CN204177781U - Oil hydrogenation catalyst evaluation device - Google Patents
Oil hydrogenation catalyst evaluation device Download PDFInfo
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- CN204177781U CN204177781U CN201420593788.7U CN201420593788U CN204177781U CN 204177781 U CN204177781 U CN 204177781U CN 201420593788 U CN201420593788 U CN 201420593788U CN 204177781 U CN204177781 U CN 204177781U
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- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 67
- 239000003054 catalyst Substances 0.000 title claims abstract description 52
- 238000011156 evaluation Methods 0.000 title abstract 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 51
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 36
- 238000006243 chemical reaction Methods 0.000 claims abstract description 33
- 238000000926 separation method Methods 0.000 claims abstract description 33
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 25
- 230000009467 reduction Effects 0.000 claims description 26
- 239000000463 material Substances 0.000 claims description 24
- 239000007789 gas Substances 0.000 claims description 21
- 238000009833 condensation Methods 0.000 claims description 20
- 230000005494 condensation Effects 0.000 claims description 20
- 239000007788 liquid Substances 0.000 claims description 17
- 238000005070 sampling Methods 0.000 claims description 17
- 238000002156 mixing Methods 0.000 claims description 15
- 238000012360 testing method Methods 0.000 claims description 13
- 239000001257 hydrogen Substances 0.000 abstract description 12
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 12
- 239000004519 grease Substances 0.000 abstract description 5
- 239000002994 raw material Substances 0.000 abstract description 3
- 229910001873 dinitrogen Inorganic materials 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 55
- 239000000047 product Substances 0.000 description 25
- 238000000034 method Methods 0.000 description 10
- 238000013461 design Methods 0.000 description 9
- 125000005456 glyceride group Chemical group 0.000 description 8
- 239000007791 liquid phase Substances 0.000 description 7
- 239000000203 mixture Substances 0.000 description 7
- 239000012071 phase Substances 0.000 description 6
- 239000002199 base oil Substances 0.000 description 5
- 238000004517 catalytic hydrocracking Methods 0.000 description 5
- 239000012263 liquid product Substances 0.000 description 5
- 239000002803 fossil fuel Substances 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 230000004044 response Effects 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000002028 Biomass Substances 0.000 description 2
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 238000005498 polishing Methods 0.000 description 2
- 238000010926 purge Methods 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 239000012749 thinning agent Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 125000001931 aliphatic group Chemical group 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 229930195734 saturated hydrocarbon Natural products 0.000 description 1
- 230000001235 sensitizing effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- UFTFJSFQGQCHQW-UHFFFAOYSA-N triformin Chemical compound O=COCC(OC=O)COC=O UFTFJSFQGQCHQW-UHFFFAOYSA-N 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 239000001993 wax Substances 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model discloses a grease hydrogenation catalyst evaluation device, include: a feeding unit, a reaction unit, a product separation and collection unit and a system control unit; the feeding unit comprises a hydrogen inlet unit, a nitrogen inlet unit and a raw material grease feeding unit; the reaction unit is connected with the hydrogen gas inlet unit, the nitrogen gas inlet unit and the raw oil and fat inlet unit; the product separation and collection unit is connected with the reaction unit; the system control unit is connected with the feeding unit, the reaction unit and the product separation and collection unit.
Description
Technical field
The utility model belongs to biomass energy technology field, particularly a kind of oil hydrogenation catalyst evaluating apparatus.
Background technology
Biomass energy has become the Hot spots for development in global range.Wherein, take animal and plant fat as raw material, adopt Catalytic Hydrogenation Techniques, make the reactions such as triglyceride generation hydrotreated lube base oil and hydrogenation deoxidation, obtain oxygen containing aliphatic saturated hydrocarbon hardly, then through the reaction such as hydroisomerizing, hydrocracking, the liquid hydrocarbon fuels such as gasoline, kerosene, diesel oil can be produced, composition and character and fossil fuel almost completely the same, have more the advantages such as renewable, clean, low stain, thus achieve significant progress in recent years.
In the R&D process of oil hydrogenation catalyst, need to carry out a large amount of evaluating catalyst work.Because oil hydrogenation technical research is also in the starting stage, currently used catalyst test apparatus does not carry out targeted design, but improves a little based on fossil fuel hydrogenation catalyst evaluating apparatus and form.
As being called in utility model name: " a kind of liquid phase circulation hydrogenation plant ", application number is: disclose a kind of liquid phase circulation hydrogenation plant in the utility model of CN201220277685.0, this utility model structural representation, as shown in Figure 1, this utility model liquid phase circulation hydrogenation plant is by mixer 300, reactor 700, first separation vessel 100, second separation vessel 120 and associated line composition, in this device, mixer 300 entrance is connected with material tank, mixer 300 outlet is connected with reactor 700 top, outlet bottom first separation vessel 100 is connected with the second separation vessel 120 entrance, first separation vessel 100 gas-phase product outlet is arranged on the first separation vessel 100 top, second separation vessel 120 lighter products outlet is arranged on the second separation vessel 120 top, and the second separation vessel 120 heavy product outlet is arranged on the second separation vessel 120 bottom.This device does not carry out special design for glyceride stock, and cause device to operate inconvenience, efficiency is lower.
In denomination of invention be: " control system method and apparatus for two phasehydroprocessing ", application number is: the invention of US20060144756A1 is also disclosing a kind of two-phase hydrogenation control system method and apparatus.In continuous print liquid-phase hydrogenatin process, eliminate recycle hydrogen, under solvent or thinning agent existent condition, by the mixing of hydrogen oil, hydrogen is greater than the solubleness in feedstock oil in the solubleness of solvent or thinning agent.Hydrogen required for hydrogenation reaction all comes from the hydrogen of liquid phase dissolved, does not need extra hydrogen.But it does not consider the H produced in hydrogenation process
2s and NH
3etc. the inhibiting effect of hydrogenation byproduct to hydrogenation reaction, cause it to accumulate in reaction system, affect the hydrogenation efficiency in the solubleness of hydrogen and course of reaction.
The hydrogenation evaluating apparatus of above-mentioned existing employing does not carry out specialized designs for glyceride stock, but improve a little based on fossil fuel hydrogenation catalyst evaluating apparatus and form, and inconvenient in operation, efficiency is not high yet.On the one hand, the different in kind of glyceride stock, oxygen level is up to more than 10%, and the fossil fuels such as oil are substantially oxygen-free; Condensation point is high, is solid under much animal and plant fat normal temperature; Density and viscosity are also all larger.On the other hand, the response characteristic of oil hydrogenation is different.Such as, because oxygen level is high, oil hydrogenation deoxidation process will produce a large amount of water, and thermal discharge is also larger; The raw material of oil hydrogenation cracking is generally C
15~ C
18straight-chain paraffin, produce boat coal time gas-phase product ratio be significantly higher than traditional wax oil hydrogenation cracking; Aromatic free in grease, hydrogenation products is almost complete to be made up of saturated alkane, also relatively simple on composition analysis.
Therefore, for glyceride stock, design is optimized to hydrogenation catalyst evaluating apparatus, for the development promoting grease Catalytic Hydrogenation Techniques, has great importance.
Utility model content
The purpose of this utility model is to provide a kind of oil hydrogenation catalyst evaluating apparatus, with solve the existing evaluating apparatus that exists in prior art due to glyceride stock different in kind and response characteristic different, and the device inconvenient operation brought, the problem that efficiency is not high.
For reaching above-mentioned purpose, the utility model proposes a kind of oil hydrogenation catalyst evaluating apparatus, comprising:
One feed unit, comprises a hydrogen gas unit, a nitrogen air admission unit and a raw oil material feed unit;
One reaction member, is connected to described hydrogen gas unit, described nitrogen air admission unit and described raw oil material feed unit;
One product separation and collector unit, be connected to described reaction member;
One system control unit, is connected to described feed unit, described reaction member and described product separation and collector unit.
Above-mentioned oil hydrogenation catalyst evaluating apparatus, described raw oil material feed unit also comprises: a material tank, a filtrator, a feedstock oil volume pump and a spark arrester, and described material tank, described filtrator, described feedstock oil volume pump and described spark arrester are sequentially connected by a feedstock pipeline.
Above-mentioned oil hydrogenation catalyst evaluating apparatus, described raw oil material feed unit also comprises: operation valve, described operation valve is connected on the described feedstock pipeline between described feedstock oil volume pump and described spark arrester, and described operation valve comprises a needle valve and a retaining valve.
Above-mentioned oil hydrogenation catalyst evaluating apparatus, described hydrogen gas unit also comprises: a filtrator, a reduction valve, a mass flowmeter and a spark arrester, and described filtrator, described reduction valve, described mass flowmeter are sequentially connected by a hydrogen gas lines with described spark arrester.
Above-mentioned oil hydrogenation catalyst evaluating apparatus, described hydrogen gas unit also comprises: operation valve, and described operation valve is connected in the described hydrogen gas lines between described mass flowmeter and described spark arrester, and described operation valve comprises a needle valve and a retaining valve.
Above-mentioned oil hydrogenation catalyst evaluating apparatus, described nitrogen air admission unit also comprises: a filtrator, a reduction valve, a mass flowmeter, a needle-valve, a retaining valve and a spark arrester, and described filtrator, described reduction valve, described mass flowmeter are sequentially connected by a nitrogen pipeline with described spark arrester.
Above-mentioned oil hydrogenation catalyst evaluating apparatus, described nitrogen air admission unit also comprises: operation valve, and described operation valve is connected between described mass flowmeter and described spark arrester on described nitrogen pipeline, and described operation valve comprises a needle valve and a retaining valve.
Above-mentioned oil hydrogenation catalyst evaluating apparatus, described reaction member also comprises:
One mixing primary heater, is connected to the described spark arrester of described grease feed unit, the described spark arrester of described hydrogen gas unit and the described spark arrester of described nitrogen air admission unit;
One reactor, is connected to described mixing primary heater.
Above-mentioned oil hydrogenation catalyst evaluating apparatus, described product separation and collector unit also comprise:
Two covers can switch the condensation separating unit of use mutually, are connected to described reaction member.
Above-mentioned oil hydrogenation catalyst evaluating apparatus, each described condensation separating unit also comprises:
Condenser, is connected to described reactor;
Knockout drum, is connected to described condenser, and the bottom of described knockout drum connects a liquid sample pipeline.
Above-mentioned oil hydrogenation catalyst evaluating apparatus, the pipeline between described condenser and described reactor is provided with operation valve, and described operation valve is needle valve.
Above-mentioned oil hydrogenation catalyst evaluating apparatus, described product separation and collector unit also comprise further:
One surge tank, be connected to described two cover condensation separating units by pipeline, the top of described surge tank connects a gas sampling pipeline;
One wet test meter, is connected to described surge tank;
One spark arrester, is connected to described wet test meter.
Above-mentioned oil hydrogenation catalyst evaluating apparatus, the pipeline between described surge tank and each described condensation separating unit is provided with operation valve, and described operation valve comprises a reduction valve, a needle valve and a retaining valve.
Above-mentioned oil hydrogenation catalyst evaluating apparatus, described condenser is connected to the described filtrator of described hydrogen gas unit by pipeline, and the pipeline between described condenser and described filtrator is provided with operation valve, and described operation valve is needle valve.
Above-mentioned oil hydrogenation catalyst evaluating apparatus, described knockout drum adopts inverted cone-shaped structure.
Compared to device of the prior art, the main beneficial effect of the utility model is: the utility model has taken into full account the special nature of glyceride stock and the response characteristic of oil hydrogenation, from charging, reaction, product separation, analysis, Systematical control etc. are many-sided, design is optimized to hydrogenation catalyst evaluating apparatus, can be used for the evaluating catalyst of the courses of reaction such as animal and plant fat hydrofining, hydrotreated lube base oil, hydroisomerizing and hydrocracking, there is the advantages such as structure is simple, easy to operate, assess effectiveness is high, data are reliable.
Accompanying drawing explanation
Fig. 1 is prior art evaluating apparatus structural representation;
Fig. 2 is the utility model oil hydrogenation catalyst evaluating apparatus structured flowchart;
Fig. 3 is the utility model specific embodiment oil hydrogenation catalyst evaluating apparatus structural representation;
Fig. 4 is the utility model feed unit structural representation;
Fig. 5 is the utility model reaction member structural representation;
Fig. 6 is the utility model product separation and collector unit structural representation.
Wherein, Reference numeral:
300 mixer 700 reactors
100 first separation vessel 120 second separation vessels
50 feed unit 20 reaction members
30 product separations and collector unit 40 system control unit
101 hydrogen gas unit 102 nitrogen air admission units
103 raw oil material feed unit
1 material tank 2 filtrator;
3 feedstock oil volume pump 41 ~ 410 needle-valves
51 ~ 55 retaining valve 61 ~ 63 reduction valve
7 mass flowmeter 81 ~ 83 spark arresters
9 mixing primary heater 10 reactors
111 condenser 112 condensers
121 knockout drum 122 knockout drums
13 surge tank 14 wet test meters
151 ~ 153 sample taps
Embodiment
Below in conjunction with the drawings and specific embodiments, the utility model is described in detail, but not as to restriction of the present utility model.
The purpose of this utility model is for glyceride stock, is optimized design to hydrogenation catalyst evaluating apparatus, makes it efficiently, is reliably applied to the R&D process of the catalyzer such as oil hydrogenation is refined, hydrotreated lube base oil, hydrocracking, hydroisomerizing.
As shown in Figure 2, a kind of oil hydrogenation catalyst evaluating apparatus that the utility model provides, comprises feed unit 50, reaction member 20, product separation and collector unit 30 and system control unit 40.Feed unit 10 comprises the independent line of hydrogen, nitrogen and raw oil material, material tank, raw oil pump, filtrator, mixing primary heater, reduction valve, mass balance and mass flowmeter etc.Reaction member 20 comprises electric furnace, trickle bed reactor, thermopair, and reactor adopts high pressure resistant stainless-steel tube to make.Product separation and collector unit 30 comprise reduction valve, wet test meter and two overlaps changeable use condenser, knockout drum, and reserved liquid product thief hatch.The equal omnidistance temperature control of pipeline of liquid phase feed and product.Gas phase, after reduction valve release, enters surge tank, and emptying after wet test meter metering, gas sampling mouth reserved by surge tank.System control unit 40 Procedure for selection control instrument, can carry out the setting parameter such as programming rate, constant temperature time, and show temperature, pressure, flow etc., control.This device can be used for the evaluating catalyst of the courses of reaction such as animal and plant fat hydrofining, hydrotreated lube base oil, hydroisomerizing and hydrocracking, has the advantages such as structure is simple, easy to operate, assess effectiveness is high, data are reliable.
Shown in composition graphs 2, Fig. 3 and Fig. 4, the utility model provides a kind of oil hydrogenation catalyst evaluating apparatus, comprising:
One feed unit 50, comprises hydrogen gas unit 101, nitrogen air admission unit 102 and a raw oil material feed unit 103; One reaction member 20, is connected to hydrogen gas unit 101, nitrogen air admission unit 102 and raw oil material feed unit 103; One product separation and collector unit 30, be connected to reaction member 20; One system control unit 40, is connected to feed unit 10, reaction member 20 and product separation and collector unit 30.
Wherein, hydrogen gas unit 101 also comprises: filtrator 22, reduction valve 61, mass flowmeter 71 and a spark arrester 81, this preferred embodiment adopts filtrator 22, reduction valve 61, mass flowmeter 71 and needle-valve 42 and a retaining valve 53, spark arrester 81 is connected to a hydrogen gas lines in order successively, but the present invention is not as limit.
Wherein, nitrogen air admission unit 102 also comprises: filtrator 23, reduction valve 62, mass flowmeter 72 and needle-valve 43 and a retaining valve 52, one spark arrester 81, this preferred embodiment middle filtrator 23, reduction valve 62, mass flowmeter 72 and needle-valve 43 and a retaining valve 52, spark arrester 81 is connected in order successively by a nitrogen pipeline, but the present invention is not as limit.
Wherein, raw oil material feed unit 103 also comprises: material tank 1, filtrator 21, feedstock oil volume pump 3 and, this preferred embodiment Raw oil tank 1, filtrator 21, feedstock oil volume pump 3 and a needle-valve 41 are connected by a feeding line in order successively with retaining valve 51 1 spark arrester 82, but the present invention is not as limit.
Hydrogen gas unit 101 is for the reaction hydrogen supply of device and ftercompction, and nitrogen air admission unit 102 is for the purging of device, drying and cooling.Two-way gas all enters reduction valve after filter dedusting, and after decompression, force value is shown by tensimeter; Flow is controlled by mass flowmeter 3, and flow value is by instrument regulable control and display; The all reserved cross-line for subsequent use of two-way gas, can without mass flowmeter to reactor 10 air feed.Liquid charging stock oil is by mass balance accurate measurement, and the omnidistance temperature control from material tank 1 to reactor 10 entrance, through filter 21 by raw oil pump continuous feed and control flow.
Wherein, shown in composition graphs 3 and Fig. 5, reaction member 20 also comprises: mixing primary heater 9 and a reactor 10, and mixing primary heater 9 is connected to spark arrester 82 and spark arrester 81; Reactor 10 is connected to mixing primary heater 9.
Further, reaction member 20 also comprises electric furnace, trickle bed reactor, thermopair, and wherein, reactor 10 adopts high pressure resistant stainless-steel tube to make, serviceability temperature 260 ~ 400 DEG C, uses pressure 1.0 ~ 10.0MPa.Whole reactor 10 adopts multistage heating to control, to ensure inside reactor constant temperature.In order to ensure temperature-controlled precision and the flat-temperature zone length of reactor, thermopair being set in heating furnace inwall most sensitizing range and being controlled by temperature controller.
Shown in composition graphs 3 and Fig. 6, in embodiments of the present invention, product separation and collector unit 30 also comprise: two condensation separating units that mutually can switch use, often overlap and all independently can connect hydrogen pipeline and carry out ftercompction, release, and be with high-precision pressure digital display, but the present invention is not as limit, be respectively condensation separating unit 301 and condensation separating unit 302, one surge tank 13, wet test meter 14, spark arrester 83; Surge tank 13 is connected to condensation separating unit 301 and condensation separating unit 302, and, surge tank 13 and be provided with reduction valve 63 between condensation separating unit 301 and condensation separating unit 302, and, be provided with needle valve 48 and a retaining valve 55 between reduction valve 63 and knockout drum 121 in order, between reduction valve 63 and knockout drum 122, be provided with needle valve 49 and a retaining valve 54 in order; The top of surge tank 13 is provided with gas sampling pipeline, gas sampling pipeline arranges gas sampling mouth 153 and a needle valve 410, controls gas sampling; Wet test meter 14 is connected to surge tank 13; Spark arrester 83 is connected to wet test meter 14.
Further, also comprise in condensation separating unit 301: condenser 111, knockout drum 121; Condenser 111 is connected to reactor 10, and, the pipeline between condenser 111 and reactor 10 is arranged a needle-valve 46; Knockout drum 121 is connected to condenser 111; The bottom of knockout drum 121 is provided with liquid sample pipeline, product liquid sampling pipeline arranges product liquid thief hatch 151 and a needle valve 44, controls product liquid sampling;
Further, also comprise in condensation separating unit 302: condenser 112, knockout drum 122; Condenser 112 is connected to reactor 10, and arranges a needle-valve 47 between condenser 112 and reactor 10; Knockout drum 122 is connected to condenser 112; The bottom of knockout drum 122 is provided with liquid sample pipeline, and on liquid sample pipeline, be provided with product liquid thief hatch 152 and a needle valve 45;
Wherein, condenser 111 and condenser 112 are connected to the filtrator 22 of hydrogen gas unit 101, and are provided with needle valve 410 between condenser 111 and hydrogen gas unit 101, are provided with needle valve 411 between condenser 112 and hydrogen gas unit 101.
Knockout drum 121 and 122 adopts back taper design, inwall polishing.The equal omnidistance temperature control of pipeline of liquid phase feed and product.Gas phase, after reduction valve release, enters surge tank 13, and emptying after wet test meter 14 measures, gas sampling mouth reserved by surge tank 13.The reserved external sampling valve in liquid product thief hatch 151 and 152 place, accurate filter, gas chromatograph or liquid chromatograph.The reserved external sampling valve in gas sampling mouth 153 place, accurate filter and gas chromatograph.
Condenser 111 and 112 can connect recirculated water, and adds the cross-line of changeable use, and outlet, entrance are all equipped with temperature instrumentation.Knockout drum 121 and 122 adopts back taper design, inwall polishing.
In the present embodiment, condensation separating unit is two covers, but the utility model is not limited to this, and this condensation separating unit can be many covers.
System control unit 40 Procedure for selection control instrument, can carry out the setting parameter such as programming rate, constant temperature time, and show temperature, pressure, flow etc., control.Temperature control precision is ± 1 DEG C, and pressure controling precision is ± 0.05MPa.
Below the concrete implementation step of the utility model and workflow are described in detail:
Charging preparation process:
Feedstock oil by mass balance real time measure, enters in mixing primary heater 9 by filtrator 21, feedstock oil volume pump 3, needle-valve 41, retaining valve 51, spark arrester 81 successively through pipeline in material tank 1;
Air inlet pressurization steps:
(1) hydrogen enters in mixing primary heater 9 by filtrator 22, reduction valve 61, mass flowmeter 71, needle-valve 42, retaining valve 52, spark arrester 81 through pipeline successively;
(2) gas-liquid mixture is mixing Homogeneous phase mixing in primary heater 9 and after being warming up to assigned temperature, entering in trickle bed reactor 10, under catalyst action, hydrogenation reaction occurs, enter condenser 111 or 112, knockout drum 121 or 122 successively afterwards.
(4), when gathering liquid product, need to switch use condenser 111 and 112 and knockout drum 121 and 122.
(5) now, close the valve before condenser 111 and 112 in using, open the valve after knockout drum 121 and 122 in using, and contrary operation is carried out to another set of piece-rate system.
(6), after gas-liquid separation completely, product liquid can discharge from sample tap 151 or 152, collect;
(7) gas enters in surge tank 13 after reduction valve 63, and surge tank 13 is reserved with gas sampling mouth 153, and during normal running, gas continues emptying after wet test meter 14 and spark arrester 83.
(8) after liquid product drains, need ftercompction operation be carried out, now open the valve 410 or 411 on ftercompction pipeline, when the pressure displayed value of gas-liquid separator reaches specified pressure, valve-off.
The back work step of nitrogen:
Nitrogen line is used for purging, the drying of device and lowers the temperature.Now, nitrogen enters in mixing primary heater 9 by filtrator 23, reduction valve 62, mass flowmeter 72, needle-valve 43, retaining valve 53, spark arrester 82 through pipeline successively, needs to take open and close operation to the valve before and after reactor 10 according to use.
Reserved liquid product thief hatch 151 or 152 place can connect sampling valve, accurate filter, gas chromatograph or liquid chromatograph.Reserved gas sampling mouth 153 place connects sampling valve, accurate filter and gas chromatograph.
In sum, the utility model has taken into full account the special nature of glyceride stock and the response characteristic of oil hydrogenation, from charging, reaction, product separation, analysis, Systematical control etc. are many-sided, design is optimized to hydrogenation catalyst evaluating apparatus, can be used for the evaluating catalyst of the courses of reaction such as animal and plant fat hydrofining, hydrotreated lube base oil, hydroisomerizing and hydrocracking, there is the advantages such as structure is simple, easy to operate, assess effectiveness is high, data are reliable.
Certainly; the utility model also can have other various embodiments; when not deviating from the utility model spirit and essence thereof; those of ordinary skill in the art are when making various corresponding change and distortion according to the utility model, but these change accordingly and are out of shape the protection domain that all should belong to the claim appended by the utility model.
Claims (15)
1. an oil hydrogenation catalyst evaluating apparatus, is characterized in that, comprising:
One feed unit, comprises a hydrogen gas unit, a nitrogen air admission unit and a raw oil material feed unit;
One reaction member, is connected to described hydrogen gas unit, described nitrogen air admission unit and described raw oil material feed unit;
One product separation and collector unit, be connected to described reaction member;
One system control unit, is connected to described feed unit, described reaction member and described product separation and collector unit.
2. oil hydrogenation catalyst evaluating apparatus according to claim 1, it is characterized in that, described raw oil material feed unit also comprises: a material tank, a filtrator, a feedstock oil volume pump and a spark arrester, and described material tank, described filtrator, described feedstock oil volume pump and described spark arrester are sequentially connected by a feedstock pipeline.
3. oil hydrogenation catalyst evaluating apparatus according to claim 2, it is characterized in that, described raw oil material feed unit also comprises: operation valve, described operation valve is connected on the described feedstock pipeline between described feedstock oil volume pump and described spark arrester, and described operation valve comprises a needle valve and a retaining valve.
4. oil hydrogenation catalyst evaluating apparatus according to claim 1, it is characterized in that, described hydrogen gas unit also comprises: a filtrator, a reduction valve, a mass flowmeter and a spark arrester, and described filtrator, described reduction valve, described mass flowmeter are sequentially connected by a hydrogen gas lines with described spark arrester.
5. oil hydrogenation catalyst evaluating apparatus according to claim 4, it is characterized in that, described hydrogen gas unit also comprises: operation valve, described operation valve is connected in the described hydrogen gas lines between described mass flowmeter and described spark arrester, and described operation valve comprises a needle valve and a retaining valve.
6. oil hydrogenation catalyst evaluating apparatus according to claim 1, it is characterized in that, described nitrogen air admission unit also comprises: a filtrator, a reduction valve, a mass flowmeter, a needle-valve, a retaining valve and a spark arrester, and described filtrator, described reduction valve, described mass flowmeter are sequentially connected by a nitrogen pipeline with described spark arrester.
7. oil hydrogenation catalyst evaluating apparatus according to claim 6, it is characterized in that, described nitrogen air admission unit also comprises: operation valve, and described operation valve is connected between described mass flowmeter and described spark arrester on described nitrogen pipeline, and described operation valve comprises a needle valve and a retaining valve.
8. oil hydrogenation catalyst evaluating apparatus according to claim 1, it is characterized in that, described reaction member also comprises:
One mixing primary heater, is connected to the spark arrester of described raw oil material feed unit, the spark arrester of described hydrogen gas unit and the spark arrester of described nitrogen air admission unit;
One reactor, is connected to described mixing primary heater.
9. oil hydrogenation catalyst evaluating apparatus according to claim 1, it is characterized in that, described product separation and collector unit also comprise:
Two covers can switch the condensation separating unit of use mutually, are connected to described reaction member.
10. oil hydrogenation catalyst evaluating apparatus according to claim 9, it is characterized in that, each described condensation separating unit also comprises:
Condenser, is connected to described reactor;
Knockout drum, is connected to described condenser, and the bottom of described knockout drum connects a liquid sample pipeline.
11. oil hydrogenation catalyst evaluating apparatus according to claim 10, it is characterized in that, the pipeline between described condenser and described reactor is provided with operation valve, described operation valve is needle valve.
12. oil hydrogenation catalyst evaluating apparatus according to claim 9, it is characterized in that, described product separation and collector unit also comprise further:
One surge tank, be connected to described two cover condensation separating units by pipeline, the top of described surge tank connects a gas sampling pipeline;
One wet test meter, is connected to described surge tank;
One spark arrester, is connected to described wet test meter.
13., according to oil hydrogenation catalyst evaluating apparatus described in claim 12, is characterized in that, the pipeline between described surge tank and each described condensation separating unit is provided with operation valve, and described operation valve comprises a reduction valve, a needle valve and a retaining valve.
14. oil hydrogenation catalyst evaluating apparatus according to claim 10, it is characterized in that, described condenser is connected to the filtrator of described hydrogen gas unit by pipeline, and, pipeline between described condenser and described filtrator is provided with operation valve, and described operation valve is needle valve.
15. oil hydrogenation catalyst evaluating apparatus according to claim 10, is characterized in that, described knockout drum adopts inverted cone-shaped structure.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420593788.7U CN204177781U (en) | 2014-10-14 | 2014-10-14 | Oil hydrogenation catalyst evaluation device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420593788.7U CN204177781U (en) | 2014-10-14 | 2014-10-14 | Oil hydrogenation catalyst evaluation device |
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| CN204177781U true CN204177781U (en) | 2015-02-25 |
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ID=52566586
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|---|---|---|---|
| CN201420593788.7U Expired - Fee Related CN204177781U (en) | 2014-10-14 | 2014-10-14 | Oil hydrogenation catalyst evaluation device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107703251A (en) * | 2017-11-22 | 2018-02-16 | 洛阳凯美胜石化设备有限公司 | A kind of catalyst test apparatus and method |
| CN109897661A (en) * | 2019-03-21 | 2019-06-18 | 山东京博石油化工有限公司 | A kind of riser catalytic cracking pilot test system |
-
2014
- 2014-10-14 CN CN201420593788.7U patent/CN204177781U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107703251A (en) * | 2017-11-22 | 2018-02-16 | 洛阳凯美胜石化设备有限公司 | A kind of catalyst test apparatus and method |
| CN109897661A (en) * | 2019-03-21 | 2019-06-18 | 山东京博石油化工有限公司 | A kind of riser catalytic cracking pilot test system |
| CN109897661B (en) * | 2019-03-21 | 2021-10-29 | 山东京博石油化工有限公司 | Riser catalytic cracking pilot system |
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