CN100371423C - Hydrocarbons hydrocracking method - Google Patents
Hydrocarbons hydrocracking method Download PDFInfo
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- CN100371423C CN100371423C CNB2006101069921A CN200610106992A CN100371423C CN 100371423 C CN100371423 C CN 100371423C CN B2006101069921 A CNB2006101069921 A CN B2006101069921A CN 200610106992 A CN200610106992 A CN 200610106992A CN 100371423 C CN100371423 C CN 100371423C
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- 238000004517 catalytic hydrocracking Methods 0.000 title claims description 54
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a hydrogenation cracking method of hydrocarbon, which consists of first reactor and second reactor, wherein the first reactor is refined hydrogen reactor or hydrogenation refining and hydrogenation cracking reactor; the second reactor is hydrogenation cracking reactor; the crude oil and flow material from second reactor enters in the first reactor with hydrogen to do hydrogenation refining reaction or hydrogenation refining and hydrogenation cracking reaction; the effluent from the first reactor is separated to obtain circulated hydrogen, object product and non-conversing oil; all or partial non-conversing oil can be circulating oil in the second reactor with hydrogen, which proceeds hydrogenation cracking reaction; the effluent from the second reactor enters in the first reactor; the composite hydrogen can be new hydrogen to supplement, which mixes gas with circulating hydrogen.
Description
Technical field
The invention belongs to the refining of petroleum field, relate to a kind of hydrocarbons hydrocracking method.
Background technology
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 adopts light, the heavy gas oil of fixed-bed reactor processing more at present.Generally, can be divided into single-stage hydrocracking and two-stage hydrocracking according to its technical process, in the high-pressure hydrocracking device that China has gone into operation, the main technique flow process adopts single hop once by flow process, unconverted oil part circulation process or recycle to extinction flow process more.The single hop circulation process refers to when outside nothing is utilized the unconverted oil demand, all unconverted oil are boosted and are looped back reactor, as required, capable of circulation to the first reactor inlet (hydrofining reactor, or be filled with the reactor of Hydrobon catalyst and hydrocracking catalyst), also capable of circulationly enter the mouth to second reactor (hydrocracking reactor).But single hop part circulation process refers to unconverted oil part discharger, and part loops back reactor and further transforms.
Hydrocracking process adopts the consecutive reaction flow process usually, and promptly raw material contacts with Hydrobon catalyst earlier and carries out hydrofining reaction, and reaction effluent contacts with hydrocracking catalyst and carries out hydrocracking reaction.
Chinese patent CN02144960.0 discloses a kind of once by " trans " hydrocracking process, be mainly used in and handle the heavy crude hydrocarbon feed, the high-quality tail oil of producing the cleaning intermediate oil and being used for the downstream unit charging, its major technique feature is a refining flow after the first cracking of employing, before hydrocracking reactor placed hydrofining reactor, fresh feed carries out hydrocracking reaction earlier, carries out hydrofining reaction again.
Chinese patent CN02144957.0 discloses a kind of " trans " circulation cracking hydrocracking method, be mainly used in and handle the heavy crude hydrocarbon feed, production high-quality intermediate oil, its major technique feature is a refining flow after the first cracking of employing, before hydrocracking reactor placed hydrofining reactor, before unconverted oil is recycled to cracking case, together carry out hydrocracking reaction earlier, carry out hydrofining reaction again with fresh feed.
Above-mentioned " trans " hydrocracking flow process, all exist fresh feed directly to carry out hydrocracking reaction without treating process, make hydrocracking catalyst be subject to the murder by poisoning of nitrogen in the raw material and the shortcoming of inactivation, so its used hydrocracking catalyst need use special high anti-nitrogen type catalyzer.
Summary of the invention
The deficiency of existing in order to overcome " trans " hydrocracking process the invention provides a kind of novel hydrogenation cracking method, and having does not have particular requirement to hydrocracking catalyst, characteristics such as while hydrogen consumption is low, reasonable energy utilization.
The technical solution used in the present invention is:
A kind of hydrocarbons hydrocracking method, comprise first reactor and second reactor, described first reactor is hydrofining reactor or hydrofining and hydrocracking reactor, second reactor is a hydrocracking reactor, it is characterized in that: stock oil, second reactor effluent and mixing hydrogen enter first reactor together, carry out hydrofining reaction, or carry out hydrofining and hydrocracking reaction; First reactor effluent is separated, separate the acquisition thing and comprise circulating hydrogen, purpose product and unconverted oil, unconverted oil is all or part of to enter second reactor as turning oil with mixing hydrogen, carry out hydrocracking reaction, second reactor effluent enters first reactor as mentioned above, and described mixing hydrogen is the additional new hydrogen and the mixed gas of circulating hydrogen.
According to the present invention, it is further characterized in that the high pressure hot separator flow process is adopted in the separation of first reactor effluent, promptly first reactor effluent advances high pressure hot separator and carries out gas, liquid and separate, the high pressure hot separator gas phase enters cold high pressure separator and carries out gas, liquid separation, the cold high pressure separator gas phase is a hydrogen-rich gas, after the desulfurization of desulphurization of recycle hydrogen system is handled, advancing circulating hydrogen compressor boosts, gas after boosting is as circulating hydrogen, circulating hydrogen is mixed into new hydrogen and mixes hydrogen, mixes hydrogen and enters first reactor and second reactor; Enter thermal low-pressure separators after the decompression of high pressure hot separator liquid phase and carry out low pressure gas, liquid separation, the thermal low-pressure separators gas phase is advanced the cold low separator and is carried out gas, liquid separation once more, and the thermal low-pressure separators liquid phase is advanced the fractionation part; The cold high pressure separator liquid phase also enters the cold low separator after decompression; Cold low separator gas phase is a hydrogen-rich gas, can advance the hydrogen recovery unit recover hydrogen or the pneumatic transmission that acts as a fuel goes out device, and the cold low separator liquid phase is advanced the fractionation part.
According to the present invention, can before first reactor and second reactor, establish two-in-one process furnace, the mixing hydrogen feed before the reaction feed before first reactor (can be to mix hydrogen or stock oil and the mixture flow of mixing hydrogen) and second reactor is heated.Two-in-one process furnace can adopt the pattern of shared radiation chamber and convection zone, also can adopt the pattern of establishing radiation chamber, shared convection zone respectively.
According to the present invention, the low-voltage variation system can before entering second reactor, turning oil be set.Described low-voltage variation system can be the guard reactor that is filled with the deferrization guard catalyst, also can be the adsorption tanks that are filled with sorbent material, can also adopt at above-mentioned adsorption tanks of above-mentioned guard reactor upstream series connection.
According to the present invention, also can utilize the temperature and pressure condition of high pressure hot separator to make high pressure hot separator upper gaseous phase logistics generation refining reaction at above-mentioned high pressure hot separator top filling catalyst for refining, components such as diesel oil are made with extra care.
According to the present invention, also can utilize the temperature and pressure condition of thermal low-pressure separators to make thermal low-pressure separators upper gaseous phase logistics generation refining reaction at thermal low-pressure separators top filling catalyst for refining, components such as gasoline, kerosene are made with extra care.
According to the present invention, also can advance the refining reaction device is set between the cold high pressure separator in the high pressure hot separator gas phase, the high pressure hot separator gas phase is made with extra care.
The inventive method compared with prior art has following beneficial effect: at first, enter the turning oil that is of second reactor, rather than fresh feed oil, because nitrogen etc. has removed to the virulent material major part of catalyzer in the turning oil, therefore the hydrocracking catalyst to second reactor does not have special high anti-nitrogen requirement, can adopt conventional hydrocracking catalyst.Second, the product of production purpose to greatest extent, because the second reactor individual curing turning oil, make that the air speed of turning oil hydrogenation reaction is relatively low, can strengthen the degree of depth of reaction, promote the turning oil drastic cracking, increase the yield of light oil, middle wet goods purpose product, thereby increase economic efficiency; The 3rd, can effectively utilize heat, proportioning according to catalyzer, the cracking reaction that second reactor takes place belongs to drastic cracking, emit a large amount of heat, this heat all takes first reactor to by second reactor effluent, the reaction that while first reactor carries out is shallow degree cracking, exothermic heat of reaction is few, second reactor effluent all enters first reactor in addition, logistics capacity increases, and temperature rise reduces relatively, can reduce the cold hydrogen consumption of the control second reactor temperature rise, such result is that the load of reactive moieties process furnace reduces, the load of circulating hydrogen compressor reduces, promptly effectively reduce the once investment of key equipments such as process furnace and compressor, simultaneously because the minimizing of fuel gas consumption and the reduction of compressor power also make process cost reduce synchronously; The 4th, hydrogen consumption reduces relatively, and this reaction process can be realized the product of production purpose to greatest extent, also can avoid the secondary cracking of existing order and inverted sequence flow process fresh feed simultaneously effectively, thereby reduce chemical hydrogen consumption and improved liquid yield, reach the purpose of increasing economic efficiency.
The further effect of the present invention also is:
Adopt two-in-one stove to solve the existing all disadvantages of flow process of a Reaktionsofen of available technology adopting, greatly reduce device with respect to the flow process of two Reaktionsofens simultaneously and once invest.If a process furnace that is used to heat first reactor feed only is set, then the required reaction potential temperature of second reactor only can obtain by heat exchange, can't be effectively guaranteed, in addition, sulfuration intensification at sulfurating stage second reactor catalyst that goes into operation does not have direct approach, after can only relying on first reactor and heating up by process furnace, effluent separates through high pressure, the a series of sepn process of fractionation part is passed through in the low pressure separation again, realize the purpose of intensification at last by the temperature of tail oil, not only to expend a large amount of time more, the loss vulcanizing agent, corrosion fractionation equipment component, pipeline, and cure efficiency can not be guaranteed.Adopt two chargings that process furnace heats two reactors respectively,, need to increase a large amount of expenses though can solve the above problems.In this case, adopt two-in-one process furnace, can in investment and operation, obtain preferably and take into account and balance.According to practical situation, two-in-one process furnace can adopt the pattern of shared radiation chamber and convection zone, also can adopt to set up radiation chamber, shared convection zone isotype.
When the low-voltage variation system being set at second reactor, can the implement device long-term operation.The major reason that iron ion causes beds to stop up often, inevitably contain a large amount of iron ions in the turning oil, very easily form " discus " and cause device to be forced to shut-down left-falling stroke head, have a strong impact on ordinary production at its second reactor head beds that returns.Guard reactor is set before turning oil boosts, filling deferrization protective material, can be more satisfactory address this problem.The tourie of sorbent material is equipped with in setting, adsorbs at condensed-nuclei aromatics in the turning oil, can avoid the accumulation of condensed-nuclei aromatics in working cycle, also the device long-term operation is had positive meaning.
When the catalyst for refining bed being set at the high-pressure separator top, the purpose that can realize producing sweet gasoline, no sulfur diesel.Along with the lasting upgrading of society, to produce the problem that the celebrated hydrogenation unit of oil product also begins to face quality product that cleans to cleaning oil product demand.On conventional hydroeracking unit, only the upgrading by catalyzer reaches the purpose that satisfies product requirement, change more and more difficult, and cost is also more and more higher.In thermoanalysis journey of the present invention, reaction effluent separates in high pressure hot separator first, hydrogen, lighter hydrocarbons, light oil even middle oil ingredient are told by the high pressure hot separator top under certain temperature, pressure, by the catalyst for refining bed being set, just can realize the hydrofining of this part oil product at its top.The temperature and pressure condition of high pressure hot separator, can not only realize the purpose of petroleum naphtha, diesel deep desulfurization, under the condition higher relatively at a kind of like this pressure simultaneously, that temperature is relatively low, more help the saturated of aromatic hydrocarbons, thereby satisfy the requirement of high standard diesel oil.
Equally, when the catalyst for refining bed being set, utilize the temperature and pressure condition of thermal low-pressure separators, also can play components such as gasoline, kerosene are carried out the purified purpose on thermal low-pressure separators top.
When having in other oil or light oil to make with extra care in the refinery, also can utilize the catalyst for refining bed that is provided with in high pressure hot separator or the thermal low-pressure separators to realize uniting refining.Introduce high pressure hot separator as installing outer diesel oil distillate, issue the reaction of production of sperm system, produce high-quality diesel oil at higher pressure and suitable air speed; Gasoline, kerosene(oil)fraction that device is outer are introduced thermal low-pressure separators, issue the reaction of production of sperm system at lower pressure and suitable air speed, produce high-quality gasoline and kerosene.This associating purified method with set up light oil separately or middle oil refining device is compared, have remarkable advantages, not only significantly cut down plant investment, and significantly reduced process cost, significantly reduce plant area simultaneously.According to practical situation, also can be chosen in the high pressure hot separator gaseous phase outlet diesel refining reactor is set separately, satisfy higher processing request.
Description of drawings
Fig. 1: first kind of typical flowchart of the present invention;
Fig. 2: second kind of typical flowchart of the present invention;
Fig. 3: the third typical flowchart of the present invention;
Fig. 4: the 4th kind of typical flowchart of the present invention;
Fig. 5: the 5th kind of typical flowchart of the present invention;
Fig. 6: the 6th kind of typical flowchart of the present invention.
Among the figure: 1-first reactor; 2-second reactor; the 3-second hydrogen process furnace; the 4-high pressure hot separator; the 5-cold high pressure separator; the 6-thermal low-pressure separators; 7-cold low separator; 8-fractionation part; 9 first hydrogen process furnace; 10-desulphurization of recycle hydrogen system; the 11-circulating hydrogen compressor; the 12-circulating oil pump; 13-stock oil; the new hydrogen of 14-; 15-mixing hydrogen; the two-in-one process furnace of 16-; 17-low-voltage variation reactor; 18-second reactor effluent; 19-first reactor effluent; 20-high pressure hot separator gas phase; 21-cold high pressure separator gas phase; the 22-circulating hydrogen; 23-high pressure hot separator liquid phase; 24-thermal low-pressure separators gas phase; 25-thermal low-pressure separators liquid phase; 26-cold low separator liquid phase; 27-cold high pressure separator liquid phase; the 28-unconverted oil; the 29-adsorption tanks; 30-turning oil; the 31-liquefied gas; the 32-petroleum naphtha; the 33-coal that navigates; 34-diesel oil; 35-cold low separator gas phase; 36-needs refined diesel oil; 37-need make with extra care light oil distillate; 38-diesel refining reactor.
Embodiment
Below in conjunction with accompanying drawing technical solution of the present invention is elaborated, accompanying drawing just in order to illustrate that substance of the present invention draws, not delimit the scope of the invention.
As shown in Figure 1, stock oil 13 accesss to plant, through with 19 heat exchange of first reactor effluent after, mix hydrogen 15 and second reactor effluent 18 is mixed into first reactor 1 with following, first reactor 1 is operated first reactor, 1 filling Hydrobon catalyst or top filling Hydrobon catalyst bottom filling hydrocracking catalyst usually under the condition of 350～450 ℃ of pressure 14.0～18.0MPa, temperature.Turning oil 30 through with 19 heat exchange of first reactor effluent after be mixed into second reactor 2 with the following hydrogen 15 that mixes, second reactor 2 is operated second reactor, 2 filling hydrocracking catalysts usually under the condition of 350～450 ℃ of pressure 14.0～18.0MPa, temperature.Mix hydrogen 15 and successively with after high pressure hot separator gas phase 20 and 19 heat exchange of first reactor effluent be divided into two-way, one the tunnel is mixed into first reactor 1 with the stock oil 13 and second reactor effluent 18 after 9 heating of the first hydrogen process furnace, another road is mixed into second reactor 2 with turning oil 30 after 3 heating of the second hydrogen process furnace.Stock oil 13 also can be before the first hydrogen process furnace 9 earlier with mixes hydrogen 15 mixing after the first hydrogen process furnace 9 is mixed into first reactor 1 with second reactor effluent 18 after heating again.
The present invention shown in Figure 1 is flow processs that the present invention recommends to the separation method of first reactor effluent 19, is the sophisticated hot high score flow process in this area.Certainly, those skilled in the art can select other separation method commonly used as required, as cold high score flow process etc., this present invention are not added restriction.
Method for hydrogen cracking of the present invention, handled stock oil is existing hydroeracking unit stock oil commonly used, as boiling range is 200-600 ℃ heavy crude hydrocarbon material, can be gas oil, vacuum distillate, deasphalted oil, catalytic cracking turning oil, shale oil, coal tar wet goods.The cut point of unconverted oil can be controlled at about 350 ℃ or be higher, and per pass conversion can be controlled at 40-80 weight %.
The operational condition of the inventive method is identical with conventional hydrocracking process, and the technician can be according to the difference of feedstock property, and the operational condition to each equipment of the present invention when technological design is optimized, and this is the normal means that adopt in this area.And can on experiment or mimic basis, adjust according to feedstock property, product requirement etc.
The Hydrobon catalyst that the present invention relates to can adopt common non-precious metal catalyst, and promptly metal component is group vib metal (mainly comprising tungsten or molybdenum) and VIII family metal (mainly comprising cobalt and nickel).Hydrocracking catalyst can adopt the molecular sieve type hydrocracking catalyst, also can be amorphously to mix the molecular sieve type hydrocracking catalyst, or the amorphous type catalyzer.The filling proportioning of Hydrobon catalyst and hydrocracking catalyst in first reactor 1 and second reactor 2 can decide according to the character of raw material and purpose product, and this also is the known technology of this area, and the present invention does not add restriction to this.
As shown in Figure 1, what enter second reactor 2 (hydrocracking reactor) is turning oil 30, rather than as fresh feed oil of the prior art, because turning oil has passed through hydrofining reaction and has removed most of to the virulent material of catalyzer, as nitrogen, heavy metal etc., therefore the hydrocracking catalyst in second reactor 2 is not just had special high anti-nitrogen requirement, can adopt conventional hydrocracking catalyst.
As shown in Figure 1, because second reactor, 2 individual curing turning oils 30, second reactor, 2 raw material oil masses to be processed are much smaller in the relative prior art of the amount of turning oil 30, this makes that the air speed of hydrogenation reaction is relatively low in second reactor 2, can strengthen the degree of depth of reaction, promote turning oil 30 drastic crackings, increase the yield of light oil, middle wet goods purpose product, thereby increase economic efficiency.On the other hand, the cracking reaction that second reactor 2 takes place belongs to drastic cracking, emit a large amount of heat, this heat all takes first reactor 1 to by second reactor effluent 18, the reaction that while first reactor 1 carries out is shallow degree cracking, exothermic heat of reaction is few, second reactor effluent 18 all enters first reactor 1 in addition, logistics capacity increases, this makes 2 temperature rises of second reactor reduce relatively, can reduce the cold hydrogen consumption of the control second reactor temperature rise, can reduce the load of reactive moieties process furnace so on the one hand, can reduce the load of circulating hydrogen compressor on the other hand, promptly effectively reduce the once investment of key equipments such as process furnace and compressor, simultaneously because the minimizing of fuel gas consumption and the reduction of compressor power make that also process cost reduces synchronously.
As shown in Figure 1, stock oil of the present invention is only handled through first reactor 1, compares with the inverted sequence flow process with existing order, can avoid the secondary cracking of stock oil effectively, thereby reduces chemical hydrogen consumption and improve liquid yield.
The difference of the inventive method shown in Figure 2 and the inventive method shown in Figure 1 only is: the first hydrogen process furnace 9 and the second hydrogen process furnace 3 are merged the two-in-one process furnace 16 of formation.As shown in Figure 2, mix hydrogen 15 and successively with after high pressure hot separator gas phase 20 and 19 heat exchange of first reactor effluent be divided into two-way, one the tunnel is mixed into first reactor 1 with the stock oil 13 and second reactor effluent 18 after two-in-one process furnace 16 heating, another road is mixed into second reactor 2 with turning oil 30 after two-in-one process furnace 16 heating.Certainly, stock oil 13 also can be before two-in-one process furnace 16 earlier with mixes hydrogen 15 mixing after two-in-one process furnace 16 is mixed into first reactor 1 with second reactor effluent 18 after heating again.According to circumstances, two-in-one process furnace 16 can adopt the pattern of shared radiation chamber and convection zone, also can adopt to set up radiation chamber, shared convection zone isotype.
The difference of the inventive method shown in Figure 3 and the inventive method shown in Figure 2 only is: low-voltage variation reactor 17 is set as the low-voltage variation system before circulating oil pump 12.As shown in Figure 2, unconverted oil 28 all at first enters low-voltage variation reactor 17 as turning oil 30, again after circulating oil pump 12 boosts, and mixes hydrogen 15 and is mixed into second reactor 2 and carries out cracking reaction.Guard reactor 17 can load the deferrization catalyzer, as industrial FZC commonly used series protective material etc.
The inventive method shown in Figure 4 is identical with the inventive method major part shown in Figure 3, and difference is: at high pressure hot separator 4 tops filling catalyst for refining, adsorption tanks 29 are set as the low-voltage variation system before circulating oil pump 12.As shown in Figure 4, first reactor effluent 19 carries out gas, liquid separation through the laggard high pressure hot separator 4 of heat exchange, high pressure hot separator gas phase 20 is the mixture of hydrogen and small molecules hydro carbons and light oil, the catalyst for refining bed that passes through to be arranged on the high pressure hot separator top from the bottom to top, carry out deep desulfuration and take off arylation reaction, leave high pressure hot separator 4 after the reaction.As shown in Figure 4, can also enter high pressure hot separator 4 with first reactor effluent 19, carry out deep desulfuration and take off arylation reaction, reach purpose diesel refining at the external need refined diesel oil 36 of high pressure hot separator 4 upstream introducing devices.As required, described high pressure hot separator 4 tops filling catalyst for refining can be conventional catalyst for refining or ultra-deep desulfurization catalyst for refining etc.
Among Fig. 4, the low-voltage variation system is adsorption tanks 29, and adsorption tanks 29 can load conventional porous adsorbing material as sorbent material, as porcelain ball, resin, coconut husk etc.
The inventive method shown in Figure 5 is identical with the inventive method major part shown in Figure 4, and difference is: at thermal low-pressure separators 6 tops filling catalyst for refining, low-voltage variation reactor 17 and adsorption tanks 29 are set simultaneously as the low-voltage variation system before circulating oil pump 12.
As shown in Figure 5, at thermal low-pressure separators 6 tops filling catalyst for refining, high pressure hot separator liquid phase 23 enters thermal low-pressure separators 6 and carries out gas, liquid separation, thermal low-pressure separators gas phase 24 is the mixture of hydrogen and small molecules hydro carbons and light oil, the catalyst for refining bed that passes through to be arranged on the thermal low-pressure separators top from the bottom to top, carry out desulfurization and take off arylation reaction, leave thermal low-pressure separators 6 after the reaction.As shown in Figure 5, can also heat up in a steamer as gasoline, kerosene at the refining light oil distillate 37 of the external need of thermal low-pressure separators 6 upstream introducing devices, together enter thermal low-pressure separators 6 with high pressure hot separator liquid phase 23, carry out desulfurization and take off arylation reaction, reach the purpose of producing purified product.Described thermal low-pressure separators 6 tops filling catalyst for refining can be conventional catalyst for refining or ultra-deep desulfurization catalyst for refining etc.
The inventive method shown in Figure 6 is identical with the inventive method major part shown in Figure 5, and difference is: on high pressure hot separator 4 tops the catalyst for refining bed is not set, and in 20 outlets of high pressure hot separator gas phase diesel refining reactor 38 is set separately.As shown in Figure 6, first reactor effluent 19 carries out gas, liquid separation through the laggard high pressure hot separator 4 of heat exchange, the outer need refined diesel oil of introducing 36 of device and high pressure hot separator gas phase 20 together from top to bottom pass through refining reaction device 38, carry out deep desulfuration and take off arylation reaction, refining reaction device 38 is left in reacted logistics 20, enters cold high pressure separator 5 after heat exchange and cooling.Diesel refining reactor 38 is set separately can be issued to the refining requirement higher not influencing high pressure hot separator 4 structures and operational condition diesel oil.
Claims (10)
1. hydrocarbons hydrocracking method, comprise first reactor (1) and second reactor (2), first reactor (1) is hydrofining reactor or hydrofining and hydrocracking reactor, second reactor (2) is a hydrocracking reactor, it is characterized in that: stock oil (13), second reactor effluent (18) and mixing hydrogen (15) enter first reactor (1) together, carry out hydrofining reaction, or carry out hydrofining and hydrocracking reaction; First reactor effluent (19) is separated, separate the acquisition thing and comprise circulating hydrogen (22), purpose product and unconverted oil (28), unconverted oil (28) is all or part of to enter second reactor (2) as turning oil (30) with mixing hydrogen (15), carry out hydrocracking reaction, second reactor effluent (18) enters first reactor (1) as mentioned above, and described mixing hydrogen (15) is the additional new hydrogen (14) and the mixed gas of circulating hydrogen (22).
2. hydrocarbons hydrocracking method according to claim 1, it is characterized in that the separation method of described first reactor effluent (19) being: first reactor effluent (19) advances high pressure hot separator (4) and carries out gas, liquid separates, high pressure hot separator gas phase (20) enters cold high pressure separator (5) and carries out gas, liquid separates, cold high pressure separator gas phase (21) is a hydrogen-rich gas, after desulphurization of recycle hydrogen system (10) desulfurization is handled, advancing circulating hydrogen compressor liter (11) presses, gas after boosting is as circulating hydrogen (22), circulating hydrogen (22) is mixed into new hydrogen (14) and mixes hydrogen (15), mixes hydrogen (15) and enters first reactor (1) and second reactor (2); Enter thermal low-pressure separators (6) after high pressure hot separator liquid phase (23) decompression and carry out low pressure gas, liquid separation, thermal low-pressure separators gas phase (24) is advanced cold low separator (7) and is carried out gas, liquid separation once more, and thermal low-pressure separators liquid phase (25) is advanced fractionation part (8); Cold high pressure separator liquid phase (27) also enters cold low separator (7) after decompression; Cold low separator gas phase (35) is a hydrogen-rich gas, advances the hydrogen recovery unit recover hydrogen or the pneumatic transmission that acts as a fuel goes out device, and cold low separator liquid phase (26) is advanced fractionation part (8).
3. hydrocarbons hydrocracking method according to claim 1 and 2, it is characterized in that: at described first reactor (1) and the preceding two-in-one process furnace (16) of establishing of second reactor (2), described two-in-one process furnace (16) heats the preceding mixing hydrogen of first reactor (1) (15) or stock oil (13) and the mixture that mixes hydrogen (15) and the preceding mixing hydrogen (15) of second reactor (2).
4. hydrocarbons hydrocracking method according to claim 1 and 2 is characterized in that: enter preceding low-voltage variation reactor (17) and/or the adsorption tanks (29) of being provided with of second reactor (2) at described turning oil (30).
5. hydrocarbons hydrocracking method according to claim 3 is characterized in that: enter preceding low-voltage variation reactor (17) and/or the adsorption tanks (29) of being provided with of second reactor (2) at described turning oil (30).
6. hydrocarbons hydrocracking method according to claim 2 is characterized in that: at described high pressure hot separator (4) top filling catalyst for refining.
7. hydrocarbons hydrocracking method according to claim 2 is characterized in that: in 20 outlets of described high pressure hot separator (4) gas phase diesel refining reactor (38) is set.
8. hydrocarbons hydrocracking method according to claim 2 is characterized in that: at described thermal low-pressure separators (6) top filling catalyst for refining.
9. according to claim 6 or 7 described hydrocarbons hydrocracking methods, it is characterized in that: at described thermal low-pressure separators (6) top filling catalyst for refining.
10. hydrocarbons hydrocracking method according to claim 9; it is characterized in that: at described first reactor (1) and the preceding two-in-one process furnace (16) of establishing of second reactor (2); described two-in-one process furnace (16) heats the preceding mixing hydrogen of first reactor (1) (15) or stock oil (13) and the mixture that mixes hydrogen (15) and the preceding mixing hydrogen (15) of second reactor (2), enters preceding low-voltage variation reactor (17) and/or the adsorption tanks (29) of being provided with of second reactor (2) at described turning oil (30).
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| CN101348235B (en) * | 2007-07-19 | 2013-08-07 | 中国石油化工集团公司 | Hydrogen recovery method for hydrogenation plant |
| CN101250434B (en) * | 2008-03-31 | 2011-12-14 | 中国石油化工集团公司 | Hydrocarbons hydrogenation conversion method |
| CN101250435B (en) * | 2008-03-31 | 2011-07-20 | 中国石油化工集团公司 | Hydrocarbons hydrogenation conversion method |
| CN102234540B (en) * | 2010-05-07 | 2013-09-11 | 中国石油化工集团公司 | Hydrogenation method and apparatus for center fractions of pyrolysis gasoline |
| US8540871B2 (en) * | 2010-07-30 | 2013-09-24 | Chevron U.S.A. Inc. | Denitrification of a hydrocarbon feed |
| CN102863985A (en) * | 2011-07-07 | 2013-01-09 | 中国石油化工股份有限公司 | Combined hydrogenation method |
| CN103102962B (en) * | 2011-11-10 | 2015-02-18 | 中国石油化工股份有限公司 | Heating furnace rear-positioned poor quality gasoline distillate series connection hydrotreating method |
| CN103421537B (en) * | 2012-05-15 | 2015-02-25 | 中国石油天然气股份有限公司 | Hydrogenation process method for ensuring heavy naphtha to meet reforming feed requirement |
| CN103725306B (en) * | 2012-10-10 | 2017-06-06 | 中国石油化工集团公司 | The separation method and device of reforming reaction product |
| CN103725313B (en) * | 2012-10-10 | 2017-07-07 | 中国石油化工集团公司 | The B-grade condensation separation method and device of catalytic reforming pre-hydrotreating reaction product |
| US9139783B2 (en) * | 2012-11-06 | 2015-09-22 | E I Du Pont Nemours And Company | Hydroprocessing light cycle oil in liquid-full reactors |
| US9617485B2 (en) * | 2013-09-24 | 2017-04-11 | E I Du Pont De Nemours And Company | Gas oil hydroprocess |
| US10160923B2 (en) * | 2014-11-05 | 2018-12-25 | Uop Llc | Processes for maximizing high quality distillate |
| CN113831935B (en) * | 2020-06-23 | 2023-04-14 | 中国石油化工股份有限公司 | Hydrocracking device |
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