CN104927905A - Atmospheric and vacuum catalytic flue gas-oil slurry heat combined device - Google Patents
Atmospheric and vacuum catalytic flue gas-oil slurry heat combined device Download PDFInfo
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Abstract
An atmospheric and vacuum device adopting catalytic flue gas and oil slurry waste heat to replace a heating furnace fuel comprises a first heating furnace, a second heating furnace, a flash evaporation tower, a jet fuel atmospheric tower and a diesel fuel vacuum tower, wherein the first heating furnace adopts a flue gas heating furnace, and a first crude oil inlet pipeline and a first crude oil outlet pipeline are arranged on the flue gas heating furnace; a second crude oil inlet main pipeline is arranged on the flash evaporation tower, and crude oil after heating by the first heating furnace and second-way crude oil enter the pipeline to be mixed; a pipeline connected with a crude oil outlet pipeline on the flash evaporation tower and a crude oil output second heating furnace pipeline are arranged on the second heating furnace; a connection port connected with the crude oil output second heating furnace pipeline is formed in the jet fuel atmospheric tower; a connection port connected with a jet fuel atmospheric tower crude oil extraction pipeline is formed in the diesel fuel vacuum tower; a heavy oil extraction pipeline is arranged at the bottom of the diesel fuel vacuum tower, and an adjusting circulating oil heat exchanger and an oil slurry heat exchanger are arranged between the heavy oil extraction pipeline and the second heating furnace. The atmospheric and vacuum device is reasonable in design, efficient and energy-saving, three waste heats including the catalytic flue gas, the oil slurry and adjusting circulating oil are sufficiently used, and the economic benefits are enhanced.
Description
Technical field
The invention belongs to Petroleum Processing Technology field, relating to is a kind of atmospheric and vacuum distillation unit, and specifically a kind of catalysis flue gas and slurry oil waste heat substitute the atmospheric and vacuum distillation unit of furnace fuel.
Background technology
Catalysis is the important production equipment in refinery, and its production technique produces liquefied gas, gasoline, bavin vapour and coke with wax oil, residual oil through catalytic pyrolysis.Catalyzed reaction, burn and produce a large amount of waste heat with still-process, wherein, the waste heat of potential temperature higher (more than 360 DEG C) is made up of three parts: 1, catalyzer burns the high-temperature flue gas that will generate tens thousand of cubic metres, in, the exhaust gas volumn that large-scale regenerator of catalytic unit is discharged be about 10-25 ten thousand stere/time (3,000,000 tons of catalytic units, flue gas about 25 ten thousand steres/time), flue gas complementary energy is divided two sections and is used: the flue gas pressures going out revivifier is about 0.25Mpa temperature about 700 DEG C, first flue gas turbine expander generating is entered, middle pressure steam produced by the middle pressure steam waste heat boiler (call in the following text catalysis more than pot) that its exiting flue gas (calling catalysis flue gas in the following text) about 500 DEG C enters a 100t/h again.2, the slurry oil waste heat that produces of main fractionating tower still-process: be introduced into during vapour generator is produced and press saturation steam, then enter pot more than catalysis and produce middle pressure steam.3, waste heat in main fractionating tower two: be introduced into middle pressure steam producer and produce saturation steam, then enter middle pressure steam waste heat boiler production middle pressure steam.
Current, the Land use systems of oil refining production equipment waste heat mainly contains three kinds:
One, with the heat exchange of this device raw material, reach the object of saving furnace fuel, refinery production equipment all generally have employed a kind of so method;
Two, the waste heat of more than 250 DEG C is utilized to produce middle pressure steam, as the waste heats such as catalytic unit flue gas, slurry oil produce middle pressure steam;
Three, utilize the waste heat production low-pressure steam of less than 250 DEG C, the low temperature exhaust heat of less than 130 DEG C produces hot water.As Atmospheric vacuum, catalysis and coker.
At present, refinery's process furnace combustion gas about 5000 yuan/ton, and refinery's steam uses coal firing boiler to produce, coal price is lower, about 500 yuan/ton.Because refinery gas price is higher, coal price is lower, and therefore, obviously adopt first method most economical, refinery under prior art conditions, adopts first method all as far as possible.
The waste heat of catalytic unit, the large temperature of heat is high, but is subject to the restriction of prior art condition, cannot adopt the method for same raw material heat exchange, and usually waste heat is used as boiler oil and produces middle pressure steam, all kinds of corrupt practices creep in for the method:
One, catalysis waste heat is used as boiler combustion to produce middle pressure steam economic benefit poor
Catalytic unit more than 360 DEG C high-temperature position waste heat amounts are large, as the catalysis of 3,000,000 tons, certain refinery, cigarette machine exiting flue gas waste heat amount about 2.4 tons mark oil/time, slurry oil waste heat about 3.2 tons mark oil/time, in two waste heat about 0.8 ton mark oil/time, add up to waste heat amount about 6.4 tons mark oil/time.Current, domestic plant catalytic high-temperature position waste heat is all used as boiler for producing middle pressure steam, as the catalysis of 3,000,000 tons, certain refinery this waste heat produced 100 tons/time middle pressure steam, and power station, refinery is the high pressure steam boiler making fuel of coal, therefore, the end-use performance of catalysis waste heat is only in working as in coal.In addition, more than catalysis, pot also needs to use a large amount of combustion gas (accounting for 30-50%) additional heat, and combustion gas is also become coal by beyond doubt, reduces economic benefit equally.
Two, catalysis waste heat boiler utilization efficiency of heat energy is lower
1, middle pressure steam generates electricity less
Boiler for producing middle pressure steam more than catalysis, the high pressure steam of producing with power station, refinery high-duty boiler compares, and presses vapour to generate electricity less 3600Kw/h in every 100t/h.There are two cover catalytic units many refineries, and remaining pot quantity of steam is about 200t/h, and the few generated energy of middle pressure vapour can reach 7200Kw/h.
2, catalysis waste heat boiler is dwarf boiler, and thermo-efficiency is lower, only has about 85%, approximately low by 8% compared with high-duty boiler (as CFB boiler thermal output 93%).
Three, safety problem
In, pot steam production about 60 ~ 100t/h more than large-scale catalytic unit, as there are two cover catalytic units a refinery, then remaining pot steam production about 120 ~ 200t/h.Refinery's process steam is born jointly by pot more than thermoelectric power station boiler and catalysis.Because the reliability of the safe steam supply of pot is poor more than catalysis, therefore, when catalytic unit is produced unstable, the safe steam supply of refinery will be on the hazard.In order to ensure the safety in production of whole refinery, the boiler that thermoelectric power station boiler operation often will retain 120 ~ 200t/h leaves unused surplus, force thermoelectric power station will be pot two 200t/h high-duty boilers for subsequent use more than catalytic unit, this not only lowers the efficiency of boiler, cause very large fiber crops numerous to the safety in production of thermoelectric power station boiler simultaneously.Some middle-size and small-size refineries produce because of pot more than catalysis the large percentage that steaming amount occupies in the steam production that refinery is total, become refinery produce in very stubborn problem.Such as, there are two cover catalytic units many refineries, remaining pot steam production about 150 ~ 200t/h, for reply catalytic unit accident causes remaining pot to stop transport, the steam underproduction 150 ~ 200t/h, thermoelectric power station boiler will be stopped 200t/h and to leave unused surplus, thermoelectric power station boiler at low load is run, reduce the efficiency of thermoelectric power station boiler, also affect safety in production simultaneously, oil refining production system cannot adopt other joint vapour measures.
Around catalysis fume afterheat, the present inventor has applied for two patents: first is application on October 28th, 2013, patent name is the Chinese patent of " a kind of be furnace fuel with catalysis flue gas crude unit ", the patent No. is 201320668582.1, this patent is just authorized, although this patent achieves the innovation of catalysis residual-heat utilization technology, create condition for second, third block UTILIZATION OF VESIDUAL HEAT IN.But technical scheme Shortcomings:
1, catalytic unit UTILIZATION OF VESIDUAL HEAT IN is imperfect: catalytic unit is used as the waste heat producing middle pressure steam and has three pieces: first piece for fume afterheat, accounts for 40%; Second piece accounts for 50% for slurry oil waste heat; 3rd piece is that in two, waste heat accounts for 10%.First patent application, has only included catalysis fume afterheat and has utilized, do not comprised second, third block UTILIZATION OF VESIDUAL HEAT IN, but create condition for second, third block UTILIZATION OF VESIDUAL HEAT IN.
2, fume afterheat profit is placed in atmospheric and vacuum distillation unit process furnace, affect catalytic unit energy-saving benefit: fume afterheat profit is placed in atmospheric and vacuum distillation unit process furnace by first patent application, because catalysis cigarette machine and atmospheric and vacuum distillation unit process furnace are at a distance of 100 ~ 200 meters, this can increase cigarette machine back pressure, cigarette acc power is made to reduce about 1000Kw, unfavorable to catalytic energy saving.
To sum up, the crude unit adjacent with catalytic unit adopts combustion gas to do furnace fuel, the consumption of combustion gas is large, and cost is higher, if catalysis flue gas and slurry oil waste heat reasonably can be utilized, catalysis flue gas and slurry oil waste heat is utilized to heat crude oil, the technique of two devices is improved, again topological design, the various problems such as usefulness, benefit and the safety that pot exists more than catalysis can not only be solved, can also combustion gas be saved, greatly increase economic efficiency.
Summary of the invention
Technical problem to be solved by this invention provides a kind of reasonable in design, energy-efficient, Atmospheric vacuum-catalysis flue gas slurry oil heat integration device of substituting furnace fuel with catalysis flue gas and slurry oil waste heat.
The present invention solves the problems of the technologies described above adopted technical scheme: a kind of Atmospheric vacuum-catalysis flue gas slurry oil heat integration device, is characterized in that: comprise the first process furnace, the second process furnace, flashing tower, boat coal atmospheric tower and diesel oil vacuum distillation tower,
Wherein the first process furnace is fume heating furnace, the bottom of the first process furnace is provided with the flue gas pipeline entered for catalysis flue gas, the top of the first process furnace is provided with flue gas discharge opening, the first process furnace is also provided with first via crude oil and enters pipeline and first via crude exports pipeline;
Flashing tower, flashing tower is provided with the second road crude oil and enters main pipe line, and the crude oil after the first process furnace heating enters pipeline phase Correspondent by first via crude exports pipeline and the second road crude oil, is provided with the second tunnel crude exports pipeline in the bottom of flashing tower;
Second process furnace is tubular oven, is divided into the second convection chamber and upper and lower two parts of radiation chamber, and the second process furnace is provided with the pipeline that is connected with the second tunnel crude exports pipeline of flashing tower and crude oil goes out the second process furnace pipeline;
Boat coal atmospheric tower is provided with and goes out the interface that the second process furnace pipeline is connected and the kerosene outlet port of being extracted out by kerosene after distilling with crude oil, is provided with crude oil and extracts pipeline out at the bottom of the tower of boat coal atmospheric tower;
Diesel oil vacuum distillation tower is provided with the pipe joint extracted pipeline with the bottom crude oil of the coal atmospheric tower that navigates out and be connected, the bottom of diesel oil vacuum distillation tower is provided with the heavy oil be connected with the second process furnace and extracts pipeline out, extracts out between pipeline and the second process furnace be provided with interchanger in slurry heat-exchanger and two at heavy oil.
As improvement, described first process furnace is divided into upper and lower two parts of the first convection chamber and combustion chamber, flue gas nozzles are provided with in combustion chamber, the bottom that combustion chamber is located at by flue gas pipeline is connected with flue gas nozzles, the flue gas discharge opening place, top of the first convection chamber is provided with discharge flue, first via crude oil enters the side, upper end that the first convection chamber is located at by pipeline, and the side, lower end of the first convection chamber is located at by first via crude exports pipeline.
As improvement, described second road crude oil enters pipeline and is provided with interchanger, and the second tunnel crude exports pipeline bottom flashing tower is provided with for the crude oil at the bottom of tower being extracted out the booster oil pump be delivered in the second process furnace convection chamber.
As improvement, described second process furnace comprises the second convection chamber setting up and down and radiation chamber, the pipeline installing be connected with the second tunnel crude exports pipeline of flashing tower is at the upper lateral part of the second convection chamber, crude oil goes out the lower side that the second process furnace pipeline is arranged on the second convection chamber, is provided with discharge flue at the top of the second convection chamber.
Improve again, radiator tube is provided with in described radiation chamber, the bottom of radiation chamber is provided with fuel gas nozzle, the side of radiation chamber is provided with the heavy oil be connected with interchanger, slurry heat-exchanger in two and enters radiation chamber pipeline, and the opposite side of radiation chamber is provided with the heavy oil be connected with wax oil vacuum flasher and goes out radiation chamber pipeline.
Improve, in described two, interchanger, slurry heat-exchanger are for being arranged in parallel again.
Further improvement, described boat coal atmospheric tower goes out the side, bottom that interface that the second process furnace pipeline is connected is arranged on the coal atmospheric tower that navigates with crude oil, kerosene outlet port is arranged on the top opposite side of boat coal atmospheric tower, is provided with gasoline removes water cooler pipeline at the top of boat coal atmospheric tower.
Further improvement, described diesel oil vacuum distillation tower be provided with from top to bottom successively the outlet port, normal two wires that two wires normal with diesel oil Product Collection System is connected, the atmosphere 3rd side cut outlet port be connected with diesel oil atmosphere 3rd side cut Product Collection System and extract with the bottom crude oil of boat coal atmospheric tower the pipe joint that pipeline is connected out, extract the heavy oil be provided with at the bottom of by tower on pipeline out at the heavy bottom oil of diesel oil vacuum distillation tower and extract the fresh feed pump entering the second process furnace out, the top of diesel oil vacuum distillation tower is provided with the tower top line be connected with vacuum jet.
Improve further, the pressure of described boat coal atmospheric tower is 0.1 ~ 0.2Mpa, and air distillation temperature is 260 ~ 300 DEG C again; The pressure of diesel oil vacuum distillation tower is 5 ~ 7Kpa, and vacuum distillation temperature is 230 ~ 240 DEG C.
Compared with prior art, the invention has the advantages that: cancel original catalysis waste heat steam boiler, first process furnace of newly-built pure convection current, cancel catalytic slurry heat recovery steam generator, interchanger in newly-built slurry heat-exchanger and two, cancel vacuum furnace and atmospheric tower, newly-built boat coal atmospheric tower, diesel oil vacuum distillation tower and the second process furnace; Improve crude oil heat exchange flow process simultaneously and reduce crude distillation temperature, transform atmospheric tower distillation as boat coal atmospheric tower and diesel oil vacuum distillation tower, make to enter the second process furnace again after interchanger heat exchange the low-temperature level heavy oil and slurry heat-exchanger, two of the extraction of diesel oil vacuum distillation tower, and the first process furnace adopts based on catalysis flue gas fuel, combustion gas is auxiliary heating in crude oil, like this three kinds of waste heats in catalysis flue gas, slurry oil, two are all used for atmospheric and vacuum distillation unit heating in crude oil, greatly save atmospheric and vacuum distillation unit furnace fuel; Owing to reducing crude distillation temperature, the heat transfer temperature difference technical barrier between just solving in crude oil and flue gas, slurry oil and two, substantially increases the economical effectiveness of heat energy utilization.Reasonable in design of the present invention, energy consumption is low, fundamentally solves the problems such as the various An full Hyperlink trouble that the heat utilization efficiency that pot exists more than catalysis is lower, energy consumption waste is large and more than catalysis, pot exists, greatly reduces energy consumption, saved combustion gas, improve economic benefit.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention.
Embodiment
Below in conjunction with accompanying drawing embodiment, the present invention is described in further detail.
As shown in Figure 1, the atmospheric and vacuum distillation unit substituting furnace fuel with catalysis flue gas and slurry oil waste heat of the present embodiment, comprise the first process furnace 1, second process furnace 2, flashing tower 3, boat coal atmospheric tower 4, diesel oil vacuum distillation tower 5, interchanger 6 and slurry heat-exchanger 7 in two, wherein the first process furnace 1 is fume heating furnace, it is the pure convection current tubular oven of a radiationless room, first process furnace 1 is divided into the first convection chamber 11 and combustion chamber about 12 two part, the bottom of the first process furnace 1 is provided with the flue gas pipeline 16 of the combustion chamber 12 entered for catalysis flue gas, flue gas nozzles 121 are provided with in combustion chamber 12, flue gas nozzles 121 use gas-fired combustion-supporting, effect is to improve flue-gas temperature, burn the carbon monoxide in flue gas, make it to become carbonic acid gas, supplement the deficiency of flue gas heat simultaneously, flue gas pipeline 16 is connected with flue gas nozzles 121, the top of the first process furnace 1 is provided with flue gas discharge opening, discharge flue 13 is provided with at flue gas discharge opening place, the side, upper end of the first convection chamber 11 is provided with first via crude oil and enters pipeline 14, the side, lower end of the first convection chamber 11 is provided with first via crude exports pipeline 15, like this from the flue gas of catalytic unit cigarette machine outlet, the flue gas nozzles 121 in combustion chamber 12 are introduced bottom combustion chamber 12, after burning the carbon monoxide in flue gas, flue gas upwards flows into the first convection chamber 11 from top, combustion chamber 12, in the first convection chamber 11, crude oil in flue gas heating convection tubes, temperature goes out the first convection chamber 11 after being reduced to 190 DEG C, upwards discharge from discharge flue 13 again, the temperature entering the first convection chamber 11 through first via crude oil pipeline 14 from the crude oil of house steward 101 is about 150-160 DEG C, and the temperature going out the first convection chamber 11 is about 260-300 DEG C, flashing tower 3 is provided with the second road crude oil and enters main pipe line 33, second road crude oil enters pipeline 31 and is provided with two interchanger 8, enter main pipe line 33 through crude oil after crude oil after the first process furnace 1 heats enters pipeline 31 phase Correspondent by first via crude exports pipeline 15 and the second crude oil from house steward 101 and enter flashing tower 3, being provided with the second tunnel crude exports pipeline 32 bottom flashing tower 3, the second tunnel crude exports pipeline 32 being provided with for the crude oil at the bottom of tower being extracted out the booster oil pump 9 be delivered in the second process furnace 2 convection chamber 21, second process furnace 2 is a complete tubular oven, be divided into the second convection chamber 21 and radiation chamber about 22 two part, the pipeline be connected with booster oil pump 9 outlet line 27 is provided with at the upper lateral part of the second convection chamber 21, be provided with crude oil in the lower side of the second convection chamber 21 and go out the second process furnace pipeline 24, discharge flue 23 is provided with at the top of the second convection chamber 21, radiator tube is provided with in radiation chamber 22, the bottom of radiation chamber 22 is provided with fuel gas nozzle, the side of radiation chamber 22 be provided with two in interchanger 6, the heavy oil that slurry heat-exchanger 7 is connected enters radiation chamber pipeline 25, the opposite side of radiation chamber 22 is provided with the heavy oil be connected with wax oil vacuum distillation tower and goes out radiation chamber pipeline 26, what such second convection chamber 21 heated is through flashing tower 3 reduced crude oil, be heated to 280-300 DEG C, enter boat coal atmospheric tower 4, and radiation chamber 22 heats is the heavy oil of interchanger 6 and slurry heat-exchanger 7 from two, pressed distillate vacuum distillation tower after heating, it is 380-390 DEG C that heavy oil is heated to temperature at radiation chamber 22, the pressure of boat coal atmospheric tower 4 is 0.1 ~ 0.2Mpa, the side, bottom of boat coal atmospheric tower 4 is provided with the interface going out the second process furnace pipeline 24 with the crude oil of the second process furnace 2 and be connected, the kerosene outlet port 41 of after the top opposite side of boat coal atmospheric tower 2 is provided with distillation, kerosene being extracted out, at the bottom of the tower of boat coal atmospheric tower 4, be provided with crude oil extract pipeline 42 out, the top of boat coal atmospheric tower 4 is provided with oily vapour and removes water cooler pipeline 43, the pressure of diesel oil vacuum distillation tower 5 is 5 ~ 7Kpa, diesel oil vacuum distillation tower 5 is provided with the outlet port, normal two wires 51 that two wires normal with diesel oil Product Collection System is connected from top to bottom successively, the atmosphere 3rd side cut outlet port 52 be connected with diesel oil atmosphere 3rd side cut Product Collection System and extract the pipe joint that pipeline 42 is connected out with the bottom crude oil of boat coal atmospheric tower 4, the bottom of diesel oil vacuum distillation tower 5 be provided with two in interchanger 6, pipeline 53 extracted out by the heavy oil that slurry heat-exchanger 7 is connected, interchanger 6 in two, slurry heat-exchanger 7 is for being arranged in parallel, heavy oil is extracted pipeline 53 out and is provided with fresh feed pump 10, from the bottom of diesel oil vacuum distillation tower 5 heavy oil out by fresh feed pump 10 respectively with two interchanger 6, slurry heat-exchanger 7 carries out heat exchange, then enter again through pipeline 25 in the radiation chamber 22 of the second process furnace 2, the heavy oil temperature gone out at the bottom of diesel oil vacuum distillation tower 5 tower is 230 ~ 240 DEG C, and interchanger 6 in two, the temperature of slurry heat-exchanger 7 is 260 ~ 360 DEG C, the top of diesel oil vacuum distillation tower 5 is provided with the tower top line 54 be connected with vacuum jet, uses the vacuum tightness pressure in vacuum jet maintenance diesel oil vacuum distillation tower 5.Such crude oil boat coal atmospheric tower 4 distills out rich gas, gasoline, kerosene at temperature 260 ~ 300 DEG C, and crude oil adopts underpressure distillation more afterwards, diesel oil vacuum distillation tower 5 distillation temperature 230 ~ 240 DEG C, transfers to diesel oil (normal two, three lines).
Concrete technology flow process is: 40 DEG C of crude oil enter atmospheric and vacuum distillation unit from tank station, with separation column out product heat exchange, temperature enters electrical desalter when rising to 150 ~ 160 DEG C, crude oil after electricity is de-is divided into two-way through main pipe line 101 and continues heating: first via crude oil (about 20 ~ 30%) enters through first via crude oil the first convection chamber 11 that pipeline 14 removes catalytic unit first process furnace 1, 250 ~ 300 DEG C are heated to through convection tubes, return atmospheric and vacuum distillation unit through first via crude exports pipeline 15 after crude oil goes out the first convection chamber 11 of the first process furnace 1 to enter pipeline 31 collaborate with the second road crude oil pipeline i.e. the second road crude oil, second road crude oil enters pipeline 31 in atmospheric and vacuum distillation unit, continues the heat exchange of same comparatively high temps product interchanger 8, after heat exchange terminates, temperature is approximately about 250-280 DEG C, the first via crude oil interflow returned with first via crude exports pipeline 15, crude oil interflow after through crude oil enter main pipe line 33 enter flashing tower 3 distillation extract most rich gas, gasoline, because flashing tower 3 distillation temperature is not high enough, small part rich gas, gasoline is so remain in crude oil, crude oil flows into bottom flashing tower 3 and enters booster oil pump 9 through crude exports pipeline 32 afterwards, the second convection chamber 21 that crude oil enters the second process furnace 2 through pump discharge pipeline 27 after booster oil pump 9 supercharging is heated to 280 ~ 300 DEG C, crude oil goes out the second convection chamber 22 afterwards, go out the second process furnace pipeline 24 through crude oil and enter distillation in boat coal atmospheric tower 4, extract remaining rich gas in crude oil, gasoline and whole boat coals, crude oil flows into boat coal atmospheric tower 4 end afterwards, rely on the pressure of self to extract pipeline 42 out through crude oil and flow into diesel oil vacuum distillation tower 5, in diesel oil vacuum distillation tower 5, diesel oil relies on the distillation of the sensible heat cab of crude oil self to extract normal two, three line diesel oil, rich gas is extracted in distillation, gasoline, after aviation kerosene and diesel oil, heavy oil called in the following text by crude oil.Heavy oil temperature is reduced to about 230 ~ 240 DEG C and flows into diesel oil vacuum distillation tower 5 end afterwards, because heavy oil temperature is lower, can realize with two in interchanger 6, the slurry oil heat exchange of about 260 ~ 360 DEG C in slurry heat-exchanger 7, diesel oil vacuum distillation tower 5 end heavy oil is extracted pipeline 53 out through heavy oil and is flowed into fresh feed pump 10, heavy oil after supercharging goes out atmospheric and vacuum distillation unit and removes catalytic unit, enter interchanger 6 and slurry heat-exchanger 7 in two to heat, after enter radiation chamber pipeline 25 through heavy oil and turn back to atmospheric and vacuum distillation unit, enter in the radiation chamber 22 of the second process furnace 2, radiation chamber 22 is gone out after radiator tube continues to be heated to 380 ~ 390 DEG C, go out radiation chamber pipeline 26 through heavy oil to enter wax oil vacuum distillation tower fractionation by distillation and go out to subtract one, two wires, subtract three line wax oils.
Just technical project design of the present invention is described in further details below.
One, know-why
1, the waste heat reclaiming process of catalytic unit is improved
(1), cancel pot more than catalysis, its middle pressure steam, by thermoelectric power station Boiler High Pressure steam supply, is equivalent to displace with coal the combustion gas and fume afterheat that pot more than catalysis uses.
(2), by catalysis flue gas, slurry oil, two medium three kinds of waste heats be used for atmospheric and vacuum distillation unit heating in crude oil, reach the target of saving pot and the combustion gas of atmospheric and vacuum distillation unit process furnace more than catalytic unit.
2, improve the technique of atmospheric and vacuum distillation unit, reduce heating crude oil temperature
Catalysis three kinds of waste heats to be used for atmospheric and vacuum distillation unit heating crude oil, key to solve the problem that between crude oil and waste heat, heat transfer temperature difference is too little: the funnel temperature of catalysis flue gas is 190 DEG C, 40 DEG C are not less than by the heat transfer temperature difference between flue gas and crude oil, as required to carry out heating in crude oil with flue gas, then the origin temp of heating crude oil can not higher than 150 DEG C; Extract 360 DEG C out in slurry oil, two, return tower oil temperature 260 DEG C, be not less than 20 DEG C by the heat transfer temperature difference in slurry oil, two and between crude oil, require that the origin temp of crude oil heat exchange can not higher than 240 DEG C equally.And crude oil is about 250 ~ 280 DEG C with the temperature after the product heat exchange of this device in atmospheric and vacuum distillation unit, the heat transfer temperature difference between causing thus in flue gas, slurry oil and two is less than zero, and heat exchange can not realize.
For this reason, present patent application improves the technique of atmospheric and vacuum distillation unit, reduces crude oil heat exchange and distillation temperature, solves the technical barrier that heat transfer temperature difference is too little.
1, improve crude oil heat exchange flow process: after electric desalting, the crude oil of 150 DEG C divides two-way to carry out heat exchange: first via crude oil (about 20 ~ 30%) goes catalytic unit flue gas heating to 250 ~ 300 DEG C, return atmospheric and vacuum distillation unit afterwards with the second crude oil pipeline interflow, road; Second road crude oil in atmospheric and vacuum distillation unit with normal pressure and the heat exchange of decompression comparatively high temps product.After heat exchange terminates, first and second crude oil interflow, road enters flashing tower distillation.
2, atmospheric and vacuum distillation unit crude distillation temperature is reduced: transform former atmospheric tower distillation as two towers: first: atmospheric tower, distillation temperature 260 ~ 300 DEG C, boat coal is transferred in distillation; Second: vacuum distillation tower, distillation temperature 230 ~ 240 DEG C, diesel oil (normal two, three lines) is transferred in distillation, crude oil temperature 230 ~ 240 DEG C remaining after distillation.This temperature is just in time applicable to (extract 360 DEG C out, return tower oil temperature 260 DEG C) heat exchange in same slurry oil, two, and heat transfer temperature difference is larger.
Two, concrete technology contents
1, the residual neat recovering systems such as the flue gas of catalytic unit and slurry oil are transformed
Cancel patent application implement before catalysis waste heat steam boiler, the first process furnace 1 changing a newly-built pure convection current tubular oven into is used for heating 150 DEG C of crude oil.Cancel patent application implement before catalytic slurry and two in heat recovery steam generator, to change in newly-built two interchanger and slurry oil-crude heat exchanger 7 and two-crude heat exchanger i.e. interchanger 6 in two into, be used for heating 230 ~ 240 DEG C of crude oil.Catalytic unit steam is supplied by power station pipe network.
2, atmospheric and vacuum distillation unit production technique is transformed
(1), process furnace the Nomenclature Composition and Structure of Complexes
Cancel atmospheric pressure kiln and and vacuum furnace.Newly-built second process furnace 2 substitutes atmospheric pressure kiln and vacuum furnace for heating in crude oil.Before patent application is implemented, atmospheric and vacuum distillation unit has two process furnace (atmospheric pressure kiln and and vacuum furnace), and wherein, atmospheric pressure kiln thermal load is comparatively large, and account for 2/3rds of two stove total heat duties, vacuum furnace thermal load is less, accounts for 1/3rd.Patent application because catalytic unit three kinds of waste heat amounts have been more than or equal to vacuum furnace thermal load, therefore, can have been cancelled vacuum furnace, atmospheric pressure kiln and vacuum furnace merged into a process furnace after implementing.So, the heating crude oil of atmospheric and vacuum distillation unit is just completed jointly by the first process furnace 1 and the second process furnace 2.
(2), Distallation systm
Before enforcement, atmospheric and vacuum distillation unit is three column distillations (atmospheric towers: distill the flashing tower of rich gas and gasoline, distillation aviation kerosene, the atmospheric tower of diesel oil and the vacuum distillation tower of a distillation wax oil) substantially.After technology implementation, atmospheric tower is changed to two towers, newly-built boat coal atmospheric tower 4 and diesel oil vacuum distillation tower 5.Crude oil first distillation in atmospheric tower (pressure 0.1 ~ 0.2Mpa, temperature 260 ~ 300 DEG C), transfers to remaining rich gas, gasoline and kerosene.Crude oil goes distillation in vacuum distillation tower afterwards, vacuum distillation tower pressure (5 ~ 7Kpa absolute pressure, distillation temperature 230 ~ 240 DEG C).Transfer to diesel oil (normal two, three lines).Crude oil goes heat exchange in the same slurry oil of catalytic unit, two afterwards.After heat exchange terminates, crude oil returns atmospheric and vacuum distillation unit again and enters the second process furnace 2 radiation chamber 22 and be heated to 380 ~ 390 DEG C, goes out the distillation of radiation chamber 22 pressed distillate vacuum distillation tower afterwards and transfers to wax oil.
The performance analysis produced after implementing:
Three, patent application implementation benefit:
1, replace the remaining pot of pressure in catalysis combustion gas with the high-duty boiler of power station fire coal to bring benefits
3000000 tons of catalysis fume afterheat amounts about 2.4 tons mark oil/time, slurry oil waste heat 3.2 tons mark oil/time, in two waste heat 0.8 ton mark oil/time, add up to waste heat amount 6.4 tons mark oil/time.These three waste heat Atmospheric vacuum heating in crude oil, make Atmospheric vacuum save combustion gas 6.4 tons mark oil/time.Cancel the remaining pot of pressure in catalysis combustion gas, catalytic unit steam is provided by the coal-fired high-duty boiler in power station.So, in catalysis, in pressure remaining pot combustion gas used 2 tons mark oil/time, is all saved.Above-mentioned two add up to 8.4 tons mark oil/time.Combustion gas with coal price difference about 4000 yuan/ton mark oil, fire coal change combustion gas bring benefits into
8.4X104X4000=3.36 hundred million yuan/year
2, energy-saving benefit
High-duty boiler electricity more multiple than medium pressure boiler:
Every 100t/h high pressure steam electric 3600Kw more multiple than low-pressure steam.Annual multiple electricity is
3600X8400=3024X104 degree/year
Electricity price 0.6 yuan/degree, many power benefits are:
3024X104X0.6 unit/degree=0.18 hundred million yuan/year
Energy-conservation total benefit is
3.36+0.18=3.54 hundred million yuan/year
3, solve the An full Hyperlink that pot exists more than catalysis to suffer from
After implementing present patent application technology, more than catalysis, pot is cancelled, and refinery's process steam is all supplied by power station, fundamentally solves the various An full Hyperlink that pot more than catalysis exists and suffers from and problem.
4, technological investment recovery time is short
A set of catalytic unit adopts present patent application technology, fume heating furnace investment about 0.5 hundred million yuan; Atmospheric vacuum transformation about 0.5 hundred million yuan adds up to patent application technology gross investment about 100,000,000 yuan.Adopt present patent application technology to bring benefits and be about 3.54 hundred million yuan/year, after deduction investment, technology pure benefit is then about 200,000,000 yuan/year, and the payback period is very short, is about three months to half a year.
Claims (9)
1. Atmospheric vacuum-catalysis flue gas slurry oil heat integration device, is characterized in that: comprise the first process furnace, the second process furnace, flashing tower, boat coal atmospheric tower and diesel oil vacuum distillation tower,
Wherein the first process furnace is fume heating furnace, the bottom of the first process furnace is provided with the flue gas pipeline entered for catalysis flue gas, the top of the first process furnace is provided with flue gas discharge opening, the first process furnace is also provided with first via crude oil and enters pipeline and first via crude exports pipeline;
Flashing tower, flashing tower is provided with the second road crude oil and enters main pipe line, and the crude oil after the first process furnace heating enters pipeline phase Correspondent by first via crude exports pipeline and the second road crude oil, is provided with the second tunnel crude exports pipeline in the bottom of flashing tower;
Second process furnace is tubular oven, is divided into the second convection chamber and upper and lower two parts of radiation chamber, and the second process furnace is provided with the pipeline that is connected with the second tunnel crude exports pipeline of flashing tower and crude oil goes out the second process furnace pipeline;
Boat coal atmospheric tower is provided with and goes out the interface that the second process furnace pipeline is connected and the kerosene outlet port of being extracted out by kerosene after distilling with crude oil, is provided with crude oil and extracts pipeline out at the bottom of the tower of boat coal atmospheric tower;
Diesel oil vacuum distillation tower is provided with the pipe joint extracted pipeline with the bottom crude oil of the coal atmospheric tower that navigates out and be connected, the bottom of diesel oil vacuum distillation tower is provided with the heavy oil be connected with the second process furnace and extracts pipeline out, extracts out between pipeline and the second process furnace be provided with interchanger in slurry heat-exchanger and two at heavy oil.
2. Atmospheric vacuum according to claim 1-catalysis flue gas slurry oil heat integration device, it is characterized in that: described first process furnace is divided into upper and lower two parts of the first convection chamber and combustion chamber, flue gas nozzles are provided with in combustion chamber, the bottom that combustion chamber is located at by flue gas pipeline is connected with flue gas nozzles, the flue gas discharge opening place, top of the first convection chamber is provided with discharge flue, first via crude oil enters the side, upper end that the first convection chamber is located at by pipeline, and the side, lower end of the first convection chamber is located at by first via crude exports pipeline.
3. Atmospheric vacuum according to claim 1-catalysis flue gas slurry oil heat integration device, it is characterized in that: described second road crude oil enters pipeline and is provided with interchanger, the second tunnel crude exports pipeline bottom flashing tower is provided with for the crude oil at the bottom of tower being extracted out the booster oil pump be delivered in the second process furnace.
4. Atmospheric vacuum according to claim 1-catalysis flue gas slurry oil heat integration device, it is characterized in that: described second process furnace comprises the second convection chamber setting up and down and radiation chamber, the pipeline installing be connected with the second tunnel crude exports pipeline of flashing tower is at the upper lateral part of the second convection chamber, crude oil goes out the lower side that the second process furnace pipeline is arranged on the second convection chamber, is provided with discharge flue at the top of the second convection chamber.
5. Atmospheric vacuum according to claim 4-catalysis flue gas slurry oil heat integration device, it is characterized in that: in described radiation chamber, be provided with radiator tube, the bottom of radiation chamber is provided with fuel gas nozzle, the side of radiation chamber is provided with the heavy oil be connected with interchanger in slurry heat-exchanger, two and enters radiation chamber pipeline, and the opposite side of radiation chamber is provided with the heavy oil be connected with wax oil vacuum distillation tower and goes out radiation chamber pipeline.
6. Atmospheric vacuum according to claim 1-catalysis flue gas slurry oil heat integration device, is characterized in that: in described two, interchanger, slurry heat-exchanger are for being arranged in parallel.
7. Atmospheric vacuum according to claim 1-catalysis flue gas slurry oil heat integration device, it is characterized in that: described boat coal atmospheric tower goes out the side, bottom that interface that the second process furnace pipeline is connected is arranged on the coal atmospheric tower that navigates with crude oil, kerosene outlet port is arranged on the top opposite side of boat coal atmospheric tower, is provided with gasoline removes water cooler pipeline at the top of boat coal atmospheric tower.
8. Atmospheric vacuum according to claim 1-catalysis flue gas slurry oil heat integration device, it is characterized in that: described diesel oil vacuum distillation tower is provided with from top to bottom successively the outlet port, normal two wires that two wires normal with diesel oil Product Collection System is connected, the atmosphere 3rd side cut outlet port be connected with diesel oil atmosphere 3rd side cut Product Collection System and extract the pipe joint that pipeline is connected out with the bottom crude oil of boat coal atmospheric tower, extract the heavy oil be provided with at the bottom of by tower on pipeline out at the heavy bottom oil of diesel oil vacuum distillation tower and extract the fresh feed pump entering the second process furnace out, the top of diesel oil vacuum distillation tower is provided with the tower top line be connected with vacuum jet.
9. Atmospheric vacuum according to claim 1-catalysis flue gas slurry oil heat integration device, is characterized in that: the pressure of described boat coal atmospheric tower is 0.1 ~ 0.2Mpa, and air distillation temperature is 260 ~ 300 DEG C; The pressure of diesel oil vacuum distillation tower is 5 ~ 7Kpa, and vacuum distillation temperature is 230 ~ 240 DEG C.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112280589A (en) * | 2020-09-04 | 2021-01-29 | 雷泽永 | Catalysis-atmospheric and vacuum distillation-hydrogenation heat combination device |
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| CN112280589B (en) * | 2020-09-04 | 2023-08-04 | 雷泽永 | Catalytic-atmospheric-vacuum-hydrogenation heat combination device |
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| CN104927905B (en) | 2017-05-10 |
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