CN1371961A - Method for separating hydrocarbon hydrocracking products - Google Patents
Method for separating hydrocarbon hydrocracking products Download PDFInfo
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- CN1371961A CN1371961A CN 02114456 CN02114456A CN1371961A CN 1371961 A CN1371961 A CN 1371961A CN 02114456 CN02114456 CN 02114456 CN 02114456 A CN02114456 A CN 02114456A CN 1371961 A CN1371961 A CN 1371961A
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- Prior art keywords
- tower
- gas
- stabilizer
- oil
- overhead
- Prior art date
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- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 97
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 96
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 51
- 238000000034 method Methods 0.000 title claims description 33
- 238000004517 catalytic hydrocracking Methods 0.000 title claims description 7
- 239000007789 gas Substances 0.000 claims abstract description 97
- 238000010521 absorption reaction Methods 0.000 claims abstract description 59
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 49
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims abstract description 49
- 238000000926 separation method Methods 0.000 claims abstract description 18
- 239000003381 stabilizer Substances 0.000 claims description 64
- 239000007788 liquid Substances 0.000 claims description 50
- 241000282326 Felis catus Species 0.000 claims description 20
- 238000007600 charging Methods 0.000 claims description 19
- 238000001816 cooling Methods 0.000 claims description 14
- 238000006477 desulfuration reaction Methods 0.000 claims description 14
- 230000023556 desulfurization Effects 0.000 claims description 11
- 238000009833 condensation Methods 0.000 claims description 9
- 230000005494 condensation Effects 0.000 claims description 9
- 230000002745 absorbent Effects 0.000 claims description 8
- 239000002250 absorbent Substances 0.000 claims description 8
- 238000002156 mixing Methods 0.000 claims description 6
- 238000006243 chemical reaction Methods 0.000 claims description 4
- 239000002904 solvent Substances 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 238000009835 boiling Methods 0.000 claims description 3
- 238000007872 degassing Methods 0.000 claims description 3
- 238000010992 reflux Methods 0.000 claims description 3
- 238000007701 flash-distillation Methods 0.000 claims description 2
- 239000000463 material Substances 0.000 abstract description 2
- 238000005406 washing Methods 0.000 abstract 3
- 230000006641 stabilisation Effects 0.000 abstract 1
- 238000011105 stabilization Methods 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 47
- 239000000047 product Substances 0.000 description 30
- 238000005260 corrosion Methods 0.000 description 13
- 230000007797 corrosion Effects 0.000 description 13
- 238000011084 recovery Methods 0.000 description 11
- 238000005194 fractionation Methods 0.000 description 8
- 229910052739 hydrogen Inorganic materials 0.000 description 6
- 239000001257 hydrogen Substances 0.000 description 6
- 239000012071 phase Substances 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 5
- 150000001412 amines Chemical class 0.000 description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 238000012856 packing Methods 0.000 description 4
- 239000003208 petroleum Substances 0.000 description 4
- 229910052717 sulfur Inorganic materials 0.000 description 4
- 239000011593 sulfur Substances 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 3
- 239000005864 Sulphur Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 230000002950 deficient Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005530 etching Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 239000003915 liquefied petroleum gas Substances 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 125000000101 thioether group Chemical group 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The separation method of hydrocracked product of hydrocarbons incldudes stabilization tower, hydrogen sulfide washing tower, debutanizing tower, deethanizing column and light hydrocarbon absorption tower. The stabilizatino tower is designed according to cutting portion or all C6 component, the absorption oil of light hydrocarbon absorption tower is from tower bottom product flow of debutanizing tower, the overhead gas of stabilizaltion tower, overhead gas of debutanizing tower and overhead gas of deethanizing column are mixed, and fed into light hydrocarbon absorption tower to recover light hydrocarbon, and the tower bottom rich absorption oi lof light-hydrocarbon absorption tower and hydrogen sulfide washing tower feeding material coming from stabilizatino tower and mixed, and fed into hydrogen sulfide washing tower. The C3 and C4 components can be completely recovered, and its liquified gas yield is high.
Description
Technical field
The present invention relates to the separation method of hydrocarbon hydrocracking products, particularly hydrocarbon hydrocracking products lighter hydrocarbons recovery and sulfur method.
Technical background
Hydroeracking unit with its process raw material that oily scope is wide, product structure flexibly, characteristics such as good product quality, liquid yield height become day by day that the balance refinery produces and the key means of the market requirement.Hydroeracking unit fractionation flow process adopts the scheme of stablizing earlier aftercut more at present, promptly earlier isolates C through stabilizer tower from the low branch oil of reactive moieties
4Following component removes C through deethanizing column again
1And C
2, reclaim liquefied gas, and C
4Above fraction is fractionated into each product component in normal, vacuum fractionation tower.This scheme flow process is simple, easy to operate, is fit to the processing of low-sulfur wax oil.But increase along with refinery's processing high-sulfur oils ratio, adopt these flow process existing problems also more and more obvious: because the increase of dissolved hydrogen sulfide amount in the high score oil, take the also corresponding increase of hydrogen sulfide of fractionation part to, thereby cause a series of problems such as product corrosion such as the liquid hydrocarbon loss is serious and light, heavy naphtha are defective, tower corrosion, these problems are more outstanding along with the raising of feed sulphur content.
Chinese patent ZL93101645.2 relates to C in a kind of recovery hydrocracking stabilizer tower overhead gas
3, C
4The method of hydrocarbon, its major technique feature is: use the hydro carbons absorption agent to reclaim C in the overhead gas in the absorption tower
3, C
4Hydrocarbon, rich absorbent leave the absorption tower and remove described stabilizer tower desorb, the C in the rich absorbent
3, C
4Hydrocarbon finally enters in the overhead hydrocarbon liquid product and is recovered, and the absorber component in the rich absorbent enters at the bottom of the tower in the oil.
Chinese patent ZL93106265.9 relates to and a kind ofly utilizes hydrocarbon hydrogenating conversion process to generate oily logistics to reclaim C in the described hydroconversion process stabilizer tower overhead gas as absorption agent
3, C
4The method of hydrocarbon, its prominent feature are to utilize the receptivity of the generation oil logistics in the hydroconversion process flow process to absorb, and finish removal process then in stabilizer tower.Its major technique feature is: be mixed into mixture with circulation gas after the generation oil step-down of hydrocarbon hydrogenating conversion process, described mixture enters light pressure separator, be to be separated into light pressure separator gas and light pressure separator hydrocarbon liquid under the operational condition of 0.5～2.7MPa at pressure, described light pressure separator gas goes out device, light pressure separator hydrocarbon liquid enter in the stabilizer tower that working pressure is 1.0～2.3MPa and be separated into tower at the bottom of heavy hydrocarbon streams, logistics of cat head lighter hydrocarbons and overhead gas, at least a portion overhead gas returns described light pressure separator, the C in the circulation gas after mixing as the oil of the generation after circulation gas and the step-down
3, C
4Hydrocarbon is absorbed and finally enters in stabilizer tower in the logistics of cat head lighter hydrocarbons by light pressure separator hydrocarbon liquid and is recovered.
Chinese patent ZL98112925.0 is the improvement to above-mentioned two patents, has further improved C
3, C
4The rate of recovery of hydrocarbon.But above-mentioned patent exists the flow process complexity, increases the process cost problem of device.
U.S. Pat 5164070 relates to a kind of processing method of hydroeracking unit fractionation flow process, this patent main purpose is for solving naphtha product hydrogen sulfide corrosion problem, but do not relate to technologies such as lighter hydrocarbons recovery and desulfurization, its major technique is characterized as: stabilizer tower cutting petroleum naphtha component, for preventing that naphtha product from carrying hydrogen sulfide, its downstream fractionator overhead distilled naphtha fraction enters debutanizing tower in the lump with stabilizer tower cat head distilled hydrocarbon ils, further removes hydrogen sulfide and liquefied gas component; The debutanizing tower bottoms stream enters that naphtha splitter is isolated gently, the heavy naphtha product.Though this patent can well be avoided the petroleum naphtha etching problem theoretically, increase naphtha splitter accordingly, thereby increased once investment and process cost, energy consumption also has corresponding increase.
Summary of the invention
The problem that exists at prior art the objective of the invention is to, and the first, the liquid hydrocarbon rate of recovery of raising hydroeracking unit increases economic benefit; The second, improve the hydroeracking unit quality product, comprise hydrogen sulfide corrosion problem light, heavy naphtha, the desulfuration of liquefied gas problem of solving; The 3rd, solve hydroeracking unit and stablize hydrogen sulfide corrosion serious problems and relevant device hydrogen sulfide corrosion problem at the bottom of the Tata; The 4th, reduce device redundancy, reduce plant investment.
The technical scheme of employing of the present invention is:
A kind of separation method of hydrocarbon hydrocracking products, reaction effluent stream from hydrogenator, earlier after high-pressure separator and light pressure separator flash distillation, the gas that light pressure separator is told is the low gas that divides, low branch gas is the hydrocarbon gas that is rich in hydrogen, the liquid of telling is the low oil that divides, and the low oil that divides is for comprising C
3, C
4The hydrocarbon liquids of hydrocarbon and above component, low gas and the low oil that divides of dividing all contains 2 S component, and its concentration rises with the raising of the sulphur content that processes raw material.The low oil that divides further separates by following step:
1) the low oil that divides enters stabilizer tower, and stabilizer tower will hang down branch oil and be divided into stabilizer tower overhead stream and stabilizer tower tower base stream, and the stabilizer tower overhead stream comprises the low part or all of C in the oil that divides
6Component, the stabilizer tower bottoms flows to separation column and further is separated into each boiling range product, the stabilizer tower overhead stream enters after the condensation cooling and carries out vapor-liquid separation in the stabilizer tower return tank of top of the tower, the stabilizer tower overhead gas goes to the lighter hydrocarbons absorption tower to reclaim liquid hydrocarbon, the stabilizer tower liquid of top of the tower is divided into two-way: the one tunnel as the stabilizer tower trim the top of column, and another road is as the charging of hydrogen sulfide scrubber tower;
2) charging of hydrogen sulfide scrubber tower is in the hydrogen sulfide scrubber tower, and with the solvent counter current contact, the liquid hydrocarbon of sloughing hydrogen sulfide flows out from the hydrogen sulfide scrubber column overhead and enters debutanizing tower;
3) debutanizing tower cat head gas phase enters debutanizing tower top return tank and carries out vapor-liquid separation after condensation cooling, the debutanizing tower overhead gas goes to the lighter hydrocarbons absorption tower to reclaim liquid hydrocarbon, the debutanizing tower overhead liquid is divided into two-way: the one tunnel as deethanizing column charging advance deethanizing column, another road is as the debutanizing tower trim the top of column; The debutanizing tower tower base stream is divided into two-way after water cooler cooling, the one tunnel goes to the lighter hydrocarbons absorption tower as absorbing oil, and another road goes out device as light naphtha product;
4) the deethanizer overhead gas phase enters deethanizing column top return tank and carries out vapor-liquid separation after condensation cooling, and deethanizer overhead gas goes to the lighter hydrocarbons absorption tower to reclaim liquid hydrocarbon, and deethanizer overhead liquid all refluxes as deethanizer overhead and returns the cat head space; Deethanizer bottoms stream goes out device as the liquefied gas product after cooling off;
5) enter lighter hydrocarbons after stabilizer tower overhead gas, debutanizing tower overhead gas and deethanizer overhead gas mix and absorb the Tata base space, absorb oil and enter cat head space, lighter hydrocarbons absorption tower, carry out the vapour-liquid contact and finish absorption process, the lighter hydrocarbons absorption tower overhead gas body desulfurization part of degassing, lighter hydrocarbons absorb rich absorbent oil at the bottom of the Tata and are mixed into the hydrogen sulfide scrubber tower with hydrogen sulfide scrubber tower charging from stabilizer tower.
The present invention recommends to comprise in the stabilizer tower overhead stream the low whole C in the oil that divide
630%～50% of component.
The present invention recommends lighter hydrocarbons absorption tower overhead gas and low divides gas to mix laggard gas sweetening tower to carry out desulfurization and handle.
Adopt technical solution of the present invention to have following beneficial effect:
Stabilizer tower in the present invention to the fractionation part charging play the effect of prefractionation, overhead gas and liquid phase are extracted the charging that is the lighter hydrocarbons recovery part out, tower base stream cuts out the product of different fractions to separation column.Therefore, the character of determining directly to have influence on the fractionation product of the cut point of this column overhead, tower base stream.The component that this column overhead is partitioned into is heavy more, hydrogen sulfide and light hydrocarbon component shared ratio in the cat head gas phase is more little, ratio shared in the cat head liquid phase is extracted out is big more, under the situation of not establishing lighter hydrocarbons absorption facility, lighter hydrocarbons ratio during the cat head liquid phase is extracted out is big more to mean that the rate of recovery of liquid hydrocarbon is high more, the possibility that while hydrogen sulfide exists in tower base stream is more little, and this two aspect all is desirable.But the component that cat head is partitioned into is heavy more, column bottom temperature is high more, causes the reboiler furnace load big, and the possibility of oil coke and high-temperature sulfur corrosion increases, therefore, select suitable cut point to the operation of this tower still be the fractionating effect of whole device all be very important.Stabilizer tower of the present invention is from removing C
6Component (hexane) beginning recommends to remove C
6Component 30%-50% operates under this condition, can obtain higher yield of liquefied gas, and it is all more satisfactory to stablize at the bottom of the Tata corrosion and energy consumption simultaneously.
Aspect the selection of lighter hydrocarbons absorption tower absorption oil and analysis mode, hydroeracking unit lighter hydrocarbons absorption tower generally adopts device hydrocarbon ils product to make to absorb oil at present, as gasoline, kerosene, diesel oil distillate and mixed fraction thereof, this absorption pattern is in present domestic and external widespread usage, and the related absorption oil of Chinese patent ZL93101645.2 also is this type of hydrocarbon ils.Compare with this absorption pattern, of the present invention with oil at the bottom of the debutanizing tower as absorbing oil, rich absorbent oil still returns debutanizing tower and resolves and have clear superiority.If from the heavy naphtha product, draw one as absorbing oil, return debutanizing tower then and resolve, then the debutanizing tower back need increase a naphtha splitter, in order to separate light, heavy naphtha.Analyze from economy, establishing naphtha splitter has increased once investment, and the heavy naphtha product is done the absorption oil require and boosted, and adds the increase that boosting pump also will cause energy consumption.The present invention with debutanizing tower at the bottom of oil (mainly be C
5And C
6) tell one as absorbing oil, oil returns the hydrogen sulfide scrubber tower at the bottom of the absorption tower, finally advancing the debutylize Tata resolves, why directly do not return debutanizing tower and resolve, making is that the hydrogen sulfide that carries in rich absorbent oil is brought into and caused that the liquefied gas product is defective, absorbs the oil phase ratio with making of heavy naphtha, need not increase naphtha splitter, and absorbing oil need not boost, and has both saved investment, has reduced process cost again.Calculation result to lighter hydrocarbons of the present invention absorption tower shows, makees absorption oil with light naphthar at the bottom of the debutanizing tower, when adopting suitable consumption, and C
3And C
4Specific absorption can reach 100%.
Aspect gas sweetening, because it is not only several strands of overhead gases such as stabilizer tower, debutanizing tower, deethanizing column that hydroeracking unit need carry out the gas of desulfurization processing, also comprise the gas that comes from the reactive moieties light pressure separator, and this strand gas is to be rich in hydrogen and to carry heavy hydrocarbon, hydrogen can reduce the gaseous phase partial pressure of light hydrocarbon component to a great extent in the existence on lighter hydrocarbons absorption tower, and this will make C
3, C
4Specific absorption reduce greatly, in other words, for reclaiming the low C that divides in the gas
3, C
4And it is fed the lighter hydrocarbons absorption tower, and not only do not reach intended purposes, can make the original C that can absorb on the contrary
3, C
4Also lose from cat head owing to the existence of hydrogen.Therefore the present invention adopts gas to absorb the scheme of desulfurization more earlier, and promptly several strands of overhead gas advance lighter hydrocarbons absorption tower recovery C
3, C
4, the low gas that divides does not absorb.The low gas that divides absorbs together desulfurization of overhead gas separately or with lighter hydrocarbons, and this scheme has following advantage: 1, avoided absorbing oil and absorbed the low C in the gas that divides
3, C
4The time heavy hydrocarbon component that will hang down in the branch gas bring the desulfuration of liquefied gas tower in the lump into; 2, divide gas and absorb overhead gas together during desulfurization when low, can also save the low gas thionizer that divides; 3, the rate of recovery of liquefied gas is not because there is to reclaim the low C that divides in the gas
3, C
4And reduce.
In sum, outstanding advantage of the present invention can be summarized as:
1, flow process is simply distinct, is guaranteeing that being provided with of tower is minimum under the product quality premise, reduces once investment; 2, enter the fractionation partial C
3, C
4Component is basic all to be reclaimed, device yield of liquefied gas height; 3, the hydrogen sulfide corrosion problem and the desulfuration of liquefied gas problem of petroleum naphtha have been solved; 4, solved hydroeracking unit and stablized Tata at the bottom of hydrogen sulfide corrosion seriously reach relevant device hydrogen sulfide corrosion problem; 5, avoided the possibility of hydrogen sulfide corrosion derived product and equipment basically.
Below in conjunction with accompanying drawing technical solution of the present invention is elaborated, accompanying drawing is just in order to illustrate that substance of the present invention draws, it does not limit content of the present invention and type of service, in fact according to the concrete operations condition, need on some pipelines to be provided with as conventional equipment or piping elements such as compressor, pump, interchanger, process furnace, mixing tank, dropping valves.
Description of drawings:
Accompanying drawing: a kind of typical flowchart of the present invention.
As shown in the figure, the low oil 10 that divides enters stabilizer tower 1, and stabilizer tower 1 will hang down branch oil 10 and be divided into stabilizer tower overhead stream 12 and stabilizer tower tower base stream 11, among the present invention stabilizer tower 1 according to practical situation by removing part or all of C
6The component operation promptly comprises the low part or all of C in the oil 10 that divides in the stabilizer tower overhead stream 12
6Component recommends to comprise in the stabilizer tower overhead stream 12 the low whole C in the oil 10 that divide
630%～50% of component, like this can with almost all hydrogen sulfide cut in the stabilizer tower overhead stream 12.Stabilizer tower 1 is operated under the condition of tower top pressure 1.0～1.8MPa, 80～120 ℃ of tower top temperatures, 260～360 ℃ of column bottom temperatures usually.Stabilizer tower tower base stream 11 advances separation column and further is separated into each boiling range product and goes out device.Stabilizer tower overhead stream 12 enters after the condensation cooling and carries out vapor-liquid separation in the stabilizer tower return tank of top of the tower 7, stabilizer tower overhead gas 13 goes to lighter hydrocarbons absorption tower 5 to reclaim liquid hydrocarbon, the stabilizer tower liquid of top of the tower is divided into two-way: the one tunnel as stabilizer tower trim the top of column 15, and another road is as hydrogen sulfide scrubber tower charging 16.The stripping mode of stabilizer tower 1 can be undertaken by reboiler furnace or steam stripped mode.
Hydrogen sulfide scrubber tower charging 16 is in hydrogen sulfide scrubber tower 2, and with the solvent counter current contact, the liquid hydrocarbon 17 of sloughing hydrogen sulfide flows out from hydrogen sulfide scrubber tower 2 cats head and enters debutanizing tower 3.The hydrogen sulfide scrubber tower can be packing tower, usually under the conditional operation of 40～60 ℃ of pressure 1.6～2.8MPa, temperature, hydrogen sulfide scrubber tower charging 16 enters the bottom space of tower, lean solvent 18 enters the headspace of tower, counter current contact is carried out in two bursts of chargings in packing section, rich amine liquid 19 goes regeneration system rapidly regeneration at the bottom of the tower, and to cause oil product to separate disorderly in order to prevent from amine liquid brought into, sloughs the liquid hydrocarbon 17 of hydrogen sulfide and preferably separate out amine liquid by minute flow container or coalescer before entering debutanizing tower 3.
Debutanizing tower cat head gas phase 20 enters debutanizing tower top return tank 8 and carries out vapor-liquid separation after the condensation cooling, debutanizing tower overhead gas 24 goes to lighter hydrocarbons absorption tower 5 to reclaim liquid hydrocarbon, the debutanizing tower overhead liquid is divided into two-way: the one tunnel as deethanizing column charging 23, and another road is as debutanizing tower trim the top of column 22; The debutanizing tower tower base stream is divided into two-way after water cooler is cooled to about 40 ℃, the one tunnel goes to lighter hydrocarbons absorption tower 5 as absorbing oil 35, and another road is as light naphtha product 21; Debutanizing tower 3 can design by tray column, operates under the condition of tower top pressure 1.4～2.4MPa, 60～100 ℃ of tower top temperatures, 100～200 ℃ of column bottom temperatures usually, and debutanizing tower 3 can adopt the stripping that heavily boils, and the stripping thermal source generally can fill load by logistics in the device.
Deethanizer overhead gas phase 25 enters deethanizing column top return tank 9 and carries out vapor-liquid separation after the condensation cooling, deethanizer overhead gas 28 goes to lighter hydrocarbons absorption tower 5 to reclaim liquid hydrocarbon, and deethanizer overhead liquid 27 all refluxes as deethanizer overhead and returns the cat head space; Deethanizer bottoms stream 26 after cooling off as the liquefied gas product; Deethanizing column 4 can design by tray column, operates under the condition of tower top pressure 2.8～3.6MPa, 60～100 ℃ of tower top temperatures, 100～200 ℃ of column bottom temperatures usually, can adopt the stripping that heavily boils, and the stripping thermal source generally can fill load by logistics in the device.
After mixing, stabilizer tower overhead gas 13, debutanizing tower overhead gas 24 and deethanizer overhead gas 28 enters lighter hydrocarbons absorption tower 5 tower base spaces, absorb oil 35 and enter 5 cat head spaces, lighter hydrocarbons absorption tower, carry out the vapour-liquid contact and finish absorption process, the lighter hydrocarbons absorption tower overhead gas 29 body desulfurization part of degassing, rich absorbent oil 36 boosted earlier at the bottom of lighter hydrocarbons absorbed Tata, was mixed into hydrogen sulfide scrubber tower 2 again through water cooler is cooled to about 40 ℃ after and from the hydrogen sulfide scrubber tower charging 16 of stabilizer tower 1.Lighter hydrocarbons absorption tower 5 can be tray column or packing tower, usually operates under the condition of 40～60 ℃ of pressure 0.8～1.6MPa, temperature.
After mixing, the absorption tower of lighter hydrocarbons shown in accompanying drawing overhead gas 29 and low branch gas 30 enters gas sweetening tower 6 bottoms, gas sweetening tower 6 can be packing tower, usually under the condition of 40～60 ℃ of pressure 0.5～1.5MPa, temperature, operate, lean solution 32 is entered the top of tower, by the gas that rises at the bottom of the tower and by the dirty lean solution counter current contact in tower of cat head, the hydrogen sulfide in the gas is absorbed by amine liquid.Cat head is through the gas after the desulfurization 31 carrying device under pressure-controlling.Rich amine liquid is reused after regenerating at the bottom of the gas sweetening Tata.
According to the difference of feedstock property, when technological design, can the operational condition of each tower of the present invention be optimized, this is this area means commonly used.The present invention recommends: hydrogen sulfide scrubber tower 2, debutanizing tower 3 and lighter hydrocarbons absorption tower 5 keep certain operating pressure difference, rely on operating pressure difference to finish fill process, can reduce process cost and energy consumption like this.
Embodiment
Adopt diagram technical process of the present invention, stabilizer tower 1 is by removing 30%C
6Component operation, the absorption oil mass on lighter hydrocarbons absorption tower 5 are that each main streams of 10 ton hours and hydrogen sulfide and liquid hydrocarbon distribution situation see the following form.
| ??H 2S ??kmol/h | ????C 3????kmol/h | ????iC 4????kmol/h | ????nC4 ????kmol/h | |
| Stabilizer tower 1 charging | ??22.68 | ????23.38 | ????21.04 | ????12.14 |
| Stabilizer tower 1 overhead gas | ??12.56 | ????8.43 | ????4.11 | ????1.86 |
| Stabilizer tower 1 tower base stream | ??4.00E-10 | ????6.17E-05 | ????0.029 | ????0.048 |
| 5 chargings of lighter hydrocarbons absorption tower | ??12.56 | ????15.26 | ????5.9 | ????2.57 |
| Lighter hydrocarbons absorption tower 5 overhead gases | ??3.62 | ????1.11E-03 | ????1.09E-08 | ????- |
| Lighter hydrocarbons absorption tower 5 tower base streams | ??8.94 | ????15.26 | ????5.9 | ????6.47E-11 |
| Debutanizing tower 3 overhead gases | ??- | ????4.04E+00 | ????1.53 | ????0.66 |
| Debutanizing tower 3 tower base streams | ??- | ????4.74E-06 | ????3.93E-03 | ????0.03 |
| Deethanizing column 4 overhead gases | ??- | ????2.81E+00 | ????0.26 | ????0.06 |
| Deethanizing column 4 tower base streams | ??- | ????23.32 | ????20.99 | ????12.05 |
Can be drawn by last table: 1, hydrogen sulfide content is approximately zero at the bottom of stabilizer tower 1 tower, has reduced the present ubiquitous material etching problem of this tower to a great extent; 2, deethanizing column 4 tower base streams can be used as liquefied petroleum gas product and directly go out device, this product is sulfide hydrogen not, mass recovery with respect to the promptly low branch oil of fractionation part charging under this operating mode is 99.64%, can regulate this rate of recovery to higher level by the operating parameters of adjusting debutanizing tower 3; 3,, thereby avoided the underproof problem of light oil products hydrogen sulfide corrosion such as petroleum naphtha to a great extent because the equal sulfide hydrogen not of stabilizer tower 1 and debutanizing tower 3 tower base streams.
Claims (3)
1, a kind of separation method of hydrocarbon hydrocracking products, reaction effluent stream from hydrogenator, earlier after high-pressure separator and light pressure separator flash distillation, the gas that light pressure separator is told is the low gas (30) that divides, the liquid of telling is the low oil (10) that divides, the low oil (10) that divides further separates, and it is characterized in that the low separating step of oil (10) that divides comprising:
1) low branch oil (10) enters stabilizer tower (1), and stabilizer tower (1) will hang down branch oil (10) and be divided into stabilizer tower overhead stream (12) and stabilizer tower tower base stream (11), and stabilizer tower overhead stream (12) comprises the low part or all of C in the oil (10) that divides
6Component, stabilizer tower tower base stream (11) advances separation column and further is separated into each boiling range product, stabilizer tower overhead stream (12) enters in the stabilizer tower return tank of top of the tower (7) after the condensation cooling and carries out vapor-liquid separation, stabilizer tower overhead gas (13) goes to lighter hydrocarbons absorption tower (5) to reclaim liquid hydrocarbon, the stabilizer tower liquid of top of the tower is divided into two-way: the one tunnel as stabilizer tower trim the top of column (15), and another road is as hydrogen sulfide scrubber tower charging (16);
2) hydrogen sulfide scrubber tower charging (16) is in hydrogen sulfide scrubber tower (2), and with the solvent counter current contact, the liquid hydrocarbon (17) of sloughing hydrogen sulfide flows out from hydrogen sulfide scrubber tower (2) cat head and enters debutanizing tower (3);
3) debutanizing tower cat head gas phase (20) enters debutanizing tower top return tank (8) and carries out vapor-liquid separation after condensation cooling, debutanizing tower overhead gas (24) goes to lighter hydrocarbons absorption tower (5) to reclaim liquid hydrocarbon, the debutanizing tower overhead liquid is divided into two-way: the one tunnel advances deethanizing column (4) as deethanizing column charging (23), and another road is as debutanizing tower trim the top of column (22); The debutanizing tower tower base stream is divided into two-way after water cooler cooling, the one tunnel goes to lighter hydrocarbons absorption tower (5) as absorbing oil (35), and another road is as light naphtha product (21);
4) deethanizer overhead gas phase (25) enters deethanizing column top return tank (9) and carries out vapor-liquid separation after condensation cooling, deethanizer overhead gas (28) goes to lighter hydrocarbons absorption tower (5) to reclaim liquid hydrocarbon, and deethanizer overhead liquid (27) all refluxes as deethanizer overhead and returns the cat head space; Deethanizer bottoms stream (26) after cooling off as the liquefied gas product;
5) stabilizer tower overhead gas (13), debutanizing tower overhead gas (24) and deethanizer overhead gas (28) enter lighter hydrocarbons absorption tower (5) tower base space after mixing, absorb oil (35) and enter cat head space, lighter hydrocarbons absorption tower (5), carry out the vapour-liquid contact and finish absorption process, lighter hydrocarbons absorption tower overhead gas (29) the body desulfurization part of degassing, lighter hydrocarbons absorb rich absorbent oil (36) at the bottom of the Tata and are mixed into hydrogen sulfide scrubber tower (2) with hydrogen sulfide scrubber tower charging (16) from stabilizer tower (1).
2, according to the described method of claim 1, it is characterized in that: comprise the low whole C in the oil (10) that divide in the stabilizer tower overhead stream (12)
630%～50% of component.
3, according to claim 1 or 2 described methods, it is characterized in that: lighter hydrocarbons absorption tower overhead gas (29) and low gas (30) the laggard gas sweetening tower of mixing (6) that divides carry out the desulfurization processing.
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