CN104710572B - The method and device of the modified C9/C5 Petropols of Trans-critical cycle reaction system hydrodesulfurization coupling - Google Patents
The method and device of the modified C9/C5 Petropols of Trans-critical cycle reaction system hydrodesulfurization coupling Download PDFInfo
- Publication number
- CN104710572B CN104710572B CN201510081990.0A CN201510081990A CN104710572B CN 104710572 B CN104710572 B CN 104710572B CN 201510081990 A CN201510081990 A CN 201510081990A CN 104710572 B CN104710572 B CN 104710572B
- Authority
- CN
- China
- Prior art keywords
- gas
- hydrogenation
- petropols
- hydrogenation reactor
- modified
- 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.)
- Active
Links
Abstract
The method of the modified C9/C5 Petropols of Trans-critical cycle reaction system hydrodesulfurization coupling, including following operating procedure：(1) by C9/C5 Petropols and solvent and add catalyst to mix, heat, dissolving；(2) it is passed through H2And CO2Mixed gas carry out hydrogenation reaction, and reaction temperature is 150 DEG C~400 DEG C, and reaction pressure is 3.0MPa~35.0MPa；(3) the gas H produced in hydrogenation process2S, remaining mixed gas H2And CO2Separated, removed H2S, H2And CO2Pressurization is returned to and carries out hydrogenation reaction recycling；(4) after 1~10h of hydrodesulfurization reaction, product is obtained final product.The inventive method is while the quality of modified C9/C5 Petropols is improved, there is provided a kind of method that can effectively remove organic sulfur in C9/C5 Petropols, optimizes reaction environment.
Description
Technical field
The invention belongs to technical field of petrochemical industry, it is related to a kind of modified C9/ of Trans-critical cycle reaction system hydrogenation-desulfurization coupling
The method and device of C5 Petropols.
Background technology
C9/C5 Petropols are the accessory substance-C_9 fraction of pyrolysis gasoline during petroleum hydrocarbon Pintsch process prepares ethylene process
Through pre-treatment, polymerization, distillation formed a kind of thermoplastic hydrocarbon resin, softening point at 60-160 DEG C, with increasing stick, cohesiveness
The characteristics of easily being mixed with other resins, and acid number is low, water-fast, resistance to ethanol and chemicals-resistant, chemical stability and heat endurance
It is good, and viscosity can be adjusted, it is widely used in paint, rubber, ink, thermosol, sticking tape and adhesive industry.Added in paint
C9/C5 Petropols, can increase paint finishes degree, improve paint attachment degree, hardness, acidproof and alkali resistance；Added in rubber
C9/C5 Petropols can play thickening, reinforcement, the effect for softening；C9/C5 Petropols are added in adhesive can improve viscous
The bonding force of mixture, acid resistance, alkali resistance and water resistance；In ink add C9/C5 Petropols can play color development, quick-drying and
The effect of blast.It is unsaturated all to there is a certain amount of double bond in the C9/C5 Petropols obtained by thermal polymerization or catalytic polymerization
Compound, color is deeper, and softness number is low, and stability is bad, easily occurs under ultraviolet, oxygen or other action of chemicals anti-
Should, resin heat endurance and oxidation stability is deteriorated, can also reduce the compatibility of resin and application.Therefore, can influence
The application field of C9/C5 Petropols, reduces its usable scope field.C9/C5 Petropols are modified by catalytic hydrogenation
Make the double bond contained in resin and part phenyl ring saturation, sulfide, halide that removing C9/C5 Petropols are remained in polymerization
Deng impurity, the photo and thermal stability and intersolubility of resin are improved to reach, reduce colourity, softening point and quality are improved, so as to expand
The application field and increase use value of hydrogenation modification C9/C5 Petropols.Such as in coating industry, C9 hydrogenation modification stones are used
Oleoresin produces marking paint, can improve its resistance to persistence and weatherability, its life-span was extended to 3 years by original 1 year.But
It is that a more thorny problem, particularly C9/C5 Petropols contain micro organic sulfur that C9/C5 hydrogenation of petroleum resin is modified,
Both it is easy to catalyst poisoning is again limited its range of application.Although having now much for hydrogenation modification C9/C5 Petropols
Research, but, except the problems such as modified C9/C5 Petropols described above are contained within micro organic sulfur influences it to use
Outward, C9/C5 Petropols quality modified at present is still unsatisfactory, and requirement of the reaction to equipment, catalysis is very high, from
And cause the increase of cost.At present, the domestic demand to hydrogenation modification Petropols is sharply increased in recent years, but it is domestic so far still
Without a C9/C5 hydrogenation of petroleum resin modified products manufacturer for independent brand.
The content of the invention
The present invention invents a kind of Trans-critical cycle reaction system hydrogenation-desulfurization coupling and changes for not enough present in above-mentioned technology
Property C9/C5 Petropols method and device, while the quality of modified C9/C5 Petropols is improved, there is provided a kind of
The method that organic sulfur in C9/C5 Petropols can effectively be removed, optimizes reaction environment.
To realize the purpose of the present invention, technical solution of the present invention is as follows：
The method of the modified C9/C5 Petropols of Trans-critical cycle reaction system hydrogenation-desulfurization coupling, including following operating procedure：
(1) by C9/C5 Petropols and solvent according to mass ratio 1:1~10:1, add catalyst mixing, heating, dissolving；
(2) it is passed through H2And CO2Mol ratio is 1:1~20:1 mixed gas carry out hydrogenation reaction, and reaction temperature is 150 DEG C
~400 DEG C, reaction pressure is 3.0MPa~35.0MPa；
(3) the gas H produced in hydrogenation process2S, remaining mixed gas H2And CO2Separated, removed H2S, H2
And CO2Pressurization is returned to and carries out hydrogenation reaction recycling；
(4) after 1~10h of hydrogenation-desulphurization reaction, material is released as blending hydrogenation from hydrogenation reactor and is changed after decompression
Property rosin and C9/C5 petroleum resin products.
Preferably, in the step (2) gas of outflow by after expanding machine, being separated into gas-liquid separator,
Resulting solvent liquid is back in hydrogenation reactor, and remaining gas is H2S、H2And CO2,Gas is passed through in absorption tower,
H is absorbed through absorption tower2After S gases, remaining H2And CO2Turbocompressor is passed through again.
Preferably, the flow that the step (3) takes out mixed gas from hydrogenation reactor is 0~12000m3/ h, will
Gas is connected by expanding machine, expanding machine with turbocompressor, toward the interior supplement CO of turbocompressor2And H2Mixed gas, then will be mixed
Gas is closed to be passed through in hydrogenation reactor.
Preferably, the amount of the catalyst for being added in step (1) is the matter of the C9/C5 Petropols and solvent total amount for adding
The 1~30% of amount；Wherein described catalyst is the catalyst of nickel-loaded or palladium.
Preferably, the temperature of gas-liquid separator is 0~50 DEG C in step (3), and pressure is 0.0~0.5MPa, liquid flow
It is 0~100m to measure3/ h, gas flow is 0~10000m3/h。
Preferably, the solvent described in step (1) is hexamethylene, ethyl cyclohexane, n- hexanes, n- heptane, mineral spirits
One kind in oil, 200# solvent naphthas.
A kind of device of hydrogenation-modified C9/C5 Petropols methods of desulfurization coupling, including：
Hydrogenation reactor, it includes：Multiple heating tubes, inside hydrogenation reactor；And gas distributor, it includes
Air inlet and multiple shower nozzles for being vented；Expanding machine, it is connected with the hydrogenation reactor；And turbocompressor, its with
The expanding machine connection, and drive the turbocompressor to work by the expanding machine, the gas outlet of the turbocompressor
It is connected with the hydrogenation reactor.
Preferably, in above-mentioned technical proposal, the gas distributor is L-shaped, and its bottom is annulus tubulose, in the annulus
Multiple shower nozzles for being vented are uniformly provided with pipe.
Preferably, in above-mentioned technical proposal, the heating tube is multiple, is distributed in the hydrogenation reactor in parallel
Portion；The gas distributor has multiple, and the multiple gas distributor is interconnected, and described each gas distributor is located at described
Between heating tube.
Preferably, in above-mentioned technical proposal, the device that hydrogenation modification is blended for rosin and C9/C5 Petropols,
Also include：Dissolution kettle, it is connected with the hydrogenation reactor, the raw material needed for for dissolving production；Gas-liquid separator, itself and institute
State expanding machine connection；Solvent pump, it is connected with the gas-liquid separator, and the liquid flux for that will isolate delivers to the hydrogenation
In reactor；And absorption tower, its air inlet is connected with the gas-liquid separator, and gas outlet is connected with the turbocompressor,
For removing H2S gases.
The inventive method adds C9/C5 Petropols and solvent to melt after heating melts in kettle and is pressed into hydrogenation reactor
It is interior, it is filled with H2And CO2Mixed gas carry out hydrogenation reaction.Due to containing micro organic sulfur in C9/C5 Petropols, easily make
Hydrogenation catalyst poisoning and deactivation, and hydrogenation byproduct H2The accumulation of S not only inhibits chemical balance towards hydrodesulfurization direction
It is mobile, and H2S also has certain corrosiveness to hydrogenation reactor, so the present invention constantly flows out gas using hydrogenation reactor
The method of phase, makes the H being hydrogenated to2S gases constantly leave hydrogenation reactor, so as to eliminate accessory substance H2S is accumulated and caused
Feedback inhibition, broken the chemical balance of C9/C5 hydrogenation of petroleum resin-desulfurization, improve hydrogenation reaction speed peace
Weighing apparatus conversion ratio, realizes the coupling of hydrogenation reaction-desulfurization.
Contain H from the gas phase of hydrogenation reactor outflow2、CO2、H2S and solvent vapo(u)r, but the material of these outflows is through swollen
After the expansion step-down of swollen machine, solvent vapo(u)r is condensed into liquid from gas-liquid separator separates out, and H2S is removed by absorption tower, therefore
Pressurized circulation back into the gas of row hydrogenation reaction be only on-condensible gas H2And CO2.Therefore drive the gas flow of expanding machine big
In the flow of turbocompressor pressurized recirculating gas, also i other words the expansion work that expanding machine is made is more than needed for turbocompressor
Work done during compression, and increased energy needed for system by reaction heat and heating coil heat supply that releasing is hydrogenated with hydrogenation reactor with
Improve solvent vapo(u)r flow；Increased energy needed for system is supplied by the reaction heat and heating coil that releasing is hydrogenated with hydrogenation reactor
To heat energy improving solvent vapo(u)r flow.H is passed through in toward turbocompressor2And CO2Mixed gas, expanding machine pushes directly on
Flat compressor pressurization H2And CO2Circulating involuting system, is then passed through in hydrogenation reactor again.Again due to H2With CO2In hydrogenation reactor
Inside constantly circulation and bubbling flowing, enhance the stirring of material and Mass and heat transfer in hydrogenation reactor, and H2With CO2Also produce
Raw " supercavity " effect, agitator that not only can be in economization hydrogenation reactor is installed but also reduces C9/C5 oil to greatest extent
Resin high viscosity storeroom transmission resistance and hydrogenation double bond steric hindrance, greatly increase C9/C5 hydrogenation of petroleum resin-
The reaction effect of desulfurization coupling.
Cyclic process of the present invention is that (steam is moved for compression → reaction → separation → Trans-critical cycle expansion → gas-liquid separation → compression
Power), from the gas phase of hydrogenation reactor outflow, wherein being specially the CO flowed out by hydrogenation reactor2, from super/subcritical state jump
It is low-temp low-pressure normality i.e. referred to as Trans-critical cycle state to move, and the change makes expander do work to drive turbocompressor, to reach
Expansion-compression self-loopa.The steam that the reaction heat or coil pipe endogenous pyrogen indirectly heat released by reaction system are vaporized directly does
Power, heat to power output efficiency is about 100%.
Compared with prior art, the beneficial effects of the invention are as follows：
1st, the present invention is using hydrogenation-desulfurization coupling Trans-critical cycle CO2The modified C9/C5 Petropols of reaction system, can be effective
The micro organic sulfur contained in C9/C5 Petropols is removed, the quality of modified C9/C5 Petropols is improved, expanding it makes
Use field；Improve modified stability, color and luster of C9/C5 Petropols etc. simultaneously.Further hydrogenation reaction mistake of the present invention
Cheng Zhongneng effectively removes the accessory substance H of generation2S, makes reaction constantly be carried out towards the direction of hydrogenation-desulfurization, improves and adds
Hydrogen-desulphurization reaction speed and equilibrium conversion.
2nd, using Trans-critical cycle CO2Expansion-compression self-circulation technology, makes the high pressure vapor from hydrogenation reactor outflow expanded
Machine expansion pushes directly on turbocompressor pressurization H2And CO2Circulating involuting system, reduces heat to power output process：Heat energy → mechanical energy
The exergy loss of → electric energy → mechanical energy, improves the heat power efficiency of heat energy conversion.
3rd, overcritical H2And CO2Constantly bubbling circulates stirring and produces " supercavity " effect in hydrogenation reactor,
Not only the mixer of economization hydrogenation reactor was installed but also reduced the biography of high viscosity C9/C5 Petropols storerooms to greatest extent
Resistance and steric hindrance are passed, the heat and mass speed and hydrogenation-desulphurization reaction effect of hydrogenation reactor is greatly increased.
4th, hydrogenation reactor is using super/subcritical H2And CO2Carry out bubbling stirring, it is not necessary to mechanical agitator is installed, is more had
Manufacture, operation, maintenance and leakproof beneficial to high-tension apparatus.
Brief description of the drawings
Fig. 1 is the modified C9/C5 Petropols method flow diagrams of hydrogenation-desulfurization coupling, wherein 1 is dissolution kettle, 2 is anti-hydrogenation
Device is answered, 3 is expanding machine, and 4 is gas-liquid separator, and 5 is absorption tower, and 6 is turbocompressor, and 7 is solvent pump.
Fig. 2 is the structural representation according to hydrogenation reactor of the present invention, wherein 21 is charging aperture, 22 is gas outlet, and 23 are
Discharging opening, 24 is heating coil, and 25 is gas distributor, and 251 is air inlet, and 252 is shower nozzle.
Fig. 3 is the structural representation according to single gas distributor in hydrogenation reactor of the present invention.
Fig. 4 is the top view according to single gas distributor in hydrogenation reactor of the present invention.
Specific embodiment
Below in conjunction with the accompanying drawings, specific embodiment of the invention is described in detail, it is to be understood that guarantor of the invention
Shield scope is not limited by specific embodiment.
Explicitly indicated that unless otherwise other, otherwise in entire disclosure and claims, term " including " or its change
Change such as "comprising" or " including " etc. and will be understood to comprise stated element or part, and do not exclude other units
Part or other parts.
Embodiment 1
As Figure 1-4, the device of hydrogenation modification is blended for rosin and C9/C5 Petropols, including：Dissolution kettle 1, plus
Hydrogen reactor 2, expanding machine 3, gas-liquid separator 4, absorption tower 5, turbocompressor 6, solvent pump 7.
The discharging opening of dissolution kettle 1 is connected with the charging aperture of the hydrogenation reactor 2, and dissolution kettle 1 is used for needed for dissolving production
Raw material.Hydrogenation reactor 2, in cylinder, the top of hydrogenation reactor is provided with charging aperture 21, gas outlet 22, and bottom is provided with out
Material mouth 23, hydrogenation reactor 2 includes heating tube 24, is heating coil, and it is located inside hydrogenation reactor；Gas distributor 25,
It includes air inlet 251 and multiple shower nozzles 252 for being vented；Expanding machine 3 is connected with the gas outlet of the hydrogenation reactor 2.
Turbocompressor 6 is connected with the expanding machine 3, and drives the turbocompressor 6 to work by the expanding machine 3, described
The gas outlet of flat compressor 6 is connected with the hydrogenation reactor 2.Gas-liquid separator 4 is connected with the expanding machine 3, for separating
The mixed gas produced after reaction, isolate gas and liquid.Solvent pump 7 is connected with gas-liquid separator 2, for that will isolate
Liquid flux is delivered in the hydrogenation reactor 2；The air inlet on absorption tower 5 is connected with the gas-liquid separator 4, gas outlet and institute
State turbocompressor 6 to connect, the gas of removal is needed for removing.
Preferably, the gas distributor 25 is L-shaped, and its bottom is annulus tubulose, is uniformly provided with the ring tube
For the shower nozzle 252 of exhaust, the shower nozzle is " L " type to multiple, is obliquely installed into same direction.It is evenly equipped with pipe annular in shape
Multiple exhaust shower nozzle, discharges gas and is more uniformly distributed so that be fully contacted as the material in hydrogenation reactor and gas, accelerates
Reaction rate.The gas that the shower nozzle being inclined to set sprays is inclined toward same direction and sprays gas, bubble is being added in contorted
Motion in hydrogen reactor 2 so that the material of reaction is fully contacted with gas, accelerates reaction speed.
Preferably, the heating tube 24 is multiple, is distributed on inside the hydrogenation reactor 2 in parallel；The gas point
Cloth device 25 has multiple, and the multiple gas distributor 25 is interconnected, and the ring tube of each gas distributor 25 is located at institute
State between heating tube 24.
A kind of method that hydrogenation modification is blended with C9/C5 Petropols as reaction unit, rosin by the use of above-mentioned device,
Comprise the following steps：By raw material C9/C5 Petropols and ethyl cyclohexane in mass ratio 1:1 adds melting kettle 1, adds raw material total
The catalyst mixing of the supported palladium of the mass fraction 1% of amount, heating melts, and mixed material is formed, by H2And CO2Mol ratio is
10:1 mixed gas are passed through 2 in hydrogenation reactor, are then heated to 150 DEG C, and are constantly filled with H2And CO2Mixed gas
Pressure is 7.0MPa in hydrogenation reactor 2, continues to be heated to 250 DEG C, then opens the gas outlet valve of hydrogenation reactor 2, is made
The H produced in hydrogenation process2S, reacts remaining gas H2With CO2Mixed gas are constantly flowed out, and control mixed gas stream
Output is 12000m3/ h, enters gas-liquid separator 4 after the throttling expansion of expanded machine 3, contain from the gas phase of the outflow of hydrogenation reactor 2
There is H2、CO2、H2S and solvent vapo(u)r, but the expanded expansion of machine 3 step-down of the material of these outflows enters gas-liquid separator 4, gas-liquid
Temperature≤50 DEG C of separator 4, pressure≤0.5MPa, fluid flow≤100m3/ h, gas flow≤10000m3/h.Solvent steams
Vapour is condensed into liquid and is separated from gas-liquid separator 4, into solvent pump 7, returns system circulation and uses.And H2、CO2、H2S
These remaining mixing gas phases enter in absorption tower 5, wherein H2S is removed by absorption tower 5, remaining gas phase H2、CO2With new supplement
H2、CO2Together returning hydrogenation reactor 2 into the pressurized circulation of turbocompressor 6 carries out hydrogenation reaction, and turbine 6 carries out acting is
The expansion work of above-mentioned expanding machine 3 promotes turbocompressor 6 to pressurize, and the flow of mixed gas outflow is about 10000m3/ h, and maintain
The pressure of hydrogenation reactor is 7.0MPa, and after reaction 1.5h, hydrogenation reactor 2 is heated to 350 DEG C, and controlling reaction temperature is protected
Hold in the range of 345 DEG C~355 DEG C, reaction pressure is 14.0MPa~15.0MPa, and 5.0h is reacted at this point in the reaction, is obtained final product
Product, modified C9/C5 Petropols flow out from the discharging opening of hydrogenation reactor 2.It is that modified C9/C5 is hydrogenated with through products obtained therefrom
Petropols, bromine number is 1.0.
Embodiment 2
The reaction unit for using is same as Example 1, by raw material C9/C5 Petropols and hexamethylene in mass ratio 3:1 adds
Enter to melt kettle 1, add the catalyst mixing of the nickel-loaded of the mass fraction 30% of raw material total amount, heating to melt, form mixture
Material, by H2And CO2Mol ratio is 1:1 mixed gas are passed through 2 in hydrogenation reactor, are then heated to 150 DEG C, and constantly
It is filled with H2And CO2Pressure is 3.0MPa in mixed gas to hydrogenation reactor 2, continues to be heated to 250 DEG C, then opens hydrogenation anti-
The gas outlet valve of device 2 is answered, makes the H produced in hydrogenation process2S, reacts remaining gas H2With CO2Mixed gas are constantly
Outflow, it is 7000m to control mixed gas influx3/ h, enters gas-liquid separator 4 after the throttling expansion of expanded machine 3, anti-from hydrogenation
The gas phase for answering device to flow out contains H2、CO2、H2S and solvent vapo(u)r, but the expanded expansion of machine 3 step-down of the material of these outflows enters
Gas-liquid separator 4, temperature≤50 DEG C of gas-liquid separator 4, pressure≤0.5MPa, fluid flow≤100m3/ h, gas flow≤
10000m3/h.Solvent vapo(u)r is condensed into liquid and is separated from gas-liquid separator 4, into solvent pump 7, returns system circulation
Use.And H2、CO2、H2S these it is remaining mixing gas phases enter absorption tower 5 in, wherein H2S is removed by absorption tower 5, remaining gas
Phase H2、CO2With the H of new supplement2、CO2Together returning hydrogenation reactor 2 into the pressurized circulation of turbocompressor 6 carries out hydrogenation reaction,
It is that the expansion work of above-mentioned expanding machine 3 promotes turbocompressor 6 to pressurize that turbine 6 carries out acting.The flow of mixed gas outflow is about
It is 5000m3/ h, and the pressure of hydrogenation reactor is maintained for 3.0MPa, after reaction 3.0h, hydrogenation reactor 2 is heated to 250
DEG C, controlling reaction temperature is maintained in the range of 250 DEG C~255 DEG C, and reaction pressure is 7.0MPa~8.0MPa, in this reaction condition
Lower reaction 5.0h, obtains final product product, and modified C9/C5 Petropols flow out from the discharging opening of hydrogenation reactor 2, and bromine number is 4.0.
Embodiment 3
The reaction unit for using is same as Example 1, by C9/C5 Petropols and 200# solvent naphthas in mass ratio 5:1 adds
Enter to melt kettle 1, add the catalyst mixing of the nickel-loaded of the mass fraction 20% of raw material total amount, heating to melt, form mixture
Material, by H2And CO2Mol ratio is 10:1 mixed gas are passed through 2 in hydrogenation reactor, are then heated to 150 DEG C, and constantly
It is filled with H2And CO2Pressure is 7.0MPa in mixed gas to hydrogenation reactor 2, continues to be heated to 250 DEG C, then opens hydrogenation anti-
The gas outlet valve of device 2 is answered, makes the H produced in hydrogenation process2S, reacts remaining gas H2With CO2Mixed gas are constantly
Outflow, it is 5000m to control mixed gas influx3/ h, enters gas-liquid separator 4 after the throttling expansion of expanded machine 3, anti-from hydrogenation
The gas phase for answering device to flow out contains H2、CO2、H2S and solvent vapo(u)r, but the expanded expansion of machine 3 step-down of the material of these outflows enters
Gas-liquid separator 4, temperature≤50 DEG C of gas-liquid separator 4, pressure≤0.5MPa, fluid flow≤100m3/ h, gas flow≤
10000m3/h.Solvent vapo(u)r is condensed into liquid and is separated from gas-liquid separator 4, into solvent pump 7, returns system circulation
Use.And H2、CO2、H2S these it is remaining mixing gas phases enter absorption tower 5 in, wherein H2S is removed by absorption tower 5, remaining gas
Phase H2、CO2With the H of new supplement2、CO2Together returning hydrogenation reactor 2 into the pressurized circulation of turbocompressor 6 carries out hydrogenation reaction,
It is that the expansion work of above-mentioned expanding machine 3 promotes turbocompressor 6 to pressurize that turbine 6 carries out acting.The flow of mixed gas outflow is about
It is 3000m3/ h, and the pressure of hydrogenation reactor is maintained for 7.0MPa, after reaction 1.5h, hydrogenation reactor 2 is heated to 300
DEG C, controlling reaction temperature is maintained in the range of 300 DEG C~310 DEG C, and reaction pressure is 14.0MPa~15.0MPa, and bar is reacted herein
7.0h is reacted under part, product is obtained final product, modified C9/C5 Petropols flow out from the discharging opening of hydrogenation reactor 2, and bromine number is ＜
1.0。
Embodiment 4
The reaction unit for using is same as Example 1, by C9/C5 Petropols and n- heptane in mass ratio 4:1 addition is molten
Solution kettle 1, adds the catalyst mixing of the supported palladium of the mass fraction 5% of raw material total amount, heating to melt, and forms mixed material, will
H2And CO2Mol ratio is 15:1 mixed gas are passed through 2 in hydrogenation reactor, are then heated to 150 DEG C, and be constantly filled with
H2And CO2Pressure is 7.0MPa in mixed gas to hydrogenation reactor 2, continues to be heated to 250 DEG C, then opens hydrogenation reactor 2
Gas outlet valve, makes the H produced in hydrogenation process2S, reacts remaining gas H2With CO2Mixed gas are constantly flowed out,
It is 3000m to control mixed gas influx3/ h, enters gas-liquid separator 4, from hydrogenation reactor after the throttling expansion of expanded machine 3
The gas phase of outflow contains H2、CO2、H2S and solvent vapo(u)r, but the expanded expansion of machine 3 step-down of the material of these outflows enters gas-liquid
Temperature≤50 DEG C of the gas-liquid separator 4 of separator 4, pressure≤0.5MPa, fluid flow≤100m3/ h, gas flow≤
10000m3/h.Solvent vapo(u)r is condensed into liquid and is separated from gas-liquid separator 4, into solvent pump 7, returns system circulation
Use.And H2、CO2、H2S these it is remaining mixing gas phases enter absorption tower 5 in, wherein H2S is removed by absorption tower 5, remaining gas
Phase H2、CO2With the H of new supplement2、CO2Together returning hydrogenation reactor 2 into the pressurized circulation of turbocompressor 6 carries out hydrogenation reaction,
It is that the expansion work of above-mentioned expanding machine 3 promotes turbocompressor 6 to pressurize that turbine 6 carries out acting.The flow of mixed gas outflow is about
It is 1000m3/ h, and the pressure of hydrogenation reactor is maintained for 7.0MPa, after reaction 1.5h, hydrogenation reactor 2 is heated to 350
DEG C, controlling reaction temperature is maintained in the range of 345 DEG C~355 DEG C, and reaction pressure is 14.0MPa~15.0MPa, and bar is reacted herein
3.0h is reacted under part, product is obtained final product, modified C9/C5 Petropols flow out from the discharging opening of hydrogenation reactor 2, and bromine number is ＜
1.0。
Embodiment 5
The reaction unit for using is same as Example 1, by C9/C5 Petropols and n- hexanes in mass ratio 7:1 addition is molten
Solution kettle 1, adds the catalyst mixing of the supported palladium of the mass fraction 10% of raw material total amount, heating to melt, and forms mixed material,
By H2And CO2Mol ratio is 12:1 mixed gas are passed through 2 in hydrogenation reactor, are then heated to 150 DEG C, and constantly fill
Enter H2And CO2Pressure is 8.0MPa in mixed gas to hydrogenation reactor 2, continues to be heated to 270 DEG C, then opens hydrogenation reaction
The gas outlet valve of device 2, makes the H produced in hydrogenation process2S, reacts remaining gas H2With CO2Mixed gas constantly flow
Go out, it is 1000m to control mixed gas influx3/ h, enters gas-liquid separator 4, from hydrogenation reaction after the throttling expansion of expanded machine 3
The gas phase of device outflow contains H2、CO2、H2S and solvent vapo(u)r, but the expanded expansion of machine 3 step-down of the material of these outflows enters gas
Liquid/gas separator 4, temperature≤50 DEG C of gas-liquid separator 4, pressure≤0.5MPa, fluid flow≤100m3/ h, gas flow≤
10000m3/h., solvent vapo(u)r is condensed into liquid and separated from gas-liquid separator 4, into solvent pump 7, returns system circulation
Use.And H2、CO2、H2S these it is remaining mixing gas phases enter absorption tower 5 in, wherein H2S is removed by absorption tower 5, remaining gas
Phase H2、CO2With the H of new supplement2、CO2Together returning hydrogenation reactor 2 into the pressurized circulation of turbocompressor 6 carries out hydrogenation reaction,
It is that the expansion work of above-mentioned expanding machine 3 promotes turbocompressor 6 to pressurize that turbine 6 carries out acting.The flow of mixed gas outflow is about
It is 500m3/ h, and the pressure of hydrogenation reactor is maintained for 8.0MPa, after reaction 1.5h, hydrogenation reactor 2 is heated to 390
DEG C, controlling reaction temperature is maintained in the range of 380 DEG C~400 DEG C, and reaction pressure is 9.0MPa~10.0MPa, and bar is reacted herein
9.0h is reacted under part, product is obtained final product, modified C9/C5 Petropols flow out from the discharging opening of hydrogenation reactor 2, and bromine number is ＜
1.0。
Embodiment 6
The reaction unit for using is same as Example 1, by C9/C5 Petropols and ethyl cyclohexane in mass ratio 6:1 adds
Enter to melt kettle 1, add the catalyst mixing of the nickel-loaded of the mass fraction 15% of raw material total amount, heating to melt, form mixture
Material, by H2And CO2Mol ratio is 13:1 mixed gas are passed through 2 in hydrogenation reactor, are then heated to 150 DEG C, and constantly
It is filled with H2And CO2Pressure is 8.0MPa in mixed gas to hydrogenation reactor 2, continues to be heated to 250 DEG C, then opens hydrogenation anti-
The gas outlet valve of device 2 is answered, makes the H produced in hydrogenation process2S, reacts remaining gas H2With CO2Mixed gas are constantly
Outflow, it is 500m to control mixed gas influx3/ h, enters gas-liquid separator 4 after the throttling expansion of expanded machine 3, anti-from hydrogenation
The gas phase for answering device to flow out contains H2、CO2、H2S and solvent vapo(u)r, but the expanded expansion of machine 3 step-down of the material of these outflows enters
Gas-liquid separator 4, temperature≤50 DEG C of gas-liquid separator 4, pressure≤0.5MPa, fluid flow≤100m3/ h, gas flow≤
10000m3/h.Solvent vapo(u)r is condensed into liquid and is separated from gas-liquid separator 4, into solvent pump 7, returns system circulation
Use.And H2、CO2、H2S these it is remaining mixing gas phases enter absorption tower 5 in, wherein H2S is removed by absorption tower 5, remaining gas
Phase H2、CO2With the H of new supplement2、CO2Together returning hydrogenation reactor 2 into the pressurized circulation of turbocompressor 6 carries out hydrogenation reaction,
It is that the expansion work of above-mentioned expanding machine 3 promotes turbocompressor 6 to pressurize that turbine 6 carries out acting.The flow of mixed gas outflow is about
It is 300m3/ h, and the pressure of hydrogenation reactor is maintained for 8.0MPa, after reaction 1.5h, hydrogenation reactor 2 is heated to 300
DEG C, controlling reaction temperature is maintained in the range of 300 DEG C~305 DEG C, and reaction pressure is 23.0MPa~25.0MPa, and bar is reacted herein
5.0h is reacted under part, product is obtained final product, modified C9/C5 Petropols flow out from the discharging opening of hydrogenation reactor 2, bromine number ＜
1.0。
Embodiment 7
The reaction unit for using is same as Example 1, by C9/C5 Petropols and 200# solvent naphthas in mass ratio 6:1 adds
Enter to melt kettle 1, add the catalyst mixing of the nickel-loaded of the mass fraction 25% of raw material total amount, heating to melt, form mixture
Material, by H2And CO2Mol ratio is 10:1 mixed gas are passed through 2 in hydrogenation reactor, are then heated to 150 DEG C, and constantly
It is filled with H2And CO2Pressure is 7.0MPa in mixed gas to hydrogenation reactor 2, continues to be heated to 250 DEG C, then opens hydrogenation anti-
The gas outlet valve of device 2 is answered, makes the H produced in hydrogenation process2S, reacts remaining gas H2With CO2Mixed gas are constantly
Outflow, it is 300m to control mixed gas influx3/ h, enters gas-liquid separator 4 after the throttling expansion of expanded machine 3, anti-from hydrogenation
The gas phase for answering device to flow out contains H2、CO2、H2S and solvent vapo(u)r, but the expanded expansion of machine 3 step-down of the material of these outflows enters
Gas-liquid separator 4, temperature≤50 DEG C of gas-liquid separator 4, pressure≤0.5MPa, fluid flow≤100m3/ h, gas flow≤
10000m3/h.Solvent vapo(u)r is condensed into liquid and is separated from gas-liquid separator 4, into solvent pump 7, returns system circulation
Use.And H2、CO2、H2S these it is remaining mixing gas phases enter absorption tower 5 in, wherein H2S is removed by absorption tower 5, remaining gas
Phase H2、CO2With the H of new supplement2、CO2Together returning hydrogenation reactor 2 into the pressurized circulation of turbocompressor 6 carries out hydrogenation reaction,
It is that the expansion work of above-mentioned expanding machine 3 promotes turbocompressor 6 to pressurize that turbine 6 carries out acting.The flow of mixed gas outflow is about
It is 100m3/ h, and the pressure of hydrogenation reactor is maintained for 7.0MPa, after reaction 1.5h, hydrogenation reactor 2 is heated to 200
DEG C, controlling reaction temperature is maintained in the range of 200 DEG C~210 DEG C, and reaction pressure is 14.0MPa~15.0MPa, and bar is reacted herein
8.0h is reacted under part, product is obtained final product, modified C9/C5 Petropols flow out from the discharging opening of hydrogenation reactor 2, and bromine number is
3.0。
Embodiment 8
The reaction unit for using is same as Example 1, by C9/C5 Petropols and hexamethylene in mass ratio 4:1 addition is molten
Solution kettle 1, adds the catalyst mixing of the supported palladium of the mass fraction 8% of raw material total amount, heating to melt, and forms mixed material, will
H2And CO2Mol ratio is 6:1 mixed gas are passed through 2 in hydrogenation reactor, are then heated to 150 DEG C, and are constantly filled with H2
And CO2Pressure is 5.0MPa in mixed gas to hydrogenation reactor 2, continues to be heated to 250 DEG C, then opens hydrogenation reactor 2
Gas outlet valve, makes the H produced in hydrogenation process2S, reacts remaining gas H2With CO2Mixed gas are constantly flowed out,
It is 50m to control mixed gas influx3/ h, enters gas-liquid separator 4, from hydrogenation reactor stream after the throttling expansion of expanded machine 3
The gas phase for going out contains H2、CO2、H2S and solvent vapo(u)r, but the expanded expansion of machine 3 step-down of the material of these outflows enters gas-liquid point
From device 4, temperature≤50 DEG C of gas-liquid separator 4, pressure≤0.5MPa, fluid flow≤100m3/ h, gas flow≤
10000m3/h.Solvent vapo(u)r is condensed into liquid and is separated from gas-liquid separator 4, into solvent pump 7, returns system circulation
Use.And H2、CO2、H2S these it is remaining mixing gas phases enter absorption tower 5 in, wherein H2S is removed by absorption tower 5, remaining gas
Phase H2、CO2With the H of new supplement2、CO2Together returning hydrogenation reactor 2 into the pressurized circulation of turbocompressor 6 carries out hydrogenation reaction,
It is that the expansion work of above-mentioned expanding machine 3 promotes turbocompressor 6 to pressurize that turbine 6 carries out acting.The flow of mixed gas outflow is about
It is 20m3/ h, and the pressure of hydrogenation reactor is maintained for 5.0MPa, after reaction 1.5h, hydrogenation reactor 2 is heated to 280
DEG C, controlling reaction temperature is maintained in the range of 280 DEG C~290 DEG C, and reaction pressure is 10.0MPa~11.0MPa, and bar is reacted herein
3.0h is reacted under part, product is obtained final product, modified C9/C5 Petropols flow out from the discharging opening of hydrogenation reactor 2, and bromine number is
2.0。
Embodiment 9
The reaction unit for using is same as Example 1, by C9/C5 Petropols and hexamethylene in mass ratio 2:1 addition is molten
Solution kettle 1, adds the catalyst mixing of the supported palladium of the mass fraction 1% of raw material total amount, heating to melt, and forms mixed material, will
H2And CO2Mol ratio is 3:1 mixed gas are passed through 2 in hydrogenation reactor, are then heated to 150 DEG C, and are constantly filled with H2
And CO2Pressure is 5.0MPa in mixed gas to hydrogenation reactor 2, continues to be heated to 250 DEG C, then opens hydrogenation reactor 2
Gas outlet valve, makes the H produced in hydrogenation process2S, reacts remaining gas H2With CO2Mixed gas are constantly flowed out,
It is 9m to control mixed gas influx3/ h, enters gas-liquid separator 4 after the throttling expansion of expanded machine 3, from hydrogenation reactor outflow
Gas phase contain H2、CO2、H2S and solvent vapo(u)r, but the expanded expansion of machine 3 step-down of the material of these outflows enters gas-liquid separation
Device 4, temperature≤50 DEG C of gas-liquid separator 4, pressure≤0.5MPa, fluid flow≤100m3/ h, gas flow≤10000m3/
h.Solvent vapo(u)r is condensed into liquid and is separated from gas-liquid separator 4, into solvent pump 7, returns system circulation and uses.And
H2、CO2、H2S these it is remaining mixing gas phases enter absorption tower 5 in, wherein H2S is removed by absorption tower 5, remaining gas phase H2、CO2
With the H of new supplement2、CO2Together returning hydrogenation reactor 2 into the pressurized circulation of turbocompressor 6 carries out hydrogenation reaction, and turbine 6 enters
Row acting is that the expansion work of above-mentioned expanding machine 3 promotes turbocompressor 6 to pressurize.The flow of mixed gas outflow is about 5m3/ h, and
The pressure for maintaining hydrogenation reactor is 5.0MPa, and after reaction 1.5h, hydrogenation reactor 2 is heated to 250 DEG C, control reaction temperature
Degree is maintained in the range of 245 DEG C~255 DEG C, and reaction pressure is 16.0MPa~17.0MPa, is reacted at this point in the reaction
10.0h, obtains final product product, and modified C9/C5 Petropols flow out from the discharging opening of hydrogenation reactor 2, and bromine number is 1.0.
Embodiment 10
The reaction unit for using is same as Example 1, by C9/C5 Petropols and ethyl cyclohexane in mass ratio 10:1 adds
Enter to melt kettle 1, add the catalyst mixing of the supported palladium of the mass fraction 12% of raw material total amount, heating to melt, form mixture
Material, by H2And CO2Mol ratio is 20:1 mixed gas are passed through 2 in hydrogenation reactor, are then heated to 150 DEG C, and constantly
It is filled with H2And CO2Pressure is 9.0MPa in mixed gas to hydrogenation reactor 2, continues to be heated to 250 DEG C, then opens hydrogenation anti-
The gas outlet valve of device 2 is answered, makes the H produced in hydrogenation process2S, reacts remaining gas H2With CO2Mixed gas are constantly
Outflow, it is 8000m to control mixed gas influx3/ h, enters gas-liquid separator 4 after the throttling expansion of expanded machine 3, anti-from hydrogenation
The gas phase for answering device to flow out contains H2、CO2、H2S and solvent vapo(u)r, but the expanded expansion of machine 3 step-down of the material of these outflows enters
Gas-liquid separator 4, temperature≤50 DEG C of gas-liquid separator 4, pressure≤0.5MPa, fluid flow≤100m3/ h, gas flow≤
10000m3/h.Solvent vapo(u)r is condensed into liquid and is separated from gas-liquid separator 4, into solvent pump 7, returns system circulation
Use.And H2、CO2、H2S these it is remaining mixing gas phases enter absorption tower 5 in, wherein H2S is removed by absorption tower 5, remaining gas
Phase H2、CO2With the H of new supplement2、CO2Together returning hydrogenation reactor 2 into the pressurized circulation of turbocompressor 6 carries out hydrogenation reaction,
It is that the expansion work of above-mentioned expanding machine 3 promotes turbocompressor 6 to pressurize that turbine 6 carries out acting.The flow of mixed gas outflow is about
It is 5000m3/ h, and the pressure of hydrogenation reactor is maintained for 9.0MPa, after reaction 1.5h, hydrogenation reactor 2 is heated to 280
DEG C, controlling reaction temperature is maintained in the range of 275 DEG C~285 DEG C, and reaction pressure is 10.0MPa~11.0MPa, and bar is reacted herein
6.0h is reacted under part, product is obtained final product, modified C9/C5 Petropols flow out from the discharging opening of hydrogenation reactor 2, bromine number ＜
1.0。
Embodiment 11
The reaction unit for using is same as Example 1, by C9/C5 Petropols and ethyl cyclohexane in mass ratio 4:1 adds
Enter to melt kettle 1, add the catalyst mixing of the nickel-loaded of the mass fraction 28% of raw material total amount, heating to melt, form mixture
Material, by H2And CO2Mol ratio is 6:1 mixed gas are passed through 2 in hydrogenation reactor, are then heated to 150 DEG C, and constantly
It is filled with H2And CO2Pressure is 28.0MPa in mixed gas to hydrogenation reactor 2, continues to be heated to 250 DEG C, then opens hydrogenation anti-
The gas outlet valve of device 2 is answered, makes the H produced in hydrogenation process2S, reacts remaining gas H2With CO2Mixed gas are constantly
Outflow, it is 4000m to control mixed gas influx3/ h, enters gas-liquid separator 4 after the throttling expansion of expanded machine 3, anti-from hydrogenation
The gas phase for answering device to flow out contains H2、CO2、H2S and solvent vapo(u)r, but the expanded expansion of machine 3 step-down of the material of these outflows enters
Gas-liquid separator 4, temperature≤50 DEG C of gas-liquid separator 4, pressure≤0.5MPa, fluid flow≤100m3/ h, gas flow≤
10000m3/h.Solvent vapo(u)r is condensed into liquid and is separated from gas-liquid separator 4, into solvent pump 7, returns system circulation
Use.And H2、CO2、H2S these it is remaining mixing gas phases enter absorption tower 5 in, wherein H2S is removed by absorption tower 5, remaining gas
Phase H2、CO2With the H of new supplement2、CO2Together returning hydrogenation reactor 2 into the pressurized circulation of turbocompressor 6 carries out hydrogenation reaction,
It is that the expansion work of above-mentioned expanding machine 3 promotes turbocompressor 6 to pressurize that turbine 6 carries out acting.The flow of mixed gas outflow is about
It is 3000m3/ h, and the pressure of hydrogenation reactor is maintained for 28.0MPa, after reaction 3.0h, hydrogenation reactor 2 is heated to
330 DEG C, controlling reaction temperature is maintained in the range of 325 DEG C~335 DEG C, and reaction pressure is 34MPa~35MPa, and bar is reacted herein
1.0h is reacted under part, product is obtained final product, modified C9/C5 Petropols flow out from the discharging opening of hydrogenation reactor 2, and bromine number is
3.0。
Embodiment 12
The reaction unit for using is same as Example 1, by C9/C5 Petropols and ethyl cyclohexane in mass ratio 2:1 adds
Enter to melt kettle 1, add the catalyst mixing of the supported palladium of the mass fraction 9% of raw material total amount, heating to melt, form mixture
Material, by H2And CO2Mol ratio is 6:1 mixed gas are passed through 2 in hydrogenation reactor, are then heated to 150 DEG C, and constantly
It is filled with H2And CO2Pressure is 5.0MPa in mixed gas to hydrogenation reactor 2, continues to be heated to 250 DEG C, then opens hydrogenation anti-
The gas outlet valve of device 2 is answered, makes the H produced in hydrogenation process2S, reacts remaining gas H2With CO2Mixed gas are constantly
Outflow, it is 6000m to control mixed gas influx3/ h, enters gas-liquid separator 4 after the throttling expansion of expanded machine 3, anti-from hydrogenation
The gas phase for answering device to flow out contains H2、CO2、H2S and solvent vapo(u)r, but the expanded expansion of machine 3 step-down of the material of these outflows enters
Gas-liquid separator 4, temperature≤50 DEG C of gas-liquid separator 4, pressure≤0.5MPa, fluid flow≤100m3/ h, gas flow≤
10000m3/h.Solvent vapo(u)r is condensed into liquid and is separated from gas-liquid separator 4, into solvent pump 7, returns system circulation
Use.And H2、CO2、H2S these it is remaining mixing gas phases enter absorption tower 5 in, wherein H2S is removed by absorption tower 5, remaining gas
Phase H2、CO2With the H of new supplement2、CO2Together returning hydrogenation reactor 2 into the pressurized circulation of turbocompressor 6 carries out hydrogenation reaction,
It is that the expansion work of above-mentioned expanding machine 3 promotes turbocompressor 6 to pressurize that turbine 6 carries out acting.The flow of mixed gas outflow is about
It is 5000m3/ h, and the pressure of hydrogenation reactor is maintained for 5.0MPa, after reaction 1.5h, hydrogenation reactor 2 is heated to 370
DEG C, controlling reaction temperature is maintained in the range of 375 DEG C~385 DEG C, and reaction pressure is 10.0MPa~11.0MPa, and bar is reacted herein
3.0h is reacted under part, product is obtained final product, modified C9/C5 Petropols flow out from the discharging opening of hydrogenation reactor 2, bromine number ＜
1.0。
Claims (10)
1. the method that the hydrogenation-desulfurization of Trans-critical cycle reaction system couples modified C9/C5 Petropols, it is characterised in that including following
Operating procedure：
(1) by C9/C5 Petropols and solvent according to mass ratio 1:1~10:1, add catalyst mixing, heating, dissolving；
(2) it is passed through H2And CO2Mol ratio is 1:1~20:1 mixed gas carry out hydrogenation reaction, and reaction temperature is 150 DEG C~400
DEG C, reaction pressure is 3.0MPa~35.0MPa；
(3) the gas H produced in hydrogenation process2S, remaining mixed gas H2And CO2Separated, removed H2S, H2With
CO2Pressurization is returned to and carries out hydrogenation reaction recycling；
(4) after 1~10h of hydrogenation-desulphurization reaction, material releases as C9/C5 Petropols from hydrogenation reactor after decompression
Product.
2. the method that the hydrogenation-desulfurization of Trans-critical cycle reaction system couples modified C9/C5 Petropols according to claim 1, its
It is characterised by：The gas of outflow is resulting by after expanding machine, being separated into gas-liquid separator in the step (2)
Solvent liquid is back in hydrogenation reactor, and remaining gas is H2S、H2And CO2, gas is passed through in absorption tower, through absorption tower
Absorb H2After S gases, remaining H2And CO2Turbocompressor is passed through again.
3. the method that the hydrogenation-desulfurization of Trans-critical cycle reaction system couples modified C9/C5 Petropols according to claim 1, its
It is characterised by：The flow that the step (3) takes out mixed gas from hydrogenation reactor is 9~12000m3/ h, gas is passed through
Expanding machine, expanding machine is connected with turbocompressor, toward the interior supplement CO of turbocompressor2And H2Mixed gas, then mixed gas are led to
Enter in hydrogenation reactor.
4. the method that the hydrogenation-desulfurization of Trans-critical cycle reaction system couples modified C9/C5 Petropols according to claim 1, its
It is characterised by：The amount of the catalyst added in step (1) is the mass fraction 1 of the C9/C5 Petropols and solvent total amount for adding
~30%, wherein described catalyst is the catalyst of nickel-loaded or palladium.
5. the method that the hydrogenation-desulfurization of Trans-critical cycle reaction system couples modified C9/C5 Petropols according to claim 2, its
It is characterised by：The temperature of gas-liquid separator is≤50 DEG C, and pressure is≤0.5MPa, and fluid flow is≤100m3/ h, gas flow
It is≤10000m3/h。
6. the method that the hydrogenation-desulfurization of Trans-critical cycle reaction system couples modified C9/C5 Petropols according to claim 1, its
It is characterised by：Solvent described in step (1) is hexamethylene, ethyl cyclohexane, n- hexanes, n- heptane, mineral essential oil, 200# are molten
One kind in agent oil.
7. the method that the hydrogenation-desulfurization of Trans-critical cycle reaction system couples modified C9/C5 Petropols according to claim 1, its
It is characterised by, the method uses following device, described device includes：
Hydrogenation reactor, it includes：Multiple heating tubes, inside hydrogenation reactor；And gas distributor, it includes air inlet
Mouth and multiple shower nozzles for being vented；Expanding machine, it is connected with the hydrogenation reactor；And turbocompressor, its with it is described
Expanding machine is connected, and drives the turbocompressor work, the gas outlet of the turbocompressor and institute by the expanding machine
State hydrogenation reactor connection.
8. the method that the hydrogenation-desulfurization of Trans-critical cycle reaction system couples modified C9/C5 Petropols according to claim 7, its
It is characterised by：The gas distributor is L-shaped, and its bottom is annulus tubulose, and being uniformly provided with multiple on the ring tube is used for
The shower nozzle of exhaust.
9. the method that the hydrogenation-desulfurization of Trans-critical cycle reaction system couples modified C9/C5 Petropols according to claim 7, its
It is characterised by：The heating tube is multiple, is distributed on inside the hydrogenation reactor in parallel；The gas distributor has many
Individual, the multiple gas distributor is interconnected, and described each gas distributor is located between the heating tube.
10. the method that the hydrogenation-desulfurization of Trans-critical cycle reaction system couples modified C9/C5 Petropols according to claim 7, its
It is characterised by：The device that hydrogenation modification is blended for C9/C5 Petropols, also includes：Dissolution kettle, it is anti-with the hydrogenation
Device is answered to connect, the raw material needed for for dissolving production；Gas-liquid separator, it is connected with the expanding machine；Solvent pump, its with it is described
Gas-liquid separator is connected, and the liquid flux for that will isolate is delivered in the hydrogenation reactor；And absorption tower, its air inlet
It is connected with the gas-liquid separator, gas outlet is connected with the turbocompressor, for removing H2S gases.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510081990.0A CN104710572B (en) | 2015-02-15 | 2015-02-15 | The method and device of the modified C9/C5 Petropols of Trans-critical cycle reaction system hydrodesulfurization coupling |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510081990.0A CN104710572B (en) | 2015-02-15 | 2015-02-15 | The method and device of the modified C9/C5 Petropols of Trans-critical cycle reaction system hydrodesulfurization coupling |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104710572A CN104710572A (en) | 2015-06-17 |
| CN104710572B true CN104710572B (en) | 2017-06-16 |
Family
ID=53410338
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510081990.0A Active CN104710572B (en) | 2015-02-15 | 2015-02-15 | The method and device of the modified C9/C5 Petropols of Trans-critical cycle reaction system hydrodesulfurization coupling |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104710572B (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6020019A (en) * | 1996-03-26 | 2000-02-01 | Miller Brewing Company | Hydrogenation of hop soft resins using CO2 |
| CN102382259A (en) * | 2010-08-30 | 2012-03-21 | 中国石油化工股份有限公司 | Industrial manufacture method for hydrogenated petroleum resin |
| CN102924659A (en) * | 2012-11-12 | 2013-02-13 | 中国石油化工股份有限公司 | Preparation method for C9 hydrogenation petroleum resin |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001172323A (en) * | 1999-12-15 | 2001-06-26 | Arakawa Chem Ind Co Ltd | Hydrogenation method of hydroxyl group-containing petroleum resin and hydroxyl group-containing petroleum resin hydride obtained by the method |
-
2015
- 2015-02-15 CN CN201510081990.0A patent/CN104710572B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6020019A (en) * | 1996-03-26 | 2000-02-01 | Miller Brewing Company | Hydrogenation of hop soft resins using CO2 |
| CN102382259A (en) * | 2010-08-30 | 2012-03-21 | 中国石油化工股份有限公司 | Industrial manufacture method for hydrogenated petroleum resin |
| CN102924659A (en) * | 2012-11-12 | 2013-02-13 | 中国石油化工股份有限公司 | Preparation method for C9 hydrogenation petroleum resin |
Non-Patent Citations (2)
| Title |
|---|
| 加氢石油树脂的生产技术与发展现状;许惠明;《中国胶粘剂》;20140430;第23卷(第4期);第47-51页 * |
| 超临界二氧化碳介质中的催化加氢反应;胡智燕等;《浙江化工》;20021231;第33卷(第1期);第21-23页 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104710572A (en) | 2015-06-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104945224B (en) | Methanol production process | |
| WO2009052764A1 (en) | A composite reaction apparatus and the chemical production method using the same | |
| CN103170218B (en) | Methane purifying method and system | |
| CN105294394A (en) | Methanol co-production recycling system | |
| CN103055526B (en) | Method for evaporating cyclohexanone-oxime | |
| CN109384647A (en) | A kind of transformation methanolizing integrated production equipment and method | |
| CN104788422B (en) | Continuous production method for preparing sulfolane from crude butadiene sulfone | |
| CN110787766B (en) | Tower type reaction device and process for preparing fatty acid butyl ester | |
| CN109438251A (en) | A kind of methanol vapor phase catalytic ammoniation method prepares the method and device thereof of trimethylamine | |
| CN104710572B (en) | The method and device of the modified C9/C5 Petropols of Trans-critical cycle reaction system hydrodesulfurization coupling | |
| CN207287416U (en) | A kind of refrigerant oil mixing apparatus | |
| CN101898930B (en) | Device for producing cyclohexane by adding hydrogen in benzene and synthesis process | |
| CN1631916A (en) | Production method of terpene resin | |
| CN110681319B (en) | System and process for producing durene through injection circulation methanol aromatic methylation reaction | |
| CN103214009B (en) | Synthesis ammonia decarburization technology | |
| CN107056570A (en) | The device and technique of a kind of isooctane refining alkyl unstripped gas | |
| CN104693359B (en) | Trans-critical cycle reaction system hydrogenation modification rosin and C9/C5 Petropols method and devices | |
| CN104694014B (en) | Trans-critical cycle CO2Catalytic esterification separation coupling prepares the method and device of rosin ester | |
| CN208627308U (en) | A kind of New Chemical Material reaction chamber | |
| CN207175838U (en) | A kind of intermittent liquid phase bulk polymerization produces polyacrylic equipment | |
| CN110075764A (en) | A kind of method allosome formula injection membrane reactor and fatty alcohol is prepared using the reactor | |
| CN108586213A (en) | A kind of waste-heat recovery device in ethene hydroformylation reaction process and its method | |
| CN102502697B (en) | Method for recovering ammonia in morpholine solution | |
| CN109200759B (en) | Recovery method of pressure energy of methanol-to-olefin device | |
| CN104674585B (en) | Transcritical CO_2 response system hydrolyzes the method and device of slurrying |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant |