CN109517624A - A kind of heavy crude catalytic hydrogenation method using methane - Google Patents
A kind of heavy crude catalytic hydrogenation method using methane Download PDFInfo
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- CN109517624A CN109517624A CN201811619636.9A CN201811619636A CN109517624A CN 109517624 A CN109517624 A CN 109517624A CN 201811619636 A CN201811619636 A CN 201811619636A CN 109517624 A CN109517624 A CN 109517624A
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- 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
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Abstract
The invention discloses a kind of heavy crude catalytic hydrogenation methods using methane, heavy crude is pumped into the hydrogenator equipped with catalyst, methane is passed through as reaction gas and carries out catalytic hydrogenation reaction, macromolecular in heavy crude is broken down into alkane and light aromatic, product oil, which flows out below hydrogenator and is passed through knockout drum, carries out gas-liquid separation, tail gas is used for subsequent processing with pipeline outflow from gas-liquid separation tank top, product oil flows into products pot from gas-liquid separation pot bottom and is collected, knockout drum connects cooling system for reducing the temperature of product oil, the viscosity of the product oil of acquisition is 107~379mPas, density is 0.9511~0.9642g/ml, total acidity is 0.02~1.55mg KOH/g, average molecular weight is 172 ~210g/mol, water content are 0.21~0.30wt.%, and product liquid yield is 96.9~104%.Present invention process process flow operation cost reduces, and effectively improves hydrogenation reaction effect, operating pressure reduces and process is environmentally protective.
Description
Technical field
The invention belongs to oil refining technical fields, and in particular to a kind of heavy crude catalytic hydrogenation side using methane
Method.
Background technique
Nowadays, petroleum is still one of most important fossil energy and industrial chemicals in the world, and it is economical to become promotion, industry
With the important motivity of social development.The demand and consumption of petrochemicals are constantly being risen in world wide.However
The reserves of traditional lightweight crude oil decline year by year, and increasingly depleted trend is presented.Therefore, including heavy crude very
It is of increasing concern to advise petroleum resources.Heavy crude rich reserves, mainly from Venezuela, Canada, Saudi Arabia.I
State has signed a series of trade agreement of heavy crude with Venezuela, while being taken by purchase corporation with foreign capital's isotype adding
Stable heavy crude source is obtained greatly.These strategic measures develop and use heavy oil resources for China and provide advantage.
Heavy crude resource is rationally efficiently utilized, it will largely improve the energy problem in China, alleviate petroleum resources
Deficiency is society, limitation brought by economic and industrial development.
However there is a series of problems for the development and utilization of heavy crude.It is transport including its higher viscosity-density
In caused difficulty and pyrolysis product the problems such as olefin(e) centent, sulfur content and high tenor.These problems it is effective
It solves, is the prerequisite for efficiently using heavy crude resource.It is viscous reducing it therefore, it is necessary to be modified to heavy crude
While spending density, hydrocarbon biggish in raw material is cracked into the high value added products such as aromatic compound, promotes weight
The quality and value of matter crude oil.
Current heavy crude modifying process generally used in the world is pyrolysis method, is cracked heavy crude by high temperature
For the product liquid of small molecule, the hydrogen then obtained using steam reforming carries out catalytic hydrogenation to pyrolysis product.Due to weight
Matter crude oil is mainly made of hydrocarbon, and phosphorus content is high.Therefore it is inevitably generated in thermal cracking processes a large amount of burnt
Charcoal causes to seriously affect to reactor with catalyst.The technique of another extensive utilization is that hydrogen is passed directly into cracking process
Gas carries out catalytic hydrogenation under the effect of the catalyst.Hydrogenation process can convert the olefinic product generated in cracking process
For the alkanes substance of saturation, while it also can remove sulphur contained in raw material, nitrogen, metal impurities.Hydrogen is introduced in cleavage step
Gas, can inhibit the condensation of organic molecule, so that the generation of coke species is effectively reduced, so that more carbon are able to enter liquid
In product, lost caused by reducing due to coke generates.But the reaction pressure of this process is between 140~280 atmospheric pressure,
It is very high to the crushing resistance and air-tightness requirement of reactor and pipeline, so that equipment cost is significantly increased.
Meanwhile both the above process requires to consume a large amount of hydrogen.Industrially preparing the main method of hydrogen is methane
Steam reforming that is, under the effect of the catalyst make natural gas and vapor that reforming reaction occur, generate hydrogen and titanium dioxide
Carbon.Steam reforming needs carried out at 800 DEG C or more of temperature and the pressure of 15~30 atmospheric pressure, cause its equipment at
Sheet and operating cost height.And these costs will all cause the raising of hydrogen price, to promote the cost of hydrogenation process.Therefore,
If the step for steam reforming can be saved, hydrogenation reaction directly is carried out to heavy crude using methane as hydrogen source, it will
The operating cost of hydrogenation process is greatly reduced.It, can be by heavy original by the way that methane molecule to be decomposed into the methyl and hydrogen atom of activation
Macromolecular in oil is converted into the higher light aromatic of economic value, completes addition to olefin component and right
Sulphur, nitrogen, the removing of metallics.At the same time, the methyl of activation, which may also participate in, is reacted into product oil, to promote liquid
The carbon dioxide row in heavy crude upgrading processes is greatly reduced while improving the economic benefit of hydrogenation process in yield
It puts, so that process is more environmentally protective.But there has been no the heavy crude methane carried out with this thinking, and hydrogen industrialization to be added to use at present.
Summary of the invention
In view of the above-mentioned deficiencies in the prior art, the technical problem to be solved by the present invention is that providing a kind of using methane
Heavy crude catalytic hydrogenation method, using methane replace hydrogen, while reducing hydrogenation process cost, further promoted production
The yield and quality of product, and the discharge of carbon dioxide is greatly reduced, so that process economy is environmentally friendly.
The invention adopts the following technical scheme:
A kind of heavy crude catalytic hydrogenation method using methane, is pumped into the hydrogenation reaction equipped with catalyst for heavy crude
In device, methane being passed through as reaction gas and carries out catalytic hydrogenation reaction, the macromolecular in heavy crude is broken down into alkane and light
Matter aromatic compound, product oil, which flows out below the hydrogenator and is passed through knockout drum, carries out gas-liquid separation, tail gas from
Gas-liquid separation tank top is used for subsequent processing with pipeline outflow, and product oil flows into products pot from gas-liquid separation pot bottom and received
Collection, knockout drum connect cooling system for reducing the temperature of product oil, the viscosity of the product oil of acquisition for 107~
379mPas, density are 0.9511~0.9642g/ml, and total acidity is 0.02~1.55mg KOH/g, average molecular weight 172
~210g/mol, water content are 0.21~0.30wt.%, and product liquid yield is 96.9~104%.
Specifically, the preheating temperature of the head tank equipped with heavy crude is 70~90 DEG C.
Specifically, reaction gas further includes one of natural gas, hydrogen and nitrogen or a variety of.
Specifically, the anti-temperature of catalytic hydrogenation is 300~500 DEG C.
Specifically, the operating pressure of hydrogenator is 1~200 atmospheric pressure.
Further, the operating pressure of hydrogenator is 30~50 atmospheric pressure.
Specifically, hydrogenator is continuous tubular reactor, continuous stirred tank reactor, batch reactor and half
One of batch reactor or multiple combinations.
Further, when reactor is flow reactor, the volume space velocity of heavy crude is 0.1~100h-1；When anti-
When to answer device be batch reactor, the mass ratio of heavy crude and catalyst is (200~1): (1~10)；When reactor is to connect
When continuous formula reactor, the volume space velocity of reaction gas is 1~1000h-1。
Further, hydrogenator is that fixed bed reactors, trickle bed reactor, moving-burden bed reactor, fluidized bed are anti-
Answer one of device and paste state bed reactor or multiple combinations.
Specifically, catalyst is fresh catalyst, the mixing of regenerated catalyst or both.
Compared with prior art, the present invention at least has the advantages that
The present invention utilizes the heavy crude catalytic hydrogenation method of methane, eliminates the step of steam reforming prepares hydrogen,
Process flow is simplified, production cost is significantly reduced, by using the reaction gas based on methane, is added to replace conventional catalyst
Hydrogen reacts used hydrogen, eliminates the step of steam reforming prepares hydrogen, simplifies process flow, significantly reduces life
Produce cost, meanwhile, the successful use of the operating procedure will be greatly decreased it is heavy-oil modified during CO2 emission, made
Cheng Gengjia is environmentally protective, and due to eliminating steam reforming step, methane participates in the upgrading processes of heavy oil and is added to final
In product liquid, so that the CO2 emission of whole process is greatly reduced, to realize the environmentally protective behaviour of heavy oil modification
Make.
Further, head tank needs to be preheated to 70~90 DEG C, to promote the mobility of heavy crude.
Further, reaction gas can be methane, natural gas, hydrogen, one of nitrogen or mixing, optimization methane.
Compared with methane, the reserves of natural gas are more abundant, and use cost is lower, can replace methane or use with methane blended to reduce
Production cost.For hydrogen reactivity better than methane but at high price, nitrogen is then inert gas.It can be by by hydrogen or nitrogen
With methane blended with the reactivity of regulating gas, to cope with different reaction requirements.
Further, range of reaction temperature is 300-500 DEG C, preferably 350-450 DEG C.If reaction temperature is excessively high, heavy is former
Excessive fragmentation is generated a large amount of coke by oil.And temperature it is too low when, the catalytic activity of catalyst is weaker or even catalytically inactive.Cause
This gives full play to catalyst activity while 300-500 DEG C of reaction temperature can guarantee low coking yield.
Further, the operating pressure of traditional hydrogen catalytic hydrogenation process be 140~280 atmospheric pressure, operational hazards,
The high requirements on the equipment.The present invention carries out hydrogenation reaction using methane, and reaction pressure can be down to 30~50 atmospheric pressure, promoted
While operational safety, requirement of the equipment to crushing resistance is reduced, equipment cost can be reduced.
Further, continuous tubular reactor, continuous stirred tank reactor, batch reactor and semibatch reaction
One of device or combination.The above reactor has been applied successfully in embodiments of the present invention, can be according to production-scale big
It is small to select suitable reactor.
Further, excessively high may reduce of the air speed of material adds hydrogen effect, and inactivates catalyst faster, reduces catalysis
The agent service life.Material air speed is too low, will lead to that catalyst service efficiency is low, causes the rising of production cost.It is numerous according to the present invention
The inspection of embodiment, the above response parameter can guarantee longer catalyst while realizing preferably catalytic hydrogenation effect
Service life and higher catalyst service efficiency.
Further, according to the difference of catalyst loading pattern, hydrogenator can be fixed bed reactors, trickle bed
One of reactor, moving-burden bed reactor, fluidized-bed reactor and paste state bed reactor or multiple combinations.The above reactor by
In the difference of catalyst loading pattern, in heat and mass, material distribution etc. has the characteristics that different.The above reactor is at this
It has been applied successfully, can have been selected according to demands such as different heat and mass and material distributions suitable anti-in inventive embodiments
Answer device.
Further, it is identical as fresh catalyst or more preferably to have verified that regenerated catalyst possesses in embodiments of the present invention
Catalytic activity.Therefore it can be reduced in production process by the mixing of regenerated catalyst or fresh catalyst and regenerated catalyst
Catalyst cost.
In conclusion present invention process process flow operation cost reduces, hydrogenation reaction effect, operating pressure drop are effectively improved
Low and process is environmentally protective.
Below by drawings and examples, technical scheme of the present invention will be described in further detail.
Detailed description of the invention
Fig. 1 is method of hydrotreating flow chart of the present invention.
Specific embodiment
The present invention provides a kind of heavy crude catalytic hydrogenation methods using methane, and device therefor includes head tank, produce
Heavy crude in head tank is pumped into hydrogenator by product tank, oil pump and cooling system, oil pump, and hydrogenator has shifted to an earlier date
Fill a certain amount of catalyst, after the completion of catalytic hydrogenation reaction, product oil flows out below hydrogenator and is passed through gas-liquid
Knockout drum；After the completion of gas-liquid separation, tail gas is flowed out from gas-liquid separation tank top with pipeline, and carries out subsequent processing, to improve liquid
Yield, knockout drum will reduce the temperature of product oil equipped with cooling system, for reducing light components contained in tail gas；
Product oil will flow into products pot from gas-liquid separation pot bottom, so as to later collection product.
Under the effect of the catalyst, methane is further activated, and is reacted in hydrogenator with heavy crude.
In order to enable crude oil can smoothly enter into hydrogenator, head tank needs to be preheated to 70~90 DEG C, to promote heavy
The mobility of crude oil, the heavy crude by preheating mix in pipeline with high pressure methane, then are passed through above fixed bed reactors.
In addition to fixed bed reactors, the invention also includes use other a variety of reactors to carry out the methyl hydride catalyzed of heavy crude
Hydrogenation reaction.By taking embodiment 3 and 4 as an example, application of the present invention in paste state bed reactor, batch reactor is illustrated.
Referring to Fig. 1, a kind of heavy crude catalytic hydrogenation method using methane of the present invention, by heavy crude and with methane
Based on reaction gas mixing after, be passed through in the hydrogenator for being filled with catalyst；Under the effect of the catalyst, what is be activated is anti-
Should gas will complete and the hydrogenation reaction of heavy crude；Macromolecular contained in heavy crude will be broken down into the lesser alkane of molecular weight
Hydrocarbon and light aromatic.
Reaction gas is one of following gas or gaseous mixture: methane, natural gas, hydrogen, nitrogen, optimization methane.
Reaction temperature is 300~500 DEG C.
Reactor operating pressure range is 1~200 atmospheric pressure, preferably 30~50 atmospheric pressure.
Hydrogenator can be one of following reactor or combination: continuous tubular reactor continuously stirs autoclave
Reactor, batch reactor, semibatch reactor.
According to the difference of catalyst loading pattern, reactor can be one of following reactor or combination: fixed bed
Reactor, trickle bed reactor, moving-burden bed reactor, fluidized-bed reactor, paste state bed reactor.
When reactor is flow reactor, the volume space velocity range of heavy crude is 0.1~100h-1。
If reactor is batch reactor, the mass ratio of heavy crude and catalyst is (200~1): (1~10).
When reactor is flow reactor, the volume space velocity range of reaction gas is 1~1000h-1。
Catalyst can be fresh catalyst, the mixing of regenerated catalyst or both.
In order to make the object, technical scheme and advantages of the embodiment of the invention clearer, below in conjunction with the embodiment of the present invention
In attached drawing, technical scheme in the embodiment of the invention is clearly and completely described, it is clear that described embodiment is
A part of the embodiment of the present invention, instead of all the embodiments.The present invention being described and shown in usually here in attached drawing is real
The component for applying example can be arranged and be designed by a variety of different configurations.Therefore, below to the present invention provided in the accompanying drawings
The detailed description of embodiment be not intended to limit the range of claimed invention, but be merely representative of of the invention selected
Embodiment.Based on the embodiments of the present invention, those of ordinary skill in the art are obtained without creative efforts
The every other embodiment obtained, shall fall within the protection scope of the present invention.
Embodiment 1
Heavy crude is preheated to 70 DEG C in head tank, the heavy crude and high pressure methane by preheating mix in pipeline
Merging is passed through the fixed bed reactors for filling HOU2-2 catalyst.Reaction temperature is 400 DEG C, and operating pressure is 50 atmosphere
Pressure.The volume space velocity (LHSV) of heavy crude is 1h-1, the volume space velocity of methane is 12h-1；Under the effect of the catalyst, methane
Catalytic hydrogenation reaction will be carried out in heavy crude；After the completion of hydrogenation reaction, product oil flows out below reactor and is passed through gas-liquid
Knockout drum carries out gas-liquid separation；The temperature of product oil is down to room temperature equipped with cooling system by knockout drum；Gas-liquid separation
After the completion, tail gas flows into after-treatment system, and product oil stream enters products pot and waits collection.
After carrying out catalytic hydrogenation reaction to heavy crude under the action of catalyst and methane, the viscosity (15.6 of product oil
DEG C) from 3,866mPas it is down to 257mPas, density (15.6 DEG C) drops to 0.9621g/ml from 0.9645g/ml.Total acidity
Drop to 1.55mg KOH/g from 2.28mg KOH/g, average molecular weight drops to 210g/mol from 228g/mol, water content from
0.33wt.% drops to 0.21wt.%, and product liquid yield is 104%.
The chemical composition of product oil greatly improves compared with heavy crude, and specific SARA analysis the results are shown in Table 2, chemistry
Composition analysis result is shown in Table 3.The boiling point of product oil reduces 100 DEG C or so compared with heavy crude, specific simulation distillation knot
Fruit is shown in Table 4.
Embodiment 2
Heavy crude is preheated to 70 DEG C in head tank, the heavy crude and high pressure methane by preheating mix in pipeline
Merging is passed through the fixed bed reactors for filling HOU 2-3 catalyst；Reaction temperature is 430 DEG C, and operating pressure is 50 atmosphere
Pressure；The volume space velocity (LHSV) of heavy crude is 0.5h-1, the volume space velocity of methane is 20h-1.Under the effect of the catalyst, first
Alkane will carry out catalytic hydrogenation reaction in heavy crude；After the completion of hydrogenation reaction, product oil flows out below reactor and is passed through gas
Liquid knockout drum carries out gas-liquid separation；The temperature of product oil is down to room temperature equipped with cooling system by knockout drum；Gas-liquid point
From after the completion, tail gas flows into after-treatment system, and product oil stream enters products pot and waits collection.
After carrying out catalytic hydrogenation reaction to heavy crude under the action of catalyst and methane, the viscosity (15.6 of product oil
DEG C) from 3,866mPas it is down to 128mPas, density (15.6 DEG C) drops to 0.9530g/ml from 0.9645g/ml；Total acidity
Drop to 0.98mg KOH/g from 2.28mg KOH/g, average molecular weight drops to 185g/mol from 228g/mol, water content from
0.33wt.% drops to 0.24wt.%；Product liquid yield is 99.5%.
The chemical composition of product oil greatly improves compared with heavy crude, and specific SARA analysis the results are shown in Table 2, chemistry
Composition analysis result is shown in Table 3.The boiling point of product oil reduces 100 DEG C or so compared with heavy crude, specific simulation distillation knot
Fruit is shown in Table 4.
Except the above, heavy crude is in differential responses gas, temperature, is catalyzed under pressure using fixed bed reactors
Add the embodiment 5-17 that the results are shown in Table in 1 of hydrogen.
Embodiment 3
Paste state bed reactor is because of the features such as its heat and mass effect is good, and material dispersion is uniform, in recent years in petrochemical industry etc.
Field presents huge development potentiality.
The present embodiment carries out the methyl hydride catalyzed hydrogenation reaction to heavy crude using gas-liquid-solid three-phase paste state bed reactor, tool
Gymnastics is made as follows:
Heavy crude is preheated to 70 DEG C in head tank, the heavy crude and catalyst by preheating are with the volume of 1:1
Than being passed through three phase slurry bed reactor after mixing, catalyst is dispersed in liquid bed；
After high pressure methane is passed through reactor, bed is passed through in the form of bubbling, and under evenly dispersed catalyst action
It is reacted with heavy crude, reaction temperature is 410 DEG C, and operating pressure is 50 atmospheric pressure；
The volume space velocity of methane is 20h-1, after the completion of hydrogenation reaction, the product oil of catalyst is mixed with below reactor
It flows out and is passed through knockout drum and carry out gas-liquid separation, the temperature of product oil is down to room temperature equipped with cooling system by knockout drum
Left and right；
After the completion of gas-liquid separation, tail gas flows into after-treatment system, and being mixed with catalyst prod oil will be separated by solid-liquid separation, point
Separating out the catalyst come can reuse after regeneration.
After carrying out catalytic hydrogenation reaction to heavy crude under the action of catalyst and methane, the viscosity (15.6 of product oil
DEG C) from 3,866mPas it is down to 107mPas, density (15.6 DEG C) drops to 0.9511g/ml from 0.9645g/ml.Total acidity
Drop to 0.95mg KOH/g from 2.28mg KOH/g, average molecular weight drops to 172g/mol from 228g/mol, water content from
0.33wt.% drops to 0.30wt.%, and product liquid yield is 101%.
Embodiment 4:
The present embodiment carries out hydrogenation reaction using the batch reactor of 300ml.
Catalyst and heavy crude are poured into reactor with the mass ratio of 1:100, backward reactor be filled with it is 30 big
The methane gas of air pressure；
It isothermal reaction 40 minutes after reactor is heated to 400 DEG C after reaction will after reactor is cooled to room temperature
The product oil for being mixed with catalyst is collected in reactor release；
After being separated by solid-liquid separation, product oil is collected.
After carrying out catalytic hydrogenation reaction to heavy crude under the action of catalyst and methane, the viscosity (25 DEG C) of product oil
It is down to 379mPas from 848,080mPas, density (25 DEG C) drops to 0.9642g/ml from 1.0275g/ml.Total acidity from
2.69mg KOH/g drops to 0.02mg KOH/g, and asphalt content drops to 9.41wt.% from 22.04wt.%, and product liquid is received
Rate is 96.9%.
Table 1: to a variety of heavy crude in differential responses gas in fixed bed reactors, temperature is catalyzed under pressure
Add hydrogen result
Table 2: heavy crude and the SARA of embodiment 1,2 analyze result
Table 3: the composition analysis result of heavy crude and embodiment 1,2
Table 4: result is distilled in the simulation of heavy crude and embodiment 1,2
The present invention greatly improves the product of heavy crude by carrying out catalytic hydrogenation reaction using methane and heavy crude
Matter, the viscosity of product oil, density, the indexs such as acidity are obviously improved, and in embodiment, the viscosity of product oil can be from initial
About 111,917cP is down to 200cP or so, and the macromoleculars such as asphalitine in heavy crude can be converted into economy after catalytic hydrogenation
It is worth higher alkane and light aromatic, improves the economic benefit of methyl hydride catalyzed hydrogenation reaction.
The above content is merely illustrative of the invention's technical idea, and this does not limit the scope of protection of the present invention, all to press
According to technical idea proposed by the present invention, any changes made on the basis of the technical scheme each falls within claims of the present invention
Protection scope within.
Claims (10)
1. a kind of heavy crude catalytic hydrogenation method using methane, which is characterized in that being pumped into heavy crude equipped with catalyst
Hydrogenator in, be passed through methane as reaction gas and carry out catalytic hydrogenation reaction, the macromolecular in heavy crude is decomposed
At alkane and light aromatic, product oil, which flows out below hydrogenator and is passed through knockout drum, carries out gas-liquid point
From tail gas is used for subsequent processing with pipeline outflow from gas-liquid separation tank top, and product oil flows into product from gas-liquid separation pot bottom
Tank is collected, and knockout drum connects cooling system for reducing the temperature of product oil, and the viscosity of the product oil of acquisition is 107
~379mPas, density are 0.9511~0.9642g/ml, and total acidity is 0.02~1.55mg KOH/g, and average molecular weight is
172~210g/mol, water content are 0.21~0.30wt.%, and product liquid yield is 96.9~104%.
2. the heavy crude catalytic hydrogenation method according to claim 1 using methane, which is characterized in that former equipped with heavy
The preheating temperature of the head tank of oil is 70~90 DEG C.
3. the heavy crude catalytic hydrogenation method according to claim 1 using methane, which is characterized in that reaction gas is also
Including one of natural gas, hydrogen and nitrogen or a variety of.
4. the heavy crude catalytic hydrogenation method according to claim 1 using methane, which is characterized in that catalytic hydrogenation is anti-
Temperature be 300~500 DEG C.
5. the heavy crude catalytic hydrogenation method according to claim 1 using methane, which is characterized in that hydrogenator
Operating pressure be 1~200 atmospheric pressure.
6. the heavy crude catalytic hydrogenation method according to claim 5 using methane, which is characterized in that hydrogenator
Operating pressure be 30~50 atmospheric pressure.
7. the heavy crude catalytic hydrogenation method according to any one of claim 1 to 6 using methane, feature exist
In hydrogenator is continuous tubular reactor, continuous stirred tank reactor, batch reactor and semibatch reactor
One of or multiple combinations.
8. the heavy crude catalytic hydrogenation method according to claim 7 using methane, which is characterized in that when reactor is
When flow reactor, the volume space velocity of heavy crude is 0.1~100h-1；When reactor is batch reactor, heavy is former
The mass ratio of oil and catalyst is (200~1): (1~10)；When reactor is flow reactor, the volume of reaction gas is empty
Speed is 1~1000h-1。
9. the heavy crude catalytic hydrogenation method according to claim 7 using methane, which is characterized in that hydrogenator
For one of fixed bed reactors, trickle bed reactor, moving-burden bed reactor, fluidized-bed reactor and paste state bed reactor or
Multiple combinations.
10. the heavy crude catalytic hydrogenation method according to claim 1 using methane, which is characterized in that catalyst is
Fresh catalyst, the mixing of regenerated catalyst or both.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110052226A (en) * | 2019-04-26 | 2019-07-26 | 上海华畅环保设备发展有限公司 | Boiling bed hydrogenation catalyst reactor online eddy flow method for activation recovering in situ and device |
| CN111437873A (en) * | 2020-04-08 | 2020-07-24 | 广西华大骄阳能源环保科技有限公司 | Catalyst for refining heavy crude oil by using natural gas as catalyst and preparation method thereof |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102311762A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Suspension bed heavy oil hydrogenation process start-up method |
| CN107029780A (en) * | 2017-04-01 | 2017-08-11 | 广西华大骄阳能源环保科技有限公司 | A kind of catalyst refined using methyl hydride catalyzed heavy crude and preparation method thereof |
-
2018
- 2018-12-28 CN CN201811619636.9A patent/CN109517624A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102311762A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Suspension bed heavy oil hydrogenation process start-up method |
| CN107029780A (en) * | 2017-04-01 | 2017-08-11 | 广西华大骄阳能源环保科技有限公司 | A kind of catalyst refined using methyl hydride catalyzed heavy crude and preparation method thereof |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110052226A (en) * | 2019-04-26 | 2019-07-26 | 上海华畅环保设备发展有限公司 | Boiling bed hydrogenation catalyst reactor online eddy flow method for activation recovering in situ and device |
| CN111437873A (en) * | 2020-04-08 | 2020-07-24 | 广西华大骄阳能源环保科技有限公司 | Catalyst for refining heavy crude oil by using natural gas as catalyst and preparation method thereof |
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