CN102732306B - Naphtha hydrogenation method and decoking tank - Google Patents
Naphtha hydrogenation method and decoking tank Download PDFInfo
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- CN102732306B CN102732306B CN201110095290.9A CN201110095290A CN102732306B CN 102732306 B CN102732306 B CN 102732306B CN 201110095290 A CN201110095290 A CN 201110095290A CN 102732306 B CN102732306 B CN 102732306B
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Abstract
The invention discloses a naphtha hydrogenation method and a decoking tank. The naphtha hydrogenation method comprises the following steps of heating a mixture of a naphtha feedstock and hydrogen in a heating surface to a temperature required by hydrofining, then carrying out decoking by the decoking tank, and then feeding the decoked mixture into a fixed bed hydrogenation reactor. The decoking tank comprises an outer cylindrical body, an upper head, a lower head and a separation assembly. The top of the upper head is provided with a material inlet. The bottom of the lower head is provided with a material outlet. The separation assembly has a cylindrical structure and is arranged in the outer cylindrical body of the decoking tank. A rain cap is arranged on a cylindrical body of the separation assembly. An outlet collection device is arranged at a lower part of the cylindrical body of the separation assembly. The outlet collection device is communicated with the material outlet arranged at the lower head. An inner layer and an outer layer of the cylindrical body of the separation assembly are inner and outer screens. A scale depositing agent is filled between the inner and outer screens. Compared with the prior art, the naphtha hydrogenation method and the decoking tank can effectively and economically prolong a naphtha hydrogenation device running period.
Description
Technical field
The present invention relates to a kind of petroleum naphtha hydrogenation method and decoking tank, specifically a kind of extend Naphtha hydrofining unit service cycle method of hydrotreating and the decoking tank that uses of the method.
Background technology
Naphtha (i.e. gasoline fraction) is important gasoline stocks and industrial chemicals, mainly for the production of the Fuel Petroleum of the various trade mark, catalytic reforming produces aromatic hydrocarbons (or high-knock rating gasoline blend component) raw material, steam cracking or catalytic pyrolysis produce the industrial chemicals such as ethene, propylene, butylene, and for the production of the raw material etc. of hydrogen.Naphtha generally derives from the straight-run naphtha that petroleum distillation obtains, the naphtha that secondary operations obtains, as coking naphtha, cat cracked naphtha, cracking naphtha etc.The various uses of various sources naphtha all needs the sulphur in raw material, nitrogen, rare hydrocarbon, metal impurities deep removal, and current hydrogen addition technology is the optimum technology removing various impurity in feed naphtha.As high-knock rating gasoline is produced in cat cracked naphtha selective hydrogenation, coking naphtha hydrogenation produces steam crack material or hydrogen feedstock, and the pre-hydrogenation of straight-run naphtha produces catalytic reforming raw material etc.
In the various hydrogen addition technologies of naphtha, generally use fixed bed hydrogenation technology, namely fixed bed hydrogenation beds is set in hydrogenation reactor, under Hydrofinishing conditions, feed naphtha and hydrogen enter reactor from top, carry out hydrofinishing by hydrogenation catalyst bed and remove various impurity in raw material, the product after refining discharges reactor from reactor bottom, obtains hydrotreated naphtha product after carrying out follow-up separation.
In petroleum naphtha hydrogenation technology, the principal element of restriction hydrogenation plant long period steady running is that the pressure drop ramp-up rate of fixed bed hydrogenation reactor is very fast, in general, when the pressure drop of hydrogenation reactor reaches 0.3MPa, and must shutdown process.
Such as concerning coking naphtha Hydrofining Technology, due in raw material containing the impurity such as alkadienes, tiny coke powder, often affect the operational stability of device.Daqing petrochemical company 300kt/a Hydrogenation of Coker Gasoline device, after the half a year that goes into operation, occurs that twice system pressure difference is too high continuously, causes being forced to stop work (analysis of coking gasoline hydrogenation refining system pressure difference aggravating reason and countermeasure, " refining and chemical industry ", the 19th volume: 20).Guangzhou Branch 300kt/a hydrogenation plant also occurs that when processing coker gasoline reactor catalyst bed pressure drop rises too fast problem.This device, once within the time of a year and a half, causes shut-down defect elimination 5 times because reaction system bed pressure drop raises (case study and countermeasures that hydrofining reaction system pressure drop raises, " China and foreign countries' energy ", the 2007,12nd volume).Anqing branch company refines oil two I Hydrogenation of Coker Gasoline devices needs cleaning in general 3 ~ 5 days filter, hydrogenation reactor will be stopped work in 1 year and be skimmed for 2 ~ 3 times, has a strong impact on normal operation (Coke Inhibitor for Coker Gasoline Hydrofining Unit, " petrochemical technology " of device, 2006,13(4): 5).There is Similar Problems all in various degree in domestic and international device of the same type, the increase of pressure differential between bed, make the inner members such as the support bar of catalyst and gripper shoe while bearing catalyst weight, again must pressure outside commitment, bring hidden trouble to the safety operation of device.Therefore, it is the conspicuous contradiction affecting coking naphtha hydrogenation plant long-term operation that bed pressure drop rises too fast always, in the urgent need to working out effective method, solves coking problem.
Also often there is the problem that above-mentioned coking naphtha hydrogenation plant is similar in cat cracked naphtha hydrogenation plant, straight-run naphtha hydrogenation plant etc., namely namely there is the problem that reactor pressure falling-rising is high in the hydrogenation plant running short period, can only to stop work the partially catalyzed agent on purge reactor beds top, again to go into operation after removable parts fresh catalyst.
Naphtha hydrofining unit running practice shows, the rising of hydrogenation reactor pressure drop all comes from the bed coking of catalyst top.Coking factor is very complicated, is deposited on beds top causes mainly due to polymerization and the upstream device of the unsaturated hydro carbons such as the alkadienes in raw material after the mechanical admixture brought into or impurity precursor are converted into deposit.Alkadienes in raw material is being easy to be polymerized, and when particularly containing other impurity as oxygen, water, iron etc. in the feed, is easier to polymerization coking.In the sample of coking, the content of general iron is also higher, may be define aphthenic acids with organic hydrocarbon after feedstock oil dissolved oxygen, the iron of naphthenic acid corrosion device generates iron naphthenate, stably be dissolved in feedstock oil, iron naphthenate is easy to hydrogenolysis occurs after mixed hydrogen, and reacts with hydrogen sulfide and generate ferrous sulfide and be deposited on reactor top bed, promote the coking reaction of coking parent, accelerate the blocking of beds.In addition, also may be one of reason of some feed naphthas coking in hydrogenation reactor containing a small amount of tiny coke powder and tiny microorganism in some raw material.Due to naphtha source varied, introduce in the production of some feed naphtha, storage, transport and cannot be filtered by raw material and the impurity removed, these impurity are oil-soluble sometimes, are the particulate suspended sometimes, effectively cannot be removed by a kind of or simple several method.Further, the feed naphtha of hydrogenation plant source is not fixed, and often changes, and therefore, also certain device can not be fixed as certain raw material of processing and use and fixing fall impurity method.
The method that existing solution petroleum naphtha hydrogenation reactor step-down raises has following several:
1, carry out the management work of raw material, adopt the modes such as nitrogen protection, avoid raw material to contact with air, at utmost reduce unsaturated hydro carbons in raw material and form the chance of colloid.This is a kind of passive raw material guard method, if the raw material mechanical admixture of upstream input is more, diene content is very high, or carries a lot of coke powders secretly, and the party's rule is helpless.
2, mix artificial coal oil or diesel oil distillate, dilute the unsaturated hydro carbons such as the alkadienes in raw material, reduce the severity of hydrogenation plant, make plant running more stable.But the method sacrifices the processing capacity of hydrogenation device for treatment feed naphtha, actually reduce the air speed to feed naphtha, also will increase follow-up separator burden (existing separator can not meet the demands), economy is poor.
3, by-pass is set between the entrance and exit of preatreating reactors, during normal production, reaction mass is by entering heating furnace after preatreating reactors, when preatreating reactors beds Pressure Drop raises, reaction mass enters heating furnace through by-pass, after the part or all of more catalyst changeout of reactor to be pre-treated, reaction mass switches to preatreating reactors again and enters heating furnace.Although the method can assurance device not operation downtime, in the not pretreated situation of raw material, larger impact can be caused to main reactor temperature rise, make to operate more difficult control.The replacing of pretreatment catalyst simultaneously also can cause economic loss.Preatreating reactors adopts the impurity in protective agent bed deposition raw material, holds impurity limited in one's ability, need the protective agent often changed in preatreating reactors.
CN1109495A discloses a kind of Rifining method for catalylic cracking gasoline by adding hydrogen, and described is connected by the pre-sulfide catalyst of two different activities and variable grain diameter.Adopt the mode of different catalysts grating to have certain effect for the coking of alleviation hydrogenation catalyst bed, but effect is not given prominence to.US4,113, alkadienes in the hydrofinishing process process drippolene of 603 report uses two sections and sulfide, first paragraph uses the catalyst removing mercaptan of nickeliferous-tungsten, second segment uses precious metals palladium catalyst removing alkadienes, this technique is comparatively complicated, can not effectively play a role with the coking of other factor for etidine hydrocarbon.
Summary of the invention
For the deficiencies in the prior art, the invention provides the decoking tank of a kind of petroleum naphtha hydrogenation method and the method use, effectively can ensure the steady running of Naphtha hydrofining unit, extend the service cycle of Naphtha hydrofining unit.
Petroleum naphtha hydrogenation method of the present invention comprises the steps:
(1) mixture of feed naphtha and hydrogen is heated to the temperature needed for hydrofinishing in heating furnace;
(2) feed naphtha after heating and the mixture of hydrogen enter decoking tank;
(3) fixed bed hydrogenation reactor is entered through the feed naphtha of decoking tank decoking and hydrogen, feed naphtha and hydrogen are by the Hydrobon catalyst bed of fixed bed hydrogenation reactor under Hydrofinishing conditions, and the naphtha after hydrofinishing and hydrogen are discharged reactor and carried out being separated obtaining hydrotreated naphtha.
Decoking tank wherein comprises outer cylinder body, upper cover, low head and separation assembly, outer cylinder body and upper cover, low head form decoking tank shell jointly, upper cover top arranges material inlet, bottom low head, material outlet is set, separation assembly is tube structure and is arranged in decoking tank shell, above separation assembly cylindrical shell, rain cap is set, separation assembly cylindrical shell bottom arranges exit collector, exit collector communicates with the material outlet that low head is arranged, internal layer and the skin of separation assembly cylindrical shell are screen cloth, fill incrustation agent between inner screen and outer screen.
In the inventive method, feed naphtha can be straight-run naphtha, coking naphtha, cat cracked naphtha, cracking naphtha etc., also can be the mixture of two or more naphtha.It is 180 ~ 350 DEG C that the refining condition of petroleum naphtha hydrogenation is generally reactor inlet temperature, and reaction pressure is 0.5 ~ 12MPa, and during the liquid of feed naphtha, volume space velocity is 0.5 ~ 20h
-1, hydrogen to oil volume ratio is 50:1 ~ 1500:1(standard state), concrete reaction condition specifically can be determined according to the quality requirement of product after the character of feed naphtha and hydrogenation.Hydrobon catalyst take generally aluminium oxide as carrier, with one or more in W, Mo, Ni and Co for hydrogenation active component, can also containing suitable auxiliary agent, and active component is generally sulphided state in use, to improve the catalytic activity of catalyst.
The decoking tank concrete structure that the inventive method uses comprises outer cylinder body, upper cover, low head and separation assembly, outer cylinder body and upper cover, low head forms decoking tank shell jointly, upper cover top arranges material inlet, bottom low head, material outlet is set, separation assembly is tube structure and is arranged in decoking tank shell, above separation assembly cylindrical shell, rain cap is set, separation assembly cylindrical shell bottom arranges exit collector, exit collector communicates with the material outlet that low head is arranged, internal layer and the skin of separation assembly cylindrical shell are screen cloth, incrustation agent is filled between inner screen and outer screen.
In decoking tank of the present invention, outer cylinder body is preferably cylindrical tube, and separation assembly cylindrical shell is cylindrical tube, and both are coaxially arranged, and separation assembly cylindrical shell is fixed on outer cylinder body inside by stay bolt assembly.The rain cap arranged above separation assembly cylindrical shell and separation assembly cylindrical shell top arrange annular space, and annular space circulation area is 5% ~ 80% of separation assembly cylindrical shell cross-sectional area.In the middle of separation assembly screen cloth, the incrustation agent of filling is particle diameter 1.1 ~ 3mm, the preferably filler of 1.2 ~ 1.5mm, the material of filler can be aluminium oxide, silica, pottery etc., and also can make spent hydroprocessing catalyst or useless hydrogenation catalyst, the thickness of filler is generally 10 ~ 200mm.Separation assembly upper end level is suitable with decoking tank outer cylinder body height.Decoking tank bottom head is arranged and lets out grey mouth, decoking tank outer cylinder body bottom arranges ash blowing mouth.Can arrange the inlet diffuser of dispersed material below decoking tank upper cover material inlet, inlet diffuser can be conventional taper or plywood structure etc.
During work, feed naphtha through heating furnace heating has at high temperature gasified as gas phase, the naphtha of gasification and hydrogen mixture are from the material inlet of decoking tank upper cover, enter decoking tank through inlet diffuser, vapor phase stream is through the barrel of separation assembly cylindrical shell, incrustation agent has suitable porosity, gas enters the inner core runner of separation assembly through incrustation agent, flows out decoking tank through exit collector.Solid impurity in gaseous phase materials is trapped, and is deposited in annular space that decoking tank urceolus and separation assembly cylindrical shell formed.Along with the accumulation of solid impurity, move on gas phase circulating area is continuous, until solid impurity floods separation assembly, the annular space of Vapor Entrainment solid matter self-separation assembly top and rain cap flows out decoking tank through separation assembly inner core runner and exit collector, and so far decoking tank loses decoking effect, excises this decoking tank from system, open and let out grey mouth and ash blowing mouth, to ash blowing mouth injecting compressed air or nitrogen, removed by the coke powder in decoking tank tank, the decoking tank after excretion coke powder can recover to use.Also pressure indicator can be set between the entrance and exit of decoking tank, judge whether to need cleaning decoking tank according to the pressure drop rise situation of decoking tank.
Show through research, in Naphtha hydrofining unit, although the reason causing hydrogenation reactor pressure drop to raise fast is that in hydrogenation reactor, beds coking and fouling causes, but these dirty thing overwhelming majority are not carry out being formed after hydrogenation reaction through hydrogenation catalyst, but feed naphtha and hydrogen are after heating furnace is heated to high temperature, along with feed naphtha transfers gas phase to from liquid phase, coking precursor assembles conversion gradually owing to gasifying, finally become coke-like solid matter, these coke-like solid matters enter in hydrogenation reactor under gaseous stream conveying effect, be deposited in beds, and then blocking catalyst bed causes hydrogenation reactor pressure drop rise.Shown by great many of experiments, naphtha and hydrogen are heated to the coking material formed in high-temperature gasification process, with heating before be diverse material, this problem cannot be solved by the filtration of raw material.Meanwhile, these coking materials are easy to deposition, can effectively be separated in suitable deposition equipment.Adopt decoking tank of the present invention, after the gaseous stream of entrained solids impurity enters decoking tank, because circulation area expands, gas flow rate reduces, solid impurity deposits because effect of inertia drops down onto decoking pot bottom fast, and can not be brought in the deposition agent of decoking tank separation assembly by gas phase major part, because now gas phase flow velocity is slower, gas phase is separated with the fluidised form of solid impurity, therefore, separation assembly can not lose efficacy by fast blocking, and only constantly can rise with deposit and bury separation assembly and partial failure, the service life of this decoking tank is very long.The present invention, by the mechanism of research above-mentioned petroleum naphtha hydrogenation process coking, arranges the incrustation tank of architecture, petroleum naphtha hydrogenation technological process reasonable in design, effectively can solve short problem hydrogenation reactor in petroleum naphtha hydrogenation technology service cycle.
Decoking tank of the present invention have structure simple, take up an area little, no-rotary part, space utilization fully, the feature such as large, the small investment of solid impurity deposition, in petroleum naphtha hydrogenation technology after heating furnace the solid impurity of material be separated very suitable.
Accompanying drawing explanation
Fig. 1 is the decoking jar structure schematic diagram that the present invention uses.
Wherein: 1-material inlet, 2-inlet diffuser, 3-upper cover, 4-separation assembly, 5-outer cylinder body, 6-ash blowing mouth, 7-exit collector, 8-material outlet, 9-skirt, 10-lets out grey mouth, 11-low head, the drop-down support component of 12-, 13-pull-up support component.
Detailed description of the invention
Further illustrate the technology contents of the inventive method and decoking tank below in conjunction with accompanying drawing, and further illustrate the technique effect of the inventive method by embodiment.
Arrange decoking tank as shown in Figure 1 between the heating furnace of petroleum naphtha hydrogenation process of the present invention in existing petroleum naphtha hydrogenation technique and hydrogenation reactor, other content does not need to change substantially.As shown in Figure 1, decoking tank forms shell body by upper cover 3, outer cylinder body 5 and low head 11, and upper cover 3 top arranges material inlet 1, material inlet 1 bottom inlet porting diffuser 2, arrange exit collector 7 bottom low head 11, exit collector 7 communicates with material outlet 8.The existing decoking tank outer cylinder body 5 of separation assembly 4 is coaxially arranged in decoking tank, and separation assembly 4 is fixed in decoking tank by drop-down support component 12 and pull-up support component 13, and separation assembly 4 is that the agent of two-layer screen cloth inside filling incrustation is formed.Arrange bottom decoking tank low head and let out grey mouth 10, decoking tank outer cylinder body 5 bottom arranges ash blowing mouth 6.Whole decoking tank is fixed on working face by skirt 9.
The result of use of the inventive method and decoking tank is further illustrated below by embodiment.The decoking jar structure that embodiment uses is: the high and diameter ratio of ratio of height to diameter 5(), separation assembly cylindrical shell thickness is 50mm, interior filling particle diameter is the alumina globule of 1.5mm, separation assembly cylinder internal diameter is identical with hydrogenation reactor suction line diameter, and between separation assembly and decoking tank shell body, annular space distance is 1 meter.Separation assembly rain cap and separation assembly do not establish gap.
Embodiment 1 and comparative example 1
Coking naphtha hydrofining technology.Coking naphtha mixes with hydrogen and is heated to 230 DEG C through heating furnace, enters hydrogenation reactor after entering decoking tank decoking.Hydrogenation catalyst FH-40A is the business Hydrobon catalyst of Sinopec Fushun Petrochemical Research Institute development and production.Feedstock property in table 1, operating condition and the results are shown in Table 2.Being distinguished as of comparative example does not arrange decoking tank.
Table 1 feedstock oil character.
| Raw material | Coking naphtha |
| Boiling range scope, DEG C | 36～192 |
| Sulphur, μ g/g | 4960 |
| Nitrogen, μ g/g | 126 |
| Bromine valency, gBr/ (100mL) | 48 |
Table 2 operating condition and product property.
| Embodiment 1 | Comparative example 1 | |
| Reaction hydrogen pressure, MPa | 4.0 | 4.0 |
| Hydrogen to oil volume ratio | 800:1 | 800:1 |
| Volume space velocity, h -1 | 2.0 | 2.0 |
| Reactor inlet temperature, DEG C | 230 | 230 |
| Hydrogenation catalyst | FH-40A | FH-40A |
| Reactor pressure decrease, MPa(30 days) | 0.10 | 0.12 |
| Reactor pressure decrease, MPa(60 days) | 0.10 | 0.20 |
| Reactor pressure decrease, MPa(90 days) | 0.10 | 0.28 |
| Reactor pressure decrease, MPa(100 days) | 0.10 | Stop work |
As can be seen from above-mentioned contrast, the inventive method can solve the pressure drop rise problem of coking naphtha hydrogenation plant, effectively can extend the service cycle of hydrogenation plant.
Embodiment 2 and comparative example 2
Catalytic cracking heavy naphtha selective hydrogenation desulfurization process.Cat cracked naphtha adopts commodity AFS-12 catalyst (University of Petroleum's production), at pressure 0.5MPa, temperature 35 DEG C ~ 45 DEG C, volume space velocity 2.0h
-1, carry out deodorization under gas-oil ratio (air/gasoline) 4:1 condition.Deodorization product is through fractionation, and cut point is 70 DEG C and obtains catalytic cracking heavy naphtha, and catalytic cracking heavy naphtha mixes with hydrogen and is heated to 250 DEG C through heating furnace, enters hydrogenation reactor after entering decoking tank decoking.Hydrogenation catalyst FGH-11 is the business catalyst for selectively hydrodesulfurizing of Sinopec Fushun Petrochemical Research Institute development and production.Feedstock property in table 3, operating condition and the results are shown in Table 4.Being distinguished as of comparative example does not arrange decoking tank.
Table 3 catalytic cracking heavy naphtha main character.
| Raw material | Cat cracked naphtha heavy distillat |
| Sulfur content, μ g/g | 900 |
| Olefin(e) centent, v% | 22 |
| Research octane number (RON), RON | 91.0 |
| Boiling range, DEG C (initial boiling point ~ end point of distillation) | 58～179 |
Table 4 operating condition and result.
| Embodiment 2 | Comparative example 2 | |
| Reaction hydrogen pressure, MPa | 1.6 | 1.6 |
| Hydrogen to oil volume ratio | 300:1 | 300:1 |
| Volume space velocity, h -1 | 2.0 | 2.0 |
| Reactor inlet temperature, DEG C | 250 | 250 |
| Hydrogenation catalyst | FGH-11 | FGH-11 |
| Reactor pressure decrease, MPa(5 days) | 0.09 | 0.15 |
| Reactor pressure decrease, MPa(10 days) | 0.09 | 0.20 |
| Reactor pressure decrease, MPa(20 days) | 0.09 | Stop work |
| Reactor pressure decrease, MPa(50 days) | 0.09 |
Embodiment 3 and comparative example 3
Straight-run naphtha is hydrogenated to catalytic reforming in advance and supplies raw materials.Straight-run naphtha mixes with hydrogen and is heated to 300 DEG C through heating furnace, enters hydrogenation reactor after entering decoking tank decoking.Hydrogenation catalyst FH-40C is the business Hydrobon catalyst of Sinopec Fushun Petrochemical Research Institute development and production.Feedstock property in table 5, operating condition and the results are shown in Table 6.Being distinguished as of comparative example does not arrange decoking tank.
Table 5 straight-run naphtha main character.
| Raw material | Straight-run naphtha |
| Source | Mixing straight-run naphtha |
| Density (20 DEG C), g/cm 3 | 0.7348 |
| Sulfur content, μ g/g | 800 |
| Nitrogen content, μ g/g | 2.8 |
Table 6 operating condition and result.
| Process conditions | Embodiment 3 | Comparative example 3 |
| Reaction pressure, MPa | 1.6 | 1.6 |
| Reaction temperature, DEG C | 300 | 300 |
| Volume space velocity, h -1 | 6.0 | 6.0 |
| Hydrogen-oil ratio, Nm 3/m 3 | 100 | 100 |
| Oil property | Refined oil | Refined oil |
| Sulfur content, μ g/g | <0.5 | <0.5 |
| Nitrogen content, μ g/g | <0.5 | <0.5 |
| Hydrogenation catalyst | FH-40C | FH-40C |
| Reactor pressure decrease, MPa(30 days) | 0.11 | 0.15 |
| Reactor pressure decrease, MPa(60 days) | 0.11 | 0.20 |
| Reactor pressure decrease, MPa(100 days) | 0.11 | 0.26 |
| Reactor pressure decrease, MPa(120 days) | 0.11 | Stop work |
Can be found out by embodiment, by using the decoking tank of suitable configurations, the pressure drop of petroleum naphtha hydrogenation reactor is not risen substantially, can estimate, can not stop work within catalyst service life because of problem of pressure drop.
Claims (10)
1. a petroleum naphtha hydrogenation method, is characterized in that comprising the steps:
(1) mixture of feed naphtha and hydrogen is heated to the temperature needed for hydrofinishing in heating furnace;
(2) feed naphtha after heating and the mixture of hydrogen enter decoking tank;
(3) fixed bed hydrogenation reactor is entered through the feed naphtha of decoking tank decoking and hydrogen, feed naphtha and hydrogen are by the Hydrobon catalyst bed of fixed bed hydrogenation reactor under Hydrofinishing conditions, and the naphtha after hydrofinishing and hydrogen are discharged reactor and carried out being separated obtaining hydrotreated naphtha;
Decoking tank wherein comprises outer cylinder body, upper cover, low head and separation assembly, outer cylinder body and upper cover, low head form decoking tank shell jointly, upper cover top arranges material inlet, bottom low head, material outlet is set, separation assembly is tube structure and is arranged in decoking tank shell, above separation assembly cylindrical shell, rain cap is set, separation assembly cylindrical shell bottom arranges exit collector, exit collector communicates with the material outlet that low head is arranged, internal layer and the skin of separation assembly cylindrical shell are screen cloth, fill incrustation agent between inner screen and outer screen.
2. in accordance with the method for claim 1, it is characterized in that: feed naphtha is straight-run naphtha, coking naphtha, cat cracked naphtha, cracking naphtha, or the mixture of two or more naphtha in aforementioned feed naphtha.
3. in accordance with the method for claim 1, it is characterized in that: the refining condition of petroleum naphtha hydrogenation is reactor inlet temperature is 180 ~ 350 DEG C, and reaction pressure is 0.5 ~ 12MPa, during the liquid of feed naphtha, volume space velocity is 0.5 ~ 20h
-1, hydrogen to oil volume ratio is 50:1 ~ 1500:1.
4. a decoking tank, it is characterized in that: decoking tank comprises outer cylinder body, upper cover, low head and separation assembly, outer cylinder body and upper cover, low head forms decoking tank shell jointly, upper cover top arranges material inlet, bottom low head, material outlet is set, separation assembly is tube structure and is arranged in decoking tank shell, above separation assembly cylindrical shell, rain cap is set, separation assembly cylindrical shell bottom arranges exit collector, exit collector communicates with the material outlet that low head is arranged, internal layer and the skin of separation assembly cylindrical shell are screen cloth, incrustation agent is filled between inner screen and outer screen.
5. according to decoking tank according to claim 4, it is characterized in that: decoking tank outer cylinder body is cylindrical tube, and separation assembly cylindrical shell is cylindrical tube, and both are coaxially arranged, it is inner that separation assembly cylindrical shell is fixed on decoking tank outer cylinder body by stay bolt assembly.
6. according to decoking tank according to claim 4, it is characterized in that: the rain cap arranged above separation assembly cylindrical shell and separation assembly cylindrical shell top arrange annular space, annular space circulation area is 5% ~ 80% of separation assembly cylindrical shell cross-sectional area.
7. according to decoking tank according to claim 4, it is characterized in that: in the middle of separation assembly screen cloth, the incrustation agent of filling is the filler of particle diameter 1.1 ~ 3mm, and the thickness of filler is 10 ~ 200mm.
8. according to decoking tank according to claim 7, it is characterized in that: the material of filler is aluminium oxide, silica, pottery or makes spent hydroprocessing catalyst or useless hydrogenation catalyst.
9. according to decoking tank according to claim 4, it is characterized in that: separation assembly upper end level is suitable with decoking tank outer cylinder body height.
10. according to decoking tank according to claim 4, it is characterized in that: arrange on decoking tank bottom head and let out grey mouth, decoking tank outer cylinder body bottom arranges ash blowing mouth.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4113603A (en) * | 1977-10-19 | 1978-09-12 | The Lummus Company | Two-stage hydrotreating of pyrolysis gasoline to remove mercaptan sulfur and dienes |
| CN1109495A (en) * | 1994-03-28 | 1995-10-04 | 中国石油化工总公司 | Rifining method for catalylic cracking gasoline by adding hydrogen |
| CN2605059Y (en) * | 2003-02-21 | 2004-03-03 | 吴江 | Centrifugal gas-tar separator |
| CN2748458Y (en) * | 2004-12-01 | 2005-12-28 | 扬州石油化工厂 | Decoking catalytic fractionating tower |
-
2011
- 2011-04-15 CN CN201110095290.9A patent/CN102732306B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4113603A (en) * | 1977-10-19 | 1978-09-12 | The Lummus Company | Two-stage hydrotreating of pyrolysis gasoline to remove mercaptan sulfur and dienes |
| CN1109495A (en) * | 1994-03-28 | 1995-10-04 | 中国石油化工总公司 | Rifining method for catalylic cracking gasoline by adding hydrogen |
| CN2605059Y (en) * | 2003-02-21 | 2004-03-03 | 吴江 | Centrifugal gas-tar separator |
| CN2748458Y (en) * | 2004-12-01 | 2005-12-28 | 扬州石油化工厂 | Decoking catalytic fractionating tower |
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