CN107227172A - A kind of method for reducing absorbing-stabilizing system power consumption - Google Patents

A kind of method for reducing absorbing-stabilizing system power consumption Download PDF

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Publication number
CN107227172A
CN107227172A CN201710558678.5A CN201710558678A CN107227172A CN 107227172 A CN107227172 A CN 107227172A CN 201710558678 A CN201710558678 A CN 201710558678A CN 107227172 A CN107227172 A CN 107227172A
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tower
gas
stabilizer
overhead
desorber
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CN107227172B (en
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李国庆
蔡楚轩
张家龙
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South China University of Technology SCUT
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South China University of Technology SCUT
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
    • C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
    • B01D3/322—Reboiler specifications
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/42—Regulation; Control
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/1044—Heavy gasoline or naphtha having a boiling range of about 100 - 180 °C
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4012—Pressure
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/02—Gasoline

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The invention discloses a kind of method for reducing absorbing-stabilizing system power consumption, core content is will to desorb column overhead operating pressure to be reduced to 0.25MPag 0.4MPag by current 1.2MPag, stable column overhead operating pressure is reduced to 0.3MPag 0.4MPag by current 1.15MPag, and change and give desorption tower overhead gas to rich gas compressor one-level entrance, and set stable tower overhead gas compressor to ensure LPG normal-temperature liquefactions.Because desorption tower overhead gas is substantially free of C3/C4, stabilizer relief flow back amount declines to a great extent, therefore the flow of two strands of gas is less, and increase compression power consumption is few, and using the anti-allowance that flies of rich gas compressor, and stable tower overhead gas compressor uses one stage of compression electricity to drive technique and be arranged in tower top platform.And desorber and stabilizer not only make heating load reduce nearly half because of reduced pressure operation, and column bottom temperature is decreased obviously, and uses hot water instead respectively and 1.0MPa steam does thermal source, remove from and being boiled again in the middle of desorber.

Description

A kind of method for reducing absorbing-stabilizing system power consumption
Technical field
The invention belongs to PETROLEUM PROCESSING field, more particularly to a kind of desorber and stabilizer reduced pressure operation, and then drop simultaneously The method of low absorption systems stabilisation energy consumption.
Background technology
The important composition for the crude oil secondary operation device such as absorbing-stabilizing system is catalytic cracking, delayed coking, be hydrocracked Part, is mainly made up of absorption tower, reabsorber, desorber, stabilizer and corresponding cold exchange device.It is to utilize absorption that it, which is acted on, The rich gas from main fractionating tower and raw gasoline (or crude naphtha) are separated into dry gas, liquid hydrocarbon and vapour pressure with the method for rectifying Qualified stable gasoline (or naphtha).
Because the arrangement of absorption and desorption is different, absorbing-stabilizing system generally has two kinds of flows of single column and double tower.Single column stream Journey collects absorption, desorbed in a tower, and double-column process is then divided among in two towers and completed, thus has more than single column flow Good absorption and desorption effect, using more.
(see Fig. 1) in double-column process, the oil gas from main fractionating tower tower top enters knockout drum, the liquid phase separated after cooling Raw gasoline enters absorption tower, and gas phase rich gas then first compress, it is solidifying to send after cooling together with desorbing tower overhead gas and absorption tower base oil again Contracting oil tank, the balance gas phase separated send absorption tower, in the presence of raw gasoline and stable gasoline (also known as supplementing absorbent), removing Therein >=C3Component, the lean gas of relative " more dry " is obtained from tower top, and rich in >=C3The rich absorbent oil of component is then extracted out by bottom of towe Return condensing oil tank.In order to ensure assimilation effect, absorption tower generally sets one or two water recirculator at middle part, to take away Exothermic dissolution, reduces the operation temperature of tower.The lean gas that self-absorption tower top comes out independently is divided then from being pressed into reabsorber bottom Evaporate the downward low temperature of the adverse current of tower (about 40 DEG C) product diesel oil further to absorb, with tower top to >=C3Constituent content is less than 3% (mol) product dry gas, and the rich diesel oil of bottom of towe saturation then returns to main fractionating tower freshening.The charging of desorber is to come from condensing oil tank Condensed oil, its effect be in the presence of bottom of towe again boiling hot amount, by be dissolved in condensed oil≤C2Component is desorbed, And drawn by tower top and give condensing oil tank, and bottom of towe deethanization gasoline is then pumped up to stabilizer, in stabilizer bottom boiling hot amount again Under effect, LPG products are obtained from tower top, bottom of towe obtains stable gasoline.After stable gasoline cools, partly go out dress as product Put, partly go to absorption tower as supplement absorbent.
Obviously, desorber bottom boil again boiled again with stabilizer bottom be above-mentioned absorbing-stabilizing system two cores power consumption, account for More than the 85% of absorbing-stabilizing system total energy consumption, because its tower top operating pressure respectively may be about 1.2MPag and 1.15MPag, correspondence Column bottom temperature respectively at 130 DEG C and 180 DEG C or so, therefore have to be flowed back with 1.0MPa steam and the stage casing of main fractionating tower first (from Potential temperature sees that the backflow of the first stage casing is the heat for producing 3.5MPa steam) do thermal source.Again because the former controls in deethanization gasoline≤C2 Constituent content is not more than in 0.3 ‰ (mol), the latter's control LPG >=C5Constituent content≤1% (mol), therefore two towers is boiling hot again Load is than larger.
The content of the invention
To solve in existing absorption stabilizing process, desorber and stabilizer due to elevated pressures operation cause separating energy consumption compared with The problem of high and higher power consumption grade, it is an object of the invention to provide the low of a kind of desorber and stabilizer reduced pressure operation simultaneously The method of power consumption absorbing-stabilizing system.
The present invention is a kind of method for reducing absorbing-stabilizing system power consumption, and described system includes desorber, stabilizer, suction Receive tower, reabsorber, it is characterised in that it is as follows that its technical scheme includes step in detail below：
1) isolated rich gas and raw gasoline after the overhead oil air cooling from main fractionating tower；
2) rich gas is first with desorption tower overhead gas mixing, and pressurization is cooled to gas liquid mixture, after being mixed with absorption tower base oil, enters The liquid that gas in condensing oil tank, condensing oil tank enters in absorption tower, condensing oil tank then enters desorber；
3) raw gasoline enters absorption tower, and tower top distillates lean gas, and bottom of towe distillates rich absorbent oil；
4) lean gas enters reabsorber, and reabsorber tower top obtains dry gas, and bottom of towe richness diesel oil then returns to main fractionation as raw material Tower；
5) the pressurized laggard stabilizer of heating of the deethanization gasoline of desorber bottom of towe outflow, desorbs the operating pressure of column overhead Control is in 0.25MPag-0.4MPag, and the reboiler of desorber does thermal source with 85~98 DEG C of hot water；
6) after stabilizer overhead gas compression cooling, tower is returned in wherein 71%wt backflows, and remaining 29%wt liquefies as product Gas is discharged, and after the gasoline cooling of stabilizer bottom of towe, wherein 60%wt is discharged as product, and 40%wt send suction as supplement absorbent Tower is received, the operating pressure of stable column overhead is controlled in 0.3MPag-0.4MPag, stabilizer overhead gas compressor delivery pressure control System is in 1.1MPag-1.2MPag, and the reboiler of stabilizer does thermal source with steam.
It is preferred that, in step (5), the operating pressure of desorption column overhead is controlled in 0.3MPag.
In step (5), desorber overhead gas feeding rich gas stage compressor.
It is preferred that, in step (5), the operating pressure of stable column overhead is controlled in 0.35MPag.
It is preferred that, in step (6), stabilizer overhead gas compressor delivery pressure is controlled in 1.15MPag.
In step (6), the Steam pressure control of the reboiler of stabilizer is in 0.5-1.0MPag.
The present invention is based on following principle：
1) reduced pressure operation is beneficial to the relative volatility for improving the separated component of distillation system, refers in the number of plates and product quality In the case that mark is certain, reflux ratio and column bottom temperature can be reduced, and then load and heat supply energy level are boiled in reduction again；
2) C can be improved by improving pressure3、C4The bubble of lower carbon number hydrocarbons, dew-point temperature, allow its normal-temperature liquefaction；
3) when low grade heat supply means identical heating load, the outside available energy of system consumption is few, thus cost is lower.
Present invention process has the following advantages that and beneficial effect：
1) reduction energy consumption and energy consumption quality.Desorber and stabilizer are while reduced pressure operation, can reduce absorbing-stabilizing system Core consumes energy, while substantially reducing its grade that consumes energy so that desorber can make thermal source of hot water, and stabilizer can use 1.0MPa steam Thermal source is done, the cooling load of correspondence system is greatly reduced.
2) flow of desorber is simplified.Load is boiled again in order to reduce bottom of towe, and desorber would generally be set with stabilizer base oil The secondary intermediate reboiler for doing thermal source.On the one hand desorber greatly reduces boils load again, is on the other hand substituted with hot water 1.0MPa steam does thermal source, therefore need not set intermediate reboiler again.
3) capacity of technique low temperature hot trap is improved.In new technological process, desorber bottom is boiled again and the heating of deethanization gasoline is equal Thermal source can be done with hot water, this helps to increase the load of refinery processes low temperature hot trap, extremely had to relaxing summer hot water surplus Benefit.
4) flow is changed little, it is easy to implemented.Desorb tower overhead gas flow less, be immediately directed against rich gas compressor one-level and enter Mouthful, route is uncomplicated, and enforcement difficulty is little；Stabilizer new compressor less, can use one stage of compression technique, stream due to pressure ratio Journey is uncomplicated, and without newly-increased cooler and point flow container.
5) compression power consumption increase is few.Because desorption tower overhead gas is substantially free of C3/C4, stabilizer relief flow back amount significantly under Drop, therefore the flow of two strands of gas is less, though desorption tower overhead gas is through rich gas compressor second-compressed, balance is to return the amount of flying, Do not increase power consumption additionally.Stabilizer reduced pressure operation, component relative volatility is improved, therefore reflux ratio is greatly reduced, therefore tower overhead gas Amount is little, and one stage of compression, and power consumption is also little, can motor driving, be conveniently arranged in tower top framework.
6) technique is suitable to old plant modification and new equipment construction.For improvement project, absorption tower and stabilizer decompression behaviour Make, main body is without change.
7) control of product quality scheme is constant, and product yield is unaffected.
Brief description of the drawings
Fig. 1 is the flow of the existing absorbing-stabilizing system of comparative example of the present invention.
Fig. 2 is a kind of desorber of the embodiment of the present invention and stabilizer while the low power consuming absorbing-stabilizing system of reduced pressure operation is new The flow of technique.
1- main fractionating tower tower top oil gas condensation coolers；2- knockout drums；3- raw gasoline pumps；4- one-level rich gas compressors；5- Interstage cooler；6- points of flow containers；Bis- grades of rich gas compressors of 7-；8- rich gas compressors export the first cooler；9- air coolers；10- Rich gas compressor exports the second cooler；The condensing oil tanks of 11-；The condensing oil pumps of 12-；13- desorber feed preheaters；14- absorbs Tower；15- absorption towers intercooler one；16- absorption towers intercooler two；17- rich absorbent oil pumps；18- reabsorbers；19- Desorber；20- desorption tower reboilers；21- deethanization petrol pumps；22- stabilizers；23- stabilizer reboilers；24- stable gasolines Pump；25- stabilizer feed preheaters；26- desalination water- to-water heat exchangers；27- stable gasoline coolers；28- stabilizer overhead oil air cooling Solidifying cooler；29- stabilizer return tanks；30- stabilizer reflux pumps；31- pressure-reducing valves；32- stabilizer feed preheaters；33- is steady Determine column overhead oil gas compressor.
Embodiment
With reference to embodiment and accompanying drawing, the present invention is described in further detail, but embodiments of the present invention are not limited In this.
By taking the heavy oil catalytically cracking equipment absorbing-stabilizing system of 800,000 tons of certain annual working ability as an example.
Comparative example 1
This comparative example is existing absorption stabilizing process, and its flow is as shown in Figure 1.It is specific as follows：Tower from main fractionating tower Top oil gas (102.7t/h, 0.19MPag, 119.3 DEG C) is cooled to 43.5 DEG C by main fractionating tower tower top oil gas condensation cooler 1 Into catch pot 2, rich gas (16400Nm is isolated to3/ h) and raw gasoline (61.8t/h).Raw gasoline is arrived through the pressure-raising of pump 3 1.9MPag enters absorption tower (tower top pressure 1.05MPag).Rich gas through one-level rich gas compressor 4, interstage cooler 5, point flow container 6, Two grades of pressure-raisings of rich gas compressor 7 are to 1.15MPag, with desorption tower overhead gas (4355Nm3/ h, 1.2MPag, 67.4 DEG C) mixing, and pass through Rich gas compressor is exported after the first cooler 8, the cooling of air cooler 9, with the absorption tower base oil (73t/ pressurizeed through rich absorbent oil pump 17 H, 1.1MPag, 41 DEG C) mixing, then through rich gas compressor export the second cooler 10 cooling enter condensing oil tank 11.Condensed oil In tank, balanced gas (13670Nm3/ h, 1.1MPag, 37.2 DEG C) be pressed into absorption tower 14 certainly, by raw gasoline and as supplement absorb The stable gasoline of agent absorbs, with remove its >=C3Component, the heat of adsorption discharged absorbs then by absorption tower intercooler 1 Tower intercooler 2 16 is taken away.Absorb tower top lean gas (9184Nm3/ h, 1.05MPag, 44.4 DEG C) remove reabsorber 18, come Absorbed from the light diesel fuel of main fractionating tower (27t/h, 2.0MPag, 28 DEG C) depth, tower top obtains >=C3Component molar content≤3% Dry gas (8241Nm3/ h, 1MPag, 34 DEG C), bottom of towe richness diesel oil then return to main fractionating tower.Condensing oil tank liquid (88.9t/h) is first 1.9MPag is pressurized to through condensing oil pump 12, then through desorber feed preheater 13, solution is sent to 65 DEG C by stable gasoline reheating Inhale tower 19.Tower top operating pressure 1.2MPag is desorbed, 125.3 DEG C of column bottom temperature of correspondence, circulation boils logistics and return 140.3 DEG C of tower, follows again Circular rector 210t/h (its mole of rate of gasification 15%, similarly hereinafter), bottom of towe desorption tower reboiler 20 does thermal source with 6t/h, 1.0MPag steam, Thermic load 338 × 104Kcal/h, to ensure in bottom of towe deethanization gasoline≤C2The molar content of component≤3 ‰.Deethanization gasoline (125.3 DEG C, 81.7t/h) is then pressurized to 1.6MPag through deethanization petrol pump 21, with stabilizer base oil once (176.1 DEG C, 71.6t/h) heat exchange is to entering stabilizer 22 after 128 DEG C.Stable tower top operating pressure 1.15MPag, correspondence tower top temperature 58.2 DEG C, cold reflux amount 32.8t/h, 176.1 DEG C of column bottom temperature, circulation boil that 184.1 DEG C of tower is returned in logistics, (it rubs internal circulating load 337t/h again That rate of gasification 20%, similarly hereinafter).The thermal source of bottom of towe stabilizer reboiler 23 be flow back once in main fractionating tower one (337 DEG C, 102.4t/h), it is in release 505 × 104After kcal/h heats, 23 return fractionating systems are left with 260 DEG C.Correspondence tower top cooling Load 345 × 104Kcal/h, obtains >=C5The LPG products 10t/h of component molar content≤1%.And stabilizer base oil (176.1 DEG C, 71.6t/h) then successively through stabilizer feed preheater 25, desorber feed preheater 13, desalination water- to-water heat exchanger 26 and stably Gasoline cooler 27, is cooled to 37 DEG C, wherein 43.7t/h goes out device as product, and 28t/h makees supplement absorbent and send absorption Tower.
Embodiment 1
A kind of desorber of the present embodiment and stabilizer are while the low power consuming absorbing-stabilizing system new technology of reduced pressure operation, it flows Journey is as shown in Figure 2.Detailed process is as follows：
Tower top oil gas (12.7t/h, 0.19MPag, 119.3 DEG C) from main fractionating tower passes through main fractionating tower tower top oil gas Condensate cooler 1 is cooled to 43.5 DEG C and enters catch pot 2, is isolated to rich gas (16400Nm3/ h) and raw gasoline (61.8t/h).Raw gasoline enters absorption tower (tower top pressure 1.05MPag) through the pressure-raising of raw gasoline pump 3 to 1.9MPag.Rich gas then first with Desorb tower overhead gas (5575Nm3/ h, 28.2 DEG C, 0.3MPag) mixing, then through one-level rich gas compressor 4, interstage cooler 5, point liquid Tank 6 and two grades of rich gas compressors 7, pressure-raising to 1.15MPag, then through the first cooler 8 of rich gas compressor outlet, air cooling 9, After being mixed with the absorption tower base oil (73t/h, 1.1MPag, 41 DEG C) pressurizeed through rich absorbent oil pump 17, through rich gas compressor outlet the The cooling of two coolers 10 enters condensing oil tank 11.In condensing oil tank, balanced gas (14225Nm3/ h, 1.1MPag, 37.2 DEG C) from Absorption tower 14 is pressed into, accompanying >=C to remove is adsorbed by raw gasoline and as the stable gasoline of supplement absorbent3Component, and The heat that absorption process is discharged then is taken away by absorption tower intercooler 1 and absorption tower intercooler 2 16.Absorption tower Push up lean gas (9243Nm3/ h, 1.05MPag, 45.1 DEG C) be pressed into reabsorber 18 certainly, by from main fractionating tower diesel oil (27t/h, 2.0MPag, 28 DEG C) further absorb, tower top obtains >=C3Dry gas (the 8266Nm of component molar content≤3%3/h、1.0MPag、 34 DEG C), bottom of towe richness diesel oil then returns to main fractionating tower.Condensing oil tank liquid (92.2t/h) then enters desorber.Now, its tower Pressure on top surface falls below 0.3MPag, overhead gas (5575Nm3/ h) change and sent rich gas compressor entrance, correspondence tower top temperature 28.2 DEG C, 58.8 DEG C of column bottom temperature, circulation boil logistics again and return 77.2 DEG C of tower temperature degree, internal circulating load 90t/h, desorption tower reboiler 20 is with 85 DEG C ~98 DEG C of hot water 122.3t/h does thermal source, thermic load 159 × 104Kcal/h, to ensure in bottom of towe deethanization gasoline≤C2Component Molar content≤3 ‰.And bottom of towe deethanization gasoline (58.8 DEG C, 82.7t/h) is then through the pressure-raising of deethanization petrol pump 21 and warp Stabilizer feed preheater 32 follows secondary (~115 DEG C) by main fractionating tower top and is heated to 81.7 DEG C of laggard stabilizers 22.Now, surely The tower top operating pressure for determining tower has dropped down to 0.40MPag, 12 DEG C of tower top temperature of correspondence, cold reflux amount 24.3t/h, column bottom temperature 105 DEG C, circulation boils logistics and returns 114.1 DEG C of tower temperature degree, internal circulating load 162.7t/h again.Tower bottom reboiler 23 5t/h, 1.0MPag steam Do thermal source, thermic load 280 × 104Kcal/h, to ensure that stable gasoline Lei Shi vapour pressures are qualified.Stabilization overhead gas (12 DEG C, 16677Nm3/ h, 34.2t/h) then through the newly-increased one stage of compression of stabilizer overhead oil air compressor 33 to 1.15MPag (70 DEG C) Afterwards, 30 DEG C are cooled to through stabilizer tower top oil gas condensation cooler 28 and enter stabilizer return tank 29, correspondence cooling load 322 × 104Kcal/h, wherein 24.3t/h are depressured to 0.4MPag, 5 DEG C (correspondence rate of gasification 15%wt) back through pressure-reducing valve 31 and return tower, Remaining 10t/h goes out device (wherein >=C as product liquefied gas5Component molar content≤1%).And stabilizer base oil (105 DEG C, 37 DEG C then 72.7t/h) are cooled to through stable gasoline cooler 27, wherein 43.7t/h goes out device as product, and 29t/h is used as benefit Fill absorbent and send absorption tower.
Embodiment 1 and the observable index of comparative example 1 compared with
In comparative example 1, desorption tower bottom reboiler consumption 1.0MPag steam 6t/h, by 210t/h circulation boil again logistics from 125.3 DEG C are heated to 140.3 DEG C, thermic load 338 × 104kcal/h；Stable tower bottom reboiler folding consumption 3.5MPag steam 9t/h Logistics is boiled into 337t/h circulations again 184.1 DEG C, thermic load 505 × 10 are heated to from 176.1 DEG C4kcal/h.Always heating is negative for two towers Lotus 843 × 104Kcal/h, consumption steam 15t/h.
In embodiment 1, desorption tower top operating pressure drops to 0.3MPag, correspondence tower bottom reboiler consumption 85 from 1.15MPag DEG C~98 DEG C of hot water 122.3t/h, logistics is boiled into 90t/h circulations again and is heated to 77.2 DEG C from 58.8 DEG C, thermic load 159 × 104Kcal/h (more former flow reduction by 53%).Stable tower top operating pressure drops to 0.40MPag from 1.15MPag, and correspondence bottom of towe is again Device consumption 1.0MPag steam 5t/h are boiled, 162.7t/h circulations are boiled into logistics again is heated to 114.1 DEG C, thermic load 280 from 105 DEG C ×104Kcal/h (more former flow reduction by 44.6%).Total two tower heating loads 439 × 104Kcal/h, consumption steam 5t/h, heat Water 122.3t/h.
In another embodiment 1,5575Nm3/ h desorbers gas returns to rich gas compressor second-compressed, does not consider that occupancy is returned and flies Allowance, (similarly hereinafter) wasted work 250kW is calculated by compressor isentropic Compression efficiency 75%；And 16677Nm3/ h stabilizers gas from 0.40MPag is compressed to 1.15MPag, wasted work 689kW.Both total 939kW.
Integrated embodiment always heats energy consumption from 843 × 10 compared with comparative example desorber and stabilizer4Kcal/h drops to 439 × 104Kcal/h, reduces 404 × 104Kcal/h, the range of decrease 47.9%, the total steam consumption quantity of correspondence drops to 5t/h, the range of decrease from 15t/h 67%, but newly-increased compression power consumption 939kW, hot water consumption 122.3t/h.Total embodiment is compared with the reduction of comparative example device total energy consumption 6.7kg marks oil/t virgin materials.Again based on monovalent 200 yuan/t, 3.5MPa steam unit price, the 250 yuan/t of 1.0MPa steam, 0.90 yuan of electricity price/ Kwh, 0.5 yuan/t of hot water unit price are calculated, and compared with comparative example reduction energy consumption cost 12,960,000 yuan/year, (other costs change such as embodiment The reduction of cooling load, the reduction of oil pump power consumption, the change of demineralized water heating load etc. are ignored).
It is equal to 0.997 kilogram of CO of emission reduction according further to 1 degree of electricity is saved2, save 1 kilogram of standard coal and be equal to emission reduction 2.493 thousand Gram CO2, the standard calorific value of one kilogram of coal is 0.7 × 104Kcal, new technology can save CO2Discharge capacity 502kg/h, converts into 4222t/ A, fall 16.9%.
Above-described embodiment is preferably embodiment, but embodiments of the present invention are not by above-described embodiment of the invention Limitation, other any Spirit Essences without departing from the present invention and the change made under principle, modification, replacement, combine, simplification, Equivalent substitute mode is should be, is included within protection scope of the present invention.

Claims (6)

1. it is a kind of reduce absorbing-stabilizing system power consumption method, it is characterised in that described system include desorber, stabilizer, Absorption tower, reabsorber, specific steps include：
1) isolated rich gas and raw gasoline after the overhead oil air cooling from main fractionating tower；
2) rich gas is first with desorption tower overhead gas mixing, and pressurization is cooled to gas liquid mixture, after being mixed with absorption tower base oil, into condensing The liquid that gas in oil tank, condensing oil tank enters in absorption tower, condensing oil tank then enters desorber；
3) raw gasoline enters absorption tower, and tower top distillates lean gas, and bottom of towe distillates rich absorbent oil；
4) lean gas enters reabsorber, and reabsorber tower top obtains dry gas, and bottom of towe richness diesel oil then returns to main fractionating tower as raw material；
5) the pressurized laggard stabilizer of heating of the deethanization gasoline of desorber bottom of towe outflow, the operating pressure control of desorption column overhead In 0.25MPag-0.4MPag, the reboiler of desorber does thermal source with 85~98 DEG C of hot water；
6) after stabilizer overhead gas compression cooling, tower is returned in wherein 71%wt backflows, and remaining 29%wt is arranged as product liquefied gas Go out, after the gasoline cooling of stabilizer bottom of towe, wherein 60%wt is discharged as product, 40%wt send absorption as supplement absorbent Tower, the operating pressure control of stable column overhead is in 0.3MPag-0.4MPag, and the Stress control after stabilizer overhead gas compress exists 1.1MPag-1.2MPag, the reboiler of stabilizer does thermal source with steam.
2. according to the method described in claim 1, it is characterised in that：
In step (5), the operating pressure of desorption column overhead is controlled in 0.3MPag.
3. according to the method described in claim 1, it is characterised in that：
In step (5), desorber overhead gas feeding rich gas stage compressor.
4. according to the method described in claim 1, it is characterised in that：
In step (6), the operating pressure of stable column overhead is controlled in 0.35MPag.
5. according to the method described in claim 1, it is characterised in that：
In step (6), the Stress control after the compression of stabilizer overhead gas is in 1.15MPag.
6. the method according to Claims 1 to 5 any one, it is characterised in that：
In step (6), the Steam pressure control of the reboiler of stabilizer is in 0.5-1.0MPag.
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