CN1247747C - 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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- CN1247747C CN1247747C CN 200410012378 CN200410012378A CN1247747C CN 1247747 C CN1247747 C CN 1247747C CN 200410012378 CN200410012378 CN 200410012378 CN 200410012378 A CN200410012378 A CN 200410012378A CN 1247747 C CN1247747 C CN 1247747C
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Abstract
The present invention relates to a method for hydrogenizing Fischer-Tropsch synthetic heavy hydrocarbons and/ or kettle bottom wax. Fe based catalysts and Fischer-Tropsch synthetic heavy hydrocarbons and/ or kettle bottom wax raw material are uniformly mixed in an oil storage tank; then, the mixture and hydrogen gas are mixed and heated to 300 to 400 DEG C and enter a suspension bed reactor to carry out hydrogenizing conversion, or the Fe based catalysts are placed in the suspension bed reactor preliminarily, the adding amount is from 0.05 to 15 wt%, and the Fischer-Tropsch synthetic heavy hydrocarbons and/ or kettle bottom wax raw and the hydrogen gas are mixed, are heated to 300 to 400 DEG C, and enter the suspension bed reactor to carry out the hydrogenizing conversion; the present invention has the hydrogenizing conversion reaction conditions that pressure is from 3.0 to 20.0MPa, reaction temperature is from 350 to 500 DEG C, the volume ratio of hydrogen to oil is 300 to 1800, and the air speed of liquid is from 0.1 to 3.0h<-1>. The catalyst has higher conversion rate and higher distillate oil yield for the Fischer-Tropsch synthetic heavy hydrocarbons and/ or kettle bottom wax raw, and good naphtha and diesel oil products can be obtained.
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 silicon oxide-aluminum oxide.
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 after preheating can 4 Hybrid Heating, enter suspended-bed reactor 6 with hydrogen and carry out hydro-conversion; Perhaps the iron-based dead catalyst is contained in the suspended-bed reactor 6 in advance, raw material and hydrogen enter suspended-bed reactor 6 and carry out hydro-conversion after preheating can 4 Hybrid Heating. Reacted product is flowed out by suspended-bed reactor 6 tops, enters hot high score and separates from system 7. Hot high score enters cold high score from system 8 from the vapor phase stream thing at system 7 tops. Cold high score then enters normal pressure knockout tower 9 from the stream thing of system 8 bottoms and directly isolates the products such as naphtha 13, diesel oil distillate 14, light wax oil 15, and tail gas 12 is flowed out by its top; Hot high score heavier component stream thing in the 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. If adopt the circulation cracking mode, isolated tail oil and wax oil are got back to oil storage tank 2 through pipeline 21, add suspended-bed reactor 6 after mixing with raw material and carry out conversion reaction.
In order to further specify all main points of the present invention, enumerate following examples, but also can carry out multiple improvement, application and variation to described embodiment, 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%.
Embodiment 7～9
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
| | 2 | 3 | 4 | 5 |
| Catalyst weight is than total amount of metal, wt% reaction conditions catalyst concn, μ g/g pressure, the MPa temperature, ℃ air speed, h -1Hydrogen/oil, v/v reaction result petroleum naphtha, the % diesel oil distillate, the % coking yield, % | 80Fe/19Cu/1K 9.6 2000 12.0 450 2.0 600 22.3 73.8 1.3 | 79Fe/21Ni 14.2 150 17.0 360 0.5 900 17.8 70.2 0.9 | 69Fe/31Co 12.7 800 4.0 480 1.4 1200 20.8 69.6 1.6 | 78Fe/6Ni/16Co 10.9 1000 9.0 390 1.0 1500 19.9 66.7 1.1 |
Table 2
| Embodiment | 7 | 8 | 9 | 10 | 11 | 12 |
| The reaction conditions catalyst concn, wt% pressure, the MPa temperature, ℃ air speed, h -1Hydrogen/oil, v/v reaction result petroleum naphtha, the % diesel oil distillate, the % coking yield, % | 2.0 4.0 400 2.0 1000 25.9 64.3 1.6 | 15.0 17.0 360 0.8 500 24.5 66.1 1.3 | 4.5 11.0 390 1.2 800 27.4 62.9 2.6 | 0.5 7.0 430 0.3 1500 45.4 35.5 2.1 | 7.8 14.0 410 0.6 1000 44.6 34.3 3.0 | 12.0 8.0 470 0.8 900 50.0 30.5 2.5 |
Claims (5)
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, obtain the hydrocracking product; 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 hydrocracking product; 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
Described water-soluble Fe is catalyst based to be 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;
The catalyst based oxide carrier of described pressed powder Fe by Fe and refractoriness form 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;
Described iron-based spent catalyst is the iron-based spent catalyst that iron-based syrup state bed Fischer Tropsch synthetic iron-based spent catalyst or water-gas shift are used.
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, the oxide carrier that it is characterized in that described refractoriness is silicon oxide, aluminum oxide or silica-alumina.
4, 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%.
5, 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
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