CN109666509A - A kind of method of hydrotreating producing aviation bio-fuel - Google Patents
A kind of method of hydrotreating producing aviation bio-fuel Download PDFInfo
- Publication number
- CN109666509A CN109666509A CN201710966961.1A CN201710966961A CN109666509A CN 109666509 A CN109666509 A CN 109666509A CN 201710966961 A CN201710966961 A CN 201710966961A CN 109666509 A CN109666509 A CN 109666509A
- Authority
- CN
- China
- Prior art keywords
- hydrogen
- oil
- pressure
- unit
- rich gas
- 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.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
- C11C3/00—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom
- C11C3/12—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by hydrogenation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2270/00—Specifically adapted fuels
- C10L2270/02—Specifically adapted fuels for internal combustion engines
- C10L2270/026—Specifically adapted fuels for internal combustion engines for diesel engines, e.g. automobiles, stationary, marine
Abstract
The invention belongs to renewable energy manufacture fields, are related to a kind of method of hydrotreating for producing aviation bio-fuel.Method includes the following steps: (1) feedstock oil and first circulation hydrogen, the first hydrogen rich gas mix after in hydrotreating unit imurity-removal；(2) hydrotreatment products enter high-pressure stripper, and the second hydrogen-rich gas phase is injected from tower bottom, and stripping separation light component, stripping top gaseous phase is recycled after gas purification units purify；(3) enter hydroconversion unit after high-pressure stripper bottom refined oil is mixed with new hydrogen and second circulation hydrogen, carry out selective cracking and isomerization reaction；(4) hydroconverted products are through gas-liquid separation, and obtained hydrogen-rich gas phase is sent respectively to hydrotreating unit and high-pressure stripper, and liquid phase obtains aviation biofuel products and byproduct after being fractionated unit separation.Not only process flow is compact by the present invention, also has many advantages, such as that plant energy consumption is low, occupied area is small, equipment investment is few.
Description
Technical field
The invention belongs to renewable energy manufacture field, more particularly, to a kind of produce aviation bio-fuel plus hydrogen
Method.
Background technique
With the fast development of World Airways industry, conventional fossil aviation fuel (aviation kerosine) becomes the maximum row of aircraft industry
Put source, CO2Discharge amount accounts for the 90% of aircraft industry total release, although aircraft industry greenhouse gas emissions only account for all temperature of the mankind
The 2%~3% of room gas discharge, but the ability of generation greenhouse effects and harm are far longer than other rows after aviation kerosine burning
Industry, aircraft industry face severe CO2Emission reduction challenge.
The aviation bio-fuel prepared using renewable biomass such as animal and plant fat or agriculture and forestry organic waste materials, Life cycle
Greenhouse gas emissions be significantly lower than fossil aviation jet fuel, greenhouse gases can 50% or more emission reduction.Aviation bio-fuel
Have the characteristics that raw material sources are extensive, environmental-friendly and reproducible, and chemical structure and physico-chemical property and fossil boat coal are close, because
This, aviation bio-fuel is the potential fossil aviation fuel substitute of tool.
Since biology boat coal technology in China's is also in the development phase, processing flow well known to the country uses two sections and adds at present
First unit (first segment adds hydrogen), reaction product strip after being depressured in low-pressure steam through hydrogenated processing for hydrogen technique, i.e. feedstock oil
Sulphur, nitrogen, oxycarbide are removed in tower, and is handled by vacuum dehydration, and water content is controlled in 300 μ g/g hereinafter, again through heating up
Sent after boosting to hydroconversion unit (second segment adds hydrogen), the product after reaction is depressured and fractionation obtain biology boat coal, diesel oil,
Naphtha and gas.
Two sets of independent high pressure reaction systems of two-stage hydrogenation process requirement and associated high voltage equipment are not only produced in hydrotreating
A large amount of energy is consumed in the desulfurization of object, dehydration and in the boost process of hydroconversion unit raw material, causes biological boat
The energy consumption of coal technology is higher, and the separation process of hydrotreatment products is longer, leads to that number of devices is more, takes up a large area and throws
Provide the various problems such as at high cost.
Relative to the disadvantages mentioned above of two-stage hydrogenation technique, one-stage hydrogenation process can avoid substantially cooling between reactor,
Pressure reduction, low energy consumption, process is short, land occupation is few, has very big advantage.However, how to remove sulphur in hydrotreatment products,
Nitrogen, oxycarbide and water become one section of coal of biology boat and add to avoid the noble metal catalyst poisoning and deactivation of hydroconversion unit
The key point of hydrogen technique.
Current related animal and plant fat adds hydrogen to prepare the patent of automotive fuel such as: CN102464997A, CN102504866A,
CN103374401A, EP1744767, EP1744768, US20090158637A1 and US20080284962A1 etc. are disclosed by moving
The technique of vegetable oil or blending mineral oil production biodiesel, it is not mentioned how removing is hydrogenated to the effective means of water, because
This catalyst activity will be seriously affected by generation water, and device often can not long-term operation.
CN102027098A discloses a kind of method of production and transport fuel from renewable raw materials, such as vegetable oil and animal
The method that diesel boiling range product and aviation boiling range product are prepared in oil.This method includes, by hydrogenation and deoxidation by renewable original
Material is handled to provide hydrocarbon fraction, carries out isomerization and selective cracking then to form diesel boiling range product and aviation boiling
Journey product.A part of diesel boiling range product, aviation boiling range product, naphtha products, LPG or any combination of them, can be optional
Be used as rectification agent in selective thermal high pressure hydrogen stripper, to reduce the product amount carried in the effluent stream of stripper top.
It is had the following problems in this method:
1) new hydrogen consumption amount is big.In isomerization and selective hydrogenation part without circulation hydrogen system in the process flow,
It is only injected with new hydrogen to maintain to react required hydrogen to oil volume ratio (generally several hundred or thousands of), it is therefore desirable to a large amount of hydrogen；
In addition, new hydrogen is injected high-pressure stripper by the technique, to meet Srteam Stripping effect, the consumption of stripping hydrogen is also larger.
2) recycle hydrogen utilization rate is low, and outlet amounts of hydrogen is big.The hydrogen-rich gas phase that the technique mesohigh strips tower top comes from two
The reaction product of hydrogenation unit (hydrogenation deoxidation unit, isomerization and selective hydrogenation unit), the purified desulfurization of hydrogen-rich gas phase take off
Carbon rear portion is back to hydrogenation deoxidation unit, rest part outlet as recycle hydrogen.According to hydrogen balance, outlet amounts of hydrogen and
The sum of total hydrogen consumption amount (including chemistry consumption hydrogen, dissolution consumption hydrogen and leakage consumption hydrogen), should be suitable with the new hydrogen amount of the system is entered.Relatively
A large amount of new hydrogen in the process flow, total hydrogen consumption proportion is lower, and therefore, which will cause outside a large amount of hydrogen-rich gas phase
Row, operating cost are uneconomical.
3) it is larger to be contaminated possibility for final product.By the liquid phase of hydrogen separator and high-pressure stripper top in the process flow
Hydrogen rich gas mix it is air-cooled into high pressure, since liquid phase is the reaction product of the low nitrogen of low-sulfur, and high-pressure stripper in hydrogen separator
Often impurity such as sulfur-bearing, nitrogen in hydrogen-rich gas phase are pushed up, reaction product and final products can be polluted.
It would therefore be highly desirable to develop a kind of biology boat coal one-stage hydrogenation technique that low energy consumption, with low investment.
Summary of the invention
In view of the deficiencies of the prior art, the present invention provides a kind of method of hydrotreating for producing aviation bio-fuel, utilizes high pressure
Stripper removes the H in hydrotreating reaction product2S、H2O, oxycarbide and lighter hydrocarbons integrate current two-stage hydrogenation process
For one-stage serial plus hydrogen process；And according to the reaction condition of different hydrogenation units, point of reasonably optimizing recycle hydrogen and hydrogen-rich gas phase
Match, reduce the consumption of new hydrogen, with process flow is compact, plant energy consumption is low, occupied area is small, equipment investment is few, flexible operation
The advantages that.
The present invention provides a kind of method of hydrotreating for producing aviation bio-fuel, method includes the following steps:
(1) after feedstock oil and first circulation hydrogen, the first hydrogen rich gas mix in hydrotreating unit imurity-removal；
(2) hydrotreatment products enter high-pressure stripper, and the second hydrogen-rich gas phase is injected from tower bottom, stripping separation light component,
Stripping top gaseous phase is recycled after gas purification units purify；
(3) enter hydroconversion unit after high-pressure stripper bottom refined oil is mixed with new hydrogen and second circulation hydrogen, selected
The cracking of selecting property and isomerization reaction；
(4) hydroconverted products through gas-liquid separation, send respectively to hydrotreating unit and high pressure vapour by obtained hydrogen-rich gas phase
Stripper, liquid phase obtain aviation biofuel products and byproduct after being fractionated unit separation.
In step (1) described hydrotreating unit, feedstock oil and first circulation hydrogen, Lai Zire from circulating hydrogen compressor
First hydrogen-rich gas phase of high score carries out a series of hydrogenation reaction under the action of high pressure, high mild catalyst, removing oxygen, sulphur,
Nitrogen, chlorine and metal impurities.The reaction condition of the hydrotreating unit preferably includes: hydrogen partial pressure be 2.5MPa~
10.0MPa, reaction temperature are 180 DEG C~400 DEG C, and hydrogen to oil volume ratio is 300~2000.To reach the required condition of reaction, add
At least one of following equipment: reactor, heating furnace, pump, heat exchanger, container can be included at least in hydrogen conversion unit.
Feedstock oil described in step (1) can be animal and plant fat.Such as it is selected from kitchen waste oil, palm oil, rapeseed oil, corn
At least one of oil, soybean oil, olive oil, peanut oil, jatropha curcas oil, wilson dogwood oil, rotten edible oil and fat.
The operating condition of high-pressure stripper described in step (2) (or high pressure hydrogen stripper) preferably includes: temperature is
100 DEG C~380 DEG C, pressure is 3.0MPa~12.0MPa；The second hydrogen rich gas in high-pressure stripper, at the top of Lai Zire high score
It is mutually injected from stripper bottom, and top-down hydrotreatment products counter current contacting, by the H in hydrotreatment products2S、H2O、
The light components such as oxycarbide and most of lighter hydrocarbons are taken out of from tower top.It is stripped by high pressure, it on the one hand will be in hydrotreatment products
H2S、H2O is removed from oily phase, can prevent the noble metal catalyst poisoning and deactivation in follow-up hydrogenation conversion unit；On the other hand,
Since the lighter hydrocarbons in hydrotreatment products are to exist in the reactor of hydroconversion unit in the form of gas phase, reactor can be reduced
In hydrogen partial pressure therefore the hydrogen partial pressure of hydroconversion unit reactor is can be improved into the removing of most of lighter hydrocarbons by stripping, is had
Saves new hydrogen dosage, reduces plant energy consumption to effect.
In step (2), the top gaseous phase of the high-pressure stripper enters cold high pressure separator after cooling, isolated
Cold high score gas phase through gas purification units purification, it is pressurized again after be divided into two strands: first circulation hydrogen and second circulation hydrogen.Tool
Body, contain H2S、H2O, the high-pressure stripper top hydrogen-rich gas phase of oxycarbide and lighter hydrocarbons through being cooled to 30~60 DEG C or so into
Enter in cold high pressure separator, light hydrocarbon component is sent after being condensed to fractionation unit, is avoided hydrogen-rich gas band liquid and is entered recycle hydrogen
System causes a series of subsequent affects (such as the foaming of amine liquid, circulating hydrogen compressor are shut down)；Isolated hydrogen-rich gas is sent to gas
Clean unit removes impurity.Means commonly used in the art, such as amine absorption, alkali cleaning, pressure-variable adsorption can be used in gas purification units
Method, by the H in hydrogen-rich gas2S、CO、CO2Equal impurity removals.It is sent as recycle hydrogen to recycle hydrogen pressure by purified gas
Contracting machine is divided into first circulation hydrogen and second circulation hydrogen after compression pressure-raising, is sent respectively to hydrotreating unit and hydro-conversion
Unit.According to the demand of respective reaction condition, the relative scale of two strands of recycle hydrogens can be adjusted flexibly, it is preferred that first can be followed
The control of the ratio of ring hydrogen and second circulation hydrogen is 10:1~0.5:1
It, can be by cold high pressure separator bottom point to carry heavy constituent in control high-pressure stripper top gas phase in step (2)
From obtained liquid phase part or whole re-injection to high pressure stripper top.
In step (3), high-pressure stripper bottom refined oil (low-sulfur, low water content) enters hydroconversion unit, respectively in hydrogen
Under the action of gas, hydrogenation conversion catalyst, heterogeneous catalyst and rear catalyst for refining, carries out selective cracking and isomerization is anti-
It answers, and is saturated the alkene of cracking reaction generation, obtain the moderate hydro-conversion material of fraction.It, can be for the flexibility of operation
Hydro-conversion feed pump is arranged in stripper bottom, if the operating pressure of hydroconversion unit need to properly increase, available plus hydrogen turns
Change feed pump to complete.
In step (3), the reaction condition of the hydroconversion unit is preferably included: hydrogen partial pressure is 3.0MPa~12.0MPa,
Reaction temperature is 150 DEG C~420 DEG C, and hydrogen to oil volume ratio is 300~1500.To reach the required condition of reaction, hydro-conversion list
At least one of following equipment: reactor, heating furnace, pump, heat exchanger, container can be included at least in member.
In step (3), new hydrogen is mixed after make-up hydrogen compressor boosts with refined oil, according to the pressure of new hydrogen and recycle hydrogen
Actual match situation, second circulation hydrogen can export in make-up hydrogen compressor and mix with new hydrogen, and new hydrogen compressed also can be injected
Between machine grade.
In step (3), according to the feature of different material oil, a part of high-pressure stripper bottom refined oil can be used as and be followed
Ring refined oil is recycled to hydrotreating part and mixes with feedstock oil, it is preferable that the mass ratio of circulation refined oil and fresh feed oil
For 0.5:1~8:1.
In step (4), the hydroconverted products preferably enter high pressure hot separator, the hydrogen-rich gas phase that top is isolated point
For two strands: first hydrogen-rich gas phases and the second hydrogen-rich gas phase.Specifically, the hydroconverted products separate in high pressure hot separator
Hydrogen-rich gas phase and oily phase, the gas phase for the high temperature and pressure that top obtains are divided into the first hydrogen-rich gas phase and the second hydrogen-rich gas phase out, respectively
It send to hydrotreating unit and high-pressure stripper.According to hydrotreating unit reaction condition and high-pressure stripper separating effect
The relative scale of two bursts of hydrogen-rich gas phases can be adjusted flexibly in demand, it is preferable that by the ratio of the first hydrogen-rich gas phase and the second hydrogen-rich gas phase
Example control is 5:1~0.2:1.
In step (4), the liquid phase that high pressure hot separator bottom obtains is sent after being depressured to fractionation unit, in fractionation unit
Further isolated liquefied gas, naphtha, biology boat coal, diesel oil distillate.Due in ASTM D7566 to aviation bio-fuel
The end point of distillation be not higher than 300 DEG C of regulation, generally can the fraction by initial boiling point higher than 280 DEG C~300 DEG C cut out and evaporated as diesel oil
Point, this part diesel oil distillate can be partly recycled to hydroconversion unit and carry out freshening according to the needs of products scheme, to increase
The yield of biology boat product of coal；Can also directly carrying device as diesel oil reconciliation product.
In step (4), means commonly used in the art, such as setting degassing tower, product fractionation is can be used in the setting of fractionation unit
Tower or naphtha stabilizer etc..
In the method for the present invention, to realize different hydrogenating functions, the hydrotreating unit and hydroconversion unit can be each
From including one or more reactors, one or more hydrogenation catalysts are at least loaded.It can basis in specific production design
Process scale, specification of equipment, feedstock property, product quality require difference and be configured.
In the method for the present invention, hydrogenation catalyst can be this field conventional catalyst.The catalysis loaded in hydrotreating unit
Active component of the agent under reactiveness is at least one of Ni, Mo and W of reduction-state.Hydroconversion unit loads respectively to be added
Hydrogen reforming catalyst and hydroisomerization catalyst, its active component is the Pt and/or Pd of reduction-state under reactiveness.
In the method for the present invention, the hydrogenator shares a hydrogen gas system, simplifies the process of hydrogen gas system, reduces
The energy consumption of device.
Compared with the prior art, the present invention has the advantages that
1) hydrogen process is added using one-stage serial, hydrotreatment products, which are not required to substantially boost, can enter concatenated hydro-conversion
Unit avoids in conventional two-stage process first decrease temperature and pressure a large amount of energy losses caused by increasing temperature and pressure again, saves device energy
Consumption.
2) high-pressure stripper is set, by injecting hydrogen-rich gas in tower bottom, first is that preventing the H in hydrotreatment products2S、
H2O etc. enters subsequent hydroconversion unit, causes noble metal catalyst poisoning and deactivation, second is that hydrotreating reaction is generated
Oxycarbide, C1~C4 light hydrocarbon component remove in time, and preventing it from entering in subsequent reactor reduces hydrogen partial pressure, not only contribute to add
The reaction effect of hydrogen isomery and hydrofinishing, and reduce the gas phase load of subsequent reactor.
3) reaction condition is optimized.In consumption hydrogen is big, hydrogen-oil ratio is high hydrotreating unit, using a large amount of hydrogen circulation (the
One recycle hydrogen)；To impurity (H2S、H2O etc.) content has higher requirements, consumes that hydrogen is few, the lower hydroconversion unit of hydrogen-oil ratio, it adopts
(second circulation hydrogen) is recycled with a small amount of hydrogen, the mode of additional new hydrogen injection improves the hydrogen partial pressure of hydroconversion unit, adds hydrogen
The control means of reaction depth are more flexible.
4) pressure rating matching is reasonable.The pressure as needed for hydrogenation deoxidation, desulphurization reaction is often below hydrocracking reaction,
Hot high score gas (hydrogen-rich gas) a part of hydroconversion unit is injected into high-pressure stripper as stripping hydrogen in the present invention, it is another
Injection hydrotreating unit in part realizes the circulation and circulation of two hydrogenation unit hydrogen without mechanical booster apparatus.
5) a set of circulation hydrogen system is used, by two-stage hydrogenation process high integration, process arrangement is compact, equipment dosage is few,
Reduce plant area and equipment investment.
Other features and advantages of the present invention will then part of the detailed description can be specified.
Detailed description of the invention
Exemplary embodiment of the invention is described in more detail in conjunction with the accompanying drawings.
Fig. 1 is process flow diagram of the invention.
Description of symbols:
Feedstock oil 1, first circulation hydrogen 2, second circulation hydrogen 3, hydrotreatment products 4, high-pressure stripper base oil 5 add hydrogen to turn
Change product 6, the second hydrogen-rich gas phase 7, the first hydrogen-rich gas phase 8, hot high score oil 9, high-pressure stripper top gas 10, cold high score gas 11 are cold
High score reflux 12, cold high score oil 13, gas 14, naphtha 15, biology boat coal 16, diesel oil 17, circulation diesel oil 18, recycle hydrogen 19,
New hydrogen 20, mixes hydrogen 21, recycles refined oil 22.
A- hydrotreating unit, B- high-pressure stripper, C- hydroconversion unit, D- high pressure hot separator, E- cold anticyclone point
From device, F- fractionation unit, G- gas purification units, H- circulating hydrogen compressor, I- make-up hydrogen compressor.
Specific embodiment
The preferred embodiment of the present invention is described in more detail below.Although the following describe preferred implementations of the invention
Mode, however, it is to be appreciated that may be realized in various forms the present invention without that should be limited by the embodiments set forth herein.
Embodiment
Feedstock oil 1 is successively mixed with first circulation hydrogen 2, the first hydrogen-rich gas phase 8, into hydrotreating unit A；Adding at hydrogen
It manages heating in unit A, generate hydrotreatment products 4 after reaction, into the top high-pressure stripper B, through 7 vapour of the second hydrogen-rich gas phase
Mention the H of elimination reaction generation2S and H2O, high-pressure stripper base oil 5 is mixed with the mixing hydrogen 21 from make-up hydrogen compressor I, into adding
Hydrogen conversion unit C generates hydroconverted products 6 after being heated up, being reacted, subsequently into high pressure hot separator D.
Hydrogen-rich gas phase at the top of high pressure hot separator D is divided into two strands: first hydrogen-rich gas phases 8 as supplement hydrogen and feedstock oil 1
Mixing；Second hydrogen-rich gas phase 7 is sent as hot hydrogen is stripped to the bottom high-pressure stripper B；The heat of the bottom high pressure hot separator D separation is high
Oil 9 is divided to be sent after depressurizing to fractionation unit F.
High-pressure stripper top gas 10 is sent into cold high pressure separator E, isolated 11 air inlet body of cold high score gas after cooling
Clean unit G carry out desulfurization, decarburization, it is purified after recycle hydrogen 19 through circulating hydrogen compressor H boosting after be divided into two-way: first follows
Ring hydrogen 2 enters hydrotreating unit A after mixing with feedstock oil 1；Second circulation hydrogen 3 is mixed into make-up hydrogen compressor I with new hydrogen 20
Boosting obtains mixing hydrogen 21.Cold high score oil 13 enters separative unit F after being depressured.
Gas 14, naphtha 15, biology boat coal 16 and diesel oil 17 are isolated in fractionation unit F.
It is different according to the condition of operation, can by a part of high-pressure stripper B tower bottom liquid phase as circulation refined oil 22 with
Feedstock oil 1 is mixed into hydrotreating unit A control reaction condition；By a part of conduct of cold high pressure separator E bottom liquid phases
At the top of cold 12 injection high-pressure stripper B of high score reflux, the content of heavy constituent in high-pressure stripper top gas 10 is controlled；Diesel oil will be recycled
18 mixed with high-pressure stripper base oil 5 after enter hydroconversion unit C, control the yield of product.
Using process flow chart shown in FIG. 1, using certain waste cooking oil as raw material, (implemented with the process flow in Fig. 1 respectively
Example) and existing two-stage method hydrogenation technique (comparative example) production biology boat product of coal.The number of devices and Srteam Stripping effect of Stripping section
Difference be listed in Tables 1 and 2 respectively, quantity, the energy consumption of whole device capital equipment are listed in table 3.
The comparison of 1 Stripping section capital equipment of table
2 hydrotreating reaction product Srteam Stripping effect of table
From table 1 it follows that in the Stripping section of hydrotreatment products, capital equipment 6, comparative example needed for embodiment
Required capital equipment 11, and embodiment no setting is required pumped vacuum systems, process are more succinct.
Comparative analysis is found from table 2, the H in embodiment in stripper base oil2S and H2O content be respectively trace and
207ppb, hence it is evident that lower than H in comparative example vacuum dehydration column base oil2S and H2O content, it was demonstrated that control of the embodiment in key index
On, effect is better than comparative example.
3 capital equipment of table, energy consumption and investment ratio
As can be seen from Table 3, embodiment only increases by 1 high-pressure stripper, can save 2 high-pressure bottles, 2 high pressures into
Expect pump, 2 circulating hydrogen compressors, 1 high-pressure air cooler, 3 high pressure heat exchangers and 1 heating furnace.The specific energy consumption of comparative example
For 119kgoe/t (kilogram mark oil/ton feedstock oil), embodiment specific energy consumption is 97kgoe/t (kilogram mark oil/ton feedstock oil).Phase
Than under, the method for the present invention energy consumption reduces by 18.5%, and energy-saving effect is significant.
In addition, under conditions of creating the biological kerosene hydrogenation device of a set of 100,000 tons/year of scales, comparative example investment is about
2.8 hundred million yuan, and the construction investment of embodiment is about 2.5 hundred million yuan, reduce investment outlay about 10.7%.
Various embodiments of the present invention are described above, above description is exemplary, and non-exclusive, and
It is not limited to disclosed each embodiment.Without departing from the scope and spirit of illustrated each embodiment, for this skill
Many modifications and changes are obvious for the those of ordinary skill in art field.
Claims (10)
1. a kind of method of hydrotreating for producing aviation bio-fuel, which is characterized in that method includes the following steps:
(1) after feedstock oil and first circulation hydrogen, the first hydrogen rich gas mix in hydrotreating unit imurity-removal；
(2) hydrotreatment products enter high-pressure stripper, and the second hydrogen-rich gas phase is injected from tower bottom, stripping separation light component, stripping
Top gaseous phase is recycled after gas purification units purify；
(3) enter hydroconversion unit after high-pressure stripper bottom refined oil is mixed with new hydrogen and second circulation hydrogen, carry out selectivity
Cracking and isomerization reaction；
(4) hydroconverted products through gas-liquid separation, send respectively to hydrotreating unit and high-pressure stripper by obtained hydrogen-rich gas phase,
Liquid phase obtains aviation biofuel products and byproduct after being fractionated unit separation.
2. the method according to claim 1, wherein impurity described in step (1) include oxygen, sulphur, nitrogen, chlorine and
Metal；Light component described in step (2) includes H2S、H2O, oxycarbide and most of lighter hydrocarbons.
3. the method according to claim 1, wherein the top gaseous phase of the high-pressure stripper enters after cooling
Cold high pressure separator, isolated cold high score gas phase through gas purification units purification, it is pressurized again after be divided into two strands: the
One recycle hydrogen and second circulation hydrogen, the two ratio are preferably 10:1~0.5:1；Isolated cold high score liquid phase part or whole
Return to high-pressure stripper.
4. being pushed up the method according to claim 1, wherein the hydroconverted products enter high pressure hot separator
The hydrogen-rich gas phase that part separates out is divided into two strands: first hydrogen-rich gas phases and the second hydrogen-rich gas phase, and the two ratio is preferably 5:1~0.2:
1。
5. the method according to claim 1, wherein the reaction condition of the hydrotreating unit includes: hydrogen point
Pressure is 2.5MPa~10.0MPa, and reaction temperature is 180 DEG C~400 DEG C, and hydrogen to oil volume ratio is 300~2000.
6. the method according to claim 1, wherein the reaction condition of the hydroconversion unit includes: hydrogen point
Pressure is 3.0MPa~12.0MPa, and reaction temperature is 150 DEG C~420 DEG C, and hydrogen to oil volume ratio is 300~1500.
7. the method according to claim 1, wherein the operating condition of the high-pressure stripper includes: that temperature is
100 DEG C~380 DEG C, pressure is 3.0MPa~12.0MPa.
8. the method according to claim 1, wherein a part of high-pressure stripper bottom refined oil is as circulation essence
Liquefaction is recycled to hydrotreating unit and mixes with feedstock oil, and the mass ratio for recycling refined oil and feedstock oil is preferably 0.5:1~8:
1。
9. the method according to claim 1, wherein fractionation unit isolates the recombination that initial boiling point is greater than 280 DEG C
Point, partly or entirely it is recycled to hydroconversion unit.
10. method described in any one of -9 according to claim 1, which is characterized in that the feedstock oil is animal and plant fat,
It is oily, rotten selected from kitchen waste oil, palm oil, rapeseed oil, corn oil, soybean oil, olive oil, peanut oil, jatropha curcas oil, wilson dogwood
At least one of edible oil and fat.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710966961.1A CN109666509A (en) | 2017-10-17 | 2017-10-17 | A kind of method of hydrotreating producing aviation bio-fuel |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710966961.1A CN109666509A (en) | 2017-10-17 | 2017-10-17 | A kind of method of hydrotreating producing aviation bio-fuel |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN109666509A true CN109666509A (en) | 2019-04-23 |
Family
ID=66141440
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710966961.1A Pending CN109666509A (en) | 2017-10-17 | 2017-10-17 | A kind of method of hydrotreating producing aviation bio-fuel |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109666509A (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111909722A (en) * | 2020-08-15 | 2020-11-10 | 易高生物化工科技(张家港)有限公司 | Method for preparing biological aviation kerosene and renewable alkane by waste animal and vegetable oil hydrogenation |
| CN112521975A (en) * | 2020-11-02 | 2021-03-19 | 中国寰球工程有限公司 | Thermal hydrogen stripping method for preparing aviation biofuel by two-stage hydrogenation method |
| CN114364446A (en) * | 2019-06-07 | 2022-04-15 | 环球油品有限责任公司 | Method and apparatus for recycling hydrogen to hydrotreat a biorenewable feed |
| WO2022079051A1 (en) * | 2020-10-14 | 2022-04-21 | Shell Internationale Research Maatschappij B.V. | Systems and processes for generating a reduced chloride stripped fluid from a hydroprocessing effluent |
| CN115044388A (en) * | 2022-06-06 | 2022-09-13 | 浙江嘉澳环保科技股份有限公司 | Method and system for producing alkylated biomass aviation fuel from waste oil |
| CN115948180A (en) * | 2023-03-14 | 2023-04-11 | 新疆天利石化股份有限公司 | Energy-saving and environment-friendly process for producing mixed aromatic hydrocarbon by cracking carbon nine through hydrogenation |
| CN116075579A (en) * | 2020-09-14 | 2023-05-05 | 托普索公司 | Impurity removal in hydrocarbon product production processes |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102027098A (en) * | 2008-03-17 | 2011-04-20 | 环球油品公司 | Production of transportation fuel from renewable feedstocks |
| CN102504866A (en) * | 2011-11-08 | 2012-06-20 | 海南临高化工实业有限公司 | Method for preparing biodiesel by mixing waste edible oil with mineral diesel oil and hydrogenization |
| CN104250558A (en) * | 2013-06-27 | 2014-12-31 | 江苏佳誉信实业有限公司 | Method for producing normal paraffin by hydrogenating fatty acid ester |
| CN106281401A (en) * | 2015-05-21 | 2017-01-04 | 中国石化工程建设有限公司 | A kind of method utilizing waste animal and plant fat to produce aviation bio-fuel |
-
2017
- 2017-10-17 CN CN201710966961.1A patent/CN109666509A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102027098A (en) * | 2008-03-17 | 2011-04-20 | 环球油品公司 | Production of transportation fuel from renewable feedstocks |
| CN102504866A (en) * | 2011-11-08 | 2012-06-20 | 海南临高化工实业有限公司 | Method for preparing biodiesel by mixing waste edible oil with mineral diesel oil and hydrogenization |
| CN104250558A (en) * | 2013-06-27 | 2014-12-31 | 江苏佳誉信实业有限公司 | Method for producing normal paraffin by hydrogenating fatty acid ester |
| CN106281401A (en) * | 2015-05-21 | 2017-01-04 | 中国石化工程建设有限公司 | A kind of method utilizing waste animal and plant fat to produce aviation bio-fuel |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114364446A (en) * | 2019-06-07 | 2022-04-15 | 环球油品有限责任公司 | Method and apparatus for recycling hydrogen to hydrotreat a biorenewable feed |
| CN111909722A (en) * | 2020-08-15 | 2020-11-10 | 易高生物化工科技(张家港)有限公司 | Method for preparing biological aviation kerosene and renewable alkane by waste animal and vegetable oil hydrogenation |
| CN116075579A (en) * | 2020-09-14 | 2023-05-05 | 托普索公司 | Impurity removal in hydrocarbon product production processes |
| WO2022079051A1 (en) * | 2020-10-14 | 2022-04-21 | Shell Internationale Research Maatschappij B.V. | Systems and processes for generating a reduced chloride stripped fluid from a hydroprocessing effluent |
| CN112521975A (en) * | 2020-11-02 | 2021-03-19 | 中国寰球工程有限公司 | Thermal hydrogen stripping method for preparing aviation biofuel by two-stage hydrogenation method |
| CN115044388A (en) * | 2022-06-06 | 2022-09-13 | 浙江嘉澳环保科技股份有限公司 | Method and system for producing alkylated biomass aviation fuel from waste oil |
| WO2023236390A1 (en) * | 2022-06-06 | 2023-12-14 | 浙江嘉澳环保科技股份有限公司 | Method and system for producing alkylated biomass aviation fuel from waste oils and fats |
| CN115948180A (en) * | 2023-03-14 | 2023-04-11 | 新疆天利石化股份有限公司 | Energy-saving and environment-friendly process for producing mixed aromatic hydrocarbon by cracking carbon nine through hydrogenation |
| CN115948180B (en) * | 2023-03-14 | 2023-05-23 | 新疆天利石化股份有限公司 | Energy-saving and environment-friendly process for producing mixed aromatic hydrocarbon by cracking carbon nine and hydrogenation |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109666509A (en) | A kind of method of hydrotreating producing aviation bio-fuel | |
| CN106281401B (en) | A method of producing aviation bio-fuel using waste animal and plant fat | |
| CN100371423C (en) | Hydrocarbons hydrocracking method | |
| CN1876767B (en) | Coal tar hydrocracking method | |
| EP3266854B1 (en) | Diesel oil and jet fuel production system and method utilizing fischer-tropsch synthetic oil | |
| CN1952070A (en) | Method for producing cleaning oil from coal-tar oil | |
| CN102304387B (en) | Production method of coal-based high-density jet fuel | |
| CN103305269B (en) | Method for producing gasoline and diesel by directly hydrogenating medium and low temperature coal tar | |
| MX2014011755A (en) | Methods and apparatuses for processing renewable feedstocks. | |
| CN102146298A (en) | Hydrocarbon hydrogenation conversion process combined method | |
| CN105647581A (en) | Catalytic gasoline hydrogenation method | |
| CN104388116A (en) | High-efficiency heavy inferior oil conversion process | |
| CN101230291A (en) | Low consumption energy method for processing fischer-tropsch synthesis | |
| CN104004541A (en) | Method for preparing coal-based high aromatic potential content raw oil | |
| CN103937527B (en) | Bio-oil hydrofining-isomerization-visbreaking prepares the method for low freezing point diesel fuel component | |
| US11549061B2 (en) | Process for hydroprocessing of biological feedstocks | |
| CN100510022C (en) | Low-hydrogenloss hydrogenation of high-output qulified diesel oil | |
| CN100419044C (en) | Production of large-specific-weight aircraft liquid petroleum oil at maximum from coal liquefied oil | |
| CN102051224A (en) | Production method of coal-based high-aromatic-hydrocarbon-potential-content naphtha for catalytic reforming, product and application thereof | |
| CN112592737A (en) | Method for producing low-freezing point biodiesel by coupling liquid catalysis with heterogeneous pour point depression | |
| CN102311782B (en) | Method for producing diesel oil by purifying coal tar through hydrogenating | |
| CN105586087B (en) | A kind of method being hydrocracked | |
| CN103450933A (en) | Diesel oil hydroupgrading combination method | |
| CN103059902B (en) | Method for preparing jet fuel blending component by using animal and vegetable oils as raw materials | |
| CN1721509A (en) | Medium pressure hydrocracking process for preparing jet fuel |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20190423 |