CN203612948U - System for comprehensively recovering hydrogen and light hydrocarbons through single absorption and double desorption - Google Patents
System for comprehensively recovering hydrogen and light hydrocarbons through single absorption and double desorption Download PDFInfo
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- CN203612948U CN203612948U CN201320797486.7U CN201320797486U CN203612948U CN 203612948 U CN203612948 U CN 203612948U CN 201320797486 U CN201320797486 U CN 201320797486U CN 203612948 U CN203612948 U CN 203612948U
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model provides a system for comprehensively recovering hydrogen and light hydrocarbons through single absorption and double desorption. The system comprises a membrane separation device and an oil absorption device, wherein an inlet of the membrane separation device is communicated with first refinery dry gas, the first refinery dry gas is separated into a hydrogen product and residual gas, the hydrogen product is recovered, and the residual gas is fed into a bottom inlet of an absorption tower; the oil absorption device comprises the absorption tower, a first desorption tower, a second desorption tower and a light hydrocarbon product separation unit, the bottom inlet of the absorption tower is connected with second refinery dry gas, and light hydrocarbons in the second refinery dry gas are recycled and hydrogen in the second refinery dry gas can be purified and recovered through a pressure swing adsorption unit under the circulating action of lean absorption oil and rich absorption oil which are circulated through the system.
Description
Technical field
The utility model relates to a kind of hydrogen recovery system, also relates to a kind of light hydrocarbon recovery system, particularly a kind of hydrogen and lighter hydrocarbons comprehensive recovery system.
Background technology
Along with heaviness and the high sulfuration of peracid of processing crude oil, hydrogen becomes more and more important for the production that ensures qualified product in refinery, and high product hydrogen cost and hydrogen production bioreactor investment make the recovery of hydrogen particularly important.In the case of at present relatively ripe for the recovery technology technique of high-purity hydrogen, seem more there is realistic meaning for how reclaiming effectively economically medium and low-purity hydrogen discharge stream strand.Meanwhile, owing to containing other high value lighter hydrocarbons compositions in these discharge stream thighs, consider the comprehensive recovery of hydrogen and lighter hydrocarbons, to making rational use of resources, strengthen effects of energy saving and emission reduction, increase economic efficiency significant.
For independent hydrogen recovery, the purification that considerable refinery utilizes pressure swing adsorption process, membrane separation process to carry out hydrogen to the oil refinery dry gas of higher degree is reclaimed.This part oil refinery dry gas is generally the outer exhaust of high score, the low point of gas of desulfurization etc. of hydrogenation unit.Pressure swing adsorption process is to utilize solid adsorbent such as being contained in gac in vertical pressure vessel, molecular sieve, silica gel, the various impurity in mixed gas is carried out to selective adsorption, thereby reach the object of gas delivery.Membrane separation process is poor as impellent take the partial pressure of film both sides, utilizes the difference of gas with various infiltration rate in film, the process that it is separated with realization at film two lateral enrichments.
In refinery, independent lighter hydrocarbons recovery is common in the absorption stabilizing apparatus in the devices such as normal decompression, catalytic cracking and delayed coking, for absorbing the overhead gas of discharge in this device, decompression three top gas as usual, catalytic cracking rich gas, rich tail gas of coking plant etc.Adopt " absorption tower-desorption tower-stabilizer tower " three tower fractionation process flow processs, separate lighter hydrocarbons by absorption and desorption, to obtain the products such as light naphthar that qualified dry gas, liquefied gas and vapour pressure are qualified.Traditional oils absorption process is applicable to the C3+ lighter hydrocarbons recovery of middle and small scale.
Cold separation technology, is traditional low temperature recovery process, conventionally under elevated pressures, moves, and utilizes the poor separating effect that reaches of boiling temperature of feed component.The occasion that this technology is applicable on a large scale, polycomponent reclaims simultaneously, has the advantage that ratio defective product is high, separation purity is high.But for nitrogen, refinery gas that methane content is higher, need extremely low condensing temperature, separating energy consumption and facility investment are very high.
In above-mentioned three kinds of techniques, only have cold separation technology can consider the comprehensive recovery of hydrogen and lighter hydrocarbons, due to its facility investment and separating energy consumption higher, it is applicable to large-scale occasion, is not suitable for the relatively high stream thighs of component purity such as hydrogen, nitrogen and methane.Its isolated ethane product generally can be used as ethylene raw, but domestic this technology is immature.
Due to the restriction of hydrogen purification device to hydrogen purity in unstripped gas, make cannot be recycled by membrane sepn or psa unit compared with the hydrogen resource in the oil refinery dry gas of low-purity.Meanwhile, if there is the heavy hydrocarbon (C3+ lighter hydrocarbons) of higher degree in membrane sepn and pressure-variable adsorption raw material, for membrane sepn, may cause retentate side lime set and cause the permanent damage of film, and for pressure-variable adsorption, likely cause the inactivation of sorbent material, thereby impact operation.Meanwhile, pressure swing adsorption is relatively applicable to processing the stream thigh that hydrogen purity is greater than 50v%, and generally its rate of recovery is 90% left and right, more than product hydrogen purity can reach 99.9v%.Membrane sepn can be processed the stream thigh that hydrogen purity is lower, but its product purity is up to 98v%, and the rate of recovery is 80-92%.
For the widely used oil-absorption process of current lighter hydrocarbons recovery technology, can only reclaim C3+ light hydrocarbon product, cannot reclaim hydrogen product wherein, simultaneously, due to the restriction of absorption process, if the lighter hydrocarbons in the relatively high stream thigh of recover hydrogen purity, will have a strong impact on its assimilation effect, reduce the light hydrocarbon product rate of recovery.
Summary of the invention
The utility model provides a kind of single suction to receive two desorb hydrogen and lighter hydrocarbons comprehensive recovery system, and object is oily absorption of light hydrocarbon recovery technology to combine with technology for hydrogen purification, the stream thigh of different hydrogen purity in refinery is realized to the comprehensive reutilization of lighter hydrocarbons and hydrogen.
For achieving the above object, the technical solution adopted in the utility model is:
A kind of single suction is received two desorb hydrogen and lighter hydrocarbons comprehensive recovery system, it is characterized in that, it comprises:
Membrane separation unit, its entrance communicates with first strand of oil refinery dry gas, for being separated into hydrogen production and ooze residual air, described hydrogen production gives hydrogen recovery, described in ooze residual air and will send into the bottom inlet on following absorption tower;
Oil absorption unit, it comprises absorption tower, the first desorption tower, the second desorption tower and light hydrocarbon product separating unit, wherein:
The bottom inlet on described absorption tower is connected with second strand of oil refinery dry gas, the lean absorption oil of systemic circulation enters the tower top on described absorption tower, from going out, the tower bottom flow on described absorption tower becomes rich absorbent oil, described rich absorbent oil enters described the first desorption tower and completes after desorb for the first time, flow into again described the second desorption tower to complete desorb for the second time and to become lean absorption oil, described lean absorption oil goes out from the tower bottom flow of described the second desorption tower again, after cooling pressurization, be back to the tower top on described absorption tower, to form circulation;
The overhead gas of described the second desorption tower and described light hydrocarbon product separating unit join.
In technical scheme preferably, also can increase following technical characterictic:
Also comprise psa unit or another membrane separation unit, its entrance is connected with the 3rd strand of oil refinery dry gas, and the 3rd strand of oil refinery dry gas is separated into High Purity Hydrogen and stripping gas, and described High Purity Hydrogen gives hydrogen recovery, and described stripping gas gives fuel gas and reclaims.
The overhead gas on described absorption tower is connected with the entrance of described psa unit or another membrane separation unit.
The isolated hydrogen production of described membrane separation unit enters described psa unit and does purification again, to reach high-purity hydrogen requirement.
The overhead gas of described the first desorption tower and the bottom inlet on described absorption tower join.
The rich absorbent oil going out from the tower bottom flow on described absorption tower is divided into two strands, and wherein one enters the tower top of described the first desorption tower, and one enters the middle and upper part of described the first desorption tower in addition.
The lean absorption oil going out from the tower bottom flow of described the second desorption tower first boils and carries out the first heat exchange with the stage casing of the first desorption tower, then carry out the second heat exchange with described light hydrocarbon product separating unit, then carry out respectively the 3rd heat exchange and the 4th heat exchange with two strands of described rich absorbent oils, then pump into the tower top on described absorption tower.
Described light hydrocarbon product separating unit is the arbitrary or arbitrary combination of depropanizing tower, debutanizing tower, depentanizer.
Compared with prior art, the beneficial effect the utlity model has is:
1, the utility model organically combines technology for hydrogen purification and lighter hydrocarbons recovery technology, lighter hydrocarbons recovery common product is dry gas, liquefied gas, light naphthar, and this device has been realized on this basis to rationally effectively recovery of hydrogen in dry gas, make it be converted into high-purity hydrogen and be used.Also realized after hydrogen purification, contained the efficient recovery of lighter hydrocarbons in the more stream thigh of lighter hydrocarbons.Take into full account influencing each other of hydrogen and lighter hydrocarbons, reached the object of hydrogen, lighter hydrocarbons efficient comprehensive reutilizations.
2, the utility model is according to oil refinery dry gas feature, the multiple entry of supplying raw materials, optimized choice stream strand feed entrance point, thereby can effectively reclaim the stream thigh of each different hydrogen purity range and lighter hydrocarbons content, can not only effectively reclaim high-purity hydrogen, more make the recovery of low-purity hydrogen stream thigh become practical, thereby improved the utilising efficiency of refinery hydrogen.
3, light ends unit often adopts " absorption tower-desorption tower-stabilizer tower " three tower fractionation process flow processs, and this flow process has been set up the second desorption tower, C2 content in lighter hydrocarbons content and tower top lighter hydrocarbons be can effectively control at the bottom of the second desorption tower tower in turning oil, product yield and purity improved.
4, heat exchanger network coupling is not rationally to cause one of major reason that energy consumption is larger.In new system development, heat exchanging network is optimized coupling again.The utility model adopts heat integrated, takes into full account the waste heat recovery of circulation lean absorption oil and 3.5MPag steam, reduces steam and water coolant general facilities consumption, thereby reduces energy consumption.
5, the device of lighter hydrocarbons and hydrogen recovery is an independent covering device, the inner regeneration of this process using lean absorption oil device, thus do not rely on other devices, the independence of assurance device.
Accompanying drawing explanation
Fig. 1 is the structural representation that the single suction that provides of the utility model is received two desorb hydrogen and lighter hydrocarbons comprehensive recovery system;
Fig. 2 is the stream thigh information table in application example of the present utility model;
Fig. 3 is that in application example of the present utility model, hydrogen lighter hydrocarbons comprehensively reclaim and reclaim respectively product recovery rate contrast table;
Fig. 4 is that in application example of the present utility model, hydrogen lighter hydrocarbons comprehensively reclaim and reclaim respectively energy consumption comparison table;
Fig. 5 is that in application example of the present utility model, hydrogen lighter hydrocarbons comprehensively reclaim and reclaim respectively Efficiency Comparison table.
Description of reference numerals: first-class strand 11; Second thigh 12; The 3rd stream thigh 13; Membrane separation unit 20; Hydrogen recovery 21; Psa unit 30; Fuel gas reclaims 31; Absorption tower 41; Lean absorption oil 42A; Rich absorbent oil 42B; The first desorption tower 43; The second desorption tower 44; Depropanizing tower 45; Debutanizing tower 46; Light naphthar 51; C3 product 52; C4 product 53; The first heat exchange 61; The second heat exchange 62; The 3rd heat exchange 63; The 4th heat exchange 64; Steam-pipe 70.
Embodiment
The utility model proposes single suction and receive two desorb hydrogen and lighter hydrocarbons comprehensive recovery system, organically technology for hydrogen purification and oily absorption techniques are combined, make full use of influencing each other of hydrogen and C3+ lighter hydrocarbons, be provided with three feed(raw material)inlets, it is processed respectively:
First-class strand 11: the oil refinery dry gas with higher degree (>=50v%) hydrogen and higher (>=5v%) C3+ lighter hydrocarbons content;
Second thigh 12: have compared with the oil refinery dry gas of low-purity (< 50v%) hydrogen and higher (>=5v%) C3+ lighter hydrocarbons content;
The 3rd stream thigh 13: the oil refinery dry gas with higher degree (>=50v%) hydrogen and lower (< 5v%) C3+ lighter hydrocarbons content.
As shown in Figure 1, the single suction that the utility model provides is received two desorb hydrogen and lighter hydrocarbons comprehensive recovery system schematic diagram, and it comprises:
Oil absorption unit, it comprises absorption tower 41, the first desorption tower 43, the second desorption tower 44 and light hydrocarbon product separating unit (as depropanizing tower 45 and debutanizing tower 46), wherein:
The bottom inlet on described absorption tower 41 with compared with the second thigh 12 of low-purity hydrogen and higher C3+ lighter hydrocarbons content, described in producing in the first desorption tower 43 overhead gases and membrane separation unit 20, oozing residual air is connected, the lean absorption oil 42A of systemic circulation enters the tower top on described absorption tower 41, absorb after C3+ lighter hydrocarbons, from going out, the tower bottom flow on described absorption tower 41 becomes rich absorbent oil 42B, described rich absorbent oil 42B is divided into two strands, wherein one enters the tower top of described the first desorption tower 43, one enters the middle and upper part of described the first desorption tower 43 in addition, described the first desorption tower 43 arranges stage casing reboiler and tower bottom reboiler, tower top does not arrange backflow, two strands of rich absorbent oils are completed after desorb for the first time at the first desorption tower 43, flow into again described the second desorption tower 44 to complete desorb for the second time and to become lean absorption oil 42A, described lean absorption oil 42A goes out from the tower bottom flow of described the second desorption tower 44 again, after the cooling pressurization of heat exchange, be back to the tower top on described absorption tower 41, to form circulation,
The hydrogen, methane, the ethane enrichment that enter the stream thigh on described absorption tower 41 are overhead gas, and described overhead gas is connected with the entrance of described psa unit 30, to carry out hydrogen purification recovery; In addition, described absorption tower 41 is provided with two stage casing reflux cooling, can improve assimilated efficiency;
The overhead gas of described the first desorption tower 43 can join with the bottom inlet on described absorption tower 41, does recycling again;
The overhead gas of described the second desorption tower 44 is connected to light hydrocarbon product separating unit, as required the overhead gas of the second desorption tower 44 is separated into the light hydrocarbon product of different grades.For example in the present embodiment, the overhead gas of described the second desorption tower 44 joins with depropanizing tower 45 and debutanizing tower 46 successively, C3 product 52 is wherein separated from the tower top of described depropanizing tower 45, C4 product 53 is wherein separated from the tower top of described debutanizing tower 46, and isolates light naphthar 51 from the tower bottom of described debutanizing tower 46.
As shown in the above, the utility model, for different classes of oil refinery dry gas, adopts different recycling modes:
For hydrogen recovery, the utility model combines membrane sepn and pressure swing adsorption, for hydrogen and the higher stream thigh of C3+ lighter hydrocarbons content, considers to do lighter hydrocarbons recovery after hydrogen recovery, and after lighter hydrocarbons recovery, it is also conceivable that hydrogen recovery.
For lighter hydrocarbons recovery, consider scale and reclaim C3+ lighter hydrocarbons, adopt traditional oil-absorption process technology, be provided with single absorption tower and two desorption tower.Wherein: the stream thigh that lighter hydrocarbons content is relatively high is processed on absorption tower 41, after absorption tower 41, in overhead gas, hydrogen will be by enrichment, and C3+ lighter hydrocarbons will enrichment at the bottom of tower, and the overhead gas of high hydrogen purity can be sent to pressure-variable adsorption and do hydrogen purification.Arranging of two desorption towers is mainly to consider the content requirement of light hydrocarbon product to C2 that separate.
In addition, the utility model has also been considered hot integrated, to reduce energy consumption.As shown in Figure 1, the utility model is provided with steam-pipe 70, and boiling in the bottom of itself and the second desorption tower 44, boil in the bottom of the first desorption tower 43 and boils in the bottom of debutanizing tower 46 again again again carries out heat exchange successively, for oily absorption unit provides work required heat.And in order to reduce the energy consumption of described steam-pipe 70, the heat that the utility model utilizes lean absorption oil 42A that the tower bottom flow of described the second desorption tower 44 goes out to be rich in, make it first boil again and carry out the first heat exchange 61 with the stage casing of the first desorption tower 43, then carry out the second heat exchange 62 with described light hydrocarbon product separating unit (as boiled again the bottom of depropanizing tower 45 wherein), carry out respectively the 3rd heat exchange 63 and the 4th heat exchange 64 with two gangs of described rich absorbent oil 42B again, make it after overcooling, just pump into the tower top on described absorption tower 41.Now, because two gangs of described rich absorbent oil 42B enter the first desorption tower 43 after above-mentioned the 3rd heat exchange 63 and the 4th heat exchange 64 again, and described the first desorption tower 43 has also carried out above-mentioned the first heat exchange 61, can make institute's heat requirement of the first desorption tower significantly reduce, save the energy.In like manner, due to the heat that described depropanizing tower 45 utilizes above-mentioned the second heat exchange 62 to produce, alternative steam provides heat for it.The utilization that circulation absorbs oily heat can effectively reduce the general facilities such as water coolant and steam consumption.In traditional technology, that passes through membrane sepn oozes residual air because hydrogen purity is lower, often directly carry out fuel gas recovery, but its pressure ratio is higher, just exist certain kinetic energy waste, and the residual air of oozing producing due to membrane separation unit 20 in the utility model is sent to absorption tower 41, not only can improve the rate of recovery of C3+ lighter hydrocarbons, the more effective high pressure that has utilized membrane sepn to ooze residual air, has saved the energy.
Generally speaking, the utility model application adopts technique scheme, and compared with old product, tool has the following advantages:
1, the utility model organically combines technology for hydrogen purification and lighter hydrocarbons recovery technology, lighter hydrocarbons recovery common product is dry gas, liquefied gas, light naphthar, and this device has been realized on this basis to rationally effectively recovery of hydrogen, make it be converted into high-purity hydrogen and be used.Also realized after hydrogen purification, contained the efficient recovery of lighter hydrocarbons in the more stream thigh of lighter hydrocarbons.Take into full account influencing each other of hydrogen and lighter hydrocarbons, reached the object of hydrogen, lighter hydrocarbons efficient comprehensive reutilizations.
2, the utility model is according to oil refinery dry gas feature, the multiple entry of supplying raw materials, optimized choice stream strand feed entrance point, thereby can effectively reclaim the stream thigh of each different hydrogen purity range and lighter hydrocarbons content, can not only effectively reclaim high-purity hydrogen, more make the recovery of low-purity hydrogen stream thigh become practical, thereby improved the utilising efficiency of refinery hydrogen.
3, light ends unit often adopts " absorption tower-desorption tower-stabilizer tower " three tower fractionation process flow processs, and this flow process has been set up the second desorption tower, C2 content in lighter hydrocarbons content and tower top lighter hydrocarbons be can effectively control at the bottom of the second desorption tower tower in turning oil, product yield and purity improved.
4, heat exchanger network coupling is not rationally to cause one of major reason that energy consumption is larger.In new system development, heat exchanging network is optimized coupling again.The utility model adopts heat integrated, takes into full account the waste heat recovery of circulation lean absorption oil and 3.5MPag steam, reduces steam and water coolant general facilities consumption, thereby reduces energy consumption.
5, the device of lighter hydrocarbons and hydrogen recovery is an independent covering device, the inner regeneration of this process using lean absorption oil device, thus do not rely on other devices, the independence of assurance device.
6, the utility model is very flexible:
(1) can be according to refinery's practical situation, effectively select and change unit wherein, such as the requirement of basis to hydrogen product, hydrogen product purifying plant can be selected psa unit 30 or membrane separation unit 20 flexibly.
(2) if there is no higher degree hydrogen and be rich in the stream thigh of C3+ lighter hydrocarbons, can cancel the membrane separation unit 20 in technical process;
(3) when absorption tower 41 overhead gas hydrogen purities are lower and do not have high hydrogen purity and the less stream thigh of C3+ lighter hydrocarbons, can cancel psa unit 30;
(4) absorbing oil can select as the case may be flexibly, as diesel oil, heavy naphtha, boat coal etc.;
(5), according to product separation requirement, light hydrocarbon product separating unit can be the arbitrary or arbitrary combination in depropanizing tower, debutanizing tower, depentanizer.
5, case analysis
Take the data of a certain refinery as case: adopt single suction to receive bilingual suction flow process and carry out comprehensive recovery and the hydrogen lighter hydrocarbons of hydrogen lighter hydrocarbons and reclaim respectively (psa unit carries out hydrogen recovery, and traditional absorption-desorb-stable system is carried out lighter hydrocarbons recovery) and contrast.(refer to the stream thigh information table shown in Fig. 2.）
Other stream stock-traders' know-how desulfurization below 60v% of hydrogen purity, compression, enter absorbing tower together with oozing residual air with film after cooling at the bottom of, the lean absorption oil of systemic circulation is sent into absorption tower tower top, absorption tower arranges two stage casing reflux cooling, to improve assimilated efficiency.Absorbing tower top gas is sent into psa unit and is carried out hydrogen purification recovery.At the bottom of tower, rich absorbent oil is through points of two streams strand after heating pressure-raising, and one of them stream thigh is directly sent into the first desorption tower tower top, another one stream stock-traders' know-how cross with burst heat exchange of lean absorption oil stream after, send into the first desorption tower middle and upper part.In order to improve desorption efficiency, the first desorption tower arranges stage casing reboiler and tower bottom reboiler, and tower top does not arrange backflow.
At the bottom of the first desorption tower overhead gas is sent into absorbing tower after cooling, at the bottom of tower, after oil heating, deliver to the second desorption tower separate absorbent oil and light hydrocarbon component.Light hydrocarbon component is distillated by tower top, circulation lean absorption oil at the bottom of tower boils for boiling in the first desorption tower stage casing, at the bottom of depropanizing tower again again, the first desorption tower charging heat is provided after temperature be down to 58.5 ℃, be cooled with circulating water 40 ℃ after pressurization send into top, absorption tower as absorption agent.The second desorption tower tower top fractionates out lighter hydrocarbons, enters successively depropanizing tower, debutanizing tower, obtains C3 product, C4 product and light naphthar.
Heat is integrated:
3.5MPag steam boils at the bottom of for the second desorption tower 44 towers again, boil at the bottom of the first desorption tower 43 towers again, boil at the bottom of debutanizing tower tower and depropanizing tower charging provides heat again, and hot water finally goes out device with 86 ℃.
Turning oil boils for boiling in the first desorption tower 43 stage casings, at the bottom of depropanizing tower tower again again, the first desorption tower 43 part chargings and the first desorption tower 43 combined feed total feeds provide heat, now temperature is down to 58.5 ℃, be cooled with circulating water 40 ℃, pressurization is sent into 41 tops, absorption tower as absorption agent again.
As a comparison, we will carry out hydrogen recovery with psa unit containing the stream thigh 1-3 of more hydrogen, less lighter hydrocarbons.The stream thigh 4-11 that is rich in lighter hydrocarbons carries out lighter hydrocarbons recovery by traditional absorption-desorb-stable system, first enters absorption tower, and absorption tower arranges two stage casing reflux cooling, to improve assimilated efficiency.Absorption tower top gas is sent to fuel gas pipe network, and at the bottom of tower, rich absorbent oil flows thigh through being divided into two after heating pressure-raising, and one of them stream thigh is directly sent into desorption tower tower top, and another one stream stock-traders' know-how is sent into desorption tower middle and upper part after crossing and flowing thigh heat exchange with lean absorption oil.In order to improve desorption efficiency, desorption tower arranges stage casing reboiler and tower bottom reboiler, and tower top does not arrange backflow.Desorption tower top gas is sent bottom, absorption tower back to, at the bottom of desorption tower, oil enters light ends fractionation tower and fractionates out lighter hydrocarbons, after the circulation lean absorption oil at the bottom of tower and the reboiler heat exchange of desorption tower stage casing, with desorption tower charging heat exchange respectively, after cooling, pressurizeed by pump, send into absorption tower as poor absorption agent.Lighter hydrocarbons, through follow-up depropanizing tower, debutanizing tower, obtain C3 product, C4 product and light naphthar.
Heat is integrated:
3.5MPa steam is: at the bottom of light ends fractionation tower, boil, boiling at the bottom of desorption tower provides heat again, last hot water goes out device with 157 ℃ again.
Turning oil is: boil in desorption tower stage casing, boil at the bottom of depropanizing tower again again, boil at the bottom of debutanizing tower again, desorption tower charging and depropanizing tower charging provide heat, and temperature is down to after 96 ℃, circulating water to 40 ℃, and pump pressurization enters top, absorption tower as absorption agent.
Refer to Fig. 3, being that hydrogen lighter hydrocarbons are comprehensive reclaims and reclaims respectively product recovery rate contrast table, and consult Fig. 4, being that hydrogen lighter hydrocarbons are comprehensive reclaims and reclaims respectively energy consumption comparison table (energy consumption index basis GB/T50441-2007 " petrochemical complex design energy consumption calculation standard "), consult Fig. 5, being that hydrogen lighter hydrocarbons are comprehensive reclaims and reclaims respectively Efficiency Comparison table again.
As can be seen from the above results, the heat that the comprehensive recovery of hydrogen lighter hydrocarbons takes full advantage of turning oil and steam is to material and boil thermal source is provided, hot water finally goes out device with 86 ℃, turning oil temperature is down to 58.5 ℃, greatly optimize heat exchange process, can improve energy recovery rate, reduce the general facilities consumptions such as low-temperature receiver and thermal source.The unit consumption of energy that hydrogen lighter hydrocarbons reclaim is respectively 158.8kg/t, is 135.6kg/t and comprehensively reclaim unit consumption of energy, and unit consumption of energy decreases.
Although the comprehensive running cost reclaiming increases to some extent, but reclaim respectively with respect to hydrogen lighter hydrocarbons, comprehensive recovery can be effectively by the lighter hydrocarbons in tail gas after hydrogen recovery, and after lighter hydrocarbons recovery, the hydrogen in tail gas reclaims, obviously improve product recovery rate (all more than 88%), 6848 tons/year of the C3 of recovery products, 6630 tons/year of C4 products, 5524 tons/year of light naphthars, stand/year of hydrogen 1,323 ten thousand marks more, thus make economic benefit increase by 4,867 ten thousand yuan/year.This patent flow process effectively hydrogen, the lighter hydrocarbons in convection current thigh comprehensively reclaims, and creates more economic worth.
The comprehensive recovery system investment cost of hydrogen lighter hydrocarbons is 1.4 times of recovery system investment cost respectively, and investment cost difference payback period is 0.92
More than illustrate the utility model just illustrative; and nonrestrictive, those of ordinary skills understand, in the case of not departing from the spirit and scope that claim limits; can make many modifications, variation or equivalence, but within all falling into protection domain of the present utility model.
Claims (8)
1. single suction is received two desorb hydrogen and a lighter hydrocarbons comprehensive recovery system, it is characterized in that, it comprises:
Membrane separation unit, its entrance communicates with first strand of oil refinery dry gas, for being separated into hydrogen production and ooze residual air, described hydrogen production gives hydrogen recovery, described in ooze residual air and will send into the bottom inlet on following absorption tower;
Oil absorption unit, it comprises absorption tower, the first desorption tower, the second desorption tower and light hydrocarbon product separating unit, wherein:
The bottom inlet on described absorption tower is connected with second strand of oil refinery dry gas, the lean absorption oil of systemic circulation enters the tower top on described absorption tower, from going out, the tower bottom flow on described absorption tower becomes rich absorbent oil, described rich absorbent oil enters described the first desorption tower and completes after desorb for the first time, flow into again described the second desorption tower to complete desorb for the second time and to become lean absorption oil, described lean absorption oil goes out from the tower bottom flow of described the second desorption tower again, after cooling pressurization, be back to the tower top on described absorption tower, to form circulation;
The overhead gas of described the second desorption tower and described light hydrocarbon product separating unit join.
2. single suction according to claim 1 is received two desorb hydrogen and lighter hydrocarbons comprehensive recovery system, it is characterized in that: also comprise psa unit or another membrane separation unit, its entrance is connected with the 3rd strand of oil refinery dry gas, the 3rd strand of oil refinery dry gas is separated into High Purity Hydrogen and stripping gas, described High Purity Hydrogen gives hydrogen recovery, and described stripping gas gives fuel gas and reclaims.
3. single suction according to claim 2 is received two desorb hydrogen and lighter hydrocarbons comprehensive recovery system, it is characterized in that: the overhead gas on described absorption tower is connected with the entrance of described psa unit or another membrane separation unit.
4. single suction according to claim 2 is received two desorb hydrogen and lighter hydrocarbons comprehensive recovery system, it is characterized in that: the isolated hydrogen production of described membrane separation unit enters described psa unit and does purification again.
5. single suction according to claim 1 is received two desorb hydrogen and lighter hydrocarbons comprehensive recovery system, it is characterized in that: the overhead gas of described the first desorption tower and the bottom inlet on described absorption tower join.
6. single suction according to claim 1 is received two desorb hydrogen and lighter hydrocarbons comprehensive recovery system, it is characterized in that: the rich absorbent oil going out from the tower bottom flow on described absorption tower is divided into two strands, wherein one enters the tower top of described the first desorption tower, and one enters the middle and upper part of described the first desorption tower in addition.
7. single suction according to claim 6 is received two desorb hydrogen and lighter hydrocarbons comprehensive recovery system, it is characterized in that: the lean absorption oil going out from the tower bottom flow of described the second desorption tower first boils and carries out the first heat exchange with the stage casing of the first desorption tower, then carry out the second heat exchange with described light hydrocarbon product separating unit, then carry out respectively the 3rd heat exchange and the 4th heat exchange with two strands of described rich absorbent oils, then pump into the tower top on described absorption tower.
8. single suction according to claim 1 is received two desorb hydrogen and lighter hydrocarbons comprehensive recovery system, it is characterized in that: described light hydrocarbon product separating unit is the arbitrary or arbitrary combination of depropanizing tower, debutanizing tower, depentanizer.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104692325B (en) * | 2013-12-05 | 2017-07-07 | 北京宜能高科科技有限公司 | Single suction receives bilingual suction hydrogen and lighter hydrocarbons comprehensive recovery system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104692325B (en) * | 2013-12-05 | 2017-07-07 | 北京宜能高科科技有限公司 | Single suction receives bilingual suction hydrogen and lighter hydrocarbons comprehensive recovery system |
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