CN106433760A - Inferior hydrocarbon hydroconversion method using high-pressure displacement oil tank - Google Patents
Inferior hydrocarbon hydroconversion method using high-pressure displacement oil tank Download PDFInfo
- Publication number
- CN106433760A CN106433760A CN201610542321.3A CN201610542321A CN106433760A CN 106433760 A CN106433760 A CN 106433760A CN 201610542321 A CN201610542321 A CN 201610542321A CN 106433760 A CN106433760 A CN 106433760A
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- Prior art keywords
- oil
- displacement
- high pressure
- oil tank
- displacement oil
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- 238000006073 displacement reaction Methods 0.000 title claims abstract description 92
- 238000000034 method Methods 0.000 title claims abstract description 90
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 37
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 37
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 37
- 238000006243 chemical reaction Methods 0.000 claims abstract description 58
- 230000008569 process Effects 0.000 claims abstract description 50
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 47
- 239000011280 coal tar Substances 0.000 claims abstract description 37
- 239000001257 hydrogen Substances 0.000 claims abstract description 34
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 34
- 239000007789 gas Substances 0.000 claims abstract description 21
- 239000003054 catalyst Substances 0.000 claims abstract description 13
- 238000004939 coking Methods 0.000 claims abstract description 8
- 239000007788 liquid Substances 0.000 claims abstract description 7
- 238000011010 flushing procedure Methods 0.000 claims abstract description 6
- 239000003921 oil Substances 0.000 claims description 174
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 36
- 239000000047 product Substances 0.000 claims description 23
- 239000002994 raw material Substances 0.000 claims description 19
- 238000005194 fractionation Methods 0.000 claims description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 8
- 238000004517 catalytic hydrocracking Methods 0.000 claims description 7
- 239000000295 fuel oil Substances 0.000 claims description 7
- 239000003245 coal Substances 0.000 claims description 6
- 239000003208 petroleum Substances 0.000 claims description 6
- 239000011269 tar Substances 0.000 claims description 6
- 229910052757 nitrogen Inorganic materials 0.000 claims description 4
- 239000010734 process oil Substances 0.000 claims description 4
- 238000005406 washing Methods 0.000 claims description 4
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims description 3
- 238000009835 boiling Methods 0.000 claims description 3
- 238000007233 catalytic pyrolysis Methods 0.000 claims description 3
- 239000007795 chemical reaction product Substances 0.000 claims description 3
- 230000000694 effects Effects 0.000 claims description 3
- 239000010763 heavy fuel oil Substances 0.000 claims description 3
- 239000000463 material Substances 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 claims description 3
- 239000003079 shale oil Substances 0.000 claims description 3
- 239000011275 tar sand Substances 0.000 claims description 3
- 238000004227 thermal cracking Methods 0.000 claims description 3
- 238000004523 catalytic cracking Methods 0.000 claims 1
- 238000010790 dilution Methods 0.000 abstract description 7
- 239000012895 dilution Substances 0.000 abstract description 7
- 238000011144 upstream manufacturing Methods 0.000 abstract description 3
- 239000007859 condensation product Substances 0.000 abstract 1
- 238000010438 heat treatment Methods 0.000 abstract 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 abstract 1
- 230000014759 maintenance of location Effects 0.000 abstract 1
- 238000010521 absorption reaction Methods 0.000 description 7
- 230000008859 change Effects 0.000 description 6
- 230000008676 import Effects 0.000 description 4
- 150000001875 compounds Chemical class 0.000 description 3
- 230000005484 gravity Effects 0.000 description 2
- 230000002265 prevention Effects 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- -1 coal tar F1 inferior Chemical class 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 230000000977 initiatory effect Effects 0.000 description 1
- 238000004080 punching Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
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
- C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
-
- 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
- C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
- C10G49/10—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 with moving solid particles
- C10G49/14—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 with moving solid particles according to the "moving-bed" technique
-
- 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
- C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
- C10G49/10—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 with moving solid particles
- C10G49/16—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 with moving solid particles according to the "fluidised-bed" technique
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
An inferior hydrocarbon hydroconversion method using a high-pressure displacement oil tank is especially suitable for the hydroconversion reaction process of coal tar F1 with high content of easy-heating condensation products. Damages of temperature runaway and coking initiated by long-time retention formed by unable forward flow and hydroconversion of the coal tar F1 adsorbed by a reaction space, such as a catalyst bed, to a catalyst and a reactor under accidents, such as an emergency power-failure condition, are prevented. A high-pressure displacement oil tank D1 is arranged at the upstream of a first hydrogenation reactor R101E of the coal tar F1, so after the emergency power failure accident occurs, impelling force provided by expansion of the high-pressure gas, such as hydrogen, in the in a displacement oil tank D1 is used to pinch out displacement oil and introduce the displacement oil into the first hydrogenation reactor R101E to carry out liquid displacement flushing in order to realize hydroconversion, dilution and reaction heat discharge of forward-movement coal tar F1 adsorbed in the reaction space, such as the catalyst bed, thereby increasing the safety of an emergency shutdown process.
Description
Technical field
The present invention relates to a kind of setting high pressure replaces the hydrocarbon hydrogenating conversion process inferior of oil tank, it is particularly suitable for easy thermal condensation
The hydroconversion reactions process of the high coal tar F1 of thing content, in order to Accident prevention such as shuts off power in emergency under situation, reaction compartment is such as
Beds absorption coal tar F1 be unable to forward flow carry out hydro-conversion and formed extended stationary periods cause temperature runaway, coking and
Damage catalyst and reactor, in the upstream of the First hydrogenation reactor R101E of coal tar F1, high pressure displacement oil tank is set
D1, after accident of shutting off power in emergency occurs, the motive force providing that expands using the gases at high pressure such as hydrogen in displacement oil tank D1 will
Displacement oil pressure goes out and imports First hydrogenation reactor R101E to carry out liquid displacement flushing, realizes reaction compartment such as catalyst bed
The forward flow of the coal tar F1 of layer absorption carries out the discharge of hydro-conversion, dilution and reaction heat, increases emergency shutdown process
Security.
Background technology
The present invention relates to the hydroconversion reactions process of the easy high coal tar F1 of pyrocondensation compound content, the subject matter of concern
It is：Such as shut off power in emergency under situation in accident, how to prevent the coal tar F1 of reaction compartment such as beds absorption can not be positive
Flowing carries out hydro-conversion and forms reaction compartment such as catalyst bed in the layer extended stationary periods initiation temperature runaway, coking and damage catalysis
How agent and reactor, increase the security of emergency shutdown process.That is, such as shutting off power in emergency under situation in accident,
Through entering the coal tar F1 of reaction compartment such as beds absorption it is desirable to its energy forward flow carries out hydro-conversion and contains for high hydrogen
The relatively stable oil product of property being difficult to coking of amount, rather than keep the low hydrogen content of its coal tar F1, easy pyrocondensation compound to contain
Measure the oil conditions of high property extremely unstable.
The root causing the problems referred to above is：Such as shut off power in emergency under situation in accident, the shut-down oil product of low-pressure state cannot be defeated
It is fed into reaction compartment such as beds.
The conception of the present invention is：A kind of setting high pressure replaces the hydrocarbon hydrogenating conversion process inferior of oil tank, is particularly suitable for easily
The hydroconversion reactions process of the high coal tar F1 of pyrocondensation compound content, in order to Accident prevention such as shuts off power in emergency under situation, reaction
Space for example beds absorption coal tar F1 be unable to forward flow carry out hydro-conversion and formed extended stationary periods cause temperature runaway,
Coking and damage catalyst and reactor, in the upstream of the First hydrogenation reactor R101E of coal tar F1, high pressure displacement is set
Oil tank D1, after accident of shutting off power in emergency occurs, using the promotion expanding offer of the gases at high pressure such as hydrogen in displacement oil tank D1
Power is replaced replacing oil pressure and have oily ZHY as accident and is imported First hydrogenation reactor R101E and carry out liquid displacement flushing, real
The forward flow of the existing reaction compartment such as coal tar F1 of beds absorption carries out the row of hydro-conversion, dilution and reaction heat
Go out, increase the security of emergency shutdown process.
During device normal operating, high pressure replaces oil tank D1, is in high pressure conditions, back pressure gas can be hydrogen or nitrogen, leads to
It is often new hydrogen and/or the recycle hydrogen of proper temperature state；In high pressure displacement oil tank D1, the occupation rate general warranty of fluid space is put
The ZHY drain time t that changes oil was more than 15 minutes, best 25～60 minutes；In high pressure displacement oil tank D1, the occupation rate of the gas compartment,
The oily discharge flow rate in drain time t for the ZHY of general warranty displacement is not more than setting and is such as equal to normal operating state raw material
The 60～120% of the flow of oil.
High pressure replaces oil tank D1, can use as reaction dilution oil tank, that is, in normal operating state, the displacement of discharge
Oil enters First hydrogenation reactor R101E as flux oil gravity flow, and its flow is typically less than and replaces oily ZHY flow certainly.
Described gravity flow, referring to not against the conveying equipments such as pump boosting rest against pressure itself enter First add
Hydrogen reactor R101E.
Displacement oil, preferably has, with hydrocarbon such as coal tar F1 inferior, ability of preferably dissolving each other, and its hydrogenation is anti-with this understanding
Should be able to power more weak better.Therefore, the displacement oil of coal tar F1, can be that the hydrofinishing of coal tar F1 generates oil or is hydrocracked
Generate oil or their fractionation distillate, it is preferred for generating oil or its fractionation distillate with the hydrofinishing of coal tar F1.
To high pressure replace oil tank D1 conveying displacement oil pump, can be dedicated pump or borrow coal tar F1 plus
Hydrogen refines and generates oil or be hydrocracked the booster generating oil or their fractionation distillate, and such as hydrofinishing tail oil boosting enters
The booster of hydrocracking reaction process, the boosting of hydrofinishing tail oil enters the circulation booster of hydrofining reaction process, adds
The boosting of hydrogen cracking tail oil enters the circulation booster of hydrocracking reaction process, the high pressure washing oil of hydrogenation plant generally setting rises
Press pump.
The inventive method has no report.
The purpose of invention is to propose the hydrocarbon hydrogenating conversion process inferior that a kind of setting high pressure replaces oil tank.
Content of the invention
The present invention a kind of setting high pressure replace oil tank hydrocarbon hydrogenating conversion process inferior it is characterised in that：
1., in the first hydroconversion process R1, under hydrogen and hydrogenation catalyst existence condition, raw material hydrocarbon HDS passes through first
The reactor assembly R1E of hydrogenation reactor R101E and follow-up hydrogenation reactor that may be present composition completes the first hydro-conversion
Reaction R1R is converted into the first hydrogenation reaction product R1P and discharges reactor assembly R1E；
2. replace oil system in high pressure, with the presence of gases at high pressure BYQ and displacement oil in high pressure displacement oil tank D1, high pressure is replaced
Oil tank D1 bottom is provided with pipe-line system PIPE100 being connected with the first hydrogenation reactor R101E, and pipe-line system PIPE100 sets
There is valve V100；During displacement oil discharge, it provides the working method of displacement oil as follows：
When the first hydrogenation reactor R101E stops the charging of raw material hydrocarbon HDS, the displacement in displacement oil tank D1 is oily, internally
Under the motive force effect that gases at high pressure such as hydrogen expander provide, displacement oil pressure is gone out, imports first by pipe-line system PIPE100
Platform hydrogenation reactor R101E carries out liquid displacement flushing, and the forward flow realizing the coal tar F1 of reaction compartment carries out hydrogenation turn
The discharge of change, dilution and reaction heat, increases the security of emergency shutdown process；During displacement oil discharge, valve V100 is in and beats
Open state.
Raw material hydrocarbon HDS, can be selected from one or more of following materials：
1. coalite tar or its distillate or its hot procedure gained oil product；
2. medium temperature coal tar or its distillate or its hot procedure gained oil product；
3. high temperature coal-tar or its distillate or its hot procedure gained oil product；
4. coal liquefaction gained liquefied coal coil or its distillate or its hot procedure gained oil product；
5. shale oil or its distillate or its hot procedure gained oil product；
6. tar sand basic weight oil or its hot procedure gained oil product；
7. petroleum base wax oil thermal cracking tars；
8. petroleum based heavy fuel oils hot procedure gained oil product, hot procedure is coking heavy oil process or RFCC
Process or heavy oil catalytic pyrolysis process；
9. other polycyclic aromatic hydrocarbon concentration are higher than the hydrocarbon ils that 10%, aromatic hydrocarbons total content is higher than 40%.
Poor quality hydrocarbon hydrogenating conversion process of the present invention, operating condition is usually：
1. the operating condition of the first hydroconversion process R1 is：Temperature is 170～460 DEG C, pressure is 4.0～28.0MPa,
Hydrogen/feedstock oil volume ratio is 50～5000；
2. the operating condition of high pressure displacement oil tank D1 is：Temperature is 170～460 DEG C, pressure is 6.0～38.0MPa, displacement
The oily time of staying is 0.25～2.5 hour, and the displacement working time is 0.15～2.0 hour, and displacement oil discharge flow rate is raw material hydrocarbon
0.6～1.2 times of HDS normal work flow rate.
Poor quality hydrocarbon hydrogenating conversion process of the present invention, operating condition is generally：
1. the operating condition of the first hydroconversion process R1 is：Temperature be 230～420 DEG C, pressure be 12.0～
20.0MPa, hydrogen/feedstock oil volume ratio is 50～2500；
2. the operating condition of high pressure displacement oil tank D1 is：Temperature is 230～420 DEG C, pressure is 14.0～30.0MPa, puts
Change oil the time of staying for 0.50～1.25 hour, the displacement working time is 0.25～1.0 hour, it is raw material that displacement oil discharges flow rate
0.6～1.0 times of hydrocarbon HDS normal work flow rate.
Poor quality hydrocarbon hydrogenating conversion process of the present invention, operating condition is preferably：
1. the operating condition of the first hydroconversion process R1 is：Temperature be 250～400 DEG C, pressure be 15.0～
18.0MPa, hydrogen/feedstock oil volume ratio is 50～2500；
2. the operating condition of high pressure displacement oil tank D1 is：Temperature is 250～400 DEG C, pressure is 17.0～28.0MPa, puts
Change oil the time of staying for 0.5～1.0 hour, the displacement working time is 0.25～0.75 hour, it is raw material that displacement oil discharges flow rate
0.6～1.0 times of hydrocarbon HDS normal work flow rate.
High pressure replaces the gases at high pressure BYQ in oil tank D1, can be hydrogen and/or the gas containing nitrogen.
High pressure replaces the gases at high pressure BYQ in oil tank D1, can be new hydrogen and/or recycle hydrogen.
Displacement oil, can be that the hydrofinishing of coal tar F1 generates oil or is hydrocracked generation oil or their fractionation cut
Oil.
Replace the pump of oil tank D1 conveying displacement oil to high pressure, can be the oily booster of special displacement, or shared coal tar F1
Hydrofinishing generate oil or be hydrocracked generate oil or they fractionation distillate booster.
Replace the pump of oil tank D1 conveying displacement oil to high pressure, the boosting entrance of hydrofinishing tail oil can be shared and be hydrocracked instead
The booster of process or the boosting of hydrofinishing tail oil is answered to enter the circulation booster of hydrofining reaction process or be hydrocracked tail
Oil boosting enters the circulation booster of hydrocracking reaction process or the high pressure washing oil booster of hydrogenation plant setting.
First hydroconversion process R1, it is possible to use the hydrogenation reactor of fixed bde catalyst bed or floating bed hydrogenation are anti-
Answer device or boiling bed hydrogenation reactor or moving bed hydrogenation reactor.
Specific embodiment
The present invention a kind of setting high pressure replace oil tank hydrocarbon hydrogenating conversion process inferior it is characterised in that：
1., in the first hydroconversion process R1, under hydrogen and hydrogenation catalyst existence condition, raw material hydrocarbon HDS passes through first
The reactor assembly R1E of hydrogenation reactor R101E and follow-up hydrogenation reactor that may be present composition completes the first hydro-conversion
Reaction R1R is converted into the first hydrogenation reaction product R1P and discharges reactor assembly R1E；
2. replace oil system in high pressure, with the presence of gases at high pressure BYQ and displacement oil in high pressure displacement oil tank D1, high pressure is replaced
Oil tank D1 bottom is provided with pipe-line system PIPE100 being connected with the first hydrogenation reactor R101E, and pipe-line system PIPE100 sets
There is valve V100；During displacement oil discharge, it provides the working method of displacement oil as follows：
When the first hydrogenation reactor R101E stops the charging of raw material hydrocarbon HDS, the displacement in displacement oil tank D1 is oily, internally
Under the motive force effect that gases at high pressure such as hydrogen expander provide, displacement oil pressure is gone out, imports first by pipe-line system PIPE100
Platform hydrogenation reactor R101E carries out liquid displacement flushing, and the forward flow realizing the coal tar F1 of reaction compartment carries out hydrogenation turn
The discharge of change, dilution and reaction heat, increases the security of emergency shutdown process；During displacement oil discharge, valve V100 is in and beats
Open state.
Raw material hydrocarbon HDS, can be selected from one or more of following materials：
1. coalite tar or its distillate or its hot procedure gained oil product；
2. medium temperature coal tar or its distillate or its hot procedure gained oil product；
3. high temperature coal-tar or its distillate or its hot procedure gained oil product；
4. coal liquefaction gained liquefied coal coil or its distillate or its hot procedure gained oil product；
5. shale oil or its distillate or its hot procedure gained oil product；
6. tar sand basic weight oil or its hot procedure gained oil product；
7. petroleum base wax oil thermal cracking tars；
8. petroleum based heavy fuel oils hot procedure gained oil product, hot procedure is coking heavy oil process or RFCC
Process or heavy oil catalytic pyrolysis process；
9. other polycyclic aromatic hydrocarbon concentration are higher than the hydrocarbon ils that 10%, aromatic hydrocarbons total content is higher than 40%.
Poor quality hydrocarbon hydrogenating conversion process of the present invention, operating condition is usually：
1. the operating condition of the first hydroconversion process R1 is：Temperature is 170～460 DEG C, pressure is 4.0～28.0MPa,
Hydrogen/feedstock oil volume ratio is 50～5000；
2. the operating condition of high pressure displacement oil tank D1 is：Temperature is 170～460 DEG C, pressure is 6.0～38.0MPa, displacement
The oily time of staying is 0.25～2.5 hour, and the displacement working time is 0.15～2.0 hour, and displacement oil discharge flow rate is raw material hydrocarbon
0.6～1.2 times of HDS normal work flow rate.
Poor quality hydrocarbon hydrogenating conversion process of the present invention, operating condition is generally：
1. the operating condition of the first hydroconversion process R1 is：Temperature be 230～420 DEG C, pressure be 12.0～
20.0MPa, hydrogen/feedstock oil volume ratio is 50～2500；
2. the operating condition of high pressure displacement oil tank D1 is：Temperature is 230～420 DEG C, pressure is 14.0～30.0MPa, puts
Change oil the time of staying for 0.50～1.25 hour, the displacement working time is 0.25～1.0 hour, it is raw material that displacement oil discharges flow rate
0.6～1.0 times of hydrocarbon HDS normal work flow rate.
Poor quality hydrocarbon hydrogenating conversion process of the present invention, operating condition is preferably：
1. the operating condition of the first hydroconversion process R1 is：Temperature be 250～400 DEG C, pressure be 15.0～
18.0MPa, hydrogen/feedstock oil volume ratio is 50～2500；
2. the operating condition of high pressure displacement oil tank D1 is：Temperature is 250～400 DEG C, pressure is 17.0～28.0MPa, puts
Change oil the time of staying for 0.5～1.0 hour, the displacement working time is 0.25～0.75 hour, it is raw material that displacement oil discharges flow rate
0.6～1.0 times of hydrocarbon HDS normal work flow rate.
High pressure replaces the gases at high pressure BYQ in oil tank D1, can be hydrogen and/or the gas containing nitrogen.
High pressure replaces the gases at high pressure BYQ in oil tank D1, can be new hydrogen and/or recycle hydrogen.
Displacement oil, can be that the hydrofinishing of coal tar F1 generates oil or is hydrocracked generation oil or their fractionation cut
Oil.
Replace the pump of oil tank D1 conveying displacement oil to high pressure, can be the oily booster of special displacement, or shared coal tar F1
Hydrofinishing generate oil or be hydrocracked generate oil or they fractionation distillate booster.
Replace the pump of oil tank D1 conveying displacement oil to high pressure, the boosting entrance of hydrofinishing tail oil can be shared and be hydrocracked instead
The booster of process or the boosting of hydrofinishing tail oil is answered to enter the circulation booster of hydrofining reaction process or be hydrocracked tail
Oil boosting enters the circulation booster of hydrocracking reaction process or the high pressure washing oil booster of hydrogenation plant setting.
First hydroconversion process R1, it is possible to use the hydrogenation reactor of fixed bde catalyst bed or floating bed hydrogenation are anti-
Answer device or boiling bed hydrogenation reactor or moving bed hydrogenation reactor.
Main advantages of the present invention are：After accident such as shuts off power in emergency generation, using the gases at high pressure in displacement oil tank D1
The motive force providing that expands as hydrogen goes out and imports First hydrogenation reactor R101E to carry out liquid displacement punching by replacing oil pressure
Wash, the forward flow realizing the reaction compartment such as coal tar F1 of beds absorption carries out hydro-conversion, dilution and reaction heat
Discharge, increase emergency shutdown process security.
The present invention is suitable for new device or existing apparatus transformation.
Claims (11)
1. a kind of setting high pressure replace oil tank hydrocarbon hydrogenating conversion process inferior it is characterised in that：
1., in the first hydroconversion process R1, under hydrogen and hydrogenation catalyst existence condition, raw material hydrocarbon HDS is passed through first and is hydrogenated with
The reactor assembly R1E of reactor R101E and follow-up hydrogenation reactor that may be present composition completes the first hydroconversion reactions
R1R is converted into the first hydrogenation reaction product R1P and discharges reactor assembly R1E；
2. replace oil system in high pressure, with the presence of gases at high pressure BYQ and displacement oil in high pressure displacement oil tank D1, high pressure replaces oil tank
D1 bottom is provided with pipe-line system PIPE100 being connected with the first hydrogenation reactor R101E, and pipe-line system PIPE100 is provided with valve
Door V100；During displacement oil discharge, it provides the working method of displacement oil as follows：
When the first hydrogenation reactor R101E stops the charging of raw material hydrocarbon HDS, the displacement in displacement oil tank D1 is oily, high pressure internally
Under the motive force effect that gas such as hydrogen expander provides, displacement oil pressure is gone out, First is imported by pipe-line system PIPE100 and adds
Hydrogen reactor R101E carries out liquid displacement flushing, and the forward flow realizing the coal tar F1 of reaction compartment carries out hydro-conversion, dilute
Release the discharge with reaction heat, increase the security of emergency shutdown process；During displacement oil discharge, valve V100 is in open shape
State.
2. according to claim 1 method it is characterised in that：
Raw material hydrocarbon HDS can be selected from one or more of following materials：
1. coalite tar or its distillate or its hot procedure gained oil product；
2. medium temperature coal tar or its distillate or its hot procedure gained oil product；
3. high temperature coal-tar or its distillate or its hot procedure gained oil product；
4. coal liquefaction gained liquefied coal coil or its distillate or its hot procedure gained oil product；
5. shale oil or its distillate or its hot procedure gained oil product；
6. tar sand basic weight oil or its hot procedure gained oil product；
7. petroleum base wax oil thermal cracking tars；
8. petroleum based heavy fuel oils hot procedure gained oil product, hot procedure is coking heavy oil process or heavy oil catalytic cracking process
Or heavy oil catalytic pyrolysis process；
9. other polycyclic aromatic hydrocarbon concentration are higher than the hydrocarbon ils that 10%, aromatic hydrocarbons total content is higher than 40%.
3. according to claim 2 method it is characterised in that：
1. the operating condition of the first hydroconversion process R1 is：Temperature is 170～460 DEG C, pressure is 4.0～28.0MPa, hydrogen
Gas/feedstock oil volume ratio is 50～5000；
2. the operating condition of high pressure displacement oil tank D1 is：Temperature is 170～460 DEG C, pressure is 6.0～38.0MPa, displacement oil stops
Stay the time to be 0.25～2.5 hour, replace the working time for 0.15～2.0 hour, displacement oil discharge flow rate is for raw material hydrocarbon HDS just
0.6～1.2 times of the flow rate that often works.
4. according to claim 2 method it is characterised in that：
1. the operating condition of the first hydroconversion process R1 is：Temperature is 230～420 DEG C, pressure is 12.0～20.0MPa, hydrogen
Gas/feedstock oil volume ratio is 50～2500；
2. the operating condition of high pressure displacement oil tank D1 is：Temperature is 230～420 DEG C, pressure is 14.0～30.0MPa, displacement oil
The time of staying is 0.50～1.25 hour, and the displacement working time is 0.25～1.0 hour, and displacement oil discharge flow rate is raw material hydrocarbon
0.6～1.0 times of HDS normal work flow rate.
5. according to claim 2 method it is characterised in that：
1. the operating condition of the first hydroconversion process R1 is：Temperature is 250～400 DEG C, pressure is 15.0～18.0MPa, hydrogen
Gas/feedstock oil volume ratio is 50～2500；
2. the operating condition of high pressure displacement oil tank D1 is：Temperature is 250～400 DEG C, pressure is 17.0～28.0MPa, displacement oil
The time of staying is 0.5～1.0 hour, and the displacement working time is 0.25～0.75 hour, and displacement oil discharge flow rate is raw material hydrocarbon HDS
0.6～1.0 times of normal work flow rate.
6. according to claim 2 method it is characterised in that：
2. the gases at high pressure BYQ that high pressure replaces in oil tank D1 is hydrogen and/or the gas containing nitrogen.
7. according to claim 2 method it is characterised in that：
2. the gases at high pressure BYQ that high pressure replaces in oil tank D1 is new hydrogen and/or recycle hydrogen.
8. according to claim 2 method it is characterised in that：
2. replace oil, be that the hydrofinishing of coal tar F1 generates oil or is hydrocracked generation oil or their fractionation distillate.
9. according to claim 2 method it is characterised in that：
2. replace the pump of oil tank D1 conveying displacement oil to high pressure, be the oily booster of special displacement, or the hydrogenation of shared coal tar F1
Refined generation is oily or is hydrocracked the booster generating oil or their fractionation distillate.
10. according to claim 2 method it is characterised in that：
2. replace the pump of oil tank D1 conveying displacement oil to high pressure, shared hydrofinishing tail oil boosting enters hydrocracking reaction process
Booster or the boosting of hydrofinishing tail oil enter the circulation booster of hydrofining reaction process or hydrocracking tail oil boosting
Enter the circulation booster of hydrocracking reaction process or the high pressure washing oil booster of hydrogenation plant setting.
11. according to claim 2 method it is characterised in that：
1. the first hydroconversion process R1, using the hydrogenation reactor of fixed bde catalyst bed or floating bed hydrogenation reactor or
Boiling bed hydrogenation reactor or moving bed hydrogenation reactor.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102051203A (en) * | 2009-10-27 | 2011-05-11 | 中国石油化工股份有限公司 | Start-up method for external presulfurizing catalyst |
| CN102690685A (en) * | 2011-03-25 | 2012-09-26 | 中国石油化工股份有限公司 | On-stream method of catalytic reforming device |
| US20140027351A1 (en) * | 2011-01-10 | 2014-01-30 | IFP Energies Nouvelles | Process for hydrotreating heavy hydrocarbon feeds with switchable reactors including at least one step of progressive switching |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102051203A (en) * | 2009-10-27 | 2011-05-11 | 中国石油化工股份有限公司 | Start-up method for external presulfurizing catalyst |
| US20140027351A1 (en) * | 2011-01-10 | 2014-01-30 | IFP Energies Nouvelles | Process for hydrotreating heavy hydrocarbon feeds with switchable reactors including at least one step of progressive switching |
| CN102690685A (en) * | 2011-03-25 | 2012-09-26 | 中国石油化工股份有限公司 | On-stream method of catalytic reforming device |
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Effective date of registration: 20190506 Address after: 471003 Ruize Building 2107, 215 Heluo Road, Luoyang High-tech Development Zone, China (Henan) Free Trade Pilot Area Patentee after: Luoyang Rui Hua new energy technology development Co., Ltd. Address before: 471003 room 1503, Shen Tai Building, south section of Nanchang Road, Jianxi District, Luoyang, Henan Co-patentee before: Guo Kai Patentee before: He Jutang Co-patentee before: Li Bo |