another part of the turning oil from coking fractional distillation column, to enter knockout drum and carry out gas-liquid separation, isolated oil gas removes coking fractional distillation column, and isolated liquid phase material turns back to coking heater and continues heating;
2) step 1) in return to coking heater liquid phase material be heated to point two-way after 470 DEG C～520 DEG C and enter coke drum from the top of coke drum and bottom respectively and carry out the thermal response of the degree of depth through process furnace, the material that wherein enters tower from coke drum top along tower wall eddy flow and, the coke that thermal response generates is stayed in coke drum, and the oil gas that reaction generates leaves coking fractional distillation column fractionation from the top of coke drum;
3) from step 1) and step 2) oil gas after coking fractional distillation column fractionation, partly or entirely coking heavy oil is as turning oil, in turning oil, a part is returned to step 1) the convection zone heating that enters process furnace after mixing with fresh feed, another part returns to step 1) enter knockout drum.
15. 1 kinds of heavy oil upgrading techniques, is characterized in that comprising the following steps:
1) fresh feed after heat exchange enters the heating of coking heater convection zone after mixing with from whole turning oils of coking fractional distillation column, after being heated to 370 DEG C～450 DEG C, enter reactor through the material inlet of shallow degree thermal cracking reactor and carry out shallow degree heat cracking reaction, the material that goes out reactor enters knockout drum and carries out gas-liquid separation, isolated oil gas removes coking fractional distillation column, and isolated liquid phase material turns back to coking heater and continues heating;
2) step 1) in return to coking heater liquid phase material be heated to point two-way after 470 DEG C～520 DEG C and enter coke drum from the top of coke drum and bottom respectively and carry out the thermal response of the degree of depth through process furnace, the material that wherein enters tower from coke drum top along tower wall eddy flow and, the coke that thermal response generates is stayed in coke drum, and the oil gas that reaction generates leaves coking fractional distillation column fractionation from the top of coke drum;
3) from step 1) and step 2) oil gas after coking fractional distillation column fractionation, partly or entirely coking heavy oil is as turning oil, turning oil all returns to step 1) convection zone that enters process furnace after mixing with fresh feed heats.
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| CN201310192801.8A Pending CN104164254A (en) | 2013-05-15 | 2013-05-15 | Heavy oil processing process |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108546560A (en) * | 2018-04-08 | 2018-09-18 | 中石化（洛阳）科技有限公司 | delayed coking method and device |
| CN108587683A (en) * | 2018-04-08 | 2018-09-28 | 中石化（洛阳）科技有限公司 | delayed coking method and device |
| CN110747003A (en) * | 2019-11-06 | 2020-02-04 | 中国石油化工股份有限公司 | Coke tower and delayed coking method using same |
| CN115873631A (en) * | 2021-08-27 | 2023-03-31 | 中国石油化工股份有限公司 | Method and apparatus for delayed coking |
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| CN102220165A (en) * | 2010-04-13 | 2011-10-19 | 中国石油化工集团公司 | Process for delaying coking |
| CN102899076A (en) * | 2011-07-27 | 2013-01-30 | 中国石油化工股份有限公司 | Delayed coking method |
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| CN101597518A (en) * | 2009-06-25 | 2009-12-09 | 中国石油化工集团公司 | A kind of improved delay coking process |
| CN102220165A (en) * | 2010-04-13 | 2011-10-19 | 中国石油化工集团公司 | Process for delaying coking |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108546560A (en) * | 2018-04-08 | 2018-09-18 | 中石化（洛阳）科技有限公司 | delayed coking method and device |
| CN108587683A (en) * | 2018-04-08 | 2018-09-28 | 中石化（洛阳）科技有限公司 | delayed coking method and device |
| CN110747003A (en) * | 2019-11-06 | 2020-02-04 | 中国石油化工股份有限公司 | Coke tower and delayed coking method using same |
| CN115873631A (en) * | 2021-08-27 | 2023-03-31 | 中国石油化工股份有限公司 | Method and apparatus for delayed coking |
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