CN1313379A - Process for hydrogenating poor-quality raw material for catalytic cracking - Google Patents
Process for hydrogenating poor-quality raw material for catalytic cracking Download PDFInfo
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Abstract
A hydrogenating process of poor catalytic cracking raw material includes such steps as sequential contacting of said raw material with hydroprotecter, demetalizing hydrocatalyst and hydrorefining catalyst, reacting at 330-420 deg.C, 5-10 MPa (hydrogen), 300-(1000:1) volume ratio jof hydrogen to oil and liquid space speed of 0.2-1.2/hr with hydrogen, cooling, and separating of liquid from hydrogen. The gas product containing hydrogen can be cyclically used. The liquid product comes into fraction system. After above hydrogenating, said raw material contains less content of S, N and metals.
Description
The invention belongs to a kind of the existence under the situation of hydrogen for obtaining the method for the refining hydrocarbon ils of low boiler cut, more particularly, is a kind of method that hydrotreatment is carried out in poor-quality raw material for catalytic cracking coker gas oil and deasphalted oil.
In order to satisfy the demand to light-end products that World Oil Market increases day by day, each oil refining enterprise constantly enlarges the raw material sources of catalytic cracking (FCC) device, to improve light oil yield.The raw material of FCC apparatus mainly is vacuum gas oil (VGO), and over nearly one, 20 year, the trend that FCC apparatus is mixed coking gas oil (CGO), deasphalted oil inferior raw materials such as (DAO) constantly increases.
CGO comes from delayed coking unit, and its yield is generally 20～35 heavy % of coking raw material.Owing to sulphur, nitrogen content height, especially the alkali nitrogen content height of CGO, directly can make the acid sites poisoning of FCC cracking catalyst, active decline as the FCC raw material, finally cause light oil yield decline, the quality product of FCC to reduce.In addition, NO in the FCC regenerated flue gas
x, SO
xContent also can increase, cause environmental pollution.Usually CGO is carried out hydrotreatment, advances FCC apparatus with VGO again after removing impurity such as sulphur, nitrogen, or earlier and VGO be mixed and carry out hydrotreatment, and then carry out FCC.Hydrotreatment is a kind of effective ways that improve coker gas oil character, and the CGO behind the hydrogenation not only sulphur, nitrogen content significantly descends, and hydrogen richness, saturated hydrocarbon content increase, and can effectively improve light oil yield and the quality product of FCC.
DAO is from solvent deasphalting unit.Use C
4, C
5Alkane is as solvent, can obtain the deasphalted oil of 70 heavy % above (accounting for the diasphaltene raw material), but raising along with yield, the sulphur of DAO, nitrogen, metal impurities content increase, density increases, viscosity and carbon residue also increase, and make the cracking performance of DAO descend, and FCC directly mixes the refining DAO comparison difficulty that becomes.People such as Jacques Bousquet have compared C in " The Katalistiks ' 7th Annual, Fluid Cat Cracking Symposium, Venice, Italy, May 11～13,1986 "
3-DAO, C
4-DAO, C
5The cracking performance of-DAO before and after hydrogenation pointed out C
4-DAO or C
5It is very difficult that-DAO directly carries out catalytic cracking, but behind the hydrotreatment upgrading, can become fine FCC charging, and economic benefit is very considerable.
EP 0 683 218 A2 disclose a kind of method for transformation of residual oil, have introduced deasphalted oil that the vacuum residuum diasphaltene obtains in the method after hydrotreatment, mix with VGO and carry out hydrocracking, produce intermediate oil.Though the quality of gained intermediate oil is better, the condition of DAO hydrotreatment is very harsh, and pressure is 17.1MPa, and weight space velocity is 0.6 hour
-1, this can make plant investment increase, and process cost increases.
The objective of the invention is to provide on the basis of existing technology a kind of hydroprocessing process of processing coker gas oil and deasphalted oil simultaneously.
Method provided by the invention is: in the hydrogen dividing potential drop is that 5.0～10.0 MPas, temperature are that 350～420 ℃, hydrogen to oil volume ratio are 300～1000: 1, liquid hourly space velocity is 0.2～1.2 hour
-1Condition under, raw material is contacted with hydrogenation protecting agent, Hydrodemetalation catalyst and Hydrobon catalyst successively and without intermediate section from, reacted effluent is through refrigerated separation, hydrogen-containing gas recycles, product liquid enters fractionating system.
Specifically, the present invention thes contents are as follows:
In hydrogen dividing potential drop 5.0～10.0 MPas, best 5.5～8.0 MPas, 330～420 ℃ of temperature, best 350～400 ℃, hydrogen to oil volume ratio 300～1000: 1, best 400～800: 1, stock liquid hourly space velocity 0.2～1.2 hour
-1, best 0.4～1.0 hour
-1Reaction conditions under; raw material is contacted successively and without isolating hydrogen sulfide and ammonia in the centre with hydrogenation protecting agent, Hydrodemetalation catalyst and Hydrobon catalyst; reaction effluent enters high-pressure separator through cooling; isolated product liquid enters fractionating system, and rich hydrogenous gas circulation is returned reactor.Method provided by the invention can be implemented in fixed bed, moving-bed or suspended-bed reactor.
Raw material used among the present invention is the mixture of coker gas oil, deasphalted oil and vacuum gas oil, it is characterized in that described raw material is that coker gas oil, deasphalted oil and vacuum gas oil shared weight percentage in mixture is respectively 5～95 heavy %, 5～95 heavy % and 0～95 heavy %.
Used a kind of hydrogenation protecting agent, a kind of hydrodemetallation (HDM) (HDM) catalyzer and a kind of Hydrobon catalyst among the present invention, be respectively described below:
The hydrogenation protecting agent of using among the present invention is made up of the gamma-aluminium oxide carrier with diplopore distribution of 1.0～5.0 heavy % nickel oxide, 5.5～10.0 heavy % molybdenum oxides and surplus.This protectant specific surface ≮ 180 meter
2/ gram, pore volume ≮ 0.6 milliliter/gram, crushing strength ≮ 12 ton/millimeter.
The gama-alumina precursor that has the diplopore distribution in the above-mentioned protective material is hydrated aluminum oxide A and the hydrated aluminum oxide B that is made by alkyl aluminum hydrolysis method and Tai-Ace S 150 method, and by 0.7～1.2: 1 weight ratio mixes, and their pore size distribution is respectively:
Hydrated aluminum oxide A hydrated aluminum oxide B
＜50 dusts 95～96% 35～60%
50～100 dusts 2.0～3.0% 21～25%
100～250 dusts 0.5～1.0% 13～15%
250～500 dusts 0.2～0.5% 5.0～6.0%
Described gamma-aluminium oxide carrier be by the hydrated aluminum oxide mixture of above-mentioned two kinds of different pore size distributions and carbon powder, tensio-active agent, peptizing agent by weight 1: 0.05～0.1: 0.05～0.1: 0.02～0.05 and the suitable quantity of water mixing moulding, drying, roasting are made.
The effect of hydrogenation protecting agent mainly is the impurity such as Fe, Ca that remove in the raw material, prevents beds pressure drop rising.
The HDM catalyzer that uses among the present invention consists of: nickel oxide 1.0～5.0 heavy %, and molybdenum oxide 5～15 heavy %, all the other are the carrier gama-alumina.The pore size distribution of this catalyzer mainly concentrates on 100～200 dusts, and the pore volume of 100～200 dusts accounts for 50～90% of total pore volume, is preferably 60～80%.Total pore volume of this catalyzer is 0.4～1.0 a milliliter/gram.The HDM catalyzer mainly is the heavy metals such as Ni, V that remove in the raw material, and the Hydrobon catalyst that prevents the downstream is because of deposition heavy metal inactivation.
The Hydrobon catalyst that uses among the present invention is a disclosed catalyzer among the CN1169336A, consisting of of this catalyzer: 1～5 heavy % nickel oxide, 12～35 heavy % Tungsten oxide 99.999s, 1～9 heavy % fluorine and surplus aluminum oxide, this aluminum oxide be by-kind or multiple little porous aluminum oxide and one or more macroporous aluminium oxides be composited according to 75: 25～50: 50 weight ratio, the pore volume of these aperture aluminum oxide median pore diameter＜80 dusts accounts for total pore volume more than 95%, the pore volume of these macroporous aluminium oxide median pore diameter 60～600 dusts accounts for total pore volume more than 70%, and described pore volume is measured with B E T Brunauer Emett Teller method of nitrogen adsorption at low temperature.The precursor of described aperture and macroporous aluminium oxide is respectively a diaspore content greater than 60% with greater than 50% hydrated aluminum oxide.The alumina supporter median pore diameter of aperture and the compound gained of macroporous aluminium oxide is that the pore volume of 40～100 dusts accounts for more than 75% of total pore volume.The main effect of Hydrobon catalyst is S, the N impurity that removes in the raw material, and it is saturated to carry out suitable hydrogenation, to improve the catalytic cracking performance of raw material.
The admission space percentage ratio of hydrogenation protecting agent, HDM catalyzer and Hydrobon catalyst is respectively 2～10%, 10～40% and 50～88%, and best compound filling ratio is according to deciding the performance of raw material oil properties, catalyzer and the runtime of requirement etc.
Above-mentioned catalyzer and protective material also should carry out prevulcanized before use.Prevulcanized can be carried out according to the method for common Hydrobon catalyst or hydrocracking catalyst prevulcanized.The general gas phase sulfuration method that adopts among the present invention, vulcanizing agent can be selected dithiocarbonic anhydride or dimethyl disulfide for use, and sulfide stress is generally 3.0～8.0 MPas, and the volume ratio of recycle hydrogen gas and catalyzer is generally 300～600 during sulfuration: 1.Sulfuration is that the substep alternating temperature carries out, and generally vulcanizes 2～6 hours down at 200～240 ℃ earlier, vulcanizes 8～12 hours down at 320～360 ℃ then.
The injection rate of vulcanizing agent should be regulated according to the concentration of hydrogen sulfide in sulfurized different steps and the recycle hydrogen.The injection rate of cryogenic vulcanization stage vulcanizing agent should be controlled at and make that the concentration of hydrogen sulfide remains in 0.1～0.5% scope in the recycle hydrogen; Along with curing temperature rising gradually, the injection rate of vulcanizing agent can be controlled in the concentration of hydrogen sulfide that makes in the recycle hydrogen and is increased to 1.0%; The injection rate of vulcanizing agent then should make the concentration of hydrogen sulfide be controlled in 1.0～2.0% scopes during high temperature vulcanized stage.
After hydrotreatment, sulphur, nitrogen, metal content all have reduction in various degree to FCC stock oil inferior (referring to CGO, DAO etc.), and polycyclic aromatic hydrocarbons is by saturated, and hydrogenated oil can be used as the high quality raw material of FCC.For carbon residue or the higher raw material of metal content, before Hydrobon catalyst, add a certain amount of protective material, not only reduced the generation of coke, and guaranteed that the once stability of Hydrobon catalyst was not less than 2 years.
The following examples will give further instruction to the present invention, but therefore not limit the present invention.
Raw material among the embodiment is CGO and 7: 3 mixture of DAO weight ratio, and its character is as shown in table 1.The trade names of employed hydrogenation protecting agent, HDM catalyzer, Hydrobon catalyst are respectively RG-1, RF-220, RN-10 among the embodiment, wherein RG-1 and RN-10 are produced by China PetroChemical Corporation's Chang Ling oil-refining chemical head factory catalyst plant, RF-220 is produced by Dutch Aksu chemical company, its composition and physico-chemical property are as shown in table 2, the admission space ratio of RG-1, RF-220, three kinds of catalyzer of RN-10 is 5: 25: 70, RG-1 be seated in the-reactor top, loadings is 30 milliliters; RF-220, be seated in first reactor the bottom, loadings is 150 milliliters; RN-10 all is seated in second reactor, and loadings is 420 milliliters.
Embodiment
Raw material A and hydrogen-rise contact with Hydrobon catalyst RN-10 with protective material RG-1, HDM catalyzer RF-220 successively and without intermediate section from, reacted effluent is through refrigerated separation, hydrogen-containing gas recycles, product liquid enters fractionating system.Test conditions and result are respectively shown in table 3 and table 4.
Catalyzer at first carries out prevulcanized in reactor, vulcanizing agent is CS
2, incorporation is 2 heavy %, the prevulcanized top temperature is 290 ℃, about 30 hours of curing time.After sulfuration finishes, feed VGO, at the beginning of carrying out 24 hours under 360 ℃, live through and cross, advance the mixing raw material oil of CGO and DAO then, turn round after about 10 days (catalyst activity reaches the steady stage), carry out experiment of process conditions.Hydroprocessing technique condition and generate oil nature and material balance data sees Table 3, table 4, table 5.
From the data of table 3～table 5 as can be seen, the mixing oil of CGO and DAO is under than the demulcent hydroprocessing condition, foreign matter content such as S, N significantly reduces, the S of＞350 ℃ of cuts, N are respectively 0.26 heavy %, 0.29 heavy %, wherein basic nitrogen has only 486ppm, metal content is less than 1ppm, and carbon residue has only 0.69 heavy %, is fine FCC raw material.
Table 1
| The stock oil title | ????CGO | ????DAO | Mixing oil |
| Density (20 ℃), g/cm 3 | ????0.9616 | ????0.9772 | ????0.9672 |
| Viscosity (100 ℃), mm 2/s | ????7.15 | ????29.93 | ????10.48 |
| Carbon residue, heavy % | ????1.12 | ????4.7 | ????2.2 |
| ?C 7Insolubles, heavy % | ????0 | ????＜0.05 | ????＜0.03 |
| S, heavy % | ????3.10 | ????0.68 | ????2.37 |
| N, heavy % | ????0.53 | ????0.55 | ????0.54 |
| C, heavy % | ????85.50 | ????87.78 | ????86.15 |
| H, heavy % | ????10.64 | ????10.59 | ????10.61 |
| Basic nitrogen, ppm | ????1539 | ????1022 | ????1384 |
| ?Ni,ppm | ????＜0.1 | ????11.3 | ????3.4 |
| ?V,ppm | ????＜0.1 | ????2.6 | ????0.8 |
| ?Fe,ppm | ????1.0 | ????2.4 | ????1.5 |
Table 2
| Catalyzer | ????RG-1 | ??RF-220 | ????RN-10 |
| Chemical constitution, heavy % | |||
| ?NiO | ????1.2 | ????1.2 | ????4.0 |
| ?WO 3 | ?????- | ?????- | ????20.8 |
| ?MoO 3 | ????5.5 | ????6.5 | ????- |
| ?F | ?????- | ?????- | ????2.0 |
| Physical properties: | |||
| Specific surface area, m 2/g | ????205 | ????140 | ????230 |
| Pore volume, mL/g | ????0.68 | ????0.7 | ????0.27 |
| Crushing strength, N/mm | ????14.0 | ????13.0 | ????27.5 |
| Equivalent diameter, mm | ????3.6 | ????1.3 | ????1.2 |
| Shape | Trifolium | Trifolium |
Table 3
| Operational condition | ||
| The hydrogen dividing potential drop, MPa | ????????????6.4 | |
| Temperature of reaction, ℃ | ????????????380 | |
| Liquid hourly space velocity, h -1 | ???????????0.86 | |
| Hydrogen-oil ratio, v/v | ????????????570 | |
| Product distributes, heavy % | ||
| Gas (H 2S、NH 3、C 1-C 4) | ????????????3.2 | |
| Gasoline fraction (C 5-180℃) | ????????????0.71 | |
| Diesel oil distillate (180-350 ℃) | ???????????12.25 | |
| Gas oil fraction (＞350 ℃) | ???????????84.88 | |
| Generate oil nature | C 5-350 ℃ of cuts | ＞350 ℃ of cuts |
| Density (20 ℃), g/cm 3 | ?0.8840 | ????0.9335 |
| Viscosity (100 ℃), mm 2/s | ??- | ????9.36 |
| Carbon residue, heavy % | ??- | ????0.69 |
| ?C 7Insolubles, heavy % | ??- | ????0 |
| C, heavy % | ??- | ????87.75 |
| H, heavy % | ??- | ????11.70 |
| S, heavy % | 272ppm | ????0.26 |
| N, heavy % | 439ppm | ????0.29 |
| Basic nitrogen, ppm | ??- | ????486 |
| ?Ni,ppm | ??- | ????＜0.1 |
| ?V,ppm | ??- | ????＜0.1 |
Claims (9)
1, a kind of hydroprocessing process of poor-quality raw material for catalytic cracking; it is characterized in that raw material contacts with hydrogenation protecting agent, Hydrodemetalation catalyst and Hydrobon catalyst successively, be that 5.0～10.0 MPas, temperature are that 330～420 ℃, hydrogen to oil volume ratio are 300～1000 in the hydrogen dividing potential drop: 1, liquid hourly space velocity is 0.2～1.2 hour
-1Condition under and hydrogen reaction, reacted effluent is through refrigerated separation, hydrogen-containing gas recycles, product liquid enters fractionating system.
2, according to the method for claim 1, it is characterized in that described raw material is the mixture of coker gas oil, deasphalted oil and vacuum gas oil, it is characterized in that described raw material is that coker gas oil, deasphalted oil and vacuum gas oil shared weight percentage in mixture is respectively 5～95 heavy %, 5～95 heavy % and 0～95 heavy %.
3, according to the method for claim 1, it is characterized in that reaction conditions is: hydrogen dividing potential drop 5.5～8.0 MPas, temperature are that 350～400 ℃, hydrogen to oil volume ratio are 400～800: 1, liquid hourly space velocity is 0.4～1.0 hour
-1
4,, it is characterized in that the admission space percentage ratio of described hydrogenation protecting agent, Hydrodemetalation catalyst and Hydrobon catalyst is respectively 2～10%, 10～40% and 50～88% according to the method for claim 1.
5,, it is characterized in that described hydrogenation protecting agent is made up of the gamma-aluminium oxide carrier that diplopore distributes that has of 1.0～5.0 heavy % nickel oxide, 5.5～10.0 heavy % molybdenum oxides and surplus according to the method for claim 1 or 4.
6, according to the method for claim 5, it is characterized in that described gama-alumina precursor with diplopore distribution is hydrated aluminum oxide A and the hydrated aluminum oxide B that is made by alkyl aluminum hydrolysis method and Tai-Ace S 150 method, by 0.7～1.2: 1 weight ratio mixes, and their pore size distribution is respectively:
Hydrated aluminum oxide A hydrated aluminum oxide B
＜50 dusts 95～96% 35～60%
50～100 dusts 2.0～3.0% 21～25%
100～250 dusts 0.5～1.0% 13～15%
250～500 dusts 0.2～0.5% 5.0～6.0%
7, according to the method for claim 1 or 4, it is characterized in that described Hydrodemetalation catalyst consists of: nickel oxide 1.0～5.0 heavy %, molybdenum oxide 5～15 heavy %, all the other are the carrier gama-alumina, the pore size distribution of this catalyzer mainly concentrates on 100～200 dusts, and the pore volume of 100～200 dusts accounts for 50～90% of total pore volume.
8, method according to claim 1 or 4, it is characterized in that described Hydrobon catalyst consists of: 1～5 heavy % nickel oxide, 12～35 heavy % Tungsten oxide 99.999s, 1～9 heavy % fluorine and surplus aluminum oxide, this aluminum oxide is to be composited by one or more little porous aluminum oxides and one or more macroporous aluminium oxides weight ratio according to 75: 25～50: 50, the pore volume of these aperture aluminum oxide median pore diameter＜80 dusts accounts for total pore volume more than 95%, the pore volume of these macroporous aluminium oxide median pore diameter 60～600 dusts accounts for total pore volume more than 70%, and described pore volume is measured with B E T Brunauer Emett Teller method of nitrogen adsorption at low temperature.
9,, it is characterized in that the precursor of aperture and macroporous aluminium oxide in the described Hydrobon catalyst is respectively a diaspore content greater than 60% with greater than 50% hydrated aluminum oxide according to the method for claim 8.
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