CN101525544A - Heavy oil oxidation-viscosity breaking technology and double-function heavy oil processing system thereof - Google Patents
Heavy oil oxidation-viscosity breaking technology and double-function heavy oil processing system thereof Download PDFInfo
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- CN101525544A CN101525544A CN200910080355A CN200910080355A CN101525544A CN 101525544 A CN101525544 A CN 101525544A CN 200910080355 A CN200910080355 A CN 200910080355A CN 200910080355 A CN200910080355 A CN 200910080355A CN 101525544 A CN101525544 A CN 101525544A
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Abstract
The invention discloses a heavy oil oxidation-viscosity breaking technology and double-function heavy oil processing system thereof. The invention aims at protecting an oxidation and fractional distillation double-function tower as well as a heavy oil processing system comprising the double-function tower and applying the dual-function tower or the system to carry out the heavy oil oxidation-viscosity breaking. The double-function tower for oxidation and fractional distillation consists of a tower body, a water-oil double-function distributor, a tower tray, a heating coil pipe and an air-steam distributor; the tower body is provided with an inlet for asphaltum material, an inlet for viscosity breaking material, an inlet of air distribution pipe, a top outlet, a bottom outlet, a diesel outlet, a backflow inlet for viscosity breaking gasoline, a backflow inlet for viscosity breaking diesel and a water inlet. The invention has the following advantages: (1) combining technologies, saving equipment, reducing investment and occupied land; (2) two sets of technologies and strong adaptability of materials; (3) stable product quality and high pass rate; (4) integrating two sets of devices into one set, saving the control system and reducing the personnel and the cost; and (5) high oxidation effect and short time.
Description
Technical field
The present invention relates to the oxidation-viscosity breaking technology and the double-function heavy oil processing system thereof of heavy oil.
Background technology
Along with the trend of world's crude resources heaviness, poor qualityization, how to improve the processing technology of heavy oil, the economic benefit that increases heavy oil upgrading more and more comes into one's own.For the professional refinery of producing pitch and oil fuel with processing heavy crude, the based on crude character and the market requirement generally need be built two covering devices simultaneously, and viscosity breaking plant and oxidation unit are to satisfy the requirement that oil fuel and pitch are produced.Spring and summer autumn or pitch busy season of demands can be produced asphaltic products. with oxidation unit; Winter or pitch demand dull season, and when crude oil is not suitable for producing pitch, produce low-viscosity fuel oil with viscosity breaking plant.But two covering devices are a cover operation normally, another set of shut-down simultaneously, and utilization ratio of device is low, and equipment is relatively wasted.
It is vacuum residuum or the viscid bitumen that softening temperature is low, penetration degree and temperature sensitivity are big, can not satisfy customer requirements that oxidation style is produced pitch, bubbling air under the certain temperature condition, its composition is changed, softening temperature rising, penetration degree and temperature sensitivity reduce, to reach road bitumen specification index and use properties requirement.Oxidation style is produced the bituminous development and is broadly divided into three phases: intermittent type stills for air blowing stage, continous way oxidation still stage and oxidizing tower stage.Since the seventies, tower flow process is risen gradually, and newly-built oxidation unit is tower flow process entirely at present.
Viscosity breaking comes down to a kind of mild thermal cracking process, and main purpose is that the oil product with high viscosity such as atmospheric residue, vacuum residuum is a raw material, production viscosity, flash-point oil fuel up to specification, and production part light-end products.Three phases has been experienced in the development of viscosity breaking technology: downstriker reaction tower visbreaking technology, process furnace tubular type visbreaking technology and upflowing reaction tower visbreaking technology.The process characteristic of downstriker reaction tower visbreaking technology, process furnace tubular type visbreaking technology is to adopt high temperature, the operation of short reaction time, because of adopting high reaction temperature, help condensation reaction, make the coking process accelerate, but process furnace and reaction tower coking are serious, on-stream time is short, has only 1～2 month, and this technology is eliminated.The characteristics of upflowing reaction tower visbreaking technology are to adopt lower temperature of reaction and long reaction times.Because temperature of reaction is than low 30～40 ℃ of conventional visbreaking technology, the gelationus condensation reaction is suppressed substantially, compares with conventional visbreaking technology, has to improve quality product and improve the serious effect of device coking, prolong on-stream time, reduced advantages such as fuel consumption and plant investment.
Summary of the invention
Oxidation-the viscosity breaking technology and the double-function heavy oil processing system thereof that the purpose of this invention is to provide heavy oil.
The present invention protects the difunctional tower of a kind of oxidation fractionation, and protection simultaneously contains the heavy oil precessing system of described difunctional tower, and the method for protecting described difunctional tower of application or described system of processing to carry out heavy oil oxidation-viscosity breaking.
The difunctional tower of oxidation-fractionation provided by the invention, it comprises the tower body of hollow and is located at the endoceliac inner member of tower that inner member comprises: water oil difunctional sparger 3-1, column plate 3-2, heat production coil pipe 3-3 and air vapor sparger 3-4; Described tower body is provided with asphalt stock inlet 3-5, visbreaking feed(raw material)inlet 3-6, air distribution tube inlet 3-7, tower top outlet 3-8, tower bottom outlet 3-9, diesel oil outlet 3-10, visbreaking gasoline reflux inlet 3-11, visbreaking diesel oil reflux inlet 3-12 and water inlet 3-13;
The difunctional sparger 3-1 of described water oil is located at tower body chamber internal upper part; Air vapor sparger 3-4 and heat production coil pipe 3-3 are located at bottom in the tower body chamber; Heat production coil pipe 3-3 is located at air vapor sparger 3-4 top; Column plate 3-2 is located between water difunctional sparger 3-1 of oil and the heat production coil pipe 3-3;
Described tower top outlet 3-8 is located at the top of tower body; Asphalt stock inlet 3-5, air distribution tube inlet 3-7, visbreaking gasoline reflux inlet 3-11, visbreaking diesel oil reflux inlet 3-12 and water inlet 3-13 are located at the top of tower body; Visbreaking gasoline reflux inlet 3-11, visbreaking diesel oil reflux inlet 3-12 and water inlet 3-13 all are in corresponding position with the difunctional sparger 3-1 of water oil; The position of asphalt stock inlet 3-5 and air distribution tube inlet 3-7 is lower than the difunctional sparger 3-1 of water oil; Diesel oil outlet 3-10 is located at the middle part of tower body; Visbreaking feed(raw material)inlet 3-6 is located at the bottom of tower body, and the position is higher than heat production coil pipe 3-3; Tower bottom outlet 3-9 is located at the bottom of tower body, and the position is lower than air vapor sparger 3-4.
Can be provided with steam-in 3-14 on the tower body of the difunctional tower of described oxidation fractionation, described steam-in 3-14 and air vapor sparger 3-4 are in corresponding position.
In the difunctional tower of described oxidation fractionation, described column plate can be multilayer (more than two-layer), determines that according to the treatment capacity design of material generally at the 7-15 layer, the vertical range between per two described column plates can be 1200-1500mm.
In the difunctional tower of described oxidation fractionation, asphalt stock inlet 5 is positioned at different sea lines and different vertical lines with visbreaking feed(raw material)inlet 6 on tower body, in order to avoid influence the firm degree of tower body.
In the difunctional tower of described oxidation-fractionation, described column plate specifically can be conventional valve tray.
In the difunctional tower of described oxidation-fractionation, the major function of the difunctional sparger of described water oil is gone into uniform distribution behind the tower for making water or visbreaking withdrawing oil, and the conventional material sparger in the oil refining apparatus gets final product.
In the difunctional tower of described oxidation-fractionation, the major function of described air vapor sparger is gone into uniform distribution behind the tower for making air or steam, and the conventional material sparger in the oil refining apparatus gets final product.
The present invention is on the basis of oxidation unit and viscosity breaking plant, original technology is carried out organic combination, and innovative design becomes a covering device, has the difunctional of viscosity breaking and oxidized bitumen device simultaneously, it is oxidable production pitch that one covering device is realized, can produce oil fuel by visbreaking again.Not only save facility investment, save floor occupying area, production decision is more flexible simultaneously, and it is convenient that technology is switched, and intensive control further promotes original two kinds of device techniques.
The present invention also protects the oxidation-viscosity breaking double-function heavy oil processing system that contains the difunctional tower of described oxidation fractionation.
Described oxidation-viscosity breaking double-function heavy oil processing system comprises process furnace 1, visbreaking reactor 2, the difunctional tower 3 of oxidation fractionation, diesel oil stripping tower 4, fractionation return tank of top of the tower 5, saturex 6, diesel fuel tank 7, tail gas water-sealed tank 8, air compressor 9 and compressor outlet surge tank 10;
The outlet 1-3 connecting tube 11 of process furnace 1, pipeline 11 is divided into two laterals, and a lateral 11-1 is connected with the inlet 2-1 of visbreaking reactor 2, and another lateral 11-2 is connected with the asphalt stock inlet 3-5 of the difunctional tower 3 of oxidation fractionation; The outlet 2-2 of visbreaking reactor 2 is connected with the visbreaking feed(raw material)inlet 3-6 of the difunctional tower 3 of oxidation fractionation by pipeline 12; Pipeline 11-1 is provided with visbreaking Reactor inlet valve, and pipeline 12 is provided with visbreaking reactor outlet valve; Pipeline 11-2 is provided with oxidation flow process valve; Air compressor 9 is connected with the inlet 10-1 of compressor outlet surge tank 10 by pipeline 13; The outlet 10-2 of pipeline 14 1 ends and compressor outlet surge tank 10 joins, and the other end is connected with air vapor sparger 3-4 by the air distribution tube inlet 3-7 of the difunctional tower 3 of oxidation fractionation; The difunctional sparger 3-1 connecting tube 15 of water oil, pipeline 15 stretches out the difunctional tower 3 of oxidation fractionation by water inlet 3-13; The tower top outlet 3-8 connecting tube 16 of the difunctional tower 3 of oxidation fractionation, pipeline 16 is divided into two laterals, and a lateral 16-1 is connected with the inlet 5-1 of fractionation return tank of top of the tower 5, and another lateral 16-2 is connected with the gas inlet 6-2 of saturex 6; The material of fractionation return tank of top of the tower 5 reclaims outlet 5-3 connecting tube 17, pipeline 17 is divided into two laterals, a lateral 17-1 is external, and another lateral 17-2 is connected with the difunctional sparger 3-1 of water oil of the difunctional tower 3 of oxidation fractionation by the visbreaking gasoline reflux inlet 3-11 of the difunctional tower 3 of oxidation fractionation; The diesel oil outlet 3-10 of the difunctional tower 3 of oxidation fractionation is connected with the inlet 4-1 of diesel oil gas stripping column 4 by pipeline 18; The visbreaking diesel oil bypass outlet 4-3 connecting tube 19 of diesel oil vapour gas stripping column 4, pipeline 19 is connected with the difunctional sparger 3-1 of water oil of the difunctional tower 3 of oxidation fractionation by the visbreaking diesel oil reflux inlet 3-12 of the difunctional tower 3 of oxidation fractionation; The tail gas outlet 6-3 of saturex 6 is connected with the gas inlet 8-2 of tail gas water-sealed tank 8 by pipeline 20; The outlet 7-3 connecting tube 21 of diesel fuel tank 7, pipeline 21 is by being connected with the circulation diesel oil inlet 7-2 of diesel fuel tank behind the heat production coil pipe 3-3.
In described oxidation-viscosity breaking double-function heavy oil processing system, also can be provided with automatic control devices such as some variable valve according to actual needs, with the flow of material in the Controlling System etc.
In described oxidation-viscosity breaking double-function heavy oil processing system, the tower bottom outlet 3-9 of the difunctional tower 3 of described oxidation fractionation can external pitch finished product jar or residual oil finished product jar, with finished product pitch or visbreaking residue output; Described lateral 17-1 can external gasoline tank, with output gasoline; The diesel oil of described diesel oil gas stripping column 4 outlet 4-2 can external diesel oil withdrawing can, with output diesel oil; The sump oil of described saturex 6 outlet 6-4 can external slop oil tank 22, with the output sump oil.
The feed(raw material)inlet 1-1 of process furnace is used to import raw material, and fuel inlet 1-2 is used to import fuel.The waste gas outlet 5-2 of fractionation return tank of top of the tower 5 is used to export waste gas, waste gas can be re-entered the fuel inlet 1-2 of process furnace, to recycle.The water inlet 6-1 of saturex 6 is used for water is imported saturex 6.The water inlet 8-1 of tail gas water-sealed tank 8 is used for water is imported tail gas water-sealed tank 8.The additional diesel oil inlet 7-1 of diesel fuel tank 7 is used for adding diesel oil when the circulation diesel oil deficiency of diesel fuel tank.The tail gas recycle outlet 8-3 of tail gas water-sealed tank 8 is used to export tail gas, tail gas can be re-entered the fuel inlet 1-2 of process furnace, to recycle.
In described oxidation-viscosity breaking double-function heavy oil processing system, described pipeline 12 is provided with two visbreaking reactor outlet valves, near visbreaking reactor and the difunctional tower of oxidation fractionation, assembles in pipe to avoid the raw material in the oxidized bitumen technology respectively; Pipeline 11-2 is provided with two oxidation flow process valves, near pipeline 11 bifurcation with near the difunctional tower of oxidation fractionation place, assembles in pipe to avoid the raw material in the viscosity breaking technology respectively.
When carrying out viscosity breaking technology: but the steam-in 3-14 steam-out (SO) of the difunctional tower of described oxidation fractionation, with the supply heat; But described diesel oil gas stripping column 4 steam-out (SO)s are with the supply heat.
On the described pipeline 16-1, can be provided with air cooler 23, with the oil gas of cooling tower body outlet extraction.
The difunctional tower of oxidation fractionation of the present invention is that oxidizing tower and separation column are merged, and improves in design, has bifunctional characteristics.Use the difunctional tower of oxidation fractionation of the present invention, when production decision changes, only need simply switch, just can realize different process production.The difunctional tower of oxidation fractionation of the present invention is owing to increased the quantity of column plate, when oxidizing reaction, oxidising process has obtained reinforcement, make air bubble in tower, become the broken line distance to rise, the stroke lengthening, thereby the air and the duration of contact of oil reaction are increased, also reduced simultaneously the short circuit phenomenon of air bubble in uphill process, and the air pocket that in tower, is merged in the uphill process of air, column plate of every contact, just be broken into small bubbles, can keep bigger contact area and speed of response like this by column plate.Improve oxidation effectiveness, reduce oxidization time.
The present invention is on the basis of existing oxidation unit and viscosity breaking plant, carry out organic combination, innovative design newly have viscosity breaking simultaneously and the oxidized bitumen device is difunctional, one cover system is oxidable production pitch, can produce oil fuel by visbreaking again, according to the products scheme requirement of producing, carry out the complete processing switching and get final product.The present invention has following advantage:
1, technical tie-up, saving equipment reduces investment, reduces and takes up an area of.
500,000 tons of/year oxidations of a newly-built cover and visbreaking dual function system, compare with newly-built 500,000 tons of/year oxidation units of a cover and 500,000 tons of/year visbreaking units of a newly-built cover, optimization design, reduce by a process furnace, also reduce by a tower, part system shared (comprising interchanger, instrument, electric, process pipe, valve, structure etc.), a covering device is realized two covering device functions, expectation can be saved facility investment 1/4th.
2, two sets of plan is produced flexibly, two cover technologies, and adaptability to raw material is strong.
3, produce steady and constant product quality, product percent of pass height.
4, two covering devices are intensive is a cover machinery, saves Controlling System, and the minimizing personnel reduce cost.
5, oxidation effectiveness improves, and oxidization time is short, and quality product improves.
Description of drawings
Fig. 1 is the structural representation of the difunctional tower of oxidation fractionation.
Fig. 2 is the schematic flow sheet of oxidation-viscosity breaking double-function heavy oil processing system.
Embodiment
Following embodiment is convenient to understand better the present invention, but does not limit the present invention.
Experimental technique among the following embodiment if no special instructions, is ordinary method.
The application of embodiment 1, oxidation-viscosity breaking double-function heavy oil processing system
As shown in Figure 1, the difunctional tower of oxidation fractionation is the tower body of hollow and is located at the endoceliac inner member of tower that inner member comprises: the difunctional sparger 3-1 of water oil, seven layers of column plate 3-2, heat production coil pipe 3-3 and air vapor sparger 3-4; The difunctional sparger 3-1 of water oil is located at tower body chamber internal upper part; Air vapor sparger 3-4 and heat production coil pipe 3-3 are located at bottom in the tower body chamber; Heat production coil pipe 3-3 is located at air vapor sparger 3-4 top; Each layer column plate 3-2 disperses to be located between water difunctional sparger 3-1 of oil and the heat production coil pipe 3-3, and the vertical range between per two column plates is 1200-1500mm; Tower top outlet 3-8 is located at the top of tower body; Asphalt stock inlet 3-5, air distribution tube inlet 3-7, visbreaking gasoline reflux inlet 3-11, visbreaking diesel oil reflux inlet 3-12 and water inlet 3-13 are located at the top of tower body; Visbreaking gasoline reflux inlet 3-11, visbreaking diesel oil reflux inlet 3-12 and water inlet 3-13 all are in corresponding position with the difunctional sparger 3-1 of water oil; The position of asphalt stock inlet 3-5 and air distribution tube inlet 3-7 is lower than the difunctional sparger 3-1 of water oil; Diesel oil outlet 3-10 is located at the middle part of tower body; Visbreaking feed(raw material)inlet 3-6 is located at the bottom of tower body, and the position is higher than heat production coil pipe 3-3; Tower bottom outlet 3-9 is located at the bottom of tower body, and the position is lower than air vapor sparger 3-4; Steam-in 3-14 is positioned at air vapor sparger 3-4 and is in corresponding position.Asphalt stock inlet 3-5 is positioned at different sea lines and different vertical lines with visbreaking feed(raw material)inlet 3-6 on tower body.
Oxidation-viscosity breaking double-function heavy oil processing system is seen Fig. 2.It comprises process furnace 1, visbreaking reactor 2, the difunctional tower 3 of oxidation fractionation, diesel oil stripping tower 4, fractionation return tank of top of the tower 5, saturex 6, diesel fuel tank 7, tail gas water-sealed tank 8, air compressor 9 and compressor outlet surge tank 10;
The outlet 1-3 connecting tube 11 of process furnace 1, pipeline 11 is divided into two laterals, and a lateral 11-1 is connected with the inlet 2-1 of visbreaking reactor 2, and another lateral 11-2 is connected with the asphalt stock inlet 3-5 of the difunctional tower 3 of oxidation fractionation; The outlet 2-2 of visbreaking reactor 2 is connected with the visbreaking feed(raw material)inlet 3-6 of the difunctional tower 3 of oxidation fractionation by pipeline 12; Pipeline 11-1 is provided with visbreaking Reactor inlet valve, and pipeline 12 is provided with two visbreaking reactor outlet valves, near visbreaking reactor and the difunctional tower of oxidation fractionation, assembles in pipe to avoid the raw material in the oxidized bitumen technology respectively; Pipeline 11-2 is provided with two oxidation flow process valves, near pipeline 11 bifurcation with near the difunctional tower of oxidation fractionation place, assembles in pipe to avoid the raw material in the viscosity breaking technology respectively; Air compressor 9 is connected with the inlet 10-1 of compressor outlet surge tank 10 by pipeline 13; The outlet 10-2 of pipeline 14 1 ends and compressor outlet surge tank 10 joins, and the other end is connected with air vapor sparger 3-4 by the air distribution tube inlet 3-7 of the difunctional tower 3 of oxidation fractionation; The difunctional sparger 3-1 connecting tube 15 of water oil, pipeline 15 stretches out the difunctional tower 3 of oxidation fractionation by water inlet 3-13; The tower bottom outlet 3-9 external pitch finished product jar of the difunctional tower 3 of oxidation fractionation or residual oil finished product jar are to export finished product pitch or visbreaking residue; The tower top outlet 3-8 connecting tube 16 of the difunctional tower 3 of oxidation fractionation, pipeline 16 is divided into two laterals, a lateral 16-1 is connected with the inlet 5-1 of fractionation return tank of top of the tower 5, pipeline 16-1 is provided with air cooler 23, with the oil gas of cooling tower body outlet ejection, another lateral 16-2 is connected with the gas inlet 6-2 of saturex 6; The material of fractionation return tank of top of the tower 5 reclaims outlet 5-3 connecting tube 17, pipeline 17 is divided into two laterals, the external gasoline tank of lateral 17-1, with output gasoline, another lateral 17-2 is connected with the difunctional sparger 3-1 of water oil by the visbreaking gasoline reflux inlet 3-11 of the difunctional tower 3 of oxidation fractionation; Diesel oil outlet 3-10 is connected with the inlet 4-1 of diesel oil gas stripping column 4 by pipeline 18; The external diesel oil withdrawing can of diesel oil outlet 4-2 of diesel oil gas stripping column 4 is with output diesel oil; The visbreaking diesel oil bypass outlet 4-3 connecting tube 19 of diesel oil vapour gas stripping column 4, pipeline 19 is connected with the difunctional sparger 3-1 of water oil by the visbreaking diesel oil reflux inlet 3-12 of the difunctional tower 3 of oxidation fractionation; The tail gas outlet 6-3 of saturex 6 is connected with the gas inlet 8-2 of tail gas water-sealed tank 8 by pipeline 20; The external slop oil tank 22 of sump oil outlet 6-4 of saturex 6 is with the output sump oil; The outlet 7-3 connecting tube 21 of diesel fuel tank 7, pipeline 21 is by being connected with the circulation diesel oil inlet 7-2 of diesel fuel tank behind the heat production coil pipe 3-3.
The feed(raw material)inlet 1-1 of process furnace is used to import raw material, and fuel inlet 1-2 is used to import fuel.The waste gas outlet 5-2 of fractionation return tank of top of the tower 5 is used to export waste gas, and waste gas is re-entered the fuel inlet 1-2 of process furnace, to recycle.The water inlet 6-1 of saturex 6 is used for water is imported saturex 6.The water inlet 8-1 of tail gas water-sealed tank 8 is used for water is imported tail gas water-sealed tank 8.The additional diesel oil inlet 7-1 of diesel fuel tank 7 is used for adding diesel oil when the circulation diesel oil deficiency of diesel fuel tank.The tail gas recycle of tail gas water-sealed tank 8 outlet 8-3 is used to export tail gas, tail gas is re-entered the fuel inlet 1-2 of process furnace, to recycle.
In described oxidation-viscosity breaking double-function heavy oil processing system, also can be provided with automatic control devices such as some variable valve (as zero He among the figure according to actual needs
Shown in), with the flow of material in the Controlling System etc.
Above-mentioned oxidation-viscosity breaking double-function heavy oil processing system can be used to produce oxidized bitumen, also can be used to produce visbreaking residue (oil fuel).Can determine production decision according to the feedstock property and the market requirement, switch oxidation flow process or viscosity breaking flow process.
One, oxidation-viscosity breaking double-function heavy oil processing system is used to produce oxidized bitumen
When crude oil be fit to be produced pitch, and the market requirement is closed the inlet valve and the outlet valve of visbreaking reactor when vigorous, open oxidation flow process valve, oxidation-viscosity breaking double-function heavy oil processing system promptly is adjusted to oxidation and produces the bituminous system, can carry out the oxidizing process flow process, and is specific as follows:
It is 2-2.5 kilogram/cm that compressor produces pressure
2Air, behind the compressed machine outlet surge tank, send into the air vapor sparger of the difunctional tower of oxidation fractionation, the ejection back reacts with residual oil in the difunctional tower of oxidation fractionation.Fresh water enters the difunctional sparger of water oil of the difunctional tower of oxidation fractionation, introduces the cat head gas phase, and in the material, the control gas phase temperature is prevented and treated coking in sparger enters tower.Fresh water enters saturex and tail gas water-sealed tank.Residual oil (raw material) enters process furnace from the feed(raw material)inlet, be heated to 190 ℃ ± 5 ℃ after, enter the difunctional tower of oxidation fractionation.In the difunctional tower of oxidation fractionation, residual oil and air generation oxidizing reaction, owing to have column plate in the difunctional tower of oxidation fractionation, air bubble becomes the broken line distance to rise in tower, the stroke lengthening, thereby increased the duration of contact of air and residual oil reaction, also reduced the short circuit phenomenon of air bubble in uphill process simultaneously, can keep bigger contact area and speed of response.Asphaltic products. is extracted out from the tower bottom outlet of the difunctional tower of oxidation fractionation by discharge pump, squeezes into the finished product jar.Oxidized tail gas enters saturex by the tower top outlet of the difunctional tower of oxidation fractionation.The tail gas that does not coagulate enters the tail gas water-sealed tank by saturex, and the fuel inlet that the gas in the tail gas water-sealed tank is introduced process furnace by pipeline is burnt.Sump oil is introduced slop oil tank in the saturex, and recovery acts as a fuel.Diesel oil enters the heat production coil pipe of the difunctional tower of oxidation fractionation by diesel fuel tank, takes excess energy away, through the heat exchange circulation, returns diesel fuel tank again.When circulation diesel oil is not enough, to diesel fuel tank, add diesel oil from replenishing the diesel oil inlet.
The oxidation operation condition data sees Table 1.
| Parameter name (process conditions) | Service data |
| The oxidation feed amount | 40 tons/hour |
| Process furnace convection chamber temperature | 190±5℃ |
| The heating-furnace bore temperature | 700±10℃ |
| Furnace outlet temperature (feeding temperature of the difunctional tower of oxidation fractionation) | 192±5℃ |
| The difunctional column overhead pressure of oxidation fractionation | 53KPa |
| The difunctional column overhead temperature of oxidation fractionation | 128℃ |
| Temperature at the bottom of the difunctional Tata of oxidation fractionation | 190℃ |
| The liquid level of the difunctional tower of oxidation fractionation | 70％ |
| The compressor air quantity | 900m
3/ |
| Oxidization time | |
| 2 hours |
The character of residual oil raw material and finished product bituminous quality index see Table 2.
The character of table 2 residual oil raw material and finished product bituminous quality index
Two, oxidation-viscosity breaking double-function heavy oil processing system is used to produce oil fuel
When crude oil is not suitable for producing pitch, or fuel oil market is when in great demand, open the inlet valve and the outlet valve of visbreaking reactor, stop compressor, close oxidation flow process valve, oxidation-viscosity breaking double-function heavy oil processing system promptly is adjusted to the system that oil fuel is produced in viscosity breaking, can carry out the viscosity breaking flow process, and is specific as follows:
Residual oil (raw material) enters process furnace, be heated to about 397 ℃ after, enter in the visbreaking reactor, residual oil is at visbreaking reactor internal reaction (0.5MPa, 397 ℃).Residual oil behind the visbreaking flows out from the outlet of visbreaking reactor.The reaction product of visbreaking reaction enters the difunctional tower of oxidation fractionation, in the difunctional tower of oxidation fractionation, carry out fractionation, mass transfer and heat transfer on each column plate, according to material weight gradient, be divided into variant production (when needing, squeeze into quenching oil at the outlet conduit place of visbreaking reactor temperature is reduced and stopped reaction, in order to avoid cause way of escape coking.)。Cat head oil gas is extracted out by the tower top outlet of the difunctional tower of oxidation fractionation, enters air cooler, enters separation column top return tank after the cooling.Visbreaking gas in the fractionation return tank of top of the tower causes fuel system by pipeline, recycle, light oil part in the fractionation return tank of top of the tower is external to gasoline tank as gasoline products, another part is returned the difunctional tower of oxidation fractionation, the difunctional sparger of water oil through the difunctional tower of oxidation fractionation enters cat head top, reduce the overhead gas temperature, keep vapour-liquid item balance in the tower.After diesel oil is extracted out from the diesel oil outlet of the difunctional tower of oxidation fractionation, enter the diesel oil gas stripping column, a part is external to the diesel oil withdrawing can as diesel product, another part is returned the difunctional tower of oxidation fractionation, the difunctional sparger of water oil through the difunctional tower of oxidation fractionation enters cat head top, reduce the overhead gas temperature, keep vapour-liquid item balance in the tower.Visbreaking residue (oil fuel) in the difunctional tower of oxidation fractionation is extracted out from the tower bottom outlet of the difunctional tower of oxidation fractionation, squeezes into Residual Oil Tank.
Viscosity breaking operational condition data see Table 3.
Table 3 viscosity breaking operational condition
| Parameter name (process conditions) | Service data |
| The visbreaking inlet amount | 39 tons/hour |
| Process furnace convection chamber temperature | 418℃ |
| The heating-furnace bore temperature | 700℃ |
| Furnace outlet temperature (temperature in of visbreaking reactor) | 397℃ |
| Visbreaking reactor outlet temperature | 383℃ |
| Visbreaking reactor top pressure | 133KPa |
| The difunctional column overhead pressure of oxidation fractionation | 53KPa |
| The difunctional column overhead temperature of oxidation fractionation | 142℃ |
| Temperature at the bottom of the difunctional Tata of oxidation fractionation | 263℃ |
| The liquid level of the difunctional tower of oxidation fractionation | 68％ |
The quality index of the character of residual oil raw material and finished product oil fuel sees Table 4.
The character of table 4 residual oil raw material and finished product oil fuel quality index
Claims (10)
1, the difunctional tower of oxidation fractionation, it comprises the tower body of hollow and is located at the endoceliac water oil of tower difunctional sparger (3-1), column plate (3-2), heat production coil pipe (3-3) and air vapor sparger (3-4);
Described tower body is provided with asphalt stock inlet (3-5), visbreaking feed(raw material)inlet (3-6), air distribution tube inlet (3-7), tower top outlet (3-8), tower bottom outlet (3-9), diesel oil outlet (3-10), visbreaking gasoline reflux inlet (3-11), visbreaking diesel oil reflux inlet (3-12) and water inlet (3-13);
The described water difunctional sparger of oil (3-1) is located at tower body chamber internal upper part; Air vapor sparger (3-4) and heat production coil pipe (3-3) are located at bottom in the tower body chamber; Heat production coil pipe (3-3) is located at air vapor sparger (3-4) top; Column plate (3-2) is located between water oil difunctional sparger (3-1) and the heat production coil pipe (3-3);
Tower top outlet (3-8) is located at the top of tower body; Asphalt stock inlet (3-5), air distribution tube inlet (3-7), visbreaking gasoline reflux inlet (3-11), visbreaking diesel oil reflux inlet (3-12) and water inlet (3-13) are located at the top of tower body; Visbreaking gasoline reflux inlet (3-11), visbreaking diesel oil reflux inlet (3-12) and water inlet (3-13) all are in corresponding position with the water difunctional sparger of oil (3-1); The position of asphalt stock inlet (3-5) and air distribution tube inlet (3-7) is lower than water oil difunctional sparger (3-1); The middle part of tower body is located in diesel oil outlet (3-10); The bottom of tower body is located in visbreaking feed(raw material)inlet (3-6), and the position is higher than heat production coil pipe (3-3); Tower bottom outlet (3-9) is located at the bottom of tower body, and the position is lower than air vapor sparger (3-4).
2, the difunctional tower of oxidation fractionation as claimed in claim 1 is characterized in that: the tower body of the difunctional tower of described oxidation fractionation is provided with steam-in (3-14), and described steam-in and air vapor sparger (3-4) are in corresponding position.
3, the difunctional tower of oxidation fractionation as claimed in claim 2, it is characterized in that: described column plate is more than 2 layers; Vertical range between per two described column plates is 1200-1500mm.
4, as the difunctional tower of arbitrary described oxidation fractionation in the claim 1 to 3, it is characterized in that: asphalt stock inlet (3-5) is positioned at different sea lines and different vertical lines with described visbreaking feed(raw material)inlet (3-6) on tower body.
5, the oxidation-viscosity breaking double-function heavy oil processing system that contains the difunctional tower of arbitrary described oxidation fractionation in the claim 1 to 4.
6, oxidation as claimed in claim 5-viscosity breaking double-function heavy oil processing system is characterized in that: it comprises process furnace (1), visbreaking reactor (2), the difunctional tower of oxidation fractionation (3), diesel oil stripping tower (4), fractionation return tank of top of the tower (5), saturex (6), diesel fuel tank (7), tail gas water-sealed tank (8), air compressor (9) and compressor outlet surge tank (10);
Process furnace (1) has feed(raw material)inlet (1-1), fuel inlet (1-2) and outlet (1-3); Visbreaking reactor (2) has inlet (2-1) and outlet (2-2); Diesel oil stripping tower (4) has inlet (4-1), diesel oil outlet (4-2) and visbreaking diesel oil bypass outlet (4-3); Fractionation return tank of top of the tower (5) has inlet (5-1), waste gas outlet (5-2) and material and reclaims outlet (5-3); Saturex (6) has water inlet (6-1), gas inlet (6-2), tail gas outlet (6-3) and sump oil outlet (6-4); Diesel fuel tank (7) has additional diesel oil inlet (7-1), circulation diesel oil inlet (7-2) and outlet (7-3); Tail gas water-sealed tank (8) has water inlet (8-1), gas inlet (8-2) and tail gas recycle outlet (8-3); Compressor outlet surge tank (10) has inlet (10-1) and outlet (10-2);
Outlet (1-3) connecting tube 11 (11) of process furnace (1), pipeline 11 (11) is divided into two laterals, a lateral 11-1 (11-1) is connected with the inlet (2-1) of visbreaking reactor (2), and another lateral 11-2 (11-2) is connected with the asphalt stock inlet (3-5) of the difunctional tower of oxidation fractionation (3); The outlet (2-2) of visbreaking reactor (2) is connected with the visbreaking feed(raw material)inlet (3-6) of the difunctional tower of oxidation fractionation (3) by pipeline 12 (12); Pipeline 11-1 (11-1) is provided with visbreaking Reactor inlet valve, and pipeline 12 (12) is provided with visbreaking reactor outlet valve; Pipeline 11-2 (11-2) is provided with oxidation flow process valve; Air compressor (9) is connected with the inlet (10-1) of compressor outlet surge tank (10) by pipeline 13 (13); The outlet (10-2) of pipeline 14 (14) one ends and compressor outlet surge tank (10) is joined, and the other end is connected with air vapor sparger (3-4) by the air distribution tube inlet (3-7) of the difunctional tower of oxidation fractionation (3); Water oil difunctional sparger (3-1) connecting tube 15 (15), pipeline 15 (15) stretches out the difunctional tower of oxidation fractionation (3) by the water inlet (3-13) of the difunctional tower of oxidation fractionation (3); Tower top outlet (3-8) connecting tube 16 (16) of the difunctional tower of oxidation fractionation (3), pipeline 16 (16) is divided into two laterals, a lateral 16-1 (16-1) is connected with the inlet (5-1) of fractionation return tank of top of the tower (5), and another lateral 16-2 (16-2) is connected with the gas inlet (6-2) of saturex (6); The material of fractionation return tank of top of the tower (5) reclaims outlet (5-3) connecting tube 17 (17), pipeline 17 (17) is divided into two laterals, a lateral 17-1 (17-1) is external, and another lateral 17-2 (17-2) is connected with the water difunctional sparger of oil (3-1) by the visbreaking gasoline reflux inlet (3-11) of the difunctional tower of oxidation fractionation (3); The diesel oil outlet (3-10) of the difunctional tower of oxidation fractionation (3) is connected with the inlet (4-1) of diesel oil gas stripping column (4) by pipeline 18 (18); Visbreaking diesel oil bypass outlet (4-3) connecting tube 19 (19) of diesel oil vapour gas stripping column (4), pipeline 19 (19) is connected with the water difunctional sparger of oil (3-1) of the difunctional tower of oxidation fractionation (3) by the visbreaking diesel oil reflux inlet (3-12) of the difunctional tower of oxidation fractionation (3); The tail gas outlet (6-3) of saturex (6) is connected with the gas inlet (8-2) of tail gas water-sealed tank (8) by pipeline 20 (20); Outlet (7-3) connecting tube 21 (21) of diesel fuel tank (7), pipeline 21 (21) is connected with the circulation diesel oil inlet (7-2) of diesel fuel tank (7) by heat production coil pipe (3-3) back of the difunctional tower of oxidation fractionation (3).
7, oxidation as claimed in claim 6-viscosity breaking double-function heavy oil processing system is characterized in that: tower bottom outlet (3-9) the external pitch finished product jar of the difunctional tower of described oxidation fractionation (3) or residual oil finished product jar; The external gasoline tank of described lateral 17-1 (17-1); Diesel oil outlet (4-2) external diesel oil withdrawing can of described diesel oil gas stripping column (4); Sump oil outlet (6-4) external slop oil tank (22) of described saturex (6).
8, oxidation as claimed in claim 6-viscosity breaking double-function heavy oil processing system is characterized in that: described pipeline 12 (12) is provided with two visbreaking reactor outlet valves; Described pipeline 11-2 (11-2) is provided with two oxidation flow process valves; Described pipeline 16-1 (16-1) is provided with air cooler (23).
9, the arbitrary described oxidation-application of viscosity breaking double-function heavy oil processing system in heavy oil upgrading in the claim 5 to 8.
10, carry out the method for oxidation-viscosity breaking with arbitrary described oxidation-viscosity breaking double-function heavy oil processing system in the claim 5 to 8, comprise two processes of oxidation and viscosity breaking;
Wherein, described oxidising process may further comprise the steps:
Water enters water oil difunctional sparger (3-1), saturex (6) and the tail gas water-sealed tank (9) of the difunctional tower of oxidation fractionation (3); Behind the compressed machine outlet surge tank of the air that air compressor (9) produces (10), enter the air vapor sparger (3-4) of the difunctional tower of oxidation fractionation (3); The raw material of oxidized bitumen enters the difunctional tower of oxidation fractionation (3) after entering process furnace (1) heating; The air of air vapor sparger (3-4) ejection the difunctional tower of oxidation fractionation (3) in and the raw material of oxidized bitumen react; Asphaltic products. is extracted out from the tower bottom outlet of the difunctional tower of oxidation fractionation (3); Oxidized tail gas enters saturex (6) by the tower top outlet of the difunctional tower of oxidation fractionation (3), and the tail gas that does not coagulate enters tail gas water-sealed tank (8) by saturex (6); Diesel oil in the diesel fuel tank (7) returns diesel fuel tank (7) by the heat production coil pipe (3-3) of pipeline (21) by the difunctional tower of oxidation fractionation;
Described viscosity breaking may further comprise the steps:
The raw material of oil fuel enters process furnace (1), enters visbreaking reactor (2) after the heating, and the residual oil behind the visbreaking flows out from the outlet of visbreaking reactor (2); The reaction product of visbreaking reaction enters the difunctional tower of oxidation fractionation (3), fractionation in the difunctional tower of oxidation fractionation (3); Cat head oil gas enters fractionation return tank of top of the tower (5) by the tower top outlet output of the difunctional tower of oxidation fractionation (3); Light oil part in the fractionation return tank of top of the tower (5) is exported as gasoline, and another part is got back to the difunctional tower of oxidation fractionation (3), enters cat head top through the water of the difunctional tower of oxidation fractionation (3) the difunctional sparger of oil (3-1); Diesel oil is extracted out from the diesel oil outlet of the difunctional tower of oxidation fractionation (3), enter diesel oil gas stripping column (4), a part is as diesel oil output, and another part is returned the difunctional tower of oxidation fractionation (3), enters cat head top through the water difunctional sparger of oil (3-1) of the difunctional tower of oxidation fractionation (3); Visbreaking residue is extracted out from the tower bottom outlet of the difunctional tower of oxidation fractionation (3).
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| CN103160303A (en) * | 2011-12-19 | 2013-06-19 | 上海宝钢化工有限公司 | Adjusting device for coal tar pitch quality |
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| CN1183222C (en) * | 2001-10-30 | 2005-01-05 | 中国石油化工股份有限公司 | Method for oxidizing asphaltum |
| US7341656B1 (en) * | 2004-07-26 | 2008-03-11 | Marathon Ashland Petroleum Co. Llc | Continuous oxidation and distillation process of heavier hydrocarbon materials |
| CN101077980A (en) * | 2006-05-26 | 2007-11-28 | 华东理工大学 | Method for preparing light oil from supercritical water modified vacuum residuum |
| CN201389354Y (en) * | 2009-03-19 | 2010-01-27 | 中国海洋石油总公司 | Oxidizing and fractionating dual-function tower |
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| CN103160303A (en) * | 2011-12-19 | 2013-06-19 | 上海宝钢化工有限公司 | Adjusting device for coal tar pitch quality |
| CN103160303B (en) * | 2011-12-19 | 2014-08-20 | 上海宝钢化工有限公司 | Adjusting device for coal tar pitch quality |
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Effective date of registration: 20170221 Address after: 100010 Beijing, Chaoyangmen, North Street, No. 25, No. Patentee after: China National Offshore Oil Corporation Patentee after: China National Offshore Oil Corporation Patentee after: CNOOC Refining & Chemical Research Institute (Beijing) Co., Ltd. Address before: 100010 Beijing, Chaoyangmen, North Street, No. 25, No. Patentee before: China National Offshore Oil Corporation Patentee before: China National Offshore Oil and Gas Development and Utilization Co., Ltd. |
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Address after: 100010 Chaoyangmen North Street, Dongcheng District, Dongcheng District, Beijing Co-patentee after: China National Offshore Oil Corporation Patentee after: China Offshore Oil Group Co., Ltd. Co-patentee after: CNOOC Refining & Chemical Research Institute (Beijing) Co., Ltd. Address before: 100010 Chaoyangmen North Street, Dongcheng District, Dongcheng District, Beijing Co-patentee before: China National Offshore Oil Corporation Patentee before: China National Offshore Oil Corporation Co-patentee before: CNOOC Refining & Chemical Research Institute (Beijing) Co., Ltd. |