CN104927905B - 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, it is a kind of atmospheric and vacuum distillation unit to be related to, specifically a kind of with catalysis flue gas
With the atmospheric and vacuum distillation unit that slurry oil waste heat substitutes furnace fuel.
Background technology
Catalysis is the important process units in refinery, its production technology be with wax oil, residual oil Jing catalytic pyrolysiss production liquefied gas,
Gasoline, bavin vapour and coke.Catalytic reaction, burn and still-process produces a large amount of waste heats, wherein, potential temperature is higher（More than 360 DEG C）
Waste heat be made up of three parts：1st, catalyst burns the high-temperature flue gas that generate tens thousand of cubic metres, in, large-scale catalytic unit regeneration
Exhaust gas volumn about 10-25 that device is discharged ten thousand stere/when (3,000,000 tons of catalytic units, flue gas about 25 ten thousand steres/when), more than flue gas
Two sections can be divided to use：Go out about 700 DEG C of the flue gas pressures about 0.25Mpa temperature of regenerator, initially enter flue gas turbine expander and send out
Electricity, its exiting flue gas（Call catalysis flue gas in the following text）About 500 DEG C of middle pressure steam waste heat boilers for entering back into a 100t/h（Call catalysis in the following text
Remaining pot）Production middle pressure steam.2nd, the slurry oil waste heat that main fractionating tower still-process is produced：It is introduced into pressure in steam generator production full
And steam, enter back into the remaining pot production middle pressure steam of catalysis.3rd, waste heat in main fractionating tower two：It is introduced into the production of middle pressure steam generator
Saturated vapor, enters back into middle pressure steam waste heat boiler production middle pressure steam.
Currently, the Land use systems for refining oil process units waste heat mainly have three kinds：
First, exchange heat with this device raw material, reach the purpose for saving furnace fuel, oil plant process units is all generally adopted
Such a method；
2nd, middle pressure steam is produced using more than 250 DEG C of waste heat, such as in catalytic unit flue gas, the production of slurry oil waste heat
Pressure steam；
3rd, low-pressure steam, less than 130 DEG C of low temperature exhaust heat production hot water are produced using less than 250 DEG C of waste heat.It is as usual to subtract
Pressure, catalysis and coking plant.
At present, about 5000 yuan/ton of refinery's heating furnace combustion gas, and refinery's steam is produced using coal-burning boiler, coal price compared with
It is low, about 500 yuan/ton.Because oil plant gas price is higher, coal price is relatively low, it is, therefore, apparent that using first method most
Economy, refinery under prior art conditions, all adopts first method as far as possible.
The waste heat of catalytic unit, the big temperature of heat is high, but is limited by prior art condition, it is impossible to using same raw material
The method of heat exchange, is generally used as boiler oil production middle pressure steam by waste heat, and all kinds of corrupt practices creep in for the method：
First, be catalyzed waste heat be used as boiler combustion production middle pressure steam economic benefit it is poor
360 DEG C of high temperature above position waste heat amounts of catalytic unit are big, such as 3,000,000 tons of certain refinery catalysis, cigarette machine exiting flue gas waste heat
About 2.4 tons of marks of amount oil/when, about 3.2 tons of slurry oil waste heat mark oil/when, in two about 0.8 ton of mark of waste heat oil/when, add up to waste heat amount about
6.4 tons mark oil/when.Currently, domestic plant catalytic high-temperature position waste heat is all used as boiler for producing middle pressure steam, such as certain refinery 300
Ten thousand tons of catalysis by the waste heat produce 100 tons/when middle pressure steam, and refinery power station is the high steam pot that fuel is made of coal
Stove, therefore, the effective utilization of waste heat is catalyzed only in when in coal.In addition, the remaining pot of catalysis also needs to use a large amount of combustion gas（Account for
30-50%）Additional heat, this undoubtedly combustion gas is also become coal, equally reduces economic benefit.
2nd, it is catalyzed waste heat boiler utilization efficiency of heat energy relatively low
1st, middle pressure steam generates electricity less
The remaining boiler for producing middle pressure steam of catalysis, compares, per 100t/ with the high steam of refinery power station high-pressure boiler production
Vapour is pressed to generate electricity less 3600Kw/h in h.There are two sets of catalytic units many refineries, and remaining pot quantity of steam about 200t/h, middle pressure vapour generates electricity less
Amount can reach 7200Kw/h.
2nd, it is catalyzed waste heat boiler and is miniature boiler, the thermal efficiency is relatively low, only 85% or so, with high-pressure boiler（Such as CFB pots
Furnace thermal efficiency 93%）Compare about low by 8%.
3rd, safety problem
In, pot steam production about 60～100t/h more than large-scale catalytic unit, there are two sets of catalytic units a such as refinery, then remaining
Pot steam production about 120～200t/h.Refinery's process steam is born jointly by thermo-power station boiler and the remaining pot of catalysis.More than catalysis
The reliability of the safe steam supply of pot is poor, therefore, when catalytic unit production is unstable, the safe steam supply of refinery will be on the hazard.
In order to ensure the safety in production of whole refinery, thermo-power station operation boiler will often retain the idle surplus of boiler of 120～200t/h,
Force thermo-power station to be the standby two 200t/h high-pressure boilers of pot more than catalytic unit, this not only lowers the efficiency of boiler, while
Cause very big numb numerous to the safety in production of thermo-power station boiler.Some middle-size and small-size refineries are total in refinery because the remaining pot of catalysis produces steaming amount
The large percentage occupied in steam production, becomes very stubborn problem in refinery's production.For example, there are two sets of catalysis dresses many refineries
Put, remaining pot steam production about 150～200t/h, be that reply catalytic unit accident causes remaining pot to stop transport, the steam underproduction 150～
200t/h, thermo-power station boiler will stop the idle surpluses of 200t/h so that thermo-power station boiler at low load runs, and reduces thermo-power station
The efficiency of boiler, while having an effect on safety in production, oil refining production system cannot be using other section vapour measures.
Around catalysis fume afterheat, the present inventor has applied for two patents：First is the Shen of on October 28th, 2013
Please, patent name is《A kind of crude(oil)unit with catalysis flue gas as furnace fuel》Chinese patent, Patent No.
201320668582.1, the patent is just authorized, and although the patent realizes catalysis residual-heat utilization technology innovation, has been the
2nd, the 3rd piece of UTILIZATION OF VESIDUAL HEAT IN creates condition.But technical scheme Shortcomings：
1st, catalytic unit UTILIZATION OF VESIDUAL HEAT IN is imperfect：Catalytic unit is used as the waste heat of production middle pressure steam and has three pieces：First
Block is fume afterheat, accounts for 40%；Second piece accounts for 50% for slurry oil waste heat；3rd piece be two in waste heat account for 10%.First specially
Profit application, has only included the utilization of catalysis fume afterheat, including second, third block UTILIZATION OF VESIDUAL HEAT IN, but has been second, the
Three pieces of UTILIZATION OF VESIDUAL HEAT INs create condition.
2nd, fume afterheat profit is placed in atmospheric and vacuum distillation unit heating furnace, affects catalytic unit energy-saving benefit：First patent
Application is placed on fume afterheat profit in atmospheric and vacuum distillation unit heating furnace, due to being catalyzed cigarette machine and atmospheric and vacuum distillation unit heating furnace at a distance of 100
～200 meters, this can increase cigarette machine back pressure, make cigarette acc power reduce about 1000Kw, unfavorable to catalytic energy saving.
To sum up, the crude(oil)unit adjacent with catalytic unit is to do furnace fuel, the consumption of combustion gas using combustion gas
Greatly, it is relatively costly, if can reasonably be utilized catalysis flue gas and slurry oil waste heat, using catalysis flue gas and slurry oil waste heat pair
Crude oil is heated, and the technique of two devices is improved, again layout designs, can not only solve to be catalyzed the effect that remaining pot is present
The various problems such as energy, benefit and safety, moreover it is possible to save combustion gas, greatly improve economic benefit.
The content of the invention
The technical problem to be solved is to provide a kind of reasonable in design, height for the above-mentioned state of the art
Effect energy-conservation, the Atmospheric vacuum-catalysis flue gas slurry oil heat integration device to be catalyzed flue gas and slurry oil waste heat replacement furnace fuel.
The present invention solve the technical scheme that adopted of above-mentioned technical problem for：A kind of Atmospheric vacuum-catalysis flue gas slurry oil heat connection
Attach together and put, it is characterised in that：Including the first heating furnace, the second heating furnace, flash column, boat coal atmospheric tower and diesel oil vacuum tower,
Wherein the first heating furnace is fume heating furnace, and the bottom of the first heating furnace is provided with the fume pipe entered for catalysis flue gas
Line, is provided with flue gas discharge opening at the top of the first heating furnace, first via crude oil is additionally provided with the first heating furnace into pipeline and the
Crude exports pipeline all the way；
Flash column, is provided with the second road crude oil and enters main pipe line on flash column, the crude oil Jing after the first heating stove heat leads to
Cross first via crude exports pipeline and enter pipeline phase Correspondent with the second road crude oil, be provided with the second road crude oil in the bottom of flash column and go out
Mouth pipeline；
Second heating furnace is tubular heater, is divided into the second convection cell and upper and lower two part of radiation chamber, on the second heating furnace
It is provided with the pipeline that is connected with the second tunnel crude exports pipeline of flash column and crude oil goes out the second heating furnace pipeline；
Boat coal atmospheric tower is provided with to go out after the interface and distillation that the second heating furnace pipeline is connected with crude oil and takes out kerosene
The kerosene outlet port for going out, is provided with crude oil and extracts pipeline out in the bottom of towe of boat coal atmospheric tower；
Diesel oil vacuum tower is provided with extracts the pipe joint that pipeline is connected out with the bottom crude oil of boat coal atmospheric tower, and diesel oil subtracts
The bottom of pressure tower is provided with the heavy oil being connected with the second heating furnace and extracts pipeline out, extracts out between pipeline and the second heating furnace in heavy oil
It is provided with heat exchanger in slurry heat-exchanger and two.
Used as improvement, first heating furnace is divided into the first convection cell and upper and lower two part of combustor, and burning interior is provided with
Flue gas nozzles, flue gas pipeline is connected located at the bottom of combustor with flue gas nozzles, the top flue gas discharge opening of the first convection cell
Place is provided with discharge flue, and first via crude oil enters pipeline located at the upper end side of the first convection cell, first via crude exports pipeline
Located at the lower end side of the first convection cell.
Used as improvement, second road crude oil is provided with heat exchanger into pipeline, and the second road crude oil of flash distillation tower bottom goes out
Mouth pipeline is provided with for extracting the crude oil of bottom of towe out be delivered in the second heating furnace convection cell pressure oil pump.
Used as improvement, second heating furnace includes the second convection cell and radiation chamber setting up and down, the with flash column
The pipeline that two tunnel crude exports pipelines are connected is arranged on the upper lateral part of the second convection cell, and crude oil goes out the setting of the second heating furnace pipeline
In the following side of the second convection cell, at the top of the second convection cell discharge flue is provided with.
Improve again, the radiation interior is provided with radial canal, the bottom of radiation chamber is provided with fuel gas nozzle, and the side of radiation chamber sets
There is the heavy oil being connected with heat exchanger, slurry heat-exchanger in two to enter radiation chamber pipeline, the opposite side of radiation chamber is provided with and subtracts with wax oil
The heavy oil that pressure flash column is connected goes out radiation chamber pipeline.
Improve again, heat exchanger, slurry heat-exchanger are to be arranged in parallel in described two.
Further improve, the interface that the second heating furnace pipeline is connected is gone out with crude oil on the boat coal atmospheric tower and is arranged on boat
The bottom side of coal atmospheric tower, kerosene outlet port is arranged on the top opposite side of boat coal atmospheric tower, at the top of boat coal atmospheric tower
It is provided with gasoline and removes cooler pipeline.
Further improve, be sequentially provided with from top to bottom on the diesel oil vacuum tower and the normal two wires Product Collection System phase of diesel oil
Atmosphere 3rd side cut outlet port that normal two wires outlet port even is connected with diesel oil atmosphere 3rd side cut Product Collection System and with the coal atmospheric tower that navigates
Bottom crude oil extracts the pipe joint that pipeline is connected out, extracts out in the heavy bottom oil of diesel oil vacuum tower and is provided with bottom of towe on pipeline
Heavy oil extract out into the second heating furnace feed pump, the tower top being connected with vacuum jet is provided with the top of diesel oil vacuum tower
Line.
Further improve, the pressure of the boat coal atmospheric tower is 0.1～0.2Mpa, and air-distillation temperature is 260～300
℃；The pressure of diesel oil vacuum tower is 5～7Kpa, and vacuum distillation temperature is 230～240 DEG C.
Compared with prior art, it is an advantage of the current invention that：Cancel original catalysis waste heat steam boiler, newly-built pure convection current
The first heating furnace, cancel catalytic slurry heat recovery steam generator, heat exchanger in newly-built slurry heat-exchanger and two, cancel vacuum furnace
And atmospheric tower, newly-built boat coal atmospheric tower, diesel oil vacuum tower and the second heating furnace；Crude oil heat exchange flow process is improved simultaneously and reduces crude oil
Vapo(u)rizing temperature, transform normal pressure column distillation as boat coal atmospheric tower and diesel oil vacuum tower, makes the low temperature position extracted out from diesel oil vacuum tower
Heavy oil enters back into the second heating furnace with slurry heat-exchanger, two after heat exchanger heat exchange, and the first heating furnace adopts to be catalyzed flue gas
Based on fuel, heating in crude oil supplemented by combustion gas so all adds three kinds of waste heats in catalysis flue gas, slurry oil, two for atmospheric and vacuum distillation unit
Pyrogen oil, greatlys save atmospheric and vacuum distillation unit furnace fuel；Due to reducing crude distillation temperature, crude oil and cigarette are just solved
Heat transfer temperature difference technical barrier between in gas, slurry oil and two, substantially increases the economic effect of heat energy utilization.Present configuration sets
Meter is reasonable, and energy consumption is low, fundamentally solves that the heat utilization efficiency that the remaining pot of catalysis is present is relatively low, energy consumption wastes the remaining pot of big and catalysis
The problems such as various An full Hyperlink for existing suffer from, energy consumption is greatly reduced, saved combustion gas, improve economic benefit.
Description of the drawings
Fig. 1 is the structural representation of the present invention.
Specific embodiment
The present invention is described in further detail below in conjunction with accompanying drawing embodiment.
As shown in figure 1, the atmospheric and vacuum distillation unit to be catalyzed flue gas and slurry oil waste heat replacement furnace fuel of the present embodiment, bag
Include heat exchanger 6 and slurry oil in the first heating furnace 1, the second heating furnace 2, flash column 3, boat coal atmospheric tower 4, diesel oil vacuum tower 5, two
Heat exchanger 7, wherein the first heating furnace 1 is fume heating furnace, it is the pure convection current tubular heater of a radiationless room, first heats
About 12 two parts for the first convection cell 11 and combustor for 1 point of stove, and the bottom of the first heating furnace 1 is provided with what is entered for catalysis flue gas
The flue gas pipeline 16 of combustor 12, is provided with flue gas nozzles 121 in combustor 12, and flue gas nozzles 121 use the gas-fired combustion-supporting, effect to be
In order to improve flue-gas temperature, the carbon monoxide in flue gas is burnt, be allowed to become carbon dioxide, while supplementing flue gas heat not
Foot, flue gas pipeline 16 is connected with flue gas nozzles 121, and the top of the first heating furnace 1 is provided with flue gas discharge opening, in flue gas discharge opening
Place is provided with discharge flue 13, and the upper end side of the first convection cell 11 is provided with first via crude oil into pipeline 14, the first convection cell 11
Lower end side be provided with first via crude exports pipeline 15；So from the flue gas of catalytic unit cigarette machine outlet, from combustor 12
Bottom introduces the flue gas nozzles 121 in combustor 12, and after burning the carbon monoxide in flue gas, flue gas is pushed up upwards from combustor 12
Portion flows into the first convection cell 11, and in the first convection cell 11, crude oil in flue gas convection tube, temperature goes out after being reduced to 190 DEG C
First convection cell 11, then discharge from discharge flue 13 upwards, the crude oil Jing first via crude oil pipeline 14 from house steward 101 enters first
About 150-160 DEG C of the temperature of convection cell 11, goes out about 260-300 DEG C of the temperature of the first convection cell 11；Second is provided with flash column 3
Road crude oil enters main pipe line 33, and the second road crude oil is provided with two heat exchangers 8 into pipeline 31, Jing after the first heating furnace 1 is heated
Crude oil Jing crude oil after the phase Correspondent of pipeline 31 is entered by first via crude exports pipeline 15 and the second crude oil from house steward 101
Flash column 3 is entered into main pipe line 33, the bottom of flash column 3 is provided with the second tunnel crude exports pipeline 32, in the second tunnel crude exports
Pipeline 32 is provided with for extracting the crude oil of bottom of towe out be delivered in the convection cell 21 of the second heating furnace 2 pressure oil pump 9；Second adds
Hot stove 2 is a complete tubular heater, and about 22 two parts to be divided into the second convection cell 21 and radiation chamber, in the second convection cell
21 upper lateral part is provided with the pipeline being connected with the outlet line 27 of pressure oil pump 9, and in the following side of the second convection cell 21 original is provided with
Oil goes out the second heating furnace pipeline 24, is provided with discharge flue 23, radiation chamber 22 at the top of the second convection cell 21 and is provided with radial canal,
The bottom of radiation chamber 22 is provided with fuel gas nozzle, and the side of radiation chamber 22 is provided with and is connected with heat exchanger in two 6, slurry heat-exchanger 7
Heavy oil enter radiation chamber pipeline 25, the opposite side of radiation chamber 22 is provided with the heavy oil being connected with wax oil vacuum tower and goes out radiation chamber pipeline
26, such heating of second convection cell 21 is the reduced crude oil of Jing flash columns 3, is heated to 280-300 DEG C, into boat coal normal pressure
Tower 4, and radiation chamber 22 heating be heat exchanger 6 and slurry heat-exchanger 7 from two heavy oil, after heating pressed distillate decompression
Tower, heavy oil is heated to temperature for 380-390 DEG C in radiation chamber 22；The pressure of boat coal atmospheric tower 4 is 0.1～0.2Mpa, and boat coal is normal
The crude oil that the bottom side of pressure tower 4 is provided with the second heating furnace 2 goes out the interface that the second heating furnace pipeline 24 is connected, and navigate coal normal pressure
The top opposite side of tower 2 is provided with the kerosene outlet port 41 for extracting out kerosene after distillation, and in the bottom of towe of boat coal atmospheric tower 4 crude oil is provided with
Extract pipeline 42 out, the top of the coal atmospheric tower 4 that navigates is provided with oil and gas and removes cooler pipeline 43；The pressure of diesel oil vacuum tower 5 be 5～
7Kpa, diesel oil vacuum tower 5 be sequentially provided with from top to bottom be connected with the normal two wires Product Collection System of diesel oil normal two wires outlet port 51,
The atmosphere 3rd side cut outlet port 52 being connected with diesel oil atmosphere 3rd side cut Product Collection System and the bottom crude oil extraction pipe with boat coal atmospheric tower 4
The pipe joint that line 42 is connected, the bottom of diesel oil vacuum tower 5 is provided with the heavy oil being connected with heat exchanger in two 6, slurry heat-exchanger 7
Extract pipeline 53 out, to be arranged in parallel, heavy oil extracts pipeline 53 out and is provided with feed pump 10 for heat exchanger 6, slurry heat-exchanger 7 in two, from
The bottom of diesel oil vacuum tower 5 heavy oil out by feed pump 10 respectively with two in heat exchanger 6, slurry heat-exchanger 7 exchanged heat,
Then Jing pipelines 25 are entered back in the radiation chamber 22 of the second heating furnace 2, heavy oil go out the bottom of towe of diesel oil vacuum tower 5 temperature be 230～
240 DEG C, and heat exchanger 6, the temperature of slurry heat-exchanger 7 are 260～360 DEG C in two；The top of diesel oil vacuum tower 5 is provided with and steam
The overhead line 54 that evacuation is connected, using vacuum jet the vacuum pressure in diesel oil vacuum tower 5 is maintained.So crude oil navigates
Coal atmospheric tower 4 distills out rich gas, gasoline, kerosene at 260～300 DEG C of temperature, and afterwards crude oil adopts again vacuum distillation, diesel oil to subtract
230～240 DEG C of 5 vapo(u)rizing temperature of pressure tower, 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 farm, with fractionating column out product heat exchange, temperature
Spend and enter when rising to 150～160 DEG C electrical desalter, the crude oil Jing main pipe lines 101 after electricity is de- are divided into two-way to be continued to add
Heat：First via crude oil（About 20～30%）Jing first via crude oil goes the first couple of the first heating furnace of catalytic unit 1 into pipeline 14
Flow chamber 11, Jing convection tubes are heated to 250～300 DEG C, and crude oil goes out Jing first via crude oil after the first convection cell 11 of the first heating furnace 1
It is that the second road crude oil collaborates into pipeline 31 that outlet line 15 returns atmospheric and vacuum distillation unit with the second road crude oil pipeline；Second road crude oil
Continue same higher temperature product heat exchanger 8 in atmospheric and vacuum distillation unit into pipeline 31 to exchange heat, after heat exchange terminates, temperature is about
250-280 DEG C or so, the first via crude oil interflow returned with first via crude exports pipeline 15, Jing crude oil is entered behind crude oil interflow
Main pipe line 33 extracts most rich gas into the distillation of flash column 3, gasoline, due to the vapo(u)rizing temperature of flash column 3 it is not high enough, small part
Rich gas, gasoline is so to remain in crude oil；Afterwards crude oil flows into the bottom Jing crude exports pipeline 32 of flash column 3 and enters pressure oil pump
9, Jing after pressure oil pump 9 is pressurized crude oil Jing pump discharges pipeline 27 be heated to 280 into the second convection cell 21 of the second heating furnace 2～
300 DEG C, afterwards crude oil go out the second convection cell 22, Jing crude oil goes out the second heating furnace pipeline 24 and enters distillation in boat coal atmospheric tower 4, pulls out
Go out the boat coal of remaining rich gas, gasoline and whole in crude oil, afterwards crude oil flows into the bottom of boat coal atmospheric tower 4, by the pressure of itself
Jing crude oil extracts pipeline 42 out and flows into diesel oil vacuum tower 5, and in diesel oil vacuum tower 5, diesel oil steams by the sensible heat cab of crude oil itself
Evaporate and extract normal two, three line diesel oil, distillation is extracted crude oil after rich gas, gasoline, aerial kerosene and diesel oil and calls heavy oil in the following text.Heavy oil afterwards
Temperature is reduced to 230～240 DEG C or so and flows into the bottoms of diesel oil vacuum tower 5, because heavy oil temperature is relatively low, can realize with two in exchange heat
260～360 DEG C or so of slurry oil heat exchange in device 6, slurry heat-exchanger 7, the bottom heavy oil Jing heavy oil of diesel oil vacuum tower 5 is extracted pipeline 53 out and is flowed
Enter feed pump 10, the heavy oil after supercharging goes out atmospheric and vacuum distillation unit and removes catalytic unit, heat exchanger 6 and slurry heat-exchanger 7 add in two
Heat, after Jing heavy oil enter radiation chamber pipeline 25 and return to atmospheric and vacuum distillation unit, in the radiation chamber 22 of the second heating furnace 2, Jing spokes
Penetrate pipe and continue to be heated to 380～390 DEG C and go out radiation chamber 22 afterwards, Jing heavy oil goes out radiation chamber pipeline 26 and reduces pressure column distillation into wax oil
Isolate subtract one, two wires, the line wax oil that subtracts three.
Below just the Technology design design of the present invention is described in further details.
First, know-why
1st, the waste heat reclaiming process of catalytic unit is improved
（1）, cancel the remaining pot of catalysis, its middle pressure steam by thermo-power station Boiler High Pressure steam supply, equivalent to being displaced with coal
Combustion gas and fume afterheat that the remaining pot of catalysis is used.
（2）, will 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 saving catalysis
Pot and the target of atmospheric and vacuum distillation unit heating furnace combustion gas more than device.
2nd, the technique for improving atmospheric and vacuum distillation unit, reduces heating crude oil temperature
Three kinds of waste heats of catalysis are used for atmospheric and vacuum distillation unit heating crude oil, it is important to solve to be conducted heat between crude oil and waste heat
The too little problem of the temperature difference：The exhaust gas temperature of catalysis flue gas is 190 DEG C, and by the heat transfer temperature difference between flue gas and crude oil 40 are not less than
DEG C, such as requiring with flue gas come heating in crude oil, then the origin temp of heating crude oil is not above 150 DEG C；Slurry oil, extract 360 out in two
DEG C, 260 DEG C of tower oil temperature is returned, it is not less than 20 DEG C by the heat transfer temperature difference in slurry oil, two between crude oil, also require that crude oil heat exchange
Origin temp is not above 240 DEG C.And crude oil be about 250 with the temperature after the product heat exchange of this device in atmospheric and vacuum distillation unit～
280 DEG C, already less than zero, heat exchange can not possibly be realized the heat transfer temperature difference between thus causing in flue gas, slurry oil and two.
For this purpose, present patent application improves the technique of atmospheric and vacuum distillation unit, crude oil heat exchange and vapo(u)rizing temperature are reduced, solve to pass
The too little technical barrier of the hot temperature difference.
1st, crude oil heat exchange flow process is improved：150 DEG C of crude oil point two-way is exchanged heat after electro-desalting：First via crude oil（About
20～30%）Catalytic unit flue gas to 250～300 DEG C are removed, atmospheric and vacuum distillation unit is returned afterwards and is closed with the second road crude oil pipeline
Stream；Second road crude oil is in atmospheric and vacuum distillation unit with normal pressure and the product heat exchange of decompression higher temperature.After heat exchange terminates, first and second tunnel
Crude oil interflow enters flash distillation column distillation.
2nd, atmospheric and vacuum distillation unit crude distillation temperature is reduced：It transform former normal pressure column distillation as two towers：First：Normal pressure
Boat coal is transferred in tower, 260～300 DEG C of vapo(u)rizing temperature, distillation；Second：Vacuum tower, 230～240 DEG C of vapo(u)rizing temperature, distillation is transferred to
Diesel oil（Normal two, three lines）, 230～240 DEG C of remaining crude oil temperature after distillation.The temperature is just suitable for same slurry oil, two
（Extract 360 DEG C out, return 260 DEG C of tower oil temperature）Heat exchange, heat transfer temperature difference is larger.
2nd, particular technique content
1st, the residual neat recovering systems such as the flue gas and slurry oil of catalytic unit are transformed
Cancel the catalysis waste heat steam boiler before patent application is implemented, be changed to the of newly-built one pure convection current tubular heater
One heating furnace 1 is used for heating 150 DEG C of crude oil.Cancel heat recovery steam generator in the catalytic slurry and two before patent application is implemented,
Be changed in newly-built two heat exchangers i.e. slurry oil-crude heat exchanger 7 and two-crude heat exchanger i.e. two in heat exchanger 6, for heating
230～240 DEG C of crude oil.Catalytic unit steam is supplied by power station pipe network.
2nd, atmospheric and vacuum distillation unit production technology is transformed
（1）, heating furnace the Nomenclature Composition and Structure of Complexes
Cancel atmospheric pressure kiln and and vacuum furnace.Newly-built second heating furnace 2 substitutes atmospheric pressure kiln and vacuum furnace to be used for plus pyrogen
Oil.Before patent application is implemented, atmospheric and vacuum distillation unit has two heating furnaces（Atmospheric pressure kiln and and vacuum furnace）, wherein, atmospheric pressure kiln thermic load
It is larger, 2/3rds of two stove total heat duties are accounted for, vacuum furnace thermic load is less, accounts for 1/3rd.Patent application is implemented
Afterwards, because three kinds of waste heat amounts of catalytic unit have been more than or equal to vacuum furnace thermic load, therefore, it can cancel vacuum furnace, by atmospheric pressure kiln
A heating furnace is merged into vacuum furnace.So, the heating crude oil of atmospheric and vacuum distillation unit is just added by the first heating furnace 1 and second
Hot stove 2 is completed jointly.
（2）, Distallation systm
Before enforcement, atmospheric and vacuum distillation unit is substantially three column distillations（Atmospheric tower:The flash column of distillation rich gas and gasoline, distillation
The vacuum tower of aerial kerosene, the atmospheric tower of diesel oil and a distillation wax oil）.After technology implementation, atmospheric tower is changed to two towers, newly
Build boat coal atmospheric tower 4 and diesel oil vacuum tower 5.Crude oil is first in atmospheric tower（0.1～0.2Mpa of pressure, 260～300 DEG C of temperature）Interior steaming
Evaporate, transfer to remaining rich gas, gasoline and kerosene.Afterwards crude oil goes distillation in vacuum tower, and reduce pressure pressure tower（5～7Kpa absolute pressures, steam
Evaporate 230～240 DEG C of temperature）.Transfer to diesel oil（Normal two, three lines）.Afterwards crude oil removes the same slurry oil of catalytic unit, exchanges heat in two.Heat exchange
After end, crude oil returns again to atmospheric and vacuum distillation unit and is heated to 380～390 DEG C into the radiation chamber 22 of the second heating furnace 2, and spoke is gone out afterwards
Penetrate the pressed distillate decompression column distillation of room 22 and transfer to wax oil.
The performance analysis produced after enforcement：
3rd, patent application implementation benefit：
1st, replace discard pot in catalysis combustion gas with the coal-fired high-pressure boiler in power station to bring benefits
About 2.4 tons of marks of 3000000 tons of catalysis fume afterheat amounts oil/when, 3.2 tons of marks of slurry oil waste heat oil/when, waste heat 0.8 in two
Ton mark oil/when, add up to 6.4 tons of marks of waste heat amount oil/when.Three waste heat Atmospheric vacuum heating in crude oil, make Atmospheric vacuum save combustion gas
6.4 tons mark oil/when.Cancel discard pot in catalysis combustion gas, catalytic unit steam is provided by power station fire coal high-pressure boiler.Such one
Come, in catalysis 2 tons of combustion gas used by discard pot mark oil/when be all conserved.Above-mentioned two total 8.4 tons of marks oil/when.Combustion gas
With coal price difference about 4000 yuan/ton mark oil, fire coal change combustion gas bring benefits for
8.4X104X4000=3.36 hundred million yuan/year
2nd, energy-saving benefit
High-pressure boiler generates electricity more than medium-pressure boiler：
Generate electricity 3600Kw more per 100t/h high steams than low-pressure steam.Every year many generated energy are
3600X8400=3024X104 degree/year
0.6 yuan of electricity price/degree, many power benefits are：
3024X104X0.6 units /=0.18 hundred million yuan/year of degree
Energy-conservation total benefit is
3.36+0.18=3.54 hundred million yuan/year
3rd, the An full Hyperlink trouble that the remaining pot of catalysis is present is solved
After implementing present patent application technology, the remaining pot of catalysis is cancelled, refinery's process steam all by power station supply, from basic
On solve the various An full Hyperlink that the remaining pot of catalysis is present and suffer from and problem.
4th, technological investment recovery time is short
A set of catalytic unit adopts present patent application technology, fume heating furnace to invest about 0.5 hundred million yuan；Atmospheric vacuum is transformed about
About 100,000,000 yuan of 0.5 hundred million yuan of total patent application technologies gross investment.Using present patent application technology bring benefits about 3.54 hundred million yuan/
Year, after deducting investment, technology pure benefit then is about 200,000,000 yuan/year, and the investment payback time is very short, and about three months to half a year.
Claims (9)
1. a kind of Atmospheric vacuum-catalysis flue gas slurry oil heat integration device, it is characterised in that：Including the first heating furnace, the second heating furnace,
Flash column, boat coal atmospheric tower and diesel oil vacuum tower,
Wherein the first heating furnace is fume heating furnace, and the bottom of the first heating furnace is provided with the flue gas pipeline entered for catalysis flue gas,
Flue gas discharge opening is provided with the top of first heating furnace, first via crude oil is additionally provided with the first heating furnace into pipeline and the first via
Crude exports pipeline；
Flash column, is provided with the second road crude oil and enters main pipe line on flash column, the crude oil Jing after the first heating stove heat is by the
All the way crude exports pipeline enters pipeline phase Correspondent with the second road crude oil, and in the bottom of flash column the second tunnel crude exports pipe is provided with
Line；
Second heating furnace is tubular heater, is divided into the second convection cell and upper and lower two part of radiation chamber, and the second heating furnace is provided with
The pipeline and crude oil being connected with the second tunnel crude exports pipeline of flash column goes out the second heating furnace pipeline；
Boat coal atmospheric tower is provided with and goes out extract out kerosene after the interface and distillation that the second heating furnace pipeline is connected with crude oil
Kerosene outlet port, is provided with crude oil and extracts pipeline out in the bottom of towe of boat coal atmospheric tower；
Diesel oil vacuum tower is provided with extracts the pipe joint that pipeline is connected, diesel oil vacuum tower out with the bottom crude oil of boat coal atmospheric tower
Bottom be provided with the heavy oil that is connected with the second heating furnace and extract pipeline out, extract out in heavy oil and arranged between pipeline and the second heating furnace
There is heat exchanger in slurry heat-exchanger and two.
2. Atmospheric vacuum according to claim 1-catalysis flue gas slurry oil heat integration device, it is characterised in that：Described first adds
Hot stove is divided into the first convection cell and upper and lower two part of combustor, and burning interior is provided with flue gas nozzles, and flue gas pipeline is located at combustor
Bottom be connected with flue gas nozzles, discharge flue is provided with the top flue gas discharge opening of the first convection cell, first via crude oil enters
Enter pipeline located at the upper end side of the first convection cell, first via crude exports pipeline is located at the lower end side of the first convection cell.
3. Atmospheric vacuum according to claim 1-catalysis flue gas slurry oil heat integration device, it is characterised in that：Second tunnel
Crude oil is provided with heat exchanger into pipeline, and the second tunnel crude exports pipeline of flash distillation tower bottom is provided with for by the crude oil of bottom of towe
Extraction is delivered to the pressure oil pump in the second heating furnace.
4. Atmospheric vacuum according to claim 1-catalysis flue gas slurry oil heat integration device, it is characterised in that：Described second adds
Hot stove includes the second convection cell and radiation chamber setting up and down, the pipeline being connected with the second tunnel crude exports pipeline of flash column
The upper lateral part of the second convection cell is arranged on, crude oil goes out the following side that the second heating furnace pipeline is arranged on the second convection cell, second
Discharge flue is provided with the top of convection cell.
5. Atmospheric vacuum according to claim 4-catalysis flue gas slurry oil heat integration device, it is characterised in that：The radiation chamber
Radial canal is inside provided with, the bottom of radiation chamber is provided with fuel gas nozzle, and the side of radiation chamber is provided with and heat exchanger in slurry heat-exchanger, two
The heavy oil being connected enters radiation chamber pipeline, and the opposite side of radiation chamber is provided with the heavy oil being connected with wax oil vacuum tower and goes out radiation chamber pipe
Line.
6. Atmospheric vacuum according to claim 1-catalysis flue gas slurry oil heat integration device, it is characterised in that：Change in described two
Hot device, slurry heat-exchanger are to be arranged in parallel.
7. Atmospheric vacuum according to claim 1-catalysis flue gas slurry oil heat integration device, it is characterised in that：The boat coal is normal
Go out with crude oil the bottom side that the interface that the second heating furnace pipeline is connected is arranged on boat coal atmospheric tower, kerosene outlet port on pressure tower
The top opposite side of boat coal atmospheric tower is arranged on, gasoline is provided with the top of boat coal atmospheric tower and is removed cooler pipeline.
8. Atmospheric vacuum according to claim 1-catalysis flue gas slurry oil heat integration device, it is characterised in that：The diesel oil subtracts
The normal two wires outlet port and diesel oil atmosphere 3rd side cut being connected with the normal two wires Product Collection System of diesel oil is sequentially provided with from top to bottom on pressure tower
The connected atmosphere 3rd side cut outlet port of Product Collection System and the pipeline being connected with the bottom crude oil extraction pipeline of boat coal atmospheric tower
Interface, extracts out to be provided with pipeline and extracts the heavy oil of bottom of towe out entering into the second heating furnace in the heavy bottom oil of diesel oil vacuum tower
Material pump, is provided with the overhead line being connected with vacuum jet at the top of diesel oil vacuum tower.
9. Atmospheric vacuum according to claim 1-catalysis flue gas slurry oil heat integration device, it is characterised in that：The boat coal is normal
The pressure of pressure tower is 0.1～0.2Mpa, and air-distillation temperature is 260～300 DEG C；The pressure of diesel oil vacuum tower is 5～7Kpa, is subtracted
Pressure vapo(u)rizing temperature is 230～240 DEG C.
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| CN201410100130.2A CN104927905B (en) | 2014-03-18 | 2014-03-18 | Atmospheric and vacuum catalytic flue gas-oil slurry heat combined device |
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| CN201410100130.2A CN104927905B (en) | 2014-03-18 | 2014-03-18 | Atmospheric and vacuum catalytic flue gas-oil slurry heat combined device |
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| CN104927905B true CN104927905B (en) | 2017-05-10 |
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Citations (5)
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|---|---|---|---|---|
| JPS58152090A (en) * | 1982-03-05 | 1983-09-09 | Mitsui Eng & Shipbuild Co Ltd | Method for feeding hydraulic oil and dilution oil to heavy oil pump |
| RU2149171C1 (en) * | 1999-10-06 | 2000-05-20 | Сейфулов Рашид Ваисович | Method for production of lube oils from low-sulfur and/or sulfur and/or high-sulfur oils |
| CN102443420A (en) * | 2010-10-13 | 2012-05-09 | 中国石油化工股份有限公司 | Crude oil deep vacuum distillation process and system |
| CN202519210U (en) * | 2012-03-28 | 2012-11-07 | 东营华联石油化工厂有限公司 | Top cycle oil heat integration device of catalytic device fractionating tower |
| CN203866254U (en) * | 2014-03-18 | 2014-10-08 | 雷泽永 | Atmospheric and vacuum device adopting combined catalytic flue gas and oil slurry |
-
2014
- 2014-03-18 CN CN201410100130.2A patent/CN104927905B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS58152090A (en) * | 1982-03-05 | 1983-09-09 | Mitsui Eng & Shipbuild Co Ltd | Method for feeding hydraulic oil and dilution oil to heavy oil pump |
| RU2149171C1 (en) * | 1999-10-06 | 2000-05-20 | Сейфулов Рашид Ваисович | Method for production of lube oils from low-sulfur and/or sulfur and/or high-sulfur oils |
| CN102443420A (en) * | 2010-10-13 | 2012-05-09 | 中国石油化工股份有限公司 | Crude oil deep vacuum distillation process and system |
| CN202519210U (en) * | 2012-03-28 | 2012-11-07 | 东营华联石油化工厂有限公司 | Top cycle oil heat integration device of catalytic device fractionating tower |
| CN203866254U (en) * | 2014-03-18 | 2014-10-08 | 雷泽永 | Atmospheric and vacuum device adopting combined catalytic flue gas and oil slurry |
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