CN1043051C - Process for producing a hydrowax - Google Patents
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- CN1043051C CN1043051C CN95108983A CN95108983A CN1043051C CN 1043051 C CN1043051 C CN 1043051C CN 95108983 A CN95108983 A CN 95108983A CN 95108983 A CN95108983 A CN 95108983A CN 1043051 C CN1043051 C CN 1043051C
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Abstract
Process for producing a hydrowax comprising the steps of (a) hydrocracking a blend obtained by blending at least one distillate fraction and a deasphalted oil (DAO); (b) separating from the hydrocracker effluent a fraction of which at least 90% by weight has a boiling point of 370 .degree.C or higher (the 370+ fraction); and (c) separating the 370+ fraction in a top-fraction and a bottom-fraction at an effective cutpoint below 600 .degree.C, thus yielding the hydrowax as the top-fraction. The hydrowax thus produced is a very suitable feedstock for a steam cracker for the production of ethene. The hydrowax can also be very suitably applied as a feed for the production of lubricating base oils.
Description
The present invention relates to prepare the method for hydrowax, this paraffin is very useful aspect the raw material of raw material for preparing the light alkene class as the hot steam cracker and conduct preparation lubricating base oil.
The hot steam cracking is to be used for preparing the light alkene class, especially ethene and than the currently known methods of the propylene of low degree.It is very strong endothermic process, consists essentially of hydrocarbon oil crude material is heated to sufficiently high temperature so that cracking reaction to take place, and cooling reactor ejecta fast subsequently, and this ejecta is fractionated into different products.Steam cracker also generally is called ethylene cracking device, is made up of hot-zone and cold-zone usually.The hot-zone by cracking furnace, cooling zone and the primary fractionator that is used for separating the ejecta in cracking raffinate, pot oil (Pan oil), cracked gasoil and the reacted gas form.Steam is imported into and dilutes raw material in the cracking furnace.This helps final olefins yield, and simultaneously, the steam of interpolation can also suppress the deposition of coke in this stove.Reacted gas further is separated into various the finished product in the cold-zone, and these products are pure ethylene and propylene.Generally, this sepn process is by such realization: at first will be compressed to the pressure of about 30-40 crust from the cracker of primary fractionator, and subsequently, pressurized gas will be cooled to the temperature below-100 ℃, and be separated into various pure the finished product.Also to remove gas such as carbonic acid gas and hydrogen sulfide in the cold-zone of steam cracker.In view of the strong endothermic nature of process for steam cracking, in order to make present method economically feasible, fully and efficiently heat recuperation is very important.
The well-known raw material that is used for steam cracker is the petroleum naphtha fraction that produces in Crude Oil Processing.Atmospheric gas oil is also known to be suitable cracker raw material.For example, at british patent specification No.1,537, in 822, disclose and comprised the method for preparing light alkene of the hydrogenation gas oil feedstocks being carried out steam cracking, this raw material forms by subsequent step: thermally splitting, what hydrocarbon ils residue one was suitable is normal pressure residue one, reclaims gas oil fraction and catalytic hydrogenation liquid gas oil fraction by distillation from the thermally splitting ejecta.In German patent publication No. 1,922, in 665, the process for steam cracking of preparation alkene is disclosed, wherein dearomatization gas oil is as raw material.Important consideration is when selecting raw material, except that the potential ethylene yield, also has the H/C ratio of chemical factor such as raw material, and the stability of this price on economic factors such as cost of material and the market.Other factors is as obtaining the difficulty or ease of raw material, and the investment that the collaborative potentiality of steam cracker and refinery and steam cracker and refinery combine and involved also plays a part very important when selecting proper raw material.
From the eighties since the initial stage, with the another kind of raw material of commercial size effect.At public publication A.G.Gossens, hydrocarbon processing, in November, 1986, in the 84-86 page or leaf, it is described: hydrowax, the i.e. hydrogenation residue that is made by the single phase hydrocracking of flash distillation overhead product is fit to prepare as steam cracker the raw material of ethene, and the term " flash distillation overhead product " that uses at context refers to the distillate fraction that obtains in the vacuum flashing of normal pressure residue.This publication points out that hydrowax is excellent steam cracker feed stock, particularly because it has attracting and relative constant price, olefins yield and feed naphtha approaching, and the centralized and unified realistic possibility that provides of steam cracker and refinery is provided for it.It is also pointed out in the disclosure thing, and the fouling of transfer limes heat exchanger or TLE (reclaiming high enthalpy heat here, from the hot ejecta of the stove that is used for preparing high pressure steam) is the principal element of the cycle of operation of decision steam cracker.This fouling effect it is said be since contain in the hydrowax aromatic hydroxy compound and since in the pyrolytic process in cracking furnace the tar that forms cause.Owing to hydrowax trends towards more causing the TLE fouling than normally used feed naphtha, thereby have to take specific measure to deal with this scale problems, seriously shorten working time so that be unlikely to.In this respect, the quench tube diameter among the TLE, design maximum and operation TLE temperature out all are important variable factors.
The purpose of this invention is to provide and a kind ofly prepare the method for hydrowax from the hydrocarbon ils fraction heavier than flash distillation overhead product, this hydrowax can be suitably as the raw material in the known steam cracking method for preparing light alkene (especially ethene) with commercial attracting productive rate.
The method for preparing lubricating base oil from hydrowax is known in the prior art.For example at EP-A-0, disclosed a kind of method in 272,729, wherein, the hydrocarbon feed that contains the flash distillation overhead product that makes at the residue method for transformation is by hydrocracking, and after this, the bottom fraction of cracking ejecta is that hydrowax is dewaxed.For with existing unsaturated component hydrogenation, before or after dewaxing treatment, can carry out hydrotreatment.Preferred order is at first to dewax, and material hydrotreatment then will dewax.The dewaxing step both can be solvent dewaxing, can be again catalytic dewaxing.Last step of hydrogenation has increased the amount of existing saturated component, thereby olefin hydrogenation becomes the viscosity index (VI) of the base oil that paraffinic hydrocarbons (paraffin) and isoparaffin component help finally obtaining.
At EP-A-0,280, disclose in 476 and another kind ofly prepared the appropriate method of lubricating base oil,, hydrowax has been carried out hydrotreatment through comprising as the β zeolite of acidic components and the hydrotreating catalyst of hydrogenation-dehydrogenation component (platinum is proper) according to this method from hydrowax.Subsequently, the hydrotreatment product separation is become lower boiling fraction and lubricating base oil raffinate, the latter preferably carries out the aromatic hydrocarbons extraction steps, can also carry out the hydrofining step subsequently, obtains lubricating base oil.
A further object of the invention provides the method for preparing hydrowax, and this paraffin can be very suitably as the raw material for preparing lubricating base oil.Therefore, the purpose of this invention is to provide a kind of method, be fit to do the raw material of dewaxing device or hydrotreater by the hydrowax of its preparation.
So, the present invention relates to prepare the method for hydrowax, this method may further comprise the steps:
(a) the blend hydrocracking that will obtain by at least a overhead product fraction of blending and deasphalted oil (DAO);
(b) isolate a kind of fraction from hydrocracker, at least 90% (weight) in this fraction, preferred 95% (weight) have the boiling point (370+ fraction) more than 370 ℃ or 370 ℃; With
(c) be lower than 600 ℃, the suitable effective cut point that is lower than 580 ℃ is separated into top fraction and bottom fraction with the 370+ fraction, thereby obtains the hydrowax as the top fraction.
Because heavy metal has disadvantageous effect to the activity of hydrocracking catalyst usually, the blend of DAO and overhead product fraction should have enough low heavy metal content.Therefore, the heavy metal content of the raw material of reduction hydrocracker is preferred before hydrocracking.This means or DAO with the blending of overhead product fraction before by hydrodemetallation (HDM), perhaps the blend of DAO and overhead product fraction before carrying out hydrocracking by hydrodemetallation (HDM).Implement first kind of selection, it is preferred being about to the DAO hydrodemetallation (HDM), because the heavy metal among all or nearly all blend that is present in DAO and overhead product fraction still is contained among the DAO at first, thereby, be more effective economically with the DAO hydrodemetallation (HDM).When whether determining actual needs hydrodemetallation (HDM) step, two principal elements are arranged.At first, the type of crude oil (obtaining DAO) from it, secondly, the degree of depth that diasphaltene is handled, i.e. the asphalt component degree of removing.Obtain at the crude oil that exists naturally with high level from heavy metal wherein under the situation of DAO, this DAO has high heavy metal content probably.In addition, if the diasphaltene degree of depth is darker in the diasphaltene processing, promptly have only most heavy bitumen components to be removed, so, compare with the diasphaltene raw material, DAO still contains the heavy metal of q.s.On the other hand, if this degree of depth is more shallow, promptly except the heavy bitumen component, also remove some lighter pitches, so, heavy metal content is starkly lower than the heavy metal content of diasphaltene raw material among the DAO, and need not to carry out independent demetalization step.
Very surprisingly, than heavy duty divide as the deasphalted oil of hydrodemetallation (HDM) can be used to prepare hydrowax, it is the suitable feedstock of steam cracker.Up to now, think all generally that hydrowax should only be produced from flash distillation overhead product fraction, the use that is divided by heavy duty can cause fouling too many among the TLE, thereby steam cracker is had unacceptable economically restriction working time.Have now found that, by carrying out flash distillation from flash distillation overhead product and the 370+ fraction that at random obtains the hydrocracking process of the blend of demetallated DAO under the effective cut point in 400-600 ℃ of scope, the hydrowax that divide to obtain as top stage can be well suited for the raw material as the device of the steam cracking of producing ethene and propylene, or as the dewaxing of producing lubricating base oil or the raw material of hydrotreater.
The blending ratio of overhead product fraction and DAO (it is hydrodemetallation (HDM) optionally) or weight ratio are not crucial especially, are mainly decided by the restriction of hydrocracker.Therefore, weight ratio suits at 20/80-80/20, in the preferred 40/60-70/30 scope.
The overhead product fraction and at random the blend of hydrodemetallation (HDM) DAO can carry out hydrocracking by any suitable mode well known in the prior art.In general, hydrocracking is to heat up and boosting down, carries out in the presence of hydrogen and suitable hydrocracking catalyst.Hydrocracking catalyst usually by load on carrier such as aluminum oxide, silicon oxide, silica-alumina or the zeolite, formed with one or more metals that are selected from nickel, tungsten, cobalt and molybdenum of element, oxide compound or sulphided form.The obtainable hydrocracking catalyst of many commercial sources is arranged, and they can be used for the method according to this invention suitably.For the present invention, method for hydrogen cracking can be single stage method or multistep method, and single phase method be preferred because multistep processes hydrocracking meeting causes the degree of depth hydrogenation of polyaromatic, thereby produce more poly-naphthenic.With from single phase the hydrowax that obtains of method for hydrogen cracking compare, this cycloalkanes of birdsing of the same feather flock together produces more fuel and tar and less alkene.Under the situation of single stage method, can use hydrodenitrification/fs hydrocracking catalyst stacking bed on conversion catalyst suitably.Specially suitable hydrodenitrification/fs hydrocracking catalyst is NiMo/ aluminum oxide and CoMo/ aluminum oxide, optionally promotes with phosphorus and/or fluorine.Suitable conversion catalyst comprises those catalyzer based on VI B family metal, VIII family metal and acid carrier.Promotor with the form of phosphorus (P) also can exist.The object lesson of this class catalyzer is NiW/ zeolite, NiW/ silica-alumina and NiW/ zeolite-silica-alumina.Common hydrocracking condition is, working pressure 80-250 crust, and the 100-200 crust is more suitable, and service temperature 300-500 ℃, 350-475 ℃ is more suitable.
The overhead product fraction that is used for the inventive method, or the heavy gas oil fraction that obtains from the air distillation of crude oil, or the flash distillation overhead product fraction that obtains from the vacuum flashing or the vacuum distilling of normal pressure hydrocarbon ils raffinate.For the present invention, needn't be strict with the overhead product fraction that use painstakingly defines (as obtaining), thereby preferably, this overhead product fraction is that the vacuum flashing by the lower cost of normal pressure hydrocarbon ils raffinate makes in vacuum distilling.
Used DAO can be suitably by with the residual hydrocarbon ils that heats up in a steamer, preferred vacuum (distillation) raffinate carries out diasphaltene and obtains.Diasphaltene can be carried out by any usual manner.Well-known and suitable de-asphalting method is a solvent deasphalting, and it comprises residual counter-current treatment of heating up in a steamer hydrocarbon oil crude material and extraction solvent.This extraction solvent normally contains the light hydrocarbon solvent of the paraffin compound of being with 3-8 carbon atom (as propane, butane, Trimethylmethane, pentane, iso-pentane, hexane and two or more mixture in the middle of them).Preferred alkane is to have those of 3-5 carbon atom, and butane, pentane and their mixture are most preferred.Solvent dewaxing is handled and can be used on the residual hydrocarbon oil crude material that the top enters and the extraction solvent that enters in the bottom carries out easily in rotating disc contactor or tray column.The hydrocarbon matter hydro carbons that is present in the residual hydrocarbon ils is dissolved in the extraction solvent, and discharges from the top of this device.After reclaiming extraction solvent, divide acquisition DAO from this top stage.The pitch that is insoluble to extraction solvent is discharged in bottom of device.Carrying out deasphalting various condition is known in the prior art.Suitably, be 1.5-8wt/wt at the ratio of total extraction solvent and residual hydrocarbon ils, pressure is that 1-50 crust and temperature are to carry out diasphaltene under 160-230 ℃.
The hydrodemetallation (HDM) of the blend of DAO or itself and overhead product fraction can realize by any method of hydrogenation demetalization well known in the prior art.Usually, this method comprises: in the presence of hydrogen, under high temperature and high pressure, allow raw material that desire handles upwards, or radially by one or more setting placed reactor, this reactor contains the Hydrodemetalation catalyst particulate to be fixed or moving-bed downwards.Well-known demetalization operation is warehouse flow operation (bunkerflow), fixed bed operation, fixed bed swinging operation and removable bed operation.Suitable catalyzer generally is made up of oxide carrier such as aluminum oxide, silicon oxide or silica-alumina, but on it the deposition of elements form or operate as one or more beds of metallic compound.Suitable catalyzer generally is made up of oxide carrier such as aluminum hydride, silicon oxide or silicon oxide one aluminum oxide, but on it the deposition of elements form or as the metal of VI B family or VIII family in one or more periodic table of elements of metallic compound.This type of Hydrodemetalation catalyst can obtain from many catalyzer supply merchants by commercial sources.Specially suitable catalyzer be have (as promoting agent) a kind of on alumina supporter, optionally use those catalyzer of the promoted binding substances NiMo of phosphorus (P) or CoMo.As everyone knows, the catalyzer of the above-mentioned type in fact also shows some extra activity: hydrodenitrification and/or hydrogenating desulfurization, and remove heavy hydrocarbon and boiling point is higher than 520 ℃ the hydrocarbon conversion and become low boiling component.Hydrodemetallation (HDM) is a 20-250 crust at hydrogen partial pressure normally, and temperature is 300-470 ℃, and preferred 310-440 ℃ and space velocity are 0.1-10l/l.hr, carry out under the preferred 0.2-7l/l.hr.
For the present invention, preferably, used DAO is by with the diasphaltene of vacuum hydrocarbon ils raffinate, and then optionally hydrodemetallation (HDM) makes.In general, vacuum hydrocarbon ils raffinate is that residual fraction as the vacuum distilling of normal pressure hydrocarbon ils raffinate obtains.Just as described, the overhead product fraction of using in the method according to the invention preferably also is that vacuum distilling from normal pressure hydrocarbon ils raffinate obtains.In another embodiment preferred of the present invention, this vacuum hydrocarbon ils raffinate (making DAO from it) is to obtain from same normal pressure hydrocarbon ils raffinate, as this overhead product fraction.This preferred flow process (line-up) has explanation in Fig. 1, and clearly illustrates that, when this hydrowax was used as steam cracker feed stock, the method for preparing hydrowax of the present invention provided high collaborative potentiality between refinery and steam cracker.Similarly, when the present method that will prepare hydrowax and the technical process (lin-up) of preparation lubricating base oil are centralized and unified, can recognize high collaborative potentiality.
Separating 370+ fraction (step (b)) from the hydrocracker effluent can realize by fractionation apparatus commonly used hydroeracking unit.Separation in the step (c) also can be undertaken by any currently known methods that in the prior art hydrocarbon oil crude material is separated into two or more different fractions (according to the boiling point of existing various components in this hydrocarbon oil crude material).The example of suitable separation method is included in normal pressure or decompression distillation down, as carrying out in medium vacuum flasher or molecular distillation device.Unique important parameters is effective cut point in this respect of the present invention, and promptly this temperature is represented the boiling point of the maximum boiling point component and the minimum boiling point component bottom fraction that top stage is divided.In fact this means, at least 85% (weight), preferably at least 90% (weight) and most preferably the component of the composition top fraction of at least 95% (weight) have the boiling point that is lower than effective cut point, and the component of the composition of at least 70% (weight) bottom fraction has the boiling point that is higher than effective cut point.As pointing out already, effectively cut point must be lower than 600 ℃, preferably is lower than 580 ℃.Preferred effectively cut point is higher than 400 ℃ and most preferably be higher than 450 ℃.From the viewpoint of productive rate, common preferred employing more than 500 ℃, the effective cut point more than 550 ℃ most preferably.Because, as estimation like that, low effective cut point will be a cost with the hydrowax productive rate.On the other hand, if purpose is to be that the least possible heavy hydrocarbon component is arranged, then should select low effective cut point in hydrowax.
Hydrowax obtains as the top fraction in step (c) at last, and can be directly as the raw material of steam cracker or as the raw material of the technical process of preparation lubricating base oil.The bottom fraction contains many heavy hydrocarbon compounds, and the poly-aromatic ring structure of part is arranged.In order to improve the production efficiency of hydrowax, the bottom fraction that at least a portion obtains in step (c) can be before hydrocracking and the DAO blend of any optionally hydrodemetallation (HDM).Can obtain best hydrowax productive rate from this mode.The measure that other is raised the efficiency comprises, for example, if DAO is by hydrodemetallation (HDM), with at least a portion cracking residue with or be circulated to the inlet of dewaxing device and/or the inlet of hydrodemetallation (HDM) reactor from the cracked gasoil fraction that steam cracker obtains.
Cracking prepares the raw material of light alkene and as the purposes of the raw material of preparation lubricating base oil as hot steam to the invention still further relates to the hydrowax that obtained by method of the present invention and this hydrowax.
How Fig. 1 has illustrated that the preferred embodiment with the method according to this invention is attached to refinery's one steam cracker flow process or has in the refinery of lubricating base oil production unit.
Raw material (P) enters atmospheric distillation plant (1), and here it is separated into atmospheric residue (11) and distillate fraction (cut) (10). Atmospheric residue (11) carries out vacuum flashing in vacuum flashing device (2), and is separated into one or more (vacuum) flash distillation distillate fractions (16) and vacuum residue (12). Vacuum residue (12) enters depitching district (3) and obtains bitumen fraction (14) and DAO (13) subsequently, and this DAO is HDM in HDM device (4). The DAO of HDM (15) and distillate fraction (16) connect mixed, gained blend logistics hydrocracking in hydrocracker (5). Hydrocracker effluent (17) is separated into top fraction (18) and 370+ bottom fraction (19) in fractionator (6). This 370+ fraction is separated into hydrowax (20) and bottom fraction (23) in (height) vacuum distillation plant (7), its part can with DAO (15) blending of HDM. This process dots. Hydrowax (20) is as the raw material of steam cracker (8), thereby production ethene (21). In addition, hydrowax (20) is used as the raw material of lubricating base oil production equipment (8), thereby produces lubricating base oil (21).
Further specify the present invention by the following examples.
Embodiment
Flash distillation overhead product FD and hydrodemetallation (HDM) DAO (DAO with the listed character of table I
+) with FD: the DAO+ weight ratio is carried out blending at 55: 45.By allowing DAO (, obtain with the 70%wt yield by allowing vacuum residue carry out butane deasphalting; Character is listed in the table I) in the table II, flow through common Hydrodemetalation catalyst (Ni-MoP loads on the aluminum oxide) under the condition of defined and obtain DAO
+Gained FD/DAO
+Blend carries out hydrocracking in the table II under the listed condition on common fs hydrocracking catalyst (NiMoP loads on the aluminum oxide) is in stacking bed on the special-purpose subordinate phase hydrocracking catalyst (NiW loads on amorphous silicon oxide-aluminum oxide).The hydrocracker ejecta is separated into top fraction and 370+ bottom fraction in fractionator.This 370+ fraction is separated into hydrowax (top fraction) and bottom fraction then under 570 ℃ of effective cut points in vacuum flasher.The character of hydrowax provides in the table I.
Then, allow hydrowax enter steamed cracking unit.820 ℃ of temperature, top hole pressure 2.15 crust, the stream amount of sending 49.6g/h and airshed 43.8NL/h be this steamed cracking unit of operation down.Ethylene yield is that 28.0%wt and productivity of propylene are 13.8%wt, and two weight percentage ratios all are based on the weight of raw material.
The character of table I FD, DAO and hydrowax
| FD | ?DAO | Hydrowax | |
| Carbon (%wt) | 86.1 | ?86.4 | ?85.8 |
| Hydrogen (%wt) | 12.4 | ?12.2 | ?14.2 |
| Sulphur (%wt) | 1.1 | ?1.4 | ?0.02 |
| Nitrogen (mg/kg) | 1200 | ?4200 | ?18.9 |
| ?IBP(℃) 10％wt(℃) ?30％wt(℃) 50％wt(℃) 70％wt(℃) 90％wt(℃) 96％wt(℃) | ?298 ?362 ?408 ?439 ?465 ?528 ?- | ?396 ?516 ?580 ?634 ?692 ?736 ?- | ?346 ?402 ?427 ?451 ?483 ?540 ?570 |
| ?FBP(℃) | ＞620 | ＞740 | ?616 |
The table II
Processing condition
| HDM | ?HCU | |
| Stagnation pressure (crust) is weight hourly space velocity (kg/l/h) gas flow rate (N1 H (bar) 2/ kg) temperature (℃) | 171.3 ?0.6 ?1000 ?350 | ?171.3 ?0.6 ?2000 ?389 |
Claims (15)
1. the method for preparing hydrowax comprises the following steps: the blend hydrocracking that (a) will obtain by at least a overhead product fraction of blending and deasphalted oil (DAO);
(b) isolate a kind of fraction from hydrocracker, i.e. 370+ fraction, at least 95% (weight) has the boiling point more than 370 ℃ or 370 ℃ in this fraction; With
(c) at the effective cut point that is lower than 600 ℃ the 370+ fraction is separated into top fraction and bottom fraction, thereby obtains hydrowax as the top fraction.
According to the process of claim 1 wherein DAO with the blending of overhead product fraction before by hydrodemetallation (HDM).
3. according to the method for claim 1 or 2, wherein in the blend of desiring hydrocracking the weight ratio of overhead product fraction and hydrodemetallation (HDM) DAO at random in the 20/80-80/20 scope.
4. according to the method for claim 3, wherein wt is than being 40/60-70/30.
5. according to aforementioned 1 method, wherein the overhead product fraction is that vacuum flashing by normal pressure hydrocarbon ils raffinate makes.
6. according to aforementioned 1 method, wherein DAO is by obtaining the diasphaltene of vacuum hydrocarbon ils raffinate.
7. according to the method for claim 5 and 6, wherein the vacuum hydrocarbon ils raffinate of claim 6 is that Accessory Right requires 5 the same normal pressure hydrocarbon ils raffinate as the overhead product fraction to make.
8. according to the process of claim 1 wherein that effective cut point in the step (C) is in 400-560 ℃ of scope.
9. method according to Claim 8, wherein the effective cut point in the step (C) is 450-520 ℃.
According to the process of claim 1 wherein bottom fraction that at least a portion obtains in step (C) before hydrocracking with the DAO blending of hydrodemetallation (HDM) at random.
11. the hydrowax that obtains by the method for claim 1.
12. the hydrowax of claim 11 is in that cracking prepares the purposes of the raw material of light alkene as hot steam.
13. the method for claim 1 is used for the purposes with steam cracker bonded hydrocracking refinery, in order to produce the raw material of steam cracker.
14. the hydrowax of claim 11 is as the purposes of the raw material used of preparation lubricating base oil.
15. the method for claim 1 is used for the purposes with the technical process bonded hydrocracking refinery for preparing lubricating base oil, in order to produce the raw material of this technical process.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP94202148.6 | 1994-07-22 | ||
| EP94202148 | 1994-07-22 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1116231A CN1116231A (en) | 1996-02-07 |
| CN1043051C true CN1043051C (en) | 1999-04-21 |
Family
ID=8217061
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN95108983A Expired - Fee Related CN1043051C (en) | 1994-07-22 | 1995-07-19 | Process for producing a hydrowax |
Country Status (3)
| Country | Link |
|---|---|
| CN (1) | CN1043051C (en) |
| CA (1) | CA2154313C (en) |
| DE (1) | DE69522769T2 (en) |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102041080A (en) * | 2009-10-16 | 2011-05-04 | 中国石油化工股份有限公司 | Integrated method for hydrocracking and producing ethylene cracking material |
| CN102041029B (en) * | 2009-10-21 | 2014-01-22 | 中国石油化工股份有限公司 | Comprehensive utilization method of hydrocracking tail oil |
| SG11201907036UA (en) * | 2017-02-02 | 2019-08-27 | Sabic Global Technologies Bv | A process for the preparation of a feedstock for a hydroprocessing unit and an integrated hydrotreating and steam pyrolysis process for the direct processing of a crude oil to produce olefinic and aromatic petrochemicals |
| FR3097229B1 (en) * | 2019-06-12 | 2021-06-11 | Ifp Energies Now | OLEFINS PRODUCTION PROCESS INCLUDING HYDROTREATMENT, DESASPHALTING, HYDROCRACKING AND VAPOCRAQUAGE |
| FR3098824B1 (en) * | 2019-07-17 | 2021-09-03 | Ifp Energies Now | OLEFIN PRODUCTION PROCESS INCLUDING HYDROTREATMENT, DESASPHALTING, HYDROCRACKING AND VAPOCRAQUAGE |
| FR3101637B1 (en) * | 2019-10-07 | 2021-10-22 | Ifp Energies Now | OLEFINS PRODUCTION PROCESS INCLUDING DESASPHALTING, HYDROCONVERSION, HYDROCRAQUAGE AND VAPOCRAQUAGE |
| FR3102772B1 (en) * | 2019-11-06 | 2021-12-03 | Ifp Energies Now | OLEFINS PRODUCTION PROCESS INCLUDING DESASPHALTING, HYDROCRACKING AND VAPOCRAQUAGE |
| CN113546638A (en) * | 2020-04-26 | 2021-10-26 | 中国石油天然气股份有限公司 | Paraffin hydrogenation catalyst and preparation method thereof |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0027279A1 (en) * | 1977-06-20 | 1981-04-22 | H.Lundbeck & Co., A/S | Isoxazolo(5,4-C)pyridines |
| US4640762A (en) * | 1985-06-28 | 1987-02-03 | Gulf Canada Corporation | Process for improving the yield of distillables in hydrogen donor diluent cracking |
| EP0309621A1 (en) * | 1987-09-28 | 1989-04-05 | Uop | Control of polynuclear aromatic by-products in a hydrocracking process |
| CN1043154A (en) * | 1988-12-02 | 1990-06-20 | 鲁姆斯·克雷斯特公司 | In evaporation heavy hydrocarbon process, suppress the method that burnt matter forms |
-
1995
- 1995-07-19 CN CN95108983A patent/CN1043051C/en not_active Expired - Fee Related
- 1995-07-20 CA CA 2154313 patent/CA2154313C/en not_active Expired - Fee Related
- 1995-07-21 DE DE1995622769 patent/DE69522769T2/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0027279A1 (en) * | 1977-06-20 | 1981-04-22 | H.Lundbeck & Co., A/S | Isoxazolo(5,4-C)pyridines |
| US4640762A (en) * | 1985-06-28 | 1987-02-03 | Gulf Canada Corporation | Process for improving the yield of distillables in hydrogen donor diluent cracking |
| EP0309621A1 (en) * | 1987-09-28 | 1989-04-05 | Uop | Control of polynuclear aromatic by-products in a hydrocracking process |
| CN1043154A (en) * | 1988-12-02 | 1990-06-20 | 鲁姆斯·克雷斯特公司 | In evaporation heavy hydrocarbon process, suppress the method that burnt matter forms |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1116231A (en) | 1996-02-07 |
| DE69522769T2 (en) | 2002-07-04 |
| CA2154313C (en) | 2007-02-13 |
| CA2154313A1 (en) | 1996-01-23 |
| DE69522769D1 (en) | 2001-10-25 |
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