• 专利附录
  • 专利说明
  • 权利要求
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    • 专利摘要:
    An asphaltene-containing oil hydrodesulfurization process employing stages in series with an interstage flashing step. The second stage catalyst comprises supported Group VI and Group VIII metals together with a promoting amount of Group IV-B metal. The first stage catalyst comprises supported Group VI and Group VIII metals without promotion with Group IV-B metal.
    公开号:SU736874A3
    申请号:SU762327451
    申请日:1976-03-02
    公开日:1980-05-25
    发明作者:Альберт Фраейр Джеймс；Эмиль Хилдебранд Ричард；Анджело Параскос Джон
    申请人:Галф Рисерч Энд Дивелопмент Компани (Фирма)；
    IPC主号:
    专利说明:

    (54) METHOD FOR CONSIDERATION OF ASPHALTEN METAL CONTAINING OIL RAW MATERIALS
    one
    The invention relates to methods for desulfurizing asphaltene metal-containing crude oil and may be used in the petroleum refining industry.
    Methods are known for desulfurizing asphaltene metal-containing oil feedstock by contacting the feedstock with hydrogen in the presence of a catalyst at elevated temperature and pressure 1.
    The closest to the proposed method is the desulfurization of asphaltene metal-containing oil feedstock in two stages by contacting the feedstock with hydrogen in the presence of a catalyst containing metals of groups VI and VIII on a non-cracking carrier with interstage removal of contaminant gases 2. Pressure (70 kg / cm and above) and the temperature (343-427 ° C) is the same at the process steps.
     To compensate for the loss of activity of the catalyst due to the duration of its operation in the process flow, a gradual rise in temperature is carried out (in steps).
    However, in order to carry out the process effectively, it is necessary that the catalyst
    SaSre; ™ S
    The second stage had a higher content of metals of groups VI and VIII than the catalyst of the first stage.
    The hydrogen pressure in the second stage is slightly lower than the initial pressure.
    The aim of the invention is to increase the efficiency of the process.
    This goal is achieved by the described method of desulfurizing asphaltene metal-containing raw materials in two steps by contacting the raw material with hydrogen at elevated temperature and pressure in the presence of a catalyst containing metals of groups VI and VIII on a non-cracking carrier with interstage stage. by flue gases, in which a catalyst promoted with 1–10% w / v of titanium is used as a catalyst of the second stage.
    Preferably the process is carried out at a temperature of 316-482 ° C and a pressure of 70-20 350 kg / cm 2.
    Distinctive features of the method consist in the use of a catalyst promoted with 1 to 10 wt.% Of titanium in the second stage, as well as carrying out the process with
    . ,, iys-ii.iWte4.V, .3 temperature 316-482 ° С and pressure of 70 - 350 kg / cm2. In the proposed method, the first stage uses a catalyst containing 1 VI metals and VI and VIII groups on a non-cracking carrier. Such combinations of metals of the VI and VIII groups, such as cobalt-molybdenum, nickel-tungsten and nickel-molybdenum, are used. The preferred combination is nickel-cobalt-molybdenum. The catalyst, as a rule, contains 5-30 wt.% Of metals of the VI and VIII groups, preferably 8-20 wt.% - The rest of the catalyst consists of highly porous, non-cracking support material. As the latter, alumina, silica-alumina and silica-magnesia are used. The second stage uses a catalyst consisting of the same elements that make up the first stage catalyst and promoted with titanium in an amount of 1 to 10 wt. % Thus, the first stage catalyst differs from the second stage catalyst in that it does not contain a promoter. Group IV B metal and Group VI and VIII metals impregnate the surface of the carrier, but they are not inserted into the carrier. A solution of titanium tetrachloride in n-gentan is used for impregnation. Application, more than 8-10 weight. ° / o titanium can reduce catalyst activity during desulfurization, since the use of more than one monolayer contributes to the clogging of the pores of the catalyst and prevents access of large oil molecules to the inside of the catalyst. In addition, the creation of such a layer is economically unjustified. Quantity less than 1 weight. % titanium does not promote catalyst activity. The particle diameter of the catalysts of the first and second stages is 0.0635-0.127 cm. The feedstock is first passed through a fixed bed of non-cleaned catalyst. The non-promoter catalyst removes 60-80 wt. % and more metals and sulfur. Then the raw material passes through a fixed bed of promoted catalyst. With this process, cracking of raw materials is negligible. Most of the oils produced (70-90 / o) boil, above the boiling point of the feedstock. The partial pressure of hydrogen is 70-350 kg / cm, preferably 105-175 kg / cm. The gas circulation is 17.8-356 / 100 L, preferably 35.6-178 L. Circulating gas contains 85% or more of hydrogen. The molar ratio of hydrogen to raw materials is 4: 1-80: 1, the temperature is 316-482 ° C, preferably 343 427 ° C. During the catalytic cycle, the temperature of the reactor increases. The temperature should be low enough so that no more than 30%, preferably no more than 10-20% of the raw material is cracked into fractions boiling below 343 ° C. The volumetric rate of the liquid in the reactors of both stages is 0.1-10.0 hours, preferably 0.2-1 hours - or 1.25 hours. The loading of the first stage of the process may consist entirely of crude or stripped oil containing almost all the residual asphaltenic crude oil. Asphaltenes have a relatively low H / C ratio and usually make up less than 10 ° C of the charge, but usually they contain a large proportion of the metallic components present in the total feed, for example nickel and vanadium. The non-promoted first-stage catalyst removes most of the nickel and vanadium, as well as sulfur. Metals deposited in the pores of the catalyst prevent the feedstock from entering the pores of the catalyst, which reduces the desulfurization activity of the catalyst. Removed nickel and vanadium are usually the cause of the final deactivation of the first stage desulfurization catalyst, while coke deposition during the removal of sulfur and nitrogen slightly deactivates the first stage catalyst. The remnants of the atmospheric or vacuum oil refining columns contain almost all the asphaltene fraction of crude oil and contain 95–99 wt. Nickel and vanadium or more contained in crude oil. The content of nickel and vanadium in oil residues can vary widely, for example, nickel and vanadium can be contained in an amount of 0.002-0.03 wt.% Or more, sulfur in an amount of 2-7 wt. %, based on oil. At the beginning of the first stage, the removal of nickel and vanadium from the raw material occurs as quickly as the removal of sulfur. However, over time, the deposition of metals on the catalyst leads to a deactivation of the catalyst to a greater extent than the removal of sulfur and nitrogen, since the metals are deposited on the catalyst, while sulfur and nitrogen are released in the form of hydrogen sulfide and ammonia. At this stage, nickel and vanadium gradually accumulate on the surface of the catalyst, ultimately clogging its pores. After clogging the pores, the catalyst aging rate ceases to be gradual and increases dramatically, the catalytic cycle is terminated. Although the use of a promoted catalyst in the first stage leads to an increase in desulfurization activity, it is more efficient to use such a catalyst in the second stage. In addition, the advantage of the promoted catalyst in the first stage decreases with progressive aging of the catalyst, as well as with time. Another disadvantage of using a promoted catalyst in the first stage is that the service life of any catalyst in the first stage is ultimately limited by a rapid and irreversible deactivation with metals, therefore the use of an approved catalyst in the first stage is uneconomical. The layers of the catalysts of the first and second stages can be located in one reactor or in separate reactors. Each step may consist of one or more reactors. On. second stage, the primary cause of catalyst deactivation is coking: In the known two-stage desulfurization processes, the catalyst aging rate and coke formation on the catalyst are significantly higher in the second stage than in the first because the degree of desulfurization in the second stage is higher than in the first. This is due to the fact that in the first stage, the alkyl groups of asphaltenes and other compounds create an obstacle preventing contact of the inside of the polycondensed ring of molecules with the catalyst. The use of a promoted catalyst in the second desulfurization stage allows for an increased degree of desulfurization with reduced coking. In addition, the use of promoted catalyst in the second stage leads to significant savings in hydrogen. The promoted catalyst in the second stage easily undergoes auto-regeneration by removing surface coke with increasing hydrogen pressure. In the examples (unless otherwise noted), Kuwaiti oil residues containing 3.9 weight / sulfur are used as raw materials. Non-promoted catalyst consists of 0.6 wt.% Nickel, 1.1 wt. % cobalt, 8.7 wt. % molybdenum, the rest is alumina. The promoted catalyst consists of alumina, triply alternately impregnated with molybdenum, nickel and titanium, and contains 3 wt. % nickel, 8 wt.% molybdenum, 5 wt. / about titanium, the rest - g; linosem. Example 1. FIG. Figure 1 shows a graph illustrating the results of a single-stage and two-stage, methods for the desulfurization of asphalt metal-containing raw materials using both single-stage and two-stage processes of a catalyst not made by titanium. The desulfurization processes are carried out at a hydrogen pressure of 199.5 kg / cm 2, a temperature of 414 ° C. The starting point of the first horizontal section of the curve in FIG. 1 corresponds to the sulfur content in the product of the single-stage desulfurization process carried out at a volumetric feed rate of the liquid raw material of 0.5 hours and is 0.225 weight. % As the flow rate increases to 1.0 h, the sulfur content rises to 0.61 wt. % (second horizontal part of the curve). The second horizontal section illustrates the data obtained during the overgrowth of the two-stage desulfurization process. The liquid product of the first stage is separated from the gaseous products, the pressure of the system is reduced by the datom sphere, and the second stage of the process is carried out with the addition of fresh hydrogen. The volumetric flow rate of the fluid is maintained at 1.0 h (the total volumetric rate for the feedstocks of the first and second stages is thus 0.5 hours). The initial sulfur content of the second stage product is 0.19 wt. % The latter indicates the advantage of using a two-step process for desulfurization. This advantage is obvious, since hydrogen sulphide and ammonia are removed from the system. In addition, in the second stage, an increased hydrogen pressure is used due to the removal of the pelvic contaminants. However, as can be seen from FIG. 1, deactivation of the second stage catalyst occurs quickly and the sulfur content in the product reaches 0.24 weight. % Thus, the phenomenon of deactivation of the catalyst ™ stage swarm quickly annuls the advantage of the two-step process. Consequently, the Non-Promoted Catalyst is more resistant to deactivation (aging) when using the latter in a One-Step Process. It is likely that the initially observed advantage of the two-step process is due to the higher partial pressure of hydrogen in the second stage due to interstage removal of pollutant gases. The rapid aging of the second stage catalyst is due to the fact that the removal of hydrogen sulfide and ammonia is necessary to stabilize the non-promoted catalyst against coking in the second stage. In the second stage, hydrogen sulfide and ammonia are formed in an amount insufficient for stabilization, since most of the sulfur and nitrogen is removed from the feed in the first stage. It is believed that ammonia is required to partially reduce the acidity of the catalyst, hydrogen sulfide is necessary to maintain the active persulfurized state of the catalyst. The reason that the single-stage process shows catalyst stability with the same degree of desulfurization as the two-stage process, apparently in TOMj, that the single-stage process occurs completely in the presence of an additional amount of ammonia and
    hydrogen in the system, while the work of the second stage occurs with a relatively small amount of ammonia and hydrogen sulfide produced in the second stage.
    The characteristics of the feedstock and products obtained as a result of the desulfurization processes are given in table. one.
    Example 2. A desulfurization experiment was carried out analogously to Example 1 using both single-stage and two-stage catalyst processes promoted by titanium.
    The desulfurization process is carried out at a hydrogen pressure of 194.6 kg / cm 2, a temperature of 399 ° C.
    FIG. 2 is a graph illustrating the results of the experiments of example 2.
    The starting point of the first horizontal section of the curve corresponds to the sulfur content in the product of the one-stage desulfurization process, carried out at a volumetric feed rate of liquid raw materials equal to 0.5 h. The sulfur content is 0.21 wt. %
    As the volumetric rate increases to 1.0, the sulfur content rises to 0.58 wt. % (second horizontal part of the curve). The second horizontal section 25 illustrates the data obtained during the first stage of the two-stage desulfurization process:
    The liquid product of the first stage is separated from the gaseous products, the pressure of the system is reduced to atmospheric and the second stage of the process is conducted by adding fresh hydrogen. The volumetric flow rate of the fluid is maintained at 1.0 h (the total volumetric flow rate of the raw materials in the first and second stages is thus j 0.5 h). The average sulfur content in the product of the second stage is 0.17 wt. %, which shows the advantage of a two-step process.
    In contrast to the aging characteristic of a non-promoted second-stage catalyst, where the advantage of a two-step process is maintained for only 24 hours due to the rapid deactivation of the catalyst (see Fig. 1), when using a developed SRI of a promoted catalyst, the advantage of a two-step process is maintained for 80 hours more. Thus, the promoted catalyst exhibits the ability to remain active and resistant to coking in the absence of ammonia and hydrogen sulfide.
    In addition, a comparison of the Data of examples 1 and 2 shows the advantage of a promoted catalyst over an unpromoted one during the one-stage desanning of 55 serialization. Thus, the experiments of Example 2 were performed under milder conditions, however, the degree of desulfurization of the products was higher than in the experiments of Example 1.
    Example 3. The experiment was carried out on the aging of a promoted catalyst used in the second stage of a two-stage desulfurization process. The test catalyst reduces (in the second stage) the sulfur content in the product from 1 to 0.3 wt.%. Aging is carried out at a flow rate of 1.0 h and a partial pressure of hydrogen of 128 kg / cm.
    The results of the experiment are illustrated in FIG. 3 (bottom curve). The upper curve is the aging curve of the non-promoted second stage catalyst. The tested non-promoted catalyst also reduces the sulfur content in the product from 1 to 0.3 weight. % However, the volumetric flow rate of the fluid is 0.5.
    The comparison of the curves shows that the promoted second-stage catalyst deactivates with time significantly less than the non-promoted catalyst, although the latter is aging under milder conditions (volumetric flow rate of the liquid. 0.5 h).
    From the graph shown in FIG. 3, it can be seen that after 150 days of operation with the same degree of desulfurization, when using a promoted catalyst, it is necessary to maintain a temperature of 401 ° C, while using an unprompted 416 ° C, although in the first case the feed rate of the raw material was twice as high.
    Thus, the α-promoted second-stage catalyst is more than twice as active in the long aging process as compared to the unmodified catalyst. This advantage becomes increasingly tangible over time.
    Example 4. FIG. 4 illustrates the results of experiments that show that desulphurisation of the promoted second stage catalyst, which is confirmed by the data of Example 3, is not observed during the first stage. Although a comparison of FIG. 1 and 2 shows that the promoted catalyst is superior in activity to the non-promoted catalyst used in the first stage, the comparison of FIG. 3 and 4 shows that the advantage is. The use of a promoted catalyst in the first stage of operation is significantly less than the latter when using this catalyst in the second stage of operation.
    Single-stage desulfurization processes are carried out using a promoted catalyst (volumetric flow rate of the fluid is 1.0) and a non-promoted catalyst (volumetric rate is 0.5 hours). The conditions of the experiments (except for the speed values) are the same. The hydrogen pressure is 159 kg / cm2.
    As shown in FIG. 4, the residual fractions of the atmospheric distillation of petroleum (atmospheric residues AO) containing 3.9% by weight of sulfur are treated to reduce the sulfur content to 0.82 weight. % From this graph it can be seen that when using a promoted catalyst, the temperature required is 9.5 ° C higher than when using unprompted. Then desulfurization is subjected to residual fractions of vacuum distillation of Kuwaiti oil (VO vacuum residues) containing 5.7 wt. / o sulfur, to reduce the sulfur content to 1.45%. In these experiments, the need for an increase in temperature in comparison with the use of a non-promoted catalyst gradually increases over time from 9.5 to 17.9 ° C.
    Thus, FIG. 3 shows that, despite the difference in the flow rates of the liquid, the promoted second stage catalyst exhibits a temperature advantage over the non-promoted catalyst and it increases with time. FIG. 4 shows that with the same difference in speed values in the first stage, the promoted catalyst detects a temperature deficit compared to a non-promoted catalyst and this deficiency persists or increases with time. Therefore, in a process with a long catalyst life, a promoted catalyst cannot provide an economic advantage in the first stage due to the relatively high cost of the promoted catalyst, whereas in the second stage of operation, the economic advantage of the promoted catalyst increases with the service life. Therefore, the proposed method is used in processes designed for a long time. As shown in FIG. 3, the relative advantage of the promoted catalyst increases significantly after 20 or 30 days, which corresponds to passing 137.3-206 liters of feed per 1 kg of catalyst through the second-stage catalyst.
    Example 5. Based on the experimental data, calculations are performed showing the advantage achieved with a single-stage process using a non-promoted catalyst, in which a part of the non-prothromium catalyst at the exit end of the first-stage reactor is replaced by a promoted catalyst. When calculating, it is believed that the atmospheric residues of Kuwaiti oil, having 3.9 wt. % sulfur is converted in the first stage at a temperature of 371 ° C and a hydrogen pressure of 159 kg / cm into a product containing 0.3 weight. % sulfur. In the main calculation using the non-promoted catalyst throughout the reactor, the volumetric rate in the upper part
    the reactor is 1.0 h, in the bottom of the reactor 0.3. In a comparative calculation, a non-promoted catalyst is used in the upper part of the reactor at a rate of 1.0 h, the non-promoted catalyst in the lower part of the reactor is replaced with a small amount of promoted catalyst to obtain a bulk velocity of 0.73 in the lower part. The amount of catalyst promoted corresponds to the amount needed to obtain
    g output product containing 0.3 wt.% sulfur. The calculation results show that the use of a promoted catalyst in the lower part of the reactor constitutes a catalyst saving of 58.9% (for the lower part). Hydrogen saving is 41%
    5 (at the bottom). In terms of the entire reactor, the use of a promoted catalyst in the lower part saves 45.3% for the catalyst and 18% for hydrogen.
    Example 6. In table. Figure 2 shows the data on the introduction of the second stage of a two-stage desulfurization process using promoters and non-promoted catalysts. The desulfurization is carried out by atmospheric residues of Kuwaiti oil. The sulfur content is reduced from 1 wt.% (For the product of the first stage) to 0.3 wt.%.
    The first-order reaction constant, adjusted for a temperature of 399 ° C, is a direct measure of the catalytic activity. Reaction rate constants are calculated using weight hourly rate. These data show that at the second stage the promoted catalyst is 33% more active than the non-promoted catalyst.
    From the data table. 2 that the promoted catalyst reaches the same degree of desulfurization as the non-promoted catalyst with a significantly lower hydrogen consumption. Therefore, the promoted catalyst is more selective for the desulfurization reaction than the non-promoted one. Side reactions for which hydrogen is consumed, such as hydrogene sisation, saturation of aromatic hydrocarbons, removal of metals and others, do not occur to the same extent on the promoted catalyst as on nonproducts.
    From tab. 2 it follows that when using a promoted catalyst, the same degree of desulfurization is achieved as with an unpromoted one, even if the former is operated at a significant higher space velocity. Therefore, at the same rate for the two catalysts, the promoted catalyst can achieve the desired level of desulfurization at a lower temperature than the unpromoted second stage catalyst, since at a given water pressure, the volume velocity and temperature are interchangeable parameters. Example 7. Experiments were carried out to determine the effect of changes in the hydrogen partial pressure on the aging rate of the promoted catalyst when used in the second desulfurization stage. The results of these experiments are illustrated in FIG. 5. The experiments were carried out at a constant volumetric flow rate of the liquid equal to 0.88. The zero point on the abscissa axis refers to carrying out the process using a promoted catalyst at a pressure of 128 kg / cm2. The rate of aging of the catalyst is 0.95 ° C per day. The resulting product contains 0.3 weight. / o sulfur. When the pressure is increased to 162 kg / cm after 24 hours, the catalyst acquires an equilibrium state and the processed product contains 0.25 weight. % sulfur: Further catalyst aging does not occur: With a further increase in pressure to 195 kg / cm, the equilibrium state of the catalyst is established after 24 hours and the sulfur content decreases to 0.20 weight. % without aging catalyst. As can be seen from the above data, after each increase in hydrogen pressure, only 24 hours are needed to equilibrate the catalyst. Although the increase in desulfurization is significant, the more important effect is the elimination of catalyst aging (in comparison with 0.95 ° C per day). After working at elevated pressures, the system was returned to the initial hydrogen pressure of 128 kg / cm at the same volumetric rates and temperatures, ensuring that they produce a product with a sulfur content of 0.3 wt. %, and it was found that for almost one day the sulfur content in the product was 0.25-0.26 weight. % This shows that the use of elevated hydrogen pressures causes an increase in the desulfurization activity after the initial, relatively low hydrogen pressure is established. For the sake of comparison, experiments were carried out with the use of a non-promoter catalyst at the second stage at 414 ° C and a space velocity of -0. With a hydrogen pressure of 130 kg / cm 2 sulfur content
    736874
    12 in the product was 0.3 ae. % (in the initial raw material 1 w / o sulfur). The pressure has increased. Up to 166 kg / cm2 is required. At the same time, a seven-day period of work is needed until the sulfur content in the product reaches a level of 0.21 weight. % After 13 days of work under a pressure of 166 kg / cm, the pressure of hydrogen is increased to 175 kg / cm and the sulfur content at the same time reaches 0.185% by weight. After seven days of work under a pressure of 175 kg / cm 2, the pressure of hydrogen is increased to 200 kg / cm, and four more days of work are needed until the sulfur content of the sulfur-containing product reaches 0.125 weight. /about. Thus, the promoter metal not only inhibits primarily the formation of coke on the catalyst, but also catalyzes, after an increase in pressure, the removal of coke already deposited on the catalyst. - In tab. 3 shows the conditions for conducting the experiments. In Example 7 and the quality of the feedstock and the products obtained. From the data table. 3, it follows that a promoted catalyst is a more selective desulfurization catalyst than a non-promoted catalyst. The five percent distillation temperatures also show that the fraction obtained using the promoted catalyst is higher boiling than that obtained using the non-promoted one. Consequently, in the first case, less hydrocracking and less consumption of hydrogen are observed. FIG. 6 is a schematic diagram for implementing the method. The crude oil feedstock through line 1 and recirculating hydrogen through line 2 is fed to the upper part of the reactor 3 of the first desulfurization stage, containing a fixed bed 4 of non-promoted catalyst. The product of the first stage is fed via line 5 to the instantaneous evaporation chamber 6, from which exhaust gases are removed via line 7, the liquid through line 8 is directed to the second stage reactor 9. Additional and recirculating hydrogen is fed to reactor 9 through line 10. Reactor 9 contains a fixed bed 11 of a promoted catalyst. The product of the second stage is output on line 12.
    Composition Sulfur, weight,% Nitrogen, wt.% - Carbon, Imp.% - 87.06 Hydrogen, wt.% - 12.52 Nickel, ppm.15 0.1 Vanadium, ppm, 1 S ° / Distills% by volume 5333 259 10399 295. 30 451 384 50519446 80-565 Cracked at 551 C 575 more than 69% 84% Rams coke, wt.% 9, O4 2.21
    Weight speed of raw materials, l / kg
    2
    Hydrogen pressure, kg / cm
    Average reactor temperature, C
    3 Hydrogen consumption, m / 100 l Volume hour rate, hour
       -one
    Weight hour speed
    First reaction constant
    at 399fc
    Desulfurization,%
    Table 0.90 When
    Table
    -f 84.34 12.45 1.8 0.2 1.6 OD 0.9053 0.9135 aura, C 264 287 322 301 406 390. 453 470 568 572 with 56 8s 80% 77% 2.52 3.61
    权利要求:
    Claims (2)
    [1]
    1. A method for desulfurizing asphaltene metal-containing oil feedstock in two steps by contacting the feedstock with hydrogen at elevated temperature and pressure in the presence of a catalyst containing metals of groups VI and VIII on a non-cracking carrier, with interstage removal of contaminating gases, characterized in that the purpose of improving the efficiency of the process, as a catalyst in the table
    A swarm of a step uses a catalyst proS motivated 1-10 weight. % titanium.
    [2]
    2. A method according to claim 1, characterized in that the process is carried out at a temperature of 316- 482 ° C, a pressure of 70-350 kg / cm 2.
    Sources of information taken into account in the examination
    1.Orochko, DM and others. Hydrogenation processes in oil refining, M., “Chemistry, 1971, p. 225-230.
    2. US patent number 3876530, cl. 208-210, pub. 04/03/75 (prototype).
    Comparison of a two-stage dedication with a single-stage one on an unproduced cataliesgtor
    Schaustenchypty
    First stage
    Volumetric speed, 4-1
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    同族专利:
    公开号 | 公开日
    ES446818A1|1978-03-16|
    JPS51128305A|1976-11-09|
    DE2603865A1|1976-11-11|
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    引用文献:
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    US4116817A|1977-06-28|1978-09-26|Gulf Research & Development Company|Hydrodesulfurization process employing a promoted catalyst|
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    US4816434A|1982-02-19|1989-03-28|Union Oil Company Of California|Catalytic materials of controlled geometric mean electronegativity|
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    US4687757A|1986-03-24|1987-08-18|Phillips Petroleum Company|Hydrofining catalyst composition and process for its preparation|
    US4734186A|1986-03-24|1988-03-29|Phillips Petroleum Company|Hydrofining process|
    FR2666787B1|1990-09-19|1992-12-18|Aerospatiale|HYDRAULIC ACTUATOR WITH HYDROSTATIC MODE OF PREFERRED EMERGENCY OPERATION, AND FLIGHT CONTROL SYSTEM COMPRISING SAME.|
    AU9227801A|2000-10-16|2002-04-29|Yokota Mfg|Fluid discharge device and pipeline system|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US05/572,460|US3968027A|1975-04-28|1975-04-28|Multi-stage hydrodesulfurization utilizing a second stage catalyst promoted with a group IV-B metal|
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