CN1015638B - Low-pressure hydrodenitrogenation catalyst for petroleum distillate oil - Google Patents
Low-pressure hydrodenitrogenation catalyst for petroleum distillate oilInfo
- Publication number
- CN1015638B CN1015638B CN 87101410 CN87101410A CN1015638B CN 1015638 B CN1015638 B CN 1015638B CN 87101410 CN87101410 CN 87101410 CN 87101410 A CN87101410 A CN 87101410A CN 1015638 B CN1015638 B CN 1015638B
- Authority
- CN
- China
- Prior art keywords
- oil
- catalyzer
- hydrogenation
- catalyst
- present
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
- 239000003054 catalyst Substances 0.000 title claims abstract description 22
- 239000003209 petroleum derivative Substances 0.000 title 1
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 30
- 238000000034 method Methods 0.000 claims abstract description 20
- 238000002360 preparation method Methods 0.000 claims abstract description 15
- 239000002994 raw material Substances 0.000 claims abstract description 10
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims abstract description 4
- 229910052708 sodium Inorganic materials 0.000 claims abstract description 4
- 239000011734 sodium Substances 0.000 claims abstract description 4
- 239000003292 glue Substances 0.000 claims description 6
- 239000000126 substance Substances 0.000 claims description 4
- 238000005406 washing Methods 0.000 claims description 4
- 239000004480 active ingredient Substances 0.000 claims description 3
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 claims description 3
- 238000001914 filtration Methods 0.000 claims description 3
- 229910001388 sodium aluminate Inorganic materials 0.000 claims description 3
- 229910052750 molybdenum Inorganic materials 0.000 claims description 2
- 229910052759 nickel Inorganic materials 0.000 claims description 2
- 229910052698 phosphorus Inorganic materials 0.000 claims description 2
- 239000000969 carrier Substances 0.000 claims 1
- 239000003208 petroleum Substances 0.000 claims 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 abstract description 24
- 239000002283 diesel fuel Substances 0.000 abstract description 9
- 230000008569 process Effects 0.000 abstract description 6
- 239000003350 kerosene Substances 0.000 abstract description 4
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 abstract description 3
- 230000008901 benefit Effects 0.000 abstract description 3
- 238000003763 carbonization Methods 0.000 abstract description 3
- 238000007670 refining Methods 0.000 abstract description 3
- 239000003344 environmental pollutant Substances 0.000 abstract 2
- 231100000719 pollutant Toxicity 0.000 abstract 2
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 abstract 1
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 abstract 1
- 229910017604 nitric acid Inorganic materials 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 35
- 230000000694 effects Effects 0.000 description 9
- 239000000243 solution Substances 0.000 description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 229910018104 Ni-P Inorganic materials 0.000 description 6
- 229910018536 Ni—P Inorganic materials 0.000 description 6
- 239000005864 Sulphur Substances 0.000 description 6
- 235000011089 carbon dioxide Nutrition 0.000 description 6
- 238000012360 testing method Methods 0.000 description 6
- 238000004821 distillation Methods 0.000 description 5
- 229910052739 hydrogen Inorganic materials 0.000 description 5
- 239000001257 hydrogen Substances 0.000 description 5
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 238000005299 abrasion Methods 0.000 description 4
- 238000001035 drying Methods 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 229910017318 Mo—Ni Inorganic materials 0.000 description 3
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 3
- -1 Sulphur alkene Chemical class 0.000 description 3
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- 239000004115 Sodium Silicate Substances 0.000 description 2
- CKUAXEQHGKSLHN-UHFFFAOYSA-N [C].[N] Chemical group [C].[N] CKUAXEQHGKSLHN-UHFFFAOYSA-N 0.000 description 2
- CKQGJVKHBSPKST-UHFFFAOYSA-N [Ni].P#[Mo] Chemical compound [Ni].P#[Mo] CKQGJVKHBSPKST-UHFFFAOYSA-N 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 229910052681 coesite Inorganic materials 0.000 description 2
- 229910052906 cristobalite Inorganic materials 0.000 description 2
- 239000008367 deionised water Substances 0.000 description 2
- 229910021641 deionized water Inorganic materials 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 235000019634 flavors Nutrition 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 229910000008 nickel(II) carbonate Inorganic materials 0.000 description 2
- ZULUUIKRFGGGTL-UHFFFAOYSA-L nickel(ii) carbonate Chemical compound [Ni+2].[O-]C([O-])=O ZULUUIKRFGGGTL-UHFFFAOYSA-L 0.000 description 2
- KBJMLQFLOWQJNF-UHFFFAOYSA-N nickel(ii) nitrate Chemical compound [Ni+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O KBJMLQFLOWQJNF-UHFFFAOYSA-N 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- 235000012239 silicon dioxide Nutrition 0.000 description 2
- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical compound [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 description 2
- 229910052911 sodium silicate Inorganic materials 0.000 description 2
- 229910052682 stishovite Inorganic materials 0.000 description 2
- 229910052905 tridymite Inorganic materials 0.000 description 2
- 101000767534 Arabidopsis thaliana Chorismate mutase 2 Proteins 0.000 description 1
- 238000006424 Flood reaction Methods 0.000 description 1
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical group [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 1
- 229910017313 Mo—Co Inorganic materials 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- 101000986989 Naja kaouthia Acidic phospholipase A2 CM-II Proteins 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- 240000007594 Oryza sativa Species 0.000 description 1
- 235000007164 Oryza sativa Nutrition 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 239000004698 Polyethylene Substances 0.000 description 1
- 229910004298 SiO 2 Inorganic materials 0.000 description 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- ABXSJIXCMARDGV-UHFFFAOYSA-N [N].[Br] Chemical compound [N].[Br] ABXSJIXCMARDGV-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- 238000007598 dipping method Methods 0.000 description 1
- 230000005183 environmental health Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000001125 extrusion Methods 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000000796 flavoring agent Substances 0.000 description 1
- 238000007429 general method Methods 0.000 description 1
- 229920001903 high density polyethylene Polymers 0.000 description 1
- 239000004700 high-density polyethylene Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 238000004898 kneading Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000011733 molybdenum Substances 0.000 description 1
- JKQOBWVOAYFWKG-UHFFFAOYSA-N molybdenum trioxide Chemical compound O=[Mo](=O)=O JKQOBWVOAYFWKG-UHFFFAOYSA-N 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000003908 quality control method Methods 0.000 description 1
- 235000009566 rice Nutrition 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 238000002791 soaking Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Hydrogenation catalyst and carrier gamma-Al used in oil refining industry2O3The traditional method is a nitric acid method, an aluminum trichloride method, an aluminum sulfate method and the like, pollutants are discharged in the process, and the cost is higher. The invention adopts a carbonization method, and the raw materials of sodium metaaluminate and CO2The catalyst has the advantages of low price, easy obtainment, simple process, no pollutant discharge in the process, low carrier cost which is only 1/4 of a common method, and higher catalyst strength. Besides diesel oil hydrogenation, the catalyst can also be applied to preparation of pentane oil by hydrogenation of shifting head oil and hydrofining of kerosene and wax oil.
Description
The invention belongs to a kind of catalyzer of chemical field, be widely used in the unifining process of multiple oil products such as diesel oil of petroleum refining industry.
Technical background: the carrier of this hydrogenation catalyst is γ-Al
2O
3, continue to use the preparation of nitrate method, alchlor process abroad always, the 60-70 age is brought into use methods such as Tai-Ace S 150 again, domesticly brings into use the Tai-Ace S 150 legal system to be equipped with carrier γ-Al that hydrogenation is used again the eighties
2O
3, as the Mo-Ni-P catalyzer of refinery, Chang Ling, this several method prepares γ-Al
2O
3Its advantage is respectively arranged, but all exist the bigger shortcoming of pollution in the preparation process, particularly preceding two kinds, soda acid decomposes emits a large amount of obnoxious flavoures, very unfavorable to operator and environmental health; γ-the Al of a kind of method preparation in back
2O
3Carrier, sulfate radical content are also higher, and cost is also than higher.In addition, also relevant for the report of Carbonization Preparation hydrogenation with carrier, as US3,285,860, but do not announce specific embodiment.
The objective of the invention is to reduce the pollution in the preparation process, and reduce cost, simplify technological process, because use the Carbonization Preparation carrier, can not emit obnoxious flavour, the CO2 raw material is easy to get, inexpensive, the applied value height, Application of Catalyst of the present invention field is also very extensive, except that can be applicable to the diesel oil hydrogenation denitrogenation, also produces pentane oil applicable to the tops hydrogenation and handles up to the hydrodenitrification of the so wide fraction oil of kerosene, wax oil.
The present invention's general introduction:
Support of the catalyst γ of the present invention-Al
2O
3Preparation be to adopt carborization, raw material is sodium metaaluminate and CO2, adds minor amount of silicon, is a kind of unbodied silica-alumina supports, active ingredient is molybdenum, nickel, phosphorus.The preparation method is as follows: will be diluted to 10-50g Al
2O
3The sodium aluminate solution of/l places into that (best concentration is 10-40g Al in the glue jar
2O
3/ l), controlled temperature 5-35 ℃, (preferably 10-30 ℃ of scope), the CO2 gas that feeds 20-50% concentration carries out neutralization reaction, (the best concentration range of CO2 is 30-40%), during the preparation silica-alumina supports, add sodium silicate solution, make SiO2 content in carrier, account for 2%, stop into glue when controlling best PH=10-12, then through filtration, washing, the drying of ordinary method, be crushed to about 180 orders, batching kneading, extruded moulding, drying roasting more promptly get catalyst carrier for hydrgenating.Above-mentioned carrier carries out the conventional bubble that gives with water purification again, and floods in the mixed solution of certain density basic nickel carbonate, molybdic oxide and phosphoric acid (concentration 1-5g/100ml), obtains the Mo-Ni-P active ingredient, and drying, roasting obtain hydrogenation catalyst again.
The physico-chemical property of hydrogenation catalyst of the present invention sees Table one.
Table one: catalyzer physico-chemical property (lab scale)
Catalyzer the present invention
Project
The shape bar shaped
Granularity (millimeter) φ 1.5
Change MoO
318-22
Learn NiO 3-5
Group P 2-3
Become SiO
2Account for carrier 2%
Heavy % Al
2O
3Surplus
Thing pore volume milliliter/gram 0.450
Reason specific surface rice/gram 203.9
Property bulk density grams per milliliter 0.88
Matter intensity kilogram/9.4
The effect of invention: not only inexpensive cost is low because raw material is easy to get for catalyzer of the present invention, and has simplified technology, and sodium metaaluminate goes on foot into glue with carbonic acid gas employing one and gets final product, and does not need two step or three steps of other technology; The filtration of carrier and washing are only with once meeting the demands, and other method then needs to carry out 4-5 time, waste time and energy, and also need to consume 1.5 times deionized water than method of the present invention more.Therefore carrier cost of the present invention only is 1/4 of a general method.Catalyst strength is also little than higher (9.4-12Kg/) abrasion, when 3000 change, uses CM-2 particle abrasion test instrument to measure, and abrasion are 0, and are better than N-22 type (6Kg/) intensity.(0.9%, under same test condition) abrasion than domestic Mo-Ni-P catalyzer are little.
Show that by hydrofining industrial practice and experiment therefore the hydrodenitrogenationactivity activity of Mo-Ni component selects the hydrogenation component of Mo-Ni as catalyzer for use than Mo-Co height, and in preparation Mo-Ni solution, add H
3PO
4, obtain the steeping fluid of Mo-Ni-P mixed solution as catalyzer, studies show that much this solution has following advantage as the steeping fluid of catalyzer: 1) solution-stabilized.2) the metal concentration variable range is big.3) the solution readjustment is used very convenient again.4) because of adopting nickelous carbonate, and do not adopt nickelous nitrate, so pollution-free during the catalyzer roasting, preparation process is seen embodiment 1:
Embodiment 1: with concentration is 40gAl
2O
3The sodium aluminate solution of/l places in the glue jar, 30 ℃ of controlled temperature, feed the CO2 gas of concentration 40%, add a certain amount of sodium silicate solution, make carrier contain SiO2 2%, needs according to the preparation aluminum oxide, control stops into glue when reaching PH=10, slurries wear out (or not aging), filter then, with deionized water washing, dry (120 ℃), the batching extrusion becomes the trilobal type after being crushed to 180 orders again, dry under 120 ℃ again, activation (550 ℃) promptly gets required alumina supporter.
The carrier for preparing is carried out bubble give processing, immerse in the Mo-Ni-P mixing solutions for preparing in advance (strength of solution MoO then
320g/100ml, Ni 3g/100ml, P 3g/100ml) dipping time 1 hour, carry out drying (120 ℃) after soaking, under 480 ℃, carry out roasting again, be the catalyzer finished product.
Application of Catalyst wide range of the present invention, except can being used in the diesel oil hydrogenation denitrogenation, can also be used in from the hydrofining of tops, kerosene up to the so wide various fraction oil of wax oil, below each table be embodiment and the effect that catalyzer of the present invention is used for different oil hydrogenations.
(1) diesel oil hydrogenation denitrification refining: catalyzer of the present invention is in the diesel oil hydrogenation process, and the performance comparison with U.S. N-22 type and Chang Ling 2#Mo-Ni-P catalyzer sees Table two.
Table two, triumph catalytic diesel oil hydrogenation comparative test result
Catalyst temperature total pressure volume space velocity hydrogen-oil ratio sulphur basic nitrogen total nitrogen bromine valency g
℃ Kg/cm
2The time
-1(V) heavy % ppm ppm Br/100g
Catalyzer 360 40 2.5 400 0.0142 6.1 157 10.41 of the present invention
N-22 360 40 2.5 400 0.0154 6.3 166 10.13
Chang Ling 2# molybdenum nickel phosphorus 360 40 2.5 400 0.0230 7.2 228 10.75
Triumph catalytic diesel oil // // 0.498 65.9 463.8 26.42
By table two result as can be seen, catalyzer of the present invention is a raw material with the triumph catalytic diesel oil, and its desulfurization, denitrogenation, alkene saturability have reached U.S. N-22 levels of catalysts, surpass the level of Chang Ling, Hunan refinery 2# molybdenum nickel phosphorus.
We show by the test to activity of such catalysts of the present invention stability and oil stability, and catalyzer of the present invention reaches or is better than foreign similar catalyst level (not tabulating at this).
(2) catalyzer of the present invention is applied in the hydrofining of shifting block oil and produces pentane oil, sees Table three.
Table three: catalyzer of the present invention is produced the industrial hydrogenation result of pentane oil
Raw material: reformation shifting block oil hydrofined oil
Sulphur alkene acidity sulphur alkene acidity
（ppm） （PPm） （ppm） （ppm） （ppm） （ppm）
8.4 1975 31.5 2.6 7.6 1.22
6.2 1197 40.1 2.9 7.6 0.92
4.9 2525 5.49 2.3 6.9 0.92
24.3 4892 50.4 2.95 7.2 1.07
Pentane oil ingredient requirement pentane oil production quality control index
＜15 ＜1400 ＜10 ＜5 ≤500 ≤2
Table three result as seen, although the foreign matter content that the pentane oil raw material has surpasses specified requirement, but the foreign matter content of hydrofined oil satisfies the product quality indicator requirement fully, illustrate that the refining ability of hydrogenation catalyst of the present invention has certain elasticity, satisfy the hydrorefined requirement of pentane oil fully, its hydrogenation activity is better.
The reaction conditions of hydrogenation: total pressure: 15Kg/cm
2, temperature of reaction 180-210 ℃, volume space velocity: 1.0
-1Hydrogen to oil volume ratio 100: 1.
Pentane oil is the used a kind of solvent of low-pressure high-density polyethylene preparation catalyzer, its specification of quality is very high, the pentane oil product all has certain requirement to sulphur, acidity, alkene, water purity etc., table three data can illustrate uses catalyzer of the present invention to produce pentane oil, impurity in the stock oil is required and can relax, active stability also is confirmed in trial production, comes into operation in the pentane oil production of Qilu Petrochemical company, and the polyethylene device condition of driving successfully to provide is provided.
(3) kerosene hydrogenation can use catalyzer of the present invention, does not give an example at this.
(4) use at wax oil hydrogenation: catalyzer of the present invention contrasts with the 3722 type catalyzer that oil three factories produce, and hydrodesulfurization activity slightly is better than 3722 type catalyzer as can be seen, sees Table four, table five.
Table four: catalyzer of the present invention and 3722 type catalyst hydrogenation comparative test result
(hydrogen dividing potential drop 6.374 * 10
6Pa(65Kg/cm
2) hydrogen to oil volume ratio 500: 1)
Project temperature air speed (time
-1) proportion sulphur alkali nitrogen total nitrogen carbon residue＜350 ℃
Title ℃ volume weight d
Ppm ppm ppm weight % volume %
Raw material isolated island ///0.9250 10,320 877 1,764 0.37 1.5
Second line of distillation
The present invention 360 0.5 0.56 0.9002 304 209 591 0.05 3.0
Catalyzer
3722 360 0.5 0.40 0.8989 431 188 535 0.05 3.2
The present invention 380 0.5 0.56 0.8912 115 60 272 0.05 11.5
Catalyzer
3722 380 0.5 0.40 0.8922 254 81 302 0.053
The present invention 380 1.0 1.12 0.8989 199 197 725 0.075 6.5
Catalyzer
3722 380 1.0 0.80 0.9010 440 255 819 0.070 5.0
The present invention 390 1.5 1.67 0.9017 374 285 923 0.033 5.1
Catalyzer
3722 390 1.5 1.20 0.9007 518 274 874 0.035
As seen table four result is raw material with isolated island axle two wires, under the identical condition of volume space velocity, the present invention's's (industry) hydrodesulfurization activity slightly is better than 3722 catalyzer, denitrification activity is suitable, pitot meter by weight, and the weight space velocity of catalyzer of the present invention is greater than 3722 catalyzer.
Table five: the present invention's (industry) and 3722 catalyst hydrogenation comparative test result
＜hydrogen dividing potential drop 6.374*10
6Pa(65Kg/cm
2) hydrogen to oil volume ratio 500: 1
The temperature air speed (time
-1) proportion sulphur alkali nitrogen total nitrogen carbon residue＜350 ℃
℃ volume weight d
Ppm ppm ppm weight % volume %
The isolated island second line of distillation:
Triumph wax tailings // 0.9122 5,900 1,335 3,205 0.32 2.5
(27:21 is heavy)
Catalyzer 390 1.0 1.1 0.3826 129 154 858 0.05 of the present invention
3722 390 1.0 0.79 0.8853 232 186 959 0.06
Table five is the result show, catalyzer of the present invention is used for the mixed gatch hydrogenation of isolated island second line of distillation wax oil and triumph wax tailings (27: 21 weights), and its desulfurization, denitrification activity slightly are better than 3722 catalyzer, and weight space velocity is big 0.31 o'clock
-1
Table four-five is the result show, for hydrogenation fraction oil, the hydrogenating materials oil quality is poor more, and the hydrogenation adaptability of catalyzer of the present invention is good more.Catalyzer of the present invention is used for isolated island second line of distillation wax oil, the mixing oil of isolated island second line of distillation wax oil and triumph wax tailings, and its hydrogenation adaptability is slightly better than 3722 catalyzer.
Claims (3)
1, a kind of petroleum cuts oil low-voltage hydrogenation denitrification catalyst, carrier is γ-Al
2O
3, active ingredient is Mo, Ni, P, the chemical constitution of this catalyzer is MoO
318-22 (Wt) %, NiO3-5 (Wt) %, P2-3 (Wt) % is characterized in that at preparation γ-Al
2O
3During carrier, the raw material sodium aluminate solution is diluted to 10-50gAl
2O
3/ L, feeding concentration in the time of 5-35 ℃ is the CO of 20-50% (V)
2Gas adds the SiO of about 2% vehicle weight
2, be under the condition of 10-12 at 10-30 ℃ of PH, employing one goes on foot into the method for glue, filtration and washing.
2, according to the catalyzer of claim 1, when it is characterized in that preparing carriers, the concentration of used sodium metaaluminate is 10-40gAl
2O
3/ L.
3, according to the catalyzer of claim 1 or 2, the hydrofining of various fraction oil in it can be used for from tops to the wax oil scope.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 87101410 CN1015638B (en) | 1987-11-22 | 1987-11-22 | Low-pressure hydrodenitrogenation catalyst for petroleum distillate oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 87101410 CN1015638B (en) | 1987-11-22 | 1987-11-22 | Low-pressure hydrodenitrogenation catalyst for petroleum distillate oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1033285A CN1033285A (en) | 1989-06-07 |
| CN1015638B true CN1015638B (en) | 1992-02-26 |
Family
ID=4813399
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 87101410 Expired CN1015638B (en) | 1987-11-22 | 1987-11-22 | Low-pressure hydrodenitrogenation catalyst for petroleum distillate oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1015638B (en) |
Families Citing this family (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1043359C (en) * | 1994-11-25 | 1999-05-12 | 中国石化齐鲁石油化工公司 | Hydrocarbon hydrodesulfurization catalyst and preparation method thereof |
| CN1041430C (en) * | 1995-05-06 | 1998-12-30 | 中国科学院山西煤炭化学研究所 | Hydro-treated catalyst and preparation method thereof |
| CN1044378C (en) * | 1996-06-28 | 1999-07-28 | 中国石油化工总公司 | Catalyst for hydro-processing heavy distillate |
| CN1107534C (en) * | 2000-05-19 | 2003-05-07 | 中国石油化工集团公司 | Prepn. of titanium-containing aluminium bydroxide |
| CN1331605C (en) * | 2004-10-29 | 2007-08-15 | 中国石油化工股份有限公司 | Alumina support containing silicon and titanium and preparation method thereof |
| CN100388973C (en) * | 2005-04-29 | 2008-05-21 | 中国石油化工股份有限公司 | Modified alumina composition and preparation thereof |
| CN101927194B (en) * | 2010-08-30 | 2011-11-09 | 淄博泰通催化技术有限公司 | Preparation method of aluminum hydroxide powder containing lanthanum, phosphorus and titanium elements |
| CN101912786A (en) * | 2010-08-30 | 2010-12-15 | 淄博泰通催化技术有限公司 | Method for preparing aluminum hydroxide powder containing lanthanum-phosphorus elements |
| CN101940956B (en) * | 2010-08-30 | 2011-11-23 | 淄博泰通催化技术有限公司 | Preparation method of aluminum hydroxide powder containing lanthanum element |
| CN102451707B (en) * | 2010-10-15 | 2015-07-22 | 中国石油化工股份有限公司 | Method for preparing hydrotreating catalyst composition |
| CN103055924B (en) * | 2011-10-21 | 2015-02-25 | 中国石油化工股份有限公司 | Preparation method of bulk phase hydrocracking catalyst |
| CN103055922B (en) * | 2011-10-21 | 2015-05-13 | 中国石油化工股份有限公司 | Preparation method of bulk phase hydrocracking catalyst |
| CN103055927B (en) * | 2011-10-21 | 2015-02-25 | 中国石油化工股份有限公司 | Preparation method of hydrocracking catalyst |
| CN103055925B (en) * | 2011-10-21 | 2015-04-01 | 中国石油化工股份有限公司 | Preparation method of hydrocracking catalyst composition |
-
1987
- 1987-11-22 CN CN 87101410 patent/CN1015638B/en not_active Expired
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| Publication number | Publication date |
|---|---|
| CN1033285A (en) | 1989-06-07 |
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