CN1594509A - Process for hydrocracking of Fischer-Tropsch synthesized heavy hydrocarbon and/or kettle bottom wax - Google Patents
Process for hydrocracking of Fischer-Tropsch synthesized heavy hydrocarbon and/or kettle bottom wax Download PDFInfo
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- CN1594509A CN1594509A CN 200410012378 CN200410012378A CN1594509A CN 1594509 A CN1594509 A CN 1594509A CN 200410012378 CN200410012378 CN 200410012378 CN 200410012378 A CN200410012378 A CN 200410012378A CN 1594509 A CN1594509 A CN 1594509A
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Abstract
The invention discloses a process for hydrocracking of Fischer-Tropsch synthesized heavy hydrocarbon and/or kettle bottom wax which comprises, mixing waste ferrum based catalyst with heavy weight hydrocarbons and / or kettle bottom wax raw material, mixing with hydrogen, heating to 300-400 deg. C, loading into suspending bed reactor for hydrogenation conversion.
Description
Technical field
The present invention relates to the method for a kind of heavy hydrocarbon and/or kettle bottom wax hydrocracking, relating to Fischer-Tropsch synthesis of heavy hydrocarbon and/or kettle bottom wax specifically is raw material, is the method for light hydrocarbon with heavy hydrocarbon and/or kettle bottom wax hydrocracking by suspended-bed reactor.
Background technology
In petroleum refining process, residual oil lighting technology is subjected to extensive attention, and each major oil companies competitively researchs and develops the hydrogenation of residual oil suspended bed technology, and especially in the lighting process of weight, residual oil, floating bed hydrogenation has unique advantage.There is more than ten kind of suspension bed hydrogenation process to be in pilot scale and industrial demonstration unit stage now, possessed industrialized condition individually.As the combination cracking process (VCC) of German VEBA company exploitation (VEBA-Combi-Cracking), this technology is the hot hydrogenolysis process of a kind of residual oil of high conversion, and under the pressure of 440～485 ℃ and 25MPa, residual oil carries out hydrocracking with One-through design; At 435～455 ℃ with approximately react under the 14MPa, the quality transformation efficiency can reach 90% to Canadian CANMET technology at oil sands bitumen; The sulfuration alum of the Aurabon process using finely powdered of American UOP company exploitation is as catalyzer, carries out hydrogenation reaction under 400～450 ℃ and 14～21MPa pressure.Also have other suspension bed hydrogenation process to be in the development phase.
Existing patent and disclosed heavy, hydrogenation of residual oil suspended bed technology are not reported at ICL for Indirect Coal Liquefaction F-T synthesis of heavy hydrocarbon floating bed hydrogenation transformed technology.In the ICL for Indirect Coal Liquefaction F-T synthetic crude product, have to be the heavy hydrocarbon of boiling point greater than 530 ℃ about 30wt%, this product is mainly straight-chain paraffin and alkene, and a small amount of oxycompound.In addition, in iron-based syrup state bed Fischer Tropsch building-up process, more also have a large amount of heavy hydrocarbons during catalyst changeout and discharge, this part heavy hydrocarbon claims kettle bottom wax again, and it is higher not only to remove boiling point, but also contains a large amount of metallic impurity.Because boiling point, alkene and the solid content of Fischer-Tropsch synthesis of heavy hydrocarbon and/or kettle bottom wax are higher, adopt fixed bed hydrogenation cracking technology, some difficulties are arranged technically.
Summary of the invention
The object of the present invention is to provide a kind of hydrogenating conversion process that is suitable for Fischer-Tropsch synthesis of heavy hydrocarbon and/or kettle bottom wax lighting.This technology can reduce coking yield to greatest extent when processing heavy hydrocarbon, obtain higher hydrogenation conversion.
Hydrogenating conversion process of the present invention comprises the steps:
Is that 0.05～10wt% or the catalyst based add-on of water-soluble Fe are that 100～2000 μ g/g oil mix with catalyst based and Fischer-Tropsch synthesis of heavy hydrocarbon of the catalyst based or water-soluble Fe of pressed powder Fe and/or kettle bottom wax raw material by the catalyst based add-on of pressed powder Fe, enter suspended-bed reactor after being mixed and heated to 300～400 ℃ with hydrogen then, carry out hydrocracking; Perhaps the iron-based spent catalyst is contained in the suspended-bed reactor in advance, add-on is 0.05～15wt%, and Fischer-Tropsch synthesis of heavy hydrocarbon and/or kettle bottom wax and hydrogen enter suspended-bed reactor after being mixed and heated to 300～400 ℃, carry out hydrocracking; The reaction conditions of hydrocracking is that reaction pressure is 3.0～20.0MPa, and the best is 4.0～17.0MPa, and temperature of reaction is 350～500 ℃, and the best is 380～480 ℃, and hydrogen to oil volume ratio is 300～1800, and the best is 600～1500, and the liquid air speed is 0.1～3.0h
-1, the best is 0.3～2.0h
-1
The hydrocracking product is flowed out by the suspended-bed reactor top, entering hot high score separates from system, the vapor phase stream thing of hot high score from the system top enters cold high score from system, the stream thing of cold high score from the system bottom then enters the normal pressure knockout tower and directly isolates product, hot high score heavy component stream thing in system then enters the vacuum fractionation tower, respectively heated up in a steamer the sectional product through decompression separation step by step, hot high score flows tail oil and the residue that thing and suspended-bed reactor bottoms obtain behind cyclone separator from the system bottom, isolated tail oil and wax oil can mix back adding reactor again and carry out conversion reaction with raw material.
Aforesaid Fe base solid powder th-1 catalyst form by the oxide carrier of Fe and refractoriness or Fe and tungsten, molybdenum, cobalt, manganese, iron, titanium, copper, calcium, magnesium, lanthanum and potassium in the oxide carrier of one or more and refractoriness form.
The oxide carrier of described refractoriness is silicon oxide, aluminum oxide or silica-alumina.
Aforesaid Fe base water-soluble catalyst forms by many metals water soluble salt is composite, as iron-nickel catalyzator, iron-cobalt catalyst, iron-Mn catalyst, iron/copper-potassium catalyzer, iron-cobalt-Mn catalyst etc., iron-manganese-copper-potassium catalyzer, iron-nickel-manganese-molybdenum catalyst etc.
Aforesaid Fe base spent catalyst is the iron-based spent catalyst used of Fe base syrup state bed Fischer Tropsch synthetic iron-based spent catalyst, water-gas shift etc.
Aforesaid solid powder th-1 catalyst add-on is 0.05～10wt%.
Aforesaid water-soluble catalyst add-on is 100～2000 μ g/g oil.
Aforesaid iron-based spent catalyst add-on is 0.1～12wt%.
In the method for heavy hydrocarbon of the present invention and/or kettle bottom wax hydrocracking, can mix back circulation cracking again with fresh feed to the processing of isolated wax oil and tail oil, also can adopt once by flow process, promptly raw material is through the freshening that no longer circulates after the hydrocracking.
In the method for heavy hydrocarbon of the present invention and/or kettle bottom wax hydrocracking, the heavy hydrocarbon that uses and/or the boiling point of kettle bottom wax are greater than 530 ℃, mainly form by straight chain hydrocarbon, alkene and a small amount of organic oxygen-containing thing, and kettle bottom wax contains a large amount of metallic impurity, forming and evident difference arranged in nature with traditional heavy, residual oil.
Characteristics of the present invention are:
1. the method for heavy hydrocarbon disclosed by the invention and/or kettle bottom wax hydrocracking at be the Fischer-Tropsch synthetic crude product.
2. method of the present invention is that Fischer-Tropsch synthesis of heavy hydrocarbon and/or kettle bottom wax can once transform by floating bed hydrogenation, also can adopt Recycle design, and promptly tail oil and wax oil can mix back circulation cracking again with raw material.Can be by changing reaction conditions and processing parameter, obtain based on naphtha fraction or based on the product of diesel oil distillate.This method is effective especially for heavy hydrocarbon of being made up of straight chain hydrocarbon, alkene and a small amount of organic oxygen-containing thing and/or kettle bottom wax processing.
3. hydrogenating conversion process of the present invention adopts the catalyst based and Fe base spent catalyst of Fe, and its metal component source is easy to get, and is with low cost, reduces this technology greatly and gets running cost.
4. hydrogenating conversion process of the present invention, heavy hydrocarbon and/or kettle bottom wax lighting reaction conditions gentleness, flexible operation.
Embodiment
Below in conjunction with the device schema embodiments of the present invention are described briefly:
Fig. 1 is a schema of the present invention.
As shown in the figure: the 1st, feeding line 2 is that storage tank 3 is that volume pump 4 is that preheating can 5 is that hydrogen 6 is that suspended-bed reactor 7 is that hot high score is that cold high score is that normal pressure knockout tower 10 is that cyclone separator 11 is that vacuum still 12 is that tail gas 13 is that petroleum naphtha 14 is that diesel oil distillate 15 is that light wax oil 16 is that wax slop 17 is that tail oil 18 is that residue 19 is that tail oil 20 is that residue 21 is circulation cracking pipelines from system 9 from system 8.
Fe base water-soluble catalyst and raw material are mixed at oil storage tank 2, then with hydrogen in advance Enter suspension bed reactor 6 after hot tank 4 Hybrid Heating and carry out hydro-conversion; Perhaps with the useless catalysis of iron-based Agent is contained in the suspension bed reactor 6 in advance, and raw material and hydrogen enter suspension after preheating can 4 Hybrid Heating Bed bioreactor 6 carries out hydro-conversion. Reacted product is flowed out by suspension bed reactor 6 tops, advances Entering hot high score separates from system 7. Hot high score enters cold high score from the gas phase stream thing at system 7 tops From system 8. Cold high score then enters normal pressure knockout tower 9 from the stream thing of system 8 bottoms and directly isolates stone The products such as cerebrol 13, diesel oil distillate 14, light wax oil 15, tail gas 12 is flowed out by its top; Heat is high Heavier component stream thing then enters vacuum fractionation tower 11 in the piece-rate system 7, obtains heavily through decompression separation step by step Wax oil 16 and tail oil 17. Hot high score is from system's 7 bottoms stream thing and suspension bed reactor 6 bottoms Enter together cyclone separator 10, isolate tail oil 19 and residue 20. If adopt circulation cracking side Formula, isolated tail oil and wax oil are got back to oil storage tank 2 through pipeline 21, add outstanding after mixing with raw material Floating bed reactor 6 transforms reaction.
In order to further specify all main points of the present invention, enumerate following examples, but to described enforcement Example also can be carried out multiple improvement, application and variation, but still within the scope of the present invention.
The active proportioning of suspension bed water-soluble catalyst is Fe: Mn: Co: Ni=80: 10: 7: 3, total metal contents in soil was 10.5wt%, and raw material is an iron-based syrup state bed Fischer Tropsch synthetic heavy hydrocarbon, and boiling point is greater than 530 ℃.
At first catalyzer and heavy hydrocarbon feedstocks being mixed at storage tank 2, is benchmark with the Fischer-Tropsch synthesis of heavy hydrocarbon, presses metal and calculates catalyzer add-on 500 μ g/g; Entering suspended-bed reactor 6 with hydrogen after preheating can 4 is mixed and heated to 400 ℃ then, is 6.0MPa in reaction pressure, and temperature of reaction is 410 ℃, and hydrogen to oil volume ratio (under the standard pressure) is 800, and the liquid air speed is 0.3h
-1Carry out hydrocracking under the condition.Reacted product is flowed out by suspended-bed reactor 6 tops, enters hot high score and separates from system 7.The vapor phase stream thing of hot high score from system 7 tops enters cold high score from system 8.The stream thing of cold high score from system 8 bottoms then enters normal pressure knockout tower 9 and directly isolates products such as petroleum naphtha 13, diesel oil distillate 14, light wax oil 15, and tail gas 12 is flowed out by its top; Hot high score heavy component stream thing in system 7 then enters vacuum fractionation tower 11, obtains wax slop 16 and tail oil 17 through decompression separation step by step.Hot high score enters cyclone separator 10 together from system's 7 bottoms stream thing and suspended-bed reactor 6 bottoms, isolates tail oil 19 and residue 20.Isolated tail oil and wax oil are got back to storage tank 2 through pipeline 21, mix back adding suspended-bed reactor with raw material and carry out conversion reaction again.Reaction product is surveyed petroleum naphtha, diesel oil distillate and coking yield respectively, reaction result: petroleum naphtha is 19.1wt%, and diesel oil distillate is 70.4wt%, and coking yield is 1.0wt%.
The method of embodiment 2～5 is with embodiment 1, but catalyzer and reaction conditions change to some extent, and operational condition and experimental result see Table 1.
Suspension bed catalyst activity set of dispense ratio is: Fe: La: Mg: Ca: SiO
2=76: 4: 8: 8: 4, be benchmark with the kettle bottom wax, the catalyzer add-on is 2.0wt%.Raw material is in the iron-based syrup state bed Fischer Tropsch building-up process, the catalyst changeout heavy hydrocarbon of discharging more, i.e. and kettle bottom wax, boiling point is greater than 530 ℃.
At first catalyzer and kettle bottom wax are mixed at storage tank 2, entering suspended-bed reactor 6 with hydrogen after preheating can 4 is mixed and heated to 400 ℃ then, is 8.0MPa in reaction pressure, and temperature of reaction is 420 ℃, hydrogen to oil volume ratio (under the standard pressure) is 900, and the liquid air speed is 0.6h
-1Carry out hydrocracking under the condition.Other operating process is with embodiment 1.Reaction product is surveyed petroleum naphtha, diesel oil distillate and coking yield respectively, reaction result: petroleum naphtha is 23.6wt%, and diesel oil distillate is 65.9wt%, and coking yield is 1.5wt%.
At first according to Chinese patent CN1128667C embodiment 1 preparation, its active ingredient proportioning is catalyzer: Fe: La: Cu: K: SiO
2=100: 0.05: 2: 3: 8, pass through Fischer-Tropsch synthesis 1000h then after, the scrap iron that swaps out from reactor is catalyst based, raw material is in the iron-based syrup state bed Fischer Tropsch building-up process, the heavy hydrocarbon of discharging during catalyst changeout more, boiling point is greater than 530 ℃.At first the iron-based spent catalyst is contained in the suspended-bed reactor 6 in advance.The synthetic kettle bottom wax of Fischer-Tropsch enters suspended-bed reactor 6 with hydrogen after preheating can 4 is mixed and heated to 400 ℃ after volume pump 3 meterings, carry out hydrocracking.Reacted product is flowed out by suspended-bed reactor 6 tops, enters hot high score and separates from system 7.The vapor phase stream thing of hot high score from system 7 tops enters cold high score from system 8.The stream thing of cold high score from system 8 bottoms then enters normal pressure knockout tower 9 and directly isolates products such as petroleum naphtha 13, diesel oil distillate 14, light wax oil 15, and tail gas 12 is flowed out by its top; Hot high score heavy component stream thing in system 7 then enters vacuum fractionation tower 11, obtains wax slop 16 and tail oil 17 through decompression separation step by step.Hot high score enters cyclone separator 10 together from system's 7 bottoms stream thing and suspended-bed reactor 6 bottoms, isolates tail oil 19 and residue 20.Isolated tail oil and wax oil are got back to storage tank 2 through pipeline 21, mix back adding suspended-bed reactor with raw material and carry out conversion reaction again.Reaction product is surveyed petroleum naphtha, diesel oil distillate and coking yield respectively, and operational condition and experimental result see Table 2.
Embodiment 10～12
Catalyzer is formed mass percent: Fe
2O
3: MnO
2: NiO: K
2O: CuO=85: 10: 3: 1.5: 0.5, catalyst based through the scrap iron that from reactor, swaps out after the water gas shift reaction, raw material is iron-based syrup state bed Fischer Tropsch synthetic heavy hydrocarbon and kettle bottom wax mixture, and mass ratio is a heavy hydrocarbon: kettle bottom wax=70: 30, boiling point is greater than 530 ℃.Method is once carried out hydrocracking by the suspension bed mode with embodiment 7～9 but adopt, and promptly isolated wax oil and tail oil are no longer handled with raw material mixing repeated hydrogenation, and operational condition and experimental result see Table 2.
The result shows that technical process provided by the invention is fit to the olefin(e) centent height and contains the Fischer-Tropsch synthesis of heavy hydrocarbon and/or the kettle bottom wax hydrocracking of a certain amount of organic oxygen-containing thing very much, and has higher diesel oil distillate selectivity.
Table 1
Embodiment 2345
Catalyzer
Weight ratio 80 Fe/19 Cu/1K 79 Fe/21 Ni 69 Fe/31 Co 78 Fe/6 Ni/16 Co
Total amount of metal, wt% 9.6 14.2 12.7 10.9
Reaction conditions
Catalyst concn, μ g/g 2,000 150 800 1000
Pressure, MPa 12.0 17.0 4.0 9.0
Temperature, ℃ 450 360 480 390
Air speed, h
-12.0 0.5 1.4 1.0
Hydrogen/oil, v/v 600 900 1,200 1500
Reaction result
Petroleum naphtha, % 22.3 17.8 20.8 19.9
Diesel oil distillate, % 73.8 70.2 69.6 66.7
Coking yield, % 1.3 0.9 1.6 1.1
Table 2
Embodiment 789 10 11 12
Reaction conditions
Catalyst concn, wt% 2.0 15.0 4.5 0.5 7.8 12.0
Pressure, MPa 4.0 17.0 11.0 7.0 14.0 8.0
Temperature, ℃ 400 360 390 430 410 470
Air speed, h
-12.0 0.8 1.2 0.3 0.6 0.8
Hydrogen/oil, v/v 1,000 500 800 1,500 1,000 900
Reaction result
Petroleum naphtha, % 25.9 24.5 27.4 45.4 44.6 50.0
Diesel oil distillate, % 64.3 66.1 62.9 35.5 34.3 30.5
Coking yield, % 1.6 1.3 2.6 2.1 3.0 2.5
Claims (10)
1, the method for a kind of Fischer-Tropsch synthesis of heavy hydrocarbon and/or kettle bottom wax hydrocracking is characterized in that comprising the steps:
Is that 0.05～10wt% or the catalyst based add-on of water-soluble Fe are that 100～2000 μ g/g oil mix with catalyst based and Fischer-Tropsch synthesis of heavy hydrocarbon of the catalyst based or water-soluble Fe of pressed powder Fe and/or kettle bottom wax raw material by the catalyst based add-on of pressed powder Fe, enter suspended-bed reactor after being mixed and heated to 300～400 ℃ with hydrogen then, carry out hydrocracking; Perhaps the iron-based spent catalyst is contained in the suspended-bed reactor in advance, add-on is 0.05～15wt%, and Fischer-Tropsch synthesis of heavy hydrocarbon and/or kettle bottom wax and hydrogen enter suspended-bed reactor after being mixed and heated to 300～400 ℃, carry out hydrocracking; The reaction conditions of hydrocracking is that reaction pressure is 3.0～20.0MPa, and temperature of reaction is 350～500 ℃, and hydrogen to oil volume ratio is 300～1800, and the liquid air speed is 0.1～3.0h
-1
2, the method of a kind of Fischer-Tropsch synthesis of heavy hydrocarbon according to claim 1 and/or kettle bottom wax hydrocracking, it is characterized in that the hydrocracking product is flowed out by the suspended-bed reactor top, entering hot high score separates from system, the vapor phase stream thing of hot high score from the system top enters cold high score from system, the stream thing of cold high score from the system bottom then enters the normal pressure knockout tower and directly isolates product, hot high score heavy component stream thing in system then enters the vacuum fractionation tower, respectively heated up in a steamer the sectional product through decompression separation step by step, hot high score flows tail oil and the residue that thing and suspended-bed reactor bottoms obtain behind cyclone separator from the system bottom, isolated tail oil and wax oil can mix back adding reactor again and carry out conversion reaction with raw material.
3, the method for a kind of Fischer-Tropsch synthesis of heavy hydrocarbon according to claim 1 and/or kettle bottom wax hydrocracking is characterized in that described Fe base water-soluble catalyst forms by many metals water soluble salt is composite.
4, the method for a kind of Fischer-Tropsch synthesis of heavy hydrocarbon according to claim 3 and/or kettle bottom wax hydrocracking is characterized in that described Fe base water-soluble catalyst is iron-nickel catalyzator, iron-cobalt catalyst, iron-Mn catalyst, iron-copper-potassium catalyzer, iron-cobalt-Mn catalyst, iron-manganese-copper-potassium catalyzer or iron-nickel-manganese-molybdenum catalyst.
4, the method for a kind of Fischer-Tropsch synthesis of heavy hydrocarbon according to claim 1 and/or kettle bottom wax hydrocracking, it is characterized in that described Fe base solid powder th-1 catalyst is made up of the oxide carrier of Fe and refractoriness or Fe and tungsten, molybdenum, cobalt, manganese, iron, titanium, copper, calcium, magnesium, lanthanum and potassium in the oxide carrier of one or more and refractoriness form.
5, the method for a kind of Fischer-Tropsch synthesis of heavy hydrocarbon according to claim 4 and/or kettle bottom wax hydrocracking, the oxide carrier that it is characterized in that described refractoriness is silicon oxide, aluminum oxide or silicon oxide-aluminum oxide.
6, the method for a kind of Fischer-Tropsch synthesis of heavy hydrocarbon according to claim 1 and/or kettle bottom wax hydrocracking is characterized in that described Fe base spent catalyst is the iron-based spent catalyst that Fe base syrup state bed Fischer Tropsch synthetic iron-based spent catalyst or water-gas shift are used.
7, the method for a kind of Fischer-Tropsch synthesis of heavy hydrocarbon according to claim 1 and/or kettle bottom wax hydrocracking is characterized in that described iron-based spent catalyst add-on is 0.1～12wt%.
8, the method for a kind of Fischer-Tropsch synthesis of heavy hydrocarbon according to claim 1 and/or kettle bottom wax hydrocracking, it is characterized in that described reaction pressure is 4.0～17.0MPa, temperature of reaction is 380～480 ℃, and hydrogen to oil volume ratio is 600～1500, and the liquid air speed is 0.3～2.0h
-1
9, the method for a kind of Fischer-Tropsch synthesis of heavy hydrocarbon according to claim 2 and/or kettle bottom wax hydrocracking, the processing that it is characterized in that described wax oil and tail oil can also adopt once by flow process, and promptly raw material is through the freshening that no longer circulates after the hydrocracking.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102260527A (en) * | 2011-06-29 | 2011-11-30 | 中国石油大学(华东) | New catalytic hydroprocessing thermal cracking-hydrotreating process of high-sulfur high-acid inferior heavy oil |
| US10563130B2 (en) | 2014-07-17 | 2020-02-18 | Sabic Global Technologies B.V. | Upgrading hydrogen deficient streams using hydrogen donor streams in a hydropyrolysis process |
-
2004
- 2004-07-02 CN CN 200410012378 patent/CN1247747C/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102260527A (en) * | 2011-06-29 | 2011-11-30 | 中国石油大学(华东) | New catalytic hydroprocessing thermal cracking-hydrotreating process of high-sulfur high-acid inferior heavy oil |
| CN102260527B (en) * | 2011-06-29 | 2014-05-28 | 中国石油大学(华东) | New catalytic hydroprocessing thermal cracking-hydrotreating process of high-sulfur high-acid inferior heavy oil |
| US10563130B2 (en) | 2014-07-17 | 2020-02-18 | Sabic Global Technologies B.V. | Upgrading hydrogen deficient streams using hydrogen donor streams in a hydropyrolysis process |
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