CN1335361A - Method and Catalyst for Selective Hydrodesulfurization of Cracked Gasoline - Google Patents
Method and Catalyst for Selective Hydrodesulfurization of Cracked Gasoline Download PDFInfo
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- CN1335361A CN1335361A CN 01131460 CN01131460A CN1335361A CN 1335361 A CN1335361 A CN 1335361A CN 01131460 CN01131460 CN 01131460 CN 01131460 A CN01131460 A CN 01131460A CN 1335361 A CN1335361 A CN 1335361A
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- hours
- catalyzer
- catalyst
- hydrotalcite
- cracked gasoline
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- 238000000034 method Methods 0.000 title claims description 20
- 239000003054 catalyst Substances 0.000 title abstract description 26
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 12
- 238000006243 chemical reaction Methods 0.000 claims abstract description 7
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 7
- 239000001257 hydrogen Substances 0.000 claims abstract description 7
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 6
- 239000007791 liquid phase Substances 0.000 claims abstract description 4
- 238000006477 desulfuration reaction Methods 0.000 claims description 21
- 230000023556 desulfurization Effects 0.000 claims description 21
- 229910052751 metal Inorganic materials 0.000 claims description 12
- 239000002184 metal Substances 0.000 claims description 12
- GDVKFRBCXAPAQJ-UHFFFAOYSA-A dialuminum;hexamagnesium;carbonate;hexadecahydroxide Chemical compound [OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[Mg+2].[Mg+2].[Mg+2].[Mg+2].[Mg+2].[Mg+2].[Al+3].[Al+3].[O-]C([O-])=O GDVKFRBCXAPAQJ-UHFFFAOYSA-A 0.000 claims description 10
- 229960001545 hydrotalcite Drugs 0.000 claims description 10
- 229910001701 hydrotalcite Inorganic materials 0.000 claims description 10
- 239000000203 mixture Substances 0.000 claims description 7
- 238000002360 preparation method Methods 0.000 claims description 7
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 6
- 239000002131 composite material Substances 0.000 claims description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- 239000012071 phase Substances 0.000 claims description 4
- 238000007598 dipping method Methods 0.000 claims description 3
- 239000007789 gas Substances 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 claims description 3
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 claims description 2
- 229910002651 NO3 Inorganic materials 0.000 claims description 2
- 239000002253 acid Substances 0.000 claims description 2
- 238000001354 calcination Methods 0.000 claims description 2
- 238000013461 design Methods 0.000 claims description 2
- 238000000227 grinding Methods 0.000 claims description 2
- 238000007654 immersion Methods 0.000 claims description 2
- 239000004615 ingredient Substances 0.000 claims description 2
- NHNBFGGVMKEFGY-UHFFFAOYSA-N nitrate group Chemical group [N+](=O)([O-])[O-] NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims description 2
- 239000012266 salt solution Substances 0.000 claims description 2
- 150000001336 alkenes Chemical class 0.000 abstract description 13
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 abstract description 13
- 238000005516 engineering process Methods 0.000 abstract description 9
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 abstract description 6
- 239000003208 petroleum Substances 0.000 description 14
- 239000000047 product Substances 0.000 description 8
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 7
- 239000005864 Sulphur Substances 0.000 description 5
- 239000003921 oil Substances 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 239000000523 sample Substances 0.000 description 3
- 229920006395 saturated elastomer Polymers 0.000 description 3
- 238000005303 weighing Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 239000012188 paraffin wax Substances 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 229910018516 Al—O Inorganic materials 0.000 description 1
- 241000640882 Condea Species 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- 238000006424 Flood reaction Methods 0.000 description 1
- 239000004480 active ingredient Substances 0.000 description 1
- 239000008186 active pharmaceutical agent Substances 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- APUPEJJSWDHEBO-UHFFFAOYSA-P ammonium molybdate Chemical compound [NH4+].[NH4+].[O-][Mo]([O-])(=O)=O APUPEJJSWDHEBO-UHFFFAOYSA-P 0.000 description 1
- 229940010552 ammonium molybdate Drugs 0.000 description 1
- 235000018660 ammonium molybdate Nutrition 0.000 description 1
- 239000011609 ammonium molybdate Substances 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000012752 auxiliary agent Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000008367 deionised water Substances 0.000 description 1
- 229910021641 deionized water Inorganic materials 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000001125 extrusion Methods 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 238000004231 fluid catalytic cracking Methods 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- -1 nitrogenous compound Chemical class 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- 238000007493 shaping process Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000004230 steam cracking Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052623 talc Inorganic materials 0.000 description 1
- 235000012222 talc Nutrition 0.000 description 1
- 239000000454 talc Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000010977 unit operation Methods 0.000 description 1
Landscapes
- Catalysts (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Compared with the traditional hydrodesulfurization catalyst and hydrogenation technology, the catalyst and the hydrogenation technology have obviously higher hydrodesulfurization selectivity, namely stronger hydrodesulfurization capacity (the hydrodesulfurization rate is 75-95%) and lower olefin saturation (the olefin saturation is 5-20%), and the desulfurized gasoline has less octane number loss (the RON loss is 2-3 units). The pressure in the reaction process is 1-4 MPa, the temperature is 250-350 ℃, and the liquid phase space velocity is 1-10 h－1The volume ratio of hydrogen to oil is 100-500.
Description
The present invention relates to the method and the Preparation of catalysts method of a kind of pressure gasoline (petroleum naphtha) selective hydrodesulfurization, it is to belong in the petroleum chemical industry the improvement and the innovation of light-end products process for refining, exactly is the selective hydrogenation desulfurization process of pressure gasoline in the presence of catalyzer (petroleum naphtha).
As everyone knows, pressure gasoline (petroleum naphtha), particularly catalytically cracked gasoline (petroleum naphtha) or heavy oil fluid catalytic cracking gasoline (petroleum naphtha) contain a large amount of sulphur.The method that reduces sulphur content has: 1) to cracking or the unitary full feedstock hydrofining of coking, 2) to these unitary hydrogenation of net product.First kind of selection is because need huge hydrotreater and consume a large amount of hydrogen, and be costly.Second kind of selection is shortcut but can causes alkene (account for the 20～80v%) saturated of raw material usually, this octane value ((RON+MON)/2) that also can reduce gasoline products reaches 10-20 unit simultaneously.The loss of octane number relevant with desulfurization is a very big impact to the octane value of refinery's gasoline product.The typical technology of previously disclosed relevant pressure gasoline (petroleum naphtha) hydrogenating desulfurization comprises:
1. U.S.Pat.No.4,140,626 (Bertolacini and Sue-A-Quan) have described a kind of selective hydrodesulfurization technology, are supported on the supported catalyst that is accounted for 70wt% by MgO at least with the metal of group vib and VIII family.More particularly, the group vib metal is Mo, and VIII family metal is Co.Catalyzer contains the CoO of 3wt% and the MoO of about 16wt%
3Be supported on the pure MgO carrier.In the hydrogenating desulfurization rate is 75～85%, degree of olefin saturation quite low (≤40wt%), the loss of octane value less (≤2 units).
2. U.S.Pat.No.4,132,632 (Yu and Myers) account for 4～6wt% except metal load is restricted to the group vib metal, and VIII family metal accounts for outside 0.5～2wt%, other very similar above-mentioned patent.And more particularly adopt group vib metal M o and VIII family metal Co.Catalyst I contains the CoO of about 1wt% and the MoO of about 5wt%
3, be supported on the pure MgO carrier.Catalyst I I contains the CoO of about 3wt% and the MoO of about 17wt%
3Carrier comprises the MgO of 80wt% (as above-mentioned U.S.Pat.No.4,140,6626 catalyzer). catalyst I is poorer than the hydrodesulfurization performance of catalyst I I usually, but catalyst I (is about 82～84%) on identical hydrogenating desulfurization level obtains lower degree of olefin saturation and higher octane value than catalyst I I, loss of octane number very little (being about 1.6 units).In addition, for two kinds of catalyzer, research the hydrogenating desulfurization scope in, degree of olefin saturation quite low (≤40wt%), the loss of octane value less (≤2.6 units).
3. (San Antonio in the 1978NPRA meeting, Texas), Coates, Myers and Sue-A-Quan have delivered the paper that is entitled as " the pressure naphtha hydrogenating desulfurization of minimal octane value loss ", have illustrated the bright prospect that Amoco is referred to as " selectivity superrefining technology ".This paper is delivered about above-mentioned patent issue the previous year.This paper is mentioned two kinds of catalyzer (probably deriving from above-mentioned two patents), and wherein selective desulfurization is the technical characterictic of this technology.Raw catalyst shows low inactivation rate than conventional hydrotreating catalyst aspect hydrogenating desulfurization.The hydrogenating desulfurization rate is that the loss value of 90% o'clock octane value be it is said 4 MON or 4.5 RON.The loss of octane number of mentioning in the document is more much higher than Amoco later patents.
4. GB2,225,731 issued contain VIB, VIII family metal hydrogenation composition homogeneous phase is supported on and contains MgO and Al
2O
3Hydrotreating catalyst on the carrier.The Mg/Al mol ratio is 3～10/1.It is said, this catalyzer be supported on Al
2O
3On similar catalyzer suitable hydrodesulfurization activity is arranged.
Purpose of the present invention provides a kind of method and Preparation of catalysts method that is used for pressure gasoline (petroleum naphtha) selective hydrodesulfurization with regard to being to avoid above-mentioned the deficiencies in the prior art part.Its major technology characteristics are exactly by the special-purpose Hydrobon catalyst of purchasing in advance, again will pending stock oil get final product in the reactor by catalyzer formation bed thus.
Its major ingredient of this catalyzer is CoO+MoO, K
2O, CuO, be the MgAlO composite oxides and and the Al of presoma with the hydrotalcite
2O
3, the weight ratio of its each component is: CoO+MoO: 6～20%; K
2O: 0～5%; CuO: 0～5%; With the hydrotalcite is the MgAlO composite oxides of presoma: 30～95%; Al
2O
3: 0～80%.
The gas phase hydrogenation process is then adopted in the selective hydrodesulfurization of pressure gasoline, promptly adopts above-mentioned special-purpose catalyst, and the reaction pressure of its process is 1～4MPa, and temperature of reaction is 250～350 ℃, and the liquid phase air speed is 1～10h
-1, hydrogen to oil volume ratio is 100～500.Use fluidized-bed or ebullated bed as much as possible, preferably fixed bed.
Below in conjunction with embodiment in detail technical characterstic of the present invention is described in detail:
(1). on Preparation of catalysts, its main step is as follows:
1. the carrier of purchasing: with hydrotalcite Mg
aAl
bCO
3(OH)
c.nH
2O, aluminium oxide Al
2O
3, water and acid, behind the mixed grinding, its mixture is forged or is pushed bar to form by the size of design requirements, 80～150 ℃ dry 10～30 hours down, then at 400～600 ℃ of following roasting 2～8h;
2. adopt the metal salt solution immersion process for preparing, used metal-salt is nitrate or carbonate, and dipping time is 6～12 hours
3. calcination process: maturing temperature is that 300～600 ℃, time are 2～8 hours; Preferably maturing temperature is that 400～500 ℃, time are 4～6 hours.
4. sulfidizing: curing temperature is 260～350 ℃, and curing time is 8～48 hours, and hydrogen to oil volume ratio is 100～50
(2). in the selection of stock oil, mainly be pressure gasoline (petroleum naphtha), can be pressure gasoline or petroleum naphtha, catalytically cracked gasoline or petroleum naphtha, coker gasoline or petroleum naphtha, the gasoline of ethylene production steam cracking or petroleum naphtha, the full range pressure gasoline (petroleum naphtha) that normally from cracking and coking unit operation, gets.Can contain 3～80% alkane, 1～80% alkene, 3～80% naphthenic hydrocarbon, 3～80% aromatic hydrocarbons and a small amount of sulfur-bearing and nitrogenous compound, its cut scope can be 25～225 ℃, also can be any cut that cuts in above scope.Wherein, sulphur content can be 100～20000ppm, and nitrogen content can be 20～2000ppm.
(3). in the use of reactor, possible use fluidized-bed or ebullated bed, preferably fixed bed although mainly be.
According to three above principles, the present invention is carried out implementation and operation, obtain following result:
Embodiment 1
Take by weighing SB powder (the German Condea product γ-Al of company of 30g
2O
3) or hydrotalcite or the mixture of the two, with the HNO of 30ml water and 0.9g
3Mix, on the catalyzer extrusion shaping machine, be extruded into the bar of diameter 1.6mm, under infrared lamp, behind the dry 5h, put in the baking oven following dry 10 hours at 120 ℃, in 500 ℃ of following roasting 5h, last porphyrize sieves out 20～40 purpose catalyst carrier particles in muffle furnace.
Embodiment 2
Take by weighing γ-Al with the method preparation of example 1
2O
3Carrier 12 g takes by weighing the Co (NO of 1.2g
3)
2.7H
2O pours carrier in the solution into the deionized water dissolving of 8g, dipping 12h, and drying is 10 hours under 120 ℃, then 500 ℃ of roasting 5h.According to above-mentioned steps with 12% MoO in the ammonium molybdate load
3, make catalyst I.Embodiment 3
Preparation process is with embodiment 2, just on the catalyzer also load 2% K
2O, this is catalyst I I.
Embodiment 4
Prepare the support of the catalyst of SB powder/hydrotalcite=1/3 with the method among the embodiment 1, and flood CoO, MoO respectively according to the method among the embodiment 2
3And K
2O makes catalyst I II.
Embodiment 5
Is the catalyzer of carrier with the preparation of the method among the embodiment 1 with the pure water talcum, and floods CoO, MoO respectively according to the method in the example 2
3And K
2O makes catalyst I V.
The general moiety of various catalyzer is as described in Table 1.
The composition of table 1 catalyzer
| Catalyzer | Carrier | Active ingredient | Charge capacity |
| ????I | ????γ-Al 2O 3 | ????Co，Mo | ?CoO＋MoO 3＝16％ ????K 2O＝2％， ???Co∶Mo＝1∶3 |
| ????II | ????γ-Al 2O 3 | ????Co，Mo，K | |
| ????III | Hydrotalcite/γ-Al 2O 3＝3/1 | ????Co，Mo，K | |
| ????IV | Hydrotalcite | ????Co，Mo，K |
The character that the used typical pressure gasoline raw material properties of hydrotreatment can be come description list 2 raw material FCC gasoline by table 2
| Sample | The FCC raw material |
| Normal paraffin (%) | ????4.29 |
| Isoparaffin (%) | ????20.29 |
| Alkene (%) | ????39.72 |
| Naphthenic hydrocarbon (%) | ????6.68 |
| Aromatic hydrocarbons (%) | ????22.41 |
| ????RON | ????94.28 |
| ????MON | ????87.52 |
| ????(RON＋MON)/2 | ????90.90 |
| Sulphur content (ppm) | ????1203 |
Each catalyst system of embodiment 2～5 all carries out the hydrogenating desulfurization test on anti-in that high pressure is little.Catalyzer is finely ground to 20～40 order sizes, with the 16ml catalyzer reactor of packing into, respectively 260 ℃, 280 ℃, 300 ℃ following times with containing 3v%CS
2Straight-run spirit prevulcanized 12h.Under probe temperature, feed FCC gasoline.Sampling analysis after 10 hours is carried out in reaction.The type reaction condition is: 260～300 ℃ of temperature, pressure 2.0Mpa, liquid air speed 3.75h
-1, hydrogen to oil volume ratio 180.
Among each embodiment, indicated 1) hydrogenating desulfurization percentage (this with feed sulfur to remove quality percentage relevant); 2) degree of olefin saturation (demonstration in the raw material) by the quality percentage of saturated alkene; 3) select the factor (with log (1-HDS%)/Log (1-HYD%) expression); 4) loss of anti-knock index (RON+MON)/2 and octane value, its result is as shown in table 3.Table 3 FCC gasoline selective hydrodesulfurizationmodification test-results
The character of hydrotreatment gained typical products FCC gasoline is as described in Table 4.
| Numbering | Temperature ℃ | Desulfurization degree HDS% | The saturated HYD% of alkene | Selectivity factor | ?(RON＋MON) ????/2 | (RON+MON)/2 loss |
| ???I | ?280 | ????97.8 | ????98.7 | ????0.8 | ????75.8 | ????13.5 |
| ???II | ?260 ?280 ?300 | ????64.2 ????61.9 ????99.0 | ????43.5 ????74.9 ????80.6 | ????1.8 ????0.7 ????2.8 | ????84.1 ????80.6 ????79.8 | ????5.2 ????8.8 ????9.5 |
| ???III | ?260 ?280 ?300 ?320 | ????42.5 ????56.0 ????62.4 ????87.9 | ????11.3 ????30.5 ????22.9 ????43.4 | ????4.6 ????2.3 ????3.8 ????3.7 | ????88.0 ????83.1 ????86.7 ????83.8 | ????2.9 ????7.8 ????4.2 ????7.1 |
| ???IV | ?280 ?300 ?320 | ????24.0 ????59.1 ????74.6 | ????3.0 ????7.0 ????16.1 | ????8.9 ????12.3 ????7.8 | ????87.9 ????87.2 ????86.5 | ????1.4 ????2.1 ????2.9 |
| ???IV- ???1 | ?320 | ????90.1 | ????39.8 | ????4.6 | ????83.7 | ????5.6 |
The composition and property of table 4 product F CC gasoline
| Sample | Product 1 | Product 2 |
| Normal paraffin (%) | ????6.31 | ????7.70 |
| Isoparaffin (%) | ????23.30 | ????24.82 |
| Alkene (%) | ????36.81 | ????33.21 |
| Naphthenic hydrocarbon (%) | ????7.67 | ????8.62 |
| Aromatic hydrocarbons (%) | ????22.63 | ????22.28 |
| ????RON | ????90.33 | ????89.55 |
| ????MON | ????84.03 | ????83.34 |
| ????(RON＋MON)/2 | ????87.18 | ????86.45 |
| Sulphur content (ppm) | ????431 | ????340 |
In sum, can draw as drawing a conclusion:
1. in the temperature and pressure scope of being tested, the technology of the present invention shows higher hydrogenating desulfurization selectivity by physical causes.
2. when carrying out hydroprocessing in conventional liquid phase air speed (LHSV) scope, the technology of the present invention is promised to undertake the target that reaches hydrogenating desulfurization 〉=60%.
3. add the metal K auxiliary agent and can improve the HDS selectivity of catalyst.
4. be the catalyzer of carrier and with modification γ-Al with the Mg-Al-O composite oxides
2O
3For having the active and lower HYD of higher H DS, the catalyzer of carrier leads.
5. be 70% o'clock in hydrogenating desulfurization, the alkene saturation exponent is about 16%, and loss of octane number is 2.9 units.
Claims (4)
1. catalyzer that is used for selective hydrogenation desulfurization of cracked gasoline, its major ingredient is CoO+MoO, K
2O, CuO, be the MgAlO composite oxides and and the Al of presoma with the hydrotalcite
2O
3, it is characterized in that the weight ratio of each component is: CoO+MoO: 6～20%; K
2O: 0～5%; CuO: 0～5%; With the hydrotalcite is the MgAlO composite oxides of presoma: 30～95%; Al
2O
3: 0～80%.
2. the method for a selective hydrogenation desulfurization of cracked gasoline is characterized in that adopting the described catalyzer of claim 1, and adopts the gas phase hydrogenation process, and the reaction pressure of its process is 1～4MPa, and temperature of reaction is 250～350 ℃, and the liquid phase air speed is 1～10h
-1, hydrogen to oil volume ratio is 100～500.
3. the method for selective hydrogenation desulfurization of cracked gasoline according to claim 2 is characterized in that described employing gas phase hydrogenation process should use fluidized-bed, ebullated bed or fixed bed.
4. the catalyzer of hydrogenating desulfurization according to claim 1 is characterized in that should adopting in preparation following steps to realize:
1. the carrier of purchasing: with hydrotalcite Mg
aAlbCO
3(OH) c.nH
2O, aluminium oxide Al
2O
3, water and acid, behind the mixed grinding, its mixture is forged or is pushed bar to form by the size of design requirements, 80～150 ℃ dry 10～30 hours down, then at 400～600 ℃ of following roasting 2～8h;
2. adopt the metal salt solution immersion process for preparing, used metal-salt is nitrate or carbonate, and dipping time is 6～12 hours
3. calcination process: maturing temperature is that 300～600 ℃, time are 2～8 hours; Preferably maturing temperature is that 400～500 ℃, time are 4～6 hours.
4. sulfidizing: curing temperature is 260～350 ℃, and curing time is 8～48 hours, and hydrogen to oil volume ratio is 100～500.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 01131460 CN1335361A (en) | 2001-09-11 | 2001-09-11 | Method and Catalyst for Selective Hydrodesulfurization of Cracked Gasoline |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 01131460 CN1335361A (en) | 2001-09-11 | 2001-09-11 | Method and Catalyst for Selective Hydrodesulfurization of Cracked Gasoline |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1335361A true CN1335361A (en) | 2002-02-13 |
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ID=4670597
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 01131460 Pending CN1335361A (en) | 2001-09-11 | 2001-09-11 | Method and Catalyst for Selective Hydrodesulfurization of Cracked Gasoline |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7556728B2 (en) | 2002-10-10 | 2009-07-07 | Nestel Oil Oyj | Process for the manufacture of a gasoline blending component |
| CN101072849B (en) * | 2003-12-05 | 2012-02-15 | 英特凯特公司 | Gasoline sulfur reduction using hydrotalcite like compounds |
| CN106512984A (en) * | 2016-12-14 | 2017-03-22 | 福州大学 | Preparation method of high-activity diesel hydrodesulfurization catalyst |
| CN106732636A (en) * | 2016-11-25 | 2017-05-31 | 福州大学 | A kind of sulphided state poor oil suspension bed hydrogenation catalyst and its preparation method and application |
| CN107486193A (en) * | 2017-07-18 | 2017-12-19 | 福州大学化肥催化剂国家工程研究中心 | A kind of hydrogenation catalyst and preparation method thereof |
-
2001
- 2001-09-11 CN CN 01131460 patent/CN1335361A/en active Pending
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7556728B2 (en) | 2002-10-10 | 2009-07-07 | Nestel Oil Oyj | Process for the manufacture of a gasoline blending component |
| CN101072849B (en) * | 2003-12-05 | 2012-02-15 | 英特凯特公司 | Gasoline sulfur reduction using hydrotalcite like compounds |
| CN106732636A (en) * | 2016-11-25 | 2017-05-31 | 福州大学 | A kind of sulphided state poor oil suspension bed hydrogenation catalyst and its preparation method and application |
| CN106732636B (en) * | 2016-11-25 | 2019-09-03 | 福州大学 | A kind of sulphided state poor oil suspension bed hydrogenation catalyst and its preparation method and application |
| CN106512984A (en) * | 2016-12-14 | 2017-03-22 | 福州大学 | Preparation method of high-activity diesel hydrodesulfurization catalyst |
| CN106512984B (en) * | 2016-12-14 | 2019-09-13 | 福州大学 | A kind of preparation method of high activity diesel hydrogenation for removal sulphur catalyst |
| CN107486193A (en) * | 2017-07-18 | 2017-12-19 | 福州大学化肥催化剂国家工程研究中心 | A kind of hydrogenation catalyst and preparation method thereof |
| CN107486193B (en) * | 2017-07-18 | 2020-09-08 | 福州大学化肥催化剂国家工程研究中心 | Hydrogenation catalyst and preparation method thereof |
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