CN102732303A - Device and method for hydrogenation reaction of naphtha - Google Patents
Device and method for hydrogenation reaction of naphtha Download PDFInfo
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- CN102732303A CN102732303A CN2011100952754A CN201110095275A CN102732303A CN 102732303 A CN102732303 A CN 102732303A CN 2011100952754 A CN2011100952754 A CN 2011100952754A CN 201110095275 A CN201110095275 A CN 201110095275A CN 102732303 A CN102732303 A CN 102732303A
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Abstract
The invention discloses a device and a method for a hydrogenation reaction of naphtha. The device for a hydrogenation reaction of naphtha comprises a feeding system, a heating furnace, a fixed bed hydrogenation reactor and a hydrogenation reaction product separation system and also comprises a decoking system, wherein the feeding system is communicated with an inlet of the heating surface by a pipe; an outlet of the heating surface is communicated with the decoking system by a pipe; the decoking system is communicated with an inlet of the fixed bed hydrogenation reactor; and an outlet of the fixed bed hydrogenation reactor is communicated with the hydrogenation reaction product separation system by a pipe. Through the method provided by the invention, the device for a hydrogenation reaction of naphtha realizes hydrofining of a naphtha feedstock under appropriate conditions. Compared with the prior art, the device and the method 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 reaction unit and process for selective hydrogenation, specifically a kind of petroleum naphtha hydrogenation reaction unit hydrogenation reaction device and process for selective hydrogenation of running period of prolonging.
Background technology
Petroleum naphtha (being gasoline fraction) is important gasoline stocks and industrial chemicals; Be mainly used in the Fuel Petroleum of producing the various trades mark; CR is produced aromatic hydrocarbons (or stop bracket gasoline blend component) raw material; Steam cracking or catalytic pyrolysis are produced industrial chemicals such as ethene, propylene, butylene, and the raw material etc. that is used to produce hydrogen.Petroleum naphtha generally derives from the virgin naphtha that petroleum distillation obtains, and the petroleum naphtha that secondary processing obtains is like coking naphtha, catalytic cracking petroleum naphtha, cracking naphtha etc.The various uses of various sources petroleum naphtha all need be with the sulphur in the raw material, nitrogen, rare hydrocarbon, metal impurities deep removal, and hydrogen addition technology is the optimum technology that removes various impurity in the feed naphtha at present.Produce stop bracket gasoline like catalytic cracking naphtha selective hydrogenation, the coking naphtha hydrogenation is produced steam crack material or hydrogen feedstock, and the preparatory hydrogenation of virgin naphtha is produced catalytic reforming raw material etc.
In the various hydrogen addition technologies of petroleum naphtha; What generally use is the fixed bed hydrogenation technology, the fixed bed hydrogenation beds promptly is set, in the hydrogenator under the unifining condition; Feed naphtha and hydrogen get into reactor drum from top; Carry out unifining through the hydrogenation catalyst bed and remove the various impurity in the raw material, the reaction product after making with extra care is discharged reactor drum from reactor bottom, carries out obtaining the hydrotreated naphtha product after the follow-up separation.
In the petroleum naphtha hydrogenation technology, the principal element of restriction hydrogenation unit LP steady running is the pressure drop rising rapid speed of fixed bed hydrogenation reactor, in general, when the pressure drop of hydrogenator reaches 0.3MPa, must stop work and handle.
For example concerning coking naphtha unifining technology,, often influence the operational stability of device owing to contain diolefine, tiny impurity such as coke powder in the raw material.Daqing petrochemical company 300kt/a coker gasoline hydrogenation unit is after the half a year that goes into operation, and it is too high to occur two subsystem pressure reduction continuously, causes compelled shut-down the (the pressure reduction rising analysis of causes of coking gasoline hydrogenation refining system and countermeasure, " oil refining and chemical industry ", the 19th volume: 20).The too fast problem of reactor catalyst bed pressure drop rising also appears in Guangzhou Branch 300kt/a hydrogenation unit when handling coker gasoline.This device once in the time of a year and a half, lacked (the analysis of causes and countermeasure that the hydrofining reaction system pressure drop raises, " China and foreign countries' energy ", 2007, the 12 volumes) 5 times because the reactive system bed pressure drop raises to cause stopping work disappearing.General 3～5 days needs of two I coker gasoline hydrogenation units of Anqing branch office oil refining clean a strainer; Hydrogenator will be stopped work in 1 year and cast aside for 2～3 times, has a strong impact on normal operation (coker gasoline hydrogenation scorch retarder, " petrochemical technology " of device; 2006,13 (4): 5).All there is similar problem in various degree in domestic and international device of the same type; The increase of pressure difference between bed; Make the inner members such as support bar and back up pad of catalyzer when bearing catalyst weight, again must the outer pressure of commitment, bring serious hidden danger for the safety operation of device.Therefore, it is the conspicuous contradiction that influences coking naphtha hydrogenation unit long-term operation that bed pressure drop rises too fast always, presses for and works out effective means, solves coking problem.
Above-mentioned coking naphtha hydrogenation unit similar problem also often appears in catalytic cracking petroleum naphtha hydrogenation device, virgin naphtha hydrogenation unit etc.; Be the hydrogenation unit running short period the high problem of reactor pressure falling-rising promptly to occur; Can only the stop work part catalyzer on purge reactor beds top goes into operation after the removable parts live catalyst again.
Petroleum naphtha hydrogenation device running practice shows that the rising of hydrogenator pressure drop all comes from the bed coking of catalyzer top.The coking factor is very complicated, is converted into mainly due to the polymerization of the unsaturated hydro carbons such as diolefine in the raw material and mechanical impurity that upstream device is brought into or impurity precursor to be deposited on beds top behind the settling and to cause.Diolefine in the raw material is being easy to take place polymerization, when particularly in raw material, containing other impurity such as oxygen, water, iron etc., is easier to polymerization coking.In the sample of coking, the content of general iron is also higher, possibly be to have formed naphthenic acid with organic hydrocarbon behind the raw oil dissolved oxygen; The iron of naphthenic acid corrosion device generates iron naphthenate; Stably be dissolved in the raw oil, iron naphthenate is easy to take place hydrogenolysis after mixing hydrogen, and is deposited on reactor drum top bed with hydrogen sulfide reaction generation Iron sulfuret; Promote the green coke reaction of coking parent, quickened the obstruction of beds.In addition, containing a spot of tiny coke powder and tiny mikrobe in some raw material also possibly be one of reason of some feed naphthas coking in hydrogenator.Because the petroleum naphtha source is varied; Introduced in the production of some feed naphtha, storage, the transportation and can't filter the impurity of removing through raw material; These impurity are oil-soluble sometimes, are the particulate that suspends sometimes, can't effectively remove through a kind of or simple several method.And the feed naphtha source of a hydrogenation unit is unfixing, often changes, and therefore, yet can not certain device is fixed as certain raw material of processing and use fixed to fall the impurity method.
The method that existing solution petroleum naphtha hydrogenation reactor drum step-down raises has following several kinds:
1, carries out the management work of raw material, adopt modes such as nitrogen protection, avoid raw material to contact, at utmost reduced unsaturated hydro carbons formation gelationus chance in the raw material with air.This is a kind of passive raw material guard method, if the raw material mechanical impurity of upper reaches input is more, diene content is very high, or carries a lot of coke powders secretly, and this method is then powerless.
2, mix artificial coal oil or diesel oil distillate, diluted the unsaturated hydro carbons such as diolefine in the raw material, reduced the severity of hydrogenation unit, make the device operation more stable.But this method has been sacrificed the amount of finish of hydrogenation device for treatment feed naphtha, has in fact reduced the air speed to feed naphtha, also will increase follow-up tripping device burden (existing tripping device can not meet the demands), and economy is relatively poor.
3, between the entrance and exit of pretreatment reaction device, by-pass is set; Reaction mass gets into process furnace after through the pretreatment reaction device during ordinary production; When the falling-rising of pretreatment reaction device catalyst bed stressor layer is high; Reaction mass gets into process furnace through by-pass, treats the pretreatment reaction device partly or entirely more behind the catalyst changeout, and reaction mass switches to the pretreatment reaction device again and gets into process furnace.Though this method can assurance device operation downtime not, raw material without pretreated situation under, can cause bigger impact to the main reactor temperature rise, make the difficult control of operation.The replacing of pretreatment catalyst simultaneously also can cause financial loss.The pretreatment reaction device is to adopt protective material bed deposition impurities in raw materials, and it is limited in one's ability to hold impurity, needs often to change the protective material in the pretreatment reaction device.
CN1109495A discloses a kind of Rifining method for catalylic cracking gasoline by adding hydrogen, and described is that the pre-sulfide catalyst of two different activities and variable grain diameter is connected.Adopt the mode of different catalysts grating to have certain effect, but effect is not outstanding for alleviating the coking of hydrogenation catalyst bed.US4; 113; 603 reports use two sections hydrofinishing process to handle diolefine and sulfide in the pyrolysis gasoline, and the catalyzer of first section nickeliferous-tungsten of use is removed mercaptan, and second section is used precious metals palladium catalyst to remove diolefine; This technology is comparatively complicated, and the coking with other factor can not play a role effectively for the etidine hydrocarbon.
Summary of the invention
To the deficiency of prior art, the present invention provides a kind of petroleum naphtha hydrogenation reaction unit and petroleum naphtha hydrogenation reaction method, can effectively guarantee the stable operation of petroleum naphtha hydrogenation reaction unit, prolongs the running period of petroleum naphtha hydrogenation device.
Petroleum naphtha hydrogenation reaction unit of the present invention comprises feed system, process furnace, decoking system, fixed bed hydrogenation reactor and hydrogenation reaction product separation system; Feed system is communicated with the process furnace inlet through pipeline; Furnace outlet is communicated with decoking system through pipeline; Decoking system is communicated with the fixed bed hydrogenation reactor inlet through pipeline, and the fixed bed hydrogenation reactor outlet is communicated with the hydrogenation reaction product separation system through pipeline; Decoking system is provided with the coke powder washing tank, and the material inlet of coke powder washing tank setting is connected with furnace outlet, and the material outlet that coke powder washing tank top is provided with is communicated with the fixed bed hydrogenation reactor inlet, and coke powder washing tank bottom is provided with the washings relief outlet.
In apparatus of the present invention, be arranged in the coke powder washing tank and be the coke powder washings of liquid phase under the user mode, generally can use kerosene, diesel oil, vacuum distillate, lubricant base, residual oil etc., be preferably diesel oil or vacuum distillate.The service temperature of coke powder washing tank is identical with the fixed bed hydrogenation reactor temperature in.The coke powder washing tank can adopt bubbling bed operating method, and promptly the bottom is provided with gas distributor in the coke powder washing tank, is used for gaseous phase materials is dispersed in the coke powder washings; The coke powder washing tank also can adopt the spray operating method, and promptly coke powder washing tank internal upper part is provided with the liquid spraying device, is used for the coke powder washings and disperses the spray washing gaseous phase materials.
In apparatus of the present invention, the coke powder separating tank can be set, the coke powder separating tank is used for the coke powder washing tank is contained the solid-liquid separation of the coke powder washings of impurity such as solid coke powder.Coke powder separating tank material inlet communicates with the washings relief outlet of coke powder washing tank bottom.
In apparatus of the present invention, the coke powder separating tank is a liquid-solid separation device, and promptly the coke powder separating tank is made up of outer hull and inner separation assembly.
The coke powder separating tank of the preferred following structure of the present invention: the coke powder separating tank is made up of the separation assembly of body skin and set inside; Body skin is provided with material inlet and material outlet; Material inlet preferably is arranged on the body skin top, and material outlet preferably is arranged on the body skin bottom.Separation assembly is a tube structure, and the internal layer of separation assembly cylindrical shell is a screen cloth with skin, fills the incrustation agent between inner screen and the outer screen.The barrel passage of separation assembly is communicated with the body skin material outlet.Separation assembly is provided with one at least, and when a plurality of separation assembly was set, separation assembly barrel passage all was communicated with the body skin material outlet, as separation assembly barrel passage manifold trunk can be set, compile the back and is communicated with the body skin material outlet.The incrustation agent of filling is particle diameter 1.1～3mm in the middle of the separation assembly screen cloth; The filler of preferred 1.2 ~ 1.5mm; The material of filler can be aluminum oxide, silicon oxide, pottery etc., also can make spent hydroprocessing catalyst or useless hydrogenation catalyst etc., and the thickness of filler is generally 10～200mm.The coke powder separating tank can be provided with automatic backwash and remove settling, but also manual finishing settling.
In apparatus of the present invention; The coke powder separating tank can operate continuously or periodical operation; During operate continuously; The coke powder washings that the coke powder washing tank contains impurity such as solid coke powder gets into the coke powder separating tank continuously, recycles through removing solid impurity coke powder washings behind the coke powder separating tank, and the coke powder washings that removes the solid impurity coke powder can be circulated to the coke powder washing tank or is circulated to the process furnace inlet or is circulated to operating method such as raw material feed naphtha mixing through pipeline.During periodical operation; The coke powder separating tank is discharged removes coke powder washings behind the solid impurity and can be circulated to the coke powder washing tank or be circulated to the process furnace inlet or be circulated to operating method such as raw material feed naphtha mixing; Also can discharge not cyclical operation, the coke powder washing tank replenishes fresh coke powder washings.
In apparatus of the present invention; Sump preferably is set in the fixed bed hydrogenation reactor upper cover; Be used for further removing the solid impurity of reaction mass; Sump can use the conventional structure in this area, the sump that uses like disclosed inside reactor such as CN200410050765.2, CN200410050800.0, CN200510069872.4, CN200520017581.6 etc.
Petroleum naphtha hydrogenation reaction method of the present invention uses the above-mentioned petroleum naphtha hydrogenation reaction unit of the present invention, specifically comprises the steps:
(1) mixture of feed naphtha and hydrogen is delivered to through feed system and is heated to the required temperature of hydrogenation reaction in the process furnace;
(2) mixture of feed naphtha after the heating and hydrogen gets into decoking system;
(3) feed naphtha and the hydrogen through the decoking system decoking gets into fixed bed hydrogenation reactor; Feed naphtha and hydrogen pass through the Hydrobon catalyst bed of fixed bed hydrogenation reactor under the unifining condition; Petroleum naphtha after the unifining and hydrogen are discharged reactor drum and are got into separation system and separate and obtain hydrotreated naphtha, separate the hydrogen recycle that obtains and use.
In the inventive method, feed naphtha can be virgin naphtha, coking naphtha, catalytic cracking petroleum naphtha, cracking naphtha etc., also can be the mixture of two or more petroleum naphtha.It is 180～350 ℃ that petroleum naphtha hydrogenation purified condition is generally reactor inlet temperature, and reaction pressure is 0.5～12MPa, and volume space velocity is 0.5～20h during the liquid of feed naphtha
-1, hydrogen to oil volume ratio is 50:1～1500:1 (standard state), concrete reaction conditions can specifically be confirmed according to the specification of quality of product behind the character of feed naphtha and the hydrogenation.Hydrobon catalyst generally is carrier with the aluminum oxide, is the hydrogenation activity component with among W, Mo, Ni and the Co one or more, can also contain suitable auxiliary agent, and active ingredient is generally sulphided state in use, to improve the catalytic activity of catalyzer.
During the inventive method work; The feed naphtha of process process furnace heating has at high temperature gasified and has been gas phase; The petroleum naphtha of gasification and hydrogen mixture get into decoking system; Coke powder washings in the decoking system gets off the solid impurity effectively catchings such as coke powder in the gas phase, and the gaseous phase materials that process removes behind the coke powder gets into fixed bed hydrogenation reactor, carries out hydrogenation reaction.Get into the coke powder separating tank removes solid impurity to the coke powder washings of having held back solid impurity continuously or intermittently.The coke powder separating tank can regularly be cleared up.
Show through research; In the petroleum naphtha hydrogenation device; Though the reason that causes the hydrogenator pressure drop to raise fast is that the beds coking and fouling causes in the hydrogenator, these dirty thing overwhelming majority are not to carry out forming after the hydrogenation reaction through hydrogenation catalyst, but feed naphtha and hydrogen are after process furnace is heated to high temperature; Along with feed naphtha transfers gas phase to from liquid phase; The coking precursor assemble to transform owing to can't gasify gradually, finally becomes burnt shape solid matter, and these burnt shape solid matters are under gaseous stream conveying effect in the entering hydrogenator; Be deposited in the beds, and then the blocking catalyst bed causes hydrogenator pressure drop rising.Show that through a large amount of experiments petroleum naphtha and hydrogen are heated to the coking material that forms in the high-temperature gasification process, with the heating before be diverse material, can't address this problem through the filtration of raw material.Simultaneously, these coking materials are easy to deposition, in suitable deposition equipment, can effectively separate.Adopt decoking system of the present invention, the gaseous stream of entrained solids impurity removes defocused through the coke powder washings, gets into fixed bed hydrogenation reactor and carries out hydrogenation reaction.
Petroleum naphtha hydrogenation reaction unit of the present invention only need increase a simple decoking system; That decoking system has is simple in structure, it is little to take up an area of, no-rotary part, space utilization fully, characteristics such as big, the less investment of solid impurity deposition, pressure reduction, to the investment of hydrogenation reaction device and process cost increase seldom.
Description of drawings
Fig. 1 is the schematic flow sheet of apparatus of the present invention decoking system set-up mode in whole device;
Wherein: 1-process furnace, 2-coke powder washing tank, 3-coke powder detergent circulator, 4-coke powder separating tank, 5 fixed bed hydrogenation reactors.
Embodiment
Further specify the technology contents of the inventive method and decoking system below in conjunction with accompanying drawing, and further specify the technique effect of the inventive method through embodiment.
Between process furnace and the hydrogenator of petroleum naphtha hydrogenation process method of the present invention in existing petroleum naphtha hydrogenation technology decoking system is set, other content need not change basically.As shown in Figure 1, reaction mass entering coke powder washing tank 2 decokings through process furnace 1 heating get into fixed bed hydrogenation reactor 5 then, carry out getting into separation system after the hydrogenation reaction.Coke powder washings in the coke powder washing tank 2 enters in the coke powder separating tank 4 continuously or intermittently, and the coke powder washings that removes behind the impurity such as solid coke powder loops back coke powder washing tank 2 through coke powder detergent circulator 3.
Further specify the effect of the inventive method and device below through embodiment.The coke powder washing tank structure that embodiment uses is: aspect ratio 3 (height and diameter ratio), adopt bubbling style washing bed, and be the coke powder washings with the refined diesel oil, coke powder washings layer thickness is 1 meter.The separation assembly cylindrical shell thickness of coke powder separating tank is 50mm, and interior filling particle diameter is the alumina globule of 1.5mm.
The coking naphtha hydrogen refining process.Coking naphtha mixes with hydrogen through process furnace and is heated to 230 ℃, gets into hydrogenator after getting into the decoking system decoking.Hydrogenation catalyst FH-40A is the commercial Hydrobon catalyst of Sinopec Fushun Petrochemical Research Institute development and production.Feedstock property is seen table 1, and operational condition and result see table 2.The difference of comparative example is not for being provided with decoking system.
Table 1 raw oil character.
| Raw material | Coking naphtha |
| The boiling range scope, ℃ | 36～192 |
| Sulphur, μ g/g | 4960 |
| Nitrogen, μ g/g | 126 |
| The bromine valency, gBr/ (100mL) | 48 |
Table 2 operational condition and product property.
| ? | |
Comparative example 1 |
| The 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, ℃ | 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 |
Can find out that from above-mentioned contrast the inventive method can solve the pressure drop rising problem of coking naphtha hydrogenation unit, can effectively prolong the running period of hydrogenation unit.
Catalytic cracking heavy naphtha selective hydrogenation desulfurization process.The catalytic cracking petroleum naphtha adopts commodity AFS-12 catalyzer (University of Petroleum's production), at pressure 0.5MPa, 35 ℃～45 ℃ of temperature, volume space velocity 2.0h
-1, carry out deodorization under gas and oil volume ratio (air/gasoline) the 4:1 condition.The deodorization product is through fractionation, and cut point is 70 ℃ and obtains catalytic cracking heavy naphtha, and catalytic cracking heavy naphtha mixes with hydrogen through process furnace and is heated to 250 ℃, gets into hydrogenator after getting into the decoking system decoking.Hydrogenation catalyst FGH-11 is the commercial catalyst for selectively hydrodesulfurizing of Sinopec Fushun Petrochemical Research Institute development and production.Feedstock property is seen table 3, and operational condition and result see table 4.The difference of comparative example is not for being provided with decoking system.
Table 3 catalytic cracking heavy naphtha main character.
| Raw material | The last running of catalytic cracking petroleum naphtha |
| Sulphur content, μ g/g | 900 |
| Olefin(e) centent, v% | 22 |
| RON, RON | 91.0 |
| Boiling range, ℃ (over point～final boiling point) | 58～179 |
Table 4 operational condition and result.
| ? | |
Comparative example 2 |
| The 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, ℃ | 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 | ? |
Virgin naphtha is hydrogenated to CR in advance and supplies raw materials.Virgin naphtha mixes with hydrogen through process furnace and is heated to 300 ℃, gets into hydrogenator after getting into the decoking system decoking.Hydrogenation catalyst FH-40C is the commercial Hydrobon catalyst of Sinopec Fushun Petrochemical Research Institute development and production.Feedstock property is seen table 5, and operational condition and result see table 6.The difference of comparative example is not for being provided with decoking system.
Table 5 virgin naphtha main character.
| Raw material | Virgin naphtha |
| The source | Mix virgin naphtha |
| Density (20 ℃), g/cm 3 | 0.7348 |
| Sulphur content, μ g/g | 800 |
| Nitrogen content, μ g/g | 2.8 |
Table 6 operational condition and result.
| | Embodiment | 3 | Comparative example 3 |
| Reaction pressure, MPa | 1.6 | 1.6 | |
| Temperature of reaction, ℃ | 300 | 300 | |
| Volume space velocity, h -1 | 6.0 | 6.0 | |
| Hydrogen-oil ratio, Nm 3/m 3 | 100 | 100 | |
| Oil property | Treated oil | Treated oil | |
| Sulphur 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 find out that through embodiment through using the decoking system of suitable structure, the pressure drop of petroleum naphtha hydrogenation reactor drum is not risen basically, can estimate, can not stop work because of problem of pressure drop in work-ing life at catalyzer.
Claims (14)
1. petroleum naphtha hydrogenation reaction unit; Comprise feed system, process furnace, fixed bed hydrogenation reactor and hydrogenation reaction product separation system; It is characterized in that: also comprise decoking system, feed system is communicated with the process furnace inlet through pipeline, and furnace outlet is communicated with decoking system through pipeline; Decoking system is communicated with the fixed bed hydrogenation reactor inlet through pipeline, and the fixed bed hydrogenation reactor outlet is communicated with the hydrogenation reaction product separation system through pipeline; Decoking system is provided with the coke powder washing tank, and the material inlet of coke powder washing tank setting is connected with furnace outlet, and the material outlet that coke powder washing tank top is provided with is communicated with the fixed bed hydrogenation reactor inlet, and coke powder washing tank bottom is provided with the washings relief outlet.
2. according to the described device of claim 1, it is characterized in that: be arranged in the coke powder washing tank and be the coke powder washings of liquid phase under the user mode.
3. according to the described device of claim 2, it is characterized in that: the coke powder washings uses kerosene, diesel oil, vacuum distillate, lubricant base or residual oil.
4. according to the described device of claim 1, it is characterized in that: the coke powder washing tank adopts bubbling bed operating method, and promptly the bottom is provided with gas distributor in the coke powder washing tank, is used for gaseous phase materials is dispersed in the coke powder washings; Perhaps the coke powder washing tank adopts the spray operating method, and promptly coke powder washing tank internal upper part is provided with the liquid spraying device, is used for the coke powder washings and disperses the spray washing gaseous phase materials.
5. according to the described device of claim 1, it is characterized in that: the coke powder separating tank is set, and coke powder separating tank material inlet communicates with the washings relief outlet of coke powder washing tank bottom, and the coke powder separating tank is a liquid-solid separation device.
6. according to the described device of claim 5; It is characterized in that: coke powder separating tank structure is made up of the separation assembly of body skin and set inside, and body skin is provided with material inlet and material outlet, and separation assembly is a tube structure; The internal layer of separation assembly cylindrical shell is a screen cloth with skin; Fill the incrustation agent between inner screen and the outer screen, the barrel passage of separation assembly is communicated with the body skin material outlet, and separation assembly is provided with one at least.
7. according to the described device of claim 6, it is characterized in that: the incrustation agent of filling is particle diameter 1.1～3mm in the middle of the separation assembly screen cloth, the filler of preferred 1.2 ~ 1.5mm.
8. according to the described device of claim 7, it is characterized in that: the material of filler is aluminum oxide, silicon oxide, pottery, perhaps makes spent hydroprocessing catalyst or useless hydrogenation catalyst, and the thickness of filler is 10～200mm.
9. according to the described device of claim 5, it is characterized in that: operate continuously of coke powder separating tank or periodical operation.
10. according to the described device of claim 9; It is characterized in that: during the operate continuously of coke powder separating tank; The coke powder washings that the coke powder washing tank contains solid coke powder impurity gets into the coke powder separating tank continuously; Recycle through removing solid impurity coke powder washings behind the coke powder separating tank, the coke powder washings that removes the solid impurity coke powder is circulated to the coke powder washing tank through pipeline or is circulated to the process furnace inlet or is circulated to raw material feed naphtha blended operating method; During the periodical operation of coke powder separating tank; The coke powder separating tank is discharged removes coke powder washings behind the solid impurity and is circulated to the coke powder washing tank or is circulated to the process furnace inlet or is circulated to raw material feed naphtha blended operating method; Perhaps discharge not cyclical operation, the coke powder washing tank replenishes fresh coke powder washings.
11., it is characterized in that: in the fixed bed hydrogenation reactor upper cover sump is set, is used for further removing the solid impurity of reaction mass according to the described device of claim 1.
12. a petroleum naphtha hydrogenation reaction method is characterized in that: use the described petroleum naphtha hydrogenation reaction unit of the arbitrary claim of claim 1 to 11, comprise the steps:
(1) mixture of feed naphtha and hydrogen is delivered to through feed system and is heated to the required temperature of hydrogenation reaction in the process furnace;
(2) mixture of feed naphtha after the heating and hydrogen gets into decoking system;
(3) feed naphtha and the hydrogen through the decoking system decoking gets into fixed bed hydrogenation reactor; Feed naphtha and hydrogen pass through the Hydrobon catalyst bed of fixed bed hydrogenation reactor under the unifining condition; Petroleum naphtha after the unifining and hydrogen are discharged reactor drum and are got into separation system and separate and obtain hydrotreated naphtha, separate the hydrogen recycle that obtains and use.
13. according to the described method of claim 12, it is characterized in that: feed naphtha is virgin naphtha, coking naphtha, catalytic cracking petroleum naphtha, cracking naphtha, or the mixture of two or more petroleum naphtha.
14. according to the described method of claim 12, it is characterized in that: petroleum naphtha hydrogenation purified condition is that reactor inlet temperature is 180～350 ℃, and reaction pressure is 0.5～12MPa, and volume space velocity is 0.5～20h during the liquid of feed naphtha
-1, hydrogen to oil volume ratio is 50:1～1500:1.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113736516A (en) * | 2020-05-29 | 2021-12-03 | 中国石油化工股份有限公司 | Treatment process for producing ethylene raw material from naphtha |
| CN114100525A (en) * | 2020-09-01 | 2022-03-01 | 中国石化工程建设有限公司 | Naphtha hydrogenation device and method |
| CN115466628A (en) * | 2021-06-10 | 2022-12-13 | 中国石油化工股份有限公司 | Liquid-phase hydrogenation reaction device and system and hydrocarbon oil liquid-phase hydrogenation method |
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| CN113736516A (en) * | 2020-05-29 | 2021-12-03 | 中国石油化工股份有限公司 | Treatment process for producing ethylene raw material from naphtha |
| CN114100525A (en) * | 2020-09-01 | 2022-03-01 | 中国石化工程建设有限公司 | Naphtha hydrogenation device and method |
| CN115466628A (en) * | 2021-06-10 | 2022-12-13 | 中国石油化工股份有限公司 | Liquid-phase hydrogenation reaction device and system and hydrocarbon oil liquid-phase hydrogenation method |
| CN115466628B (en) * | 2021-06-10 | 2023-12-12 | 中国石油化工股份有限公司 | Liquid phase hydrogenation reaction device and system and hydrocarbon oil phase hydrogenation method |
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| CN102732303B (en) | 2014-07-23 |
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