CN206258420U - A kind of device for evaluating performance of preparing propylene by dehydrogenating propane catalyst - Google Patents
A kind of device for evaluating performance of preparing propylene by dehydrogenating propane catalyst Download PDFInfo
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- CN206258420U CN206258420U CN201621389395.XU CN201621389395U CN206258420U CN 206258420 U CN206258420 U CN 206258420U CN 201621389395 U CN201621389395 U CN 201621389395U CN 206258420 U CN206258420 U CN 206258420U
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Abstract
The utility model provides a kind of device for evaluating performance of preparing propylene by dehydrogenating propane catalyst, including computer controls part, air path part, reactive moieties and analysis detection part, the air path part includes four gas pipings being in parallel, the reactive moieties include electric heating multi-stage oven and reaction tube, the analysis detection part includes tail gas switching six-way valve, chromatogram sampling six-way valve and gas chromatograph, and the computer controls part includes computer and is integrated with the electronic circuit board of PLC module and RS232 serial communication modulars.It is the utility model simple structure, reasonable in design, disclosure satisfy that the requirement of catalytic reaction and catalyst regeneration, realize catalyst reaction, regeneration and the serialization of activation three phases, improve the efficiency of catalyst performance evaluation, the device is not only suitable the reaction for doing preparing propylene by dehydrogenating propane, but also can be adapted to do the reaction such as hydrogenation, dehydrogenation, oxidation, cracking or isomerization of other alkane.
Description
Technical field
The utility model belongs to chemical experiment technique field, and in particular to a kind of property of preparing propylene by dehydrogenating propane catalyst
Can evaluating apparatus.
Background technology
The performance evaluation of catalyst is the important step of Catalyst Production and application, and catalyst performance evaluation result can be most
Directly reflect the activity of catalyst, be to judge the whether qualified standard of catalyst.Laboratory fixed bed catalyst performance evaluation
Carried out typically in fixed-bed reactor, traditional laboratory fixed-bed reactor is typically complete manually operated,
The control of the parts such as air inlet, feed liquor, catalytic reaction and analysis detection is not enough, and connecting is poor, along with various complex operations,
Human factor is more, causes the deviation of catalyst performance evaluation result larger, therefore to the inefficiency of catalyst performance evaluation,
And error is larger.
With the development of fixed bed catalyst and fixed-bed reactor, the species of fixed bed catalyst increases, to evaluating
The requirement of experiment is also improved constantly, therefore requirement higher is it is also proposed to fixed-bed reactor, and traditional laboratory is fixed
Bed reaction device can not meet the requirement of current various fixed bed catalyst performance evaluations, therefore be urged preferably to evaluate
Agent performance, laboratory fixed-bed reactor there has also been larger development.With the development of science and technology, fixed bed reaction is filled at present
The progress put is mainly reflected in the following aspects：The flow of gas is controlled using the more stable mass flowmenter of performance；Make
The flow of feed liquor is controlled with the more preferable high pressure liquid phase pump of performance；Service precision table higher and valve control and stabilization reaction pressure；
Adjusted using more advanced temperature control mode and stabilization reaction temperature；The application of on-line period and analysis system causes result
Analysis is more facilitated.The application of these new technologies copes with the requirement of catalyst performance evaluation experiment substantially, there is very big
It is progressive, but complex operation and the low problem of efficiency is still present.New, tailored version the fixed-bed reactor of research and development
Have great significance.
Chinese patent：201520609359.9, patent name：A kind of fixed bed catalyst performance online evaluating apparatus, deposit
The defect of the henchnmrk test of dehydrating alkanes catalysts is fit to do in discomfort, because dehydrating alkanes especially dehydrogenating propane system
The reaction of propylene is more special, so, the catalyst of this kind of dehydrating alkanes reaction needs special fixed-bed reactor to comment
Valency its catalytic performance.Accordingly, it would be desirable on the basis of existing technology, propose a kind of performance of preparing propylene by dehydrogenating propane catalyst
Evaluating apparatus.
Utility model content
Technical problem to be solved in the utility model is for above-mentioned the deficiencies in the prior art, there is provided a kind of propane takes off
The device for evaluating performance of hydrogen propylene catalyst, it is its simple structure, reasonable in design, disclosure satisfy that catalytic reaction and catalyst again
Raw requirement, realizes catalyst reaction, regeneration and the serialization of activation three phases, improves the efficiency of catalyst performance evaluation,
The device is not only suitable the reaction for doing preparing propylene by dehydrogenating propane, but also can be adapted to do hydrogenation, dehydrogenation, the oxygen of other alkane
The reactions such as change, cracking or isomerization.
In order to solve the above technical problems, the technical solution adopted in the utility model is：A kind of preparing propylene by dehydrogenating propane is with urging
The device for evaluating performance of agent, it is characterised in that be connected with the air path part including computer controls part, air path part
Reactive moieties and the analysis detection part that is connected with the reactive moieties；
The air path part includes four gas pipings being in parallel, four gas pipings be respectively nitrogen pipeline,
Propane pipeline, hydrogen pipeline and air pipe line, be provided with every gas piping be in series gas bottle, mass flowmenter and
Check valve；
The reactive moieties include being provided with the electric heating multi-stage oven of high temperature section, middle-temperature section and low-temperature zone, the electric heating multi-stage oven
Interior penetration type is fitted with reaction tube, and the porch of the reaction tube is provided with boost gauge, and the exit of the reaction tube sets
It is equipped with outlet pressure table and electronic counterbalance valve；
The analysis detection part includes the tail gas being connected with electronic counterbalance valve switching six-way valve, is cut installed in tail gas
Change the chromatogram sampling six-way valve of six-way valve output end and the gas chromatograph of six-way valve output end of being sampled installed in chromatogram；
The computer controls part includes computer and the electronic circuit board for real-time control connected with computer,
PLC module, a RS232 serial communication modulars and the 2nd RS232 serial communication modulars, institute are integrated with the electronic circuit board
State PLC module carries out two-way communication by a RS232 serial communication modulars and computer, and the PLC module passes through second
RS232 serial communication modulars carry out bidirectional data exchange with gas chromatograph.
A kind of device for evaluating performance of above-mentioned preparing propylene by dehydrogenating propane catalyst, it is characterised in that the reaction tube
Quantity be 1~8, the reaction tube be quartz ampoule.
The device for evaluating performance of above-mentioned a kind of preparing propylene by dehydrogenating propane catalyst, it is characterised in that the electric heating is more
The high temperature section temperature of section stove is 550 DEG C~700 DEG C, and the middle-temperature section temperature of the electric heating multi-stage oven is 350 DEG C~500 DEG C, described
The low-temperature zone temperature of electric heating multi-stage oven is 50 DEG C~120 DEG C.
A kind of device for evaluating performance of above-mentioned preparing propylene by dehydrogenating propane catalyst, it is characterised in that the quality stream
The model D07-19C of gauge, the range of the mass flowmenter is 300mL/min.
The device for evaluating performance of above-mentioned a kind of preparing propylene by dehydrogenating propane catalyst, it is characterised in that the tail gas is cut
Change six-way valve and chromatogram sampling six-way valve is electronic six-way valve.
The utility model has advantages below compared with prior art：
1st, the utility model realizes the reaction temperature of high temperature section, middle-temperature section and low-temperature zone using multi-stage oven, using mobile anti-
Should the mode of pipe the catalyst in reaction tube is moved in different temperature sections, and by computer controls and record gas circuit
The tail gas of partial four kinds of gas flows, the reaction temperature of each section of the multi-stage oven of multi-stage oven reactive moieties and analysis detection part is cut
The tail gas switching and the conversion of gas chromatograph for changing six-way valve are connected, and disclosure satisfy that the requirement of catalytic reaction and catalyst regeneration,
Catalyst reaction, regeneration and the serialization of activation three phases are realized, the efficiency of catalyst performance evaluation, automaticity is improved
It is high.
2nd, the utility model realizes the switching of tail gas using the rotation of computer controls tail gas switching six-way valve, makes difference
The tail gas of reaction tube is analyzed detection on same gas chromatograph in order, can be disappeared with same gas chromatographic detection
Except instrument error, conveniently compare the difference of catalyst performance in each reaction tube, in can simultaneously detecting 1~8 reaction tube
Tail gas, you can while realizing 1~8 performance evaluation of reaction tube catalyst, save test period, using effect is good.
In sum, the utility model simple structure, reasonable in design, disclosure satisfy that catalytic reaction and catalyst regeneration will
Ask, realize catalyst reaction, regeneration and the serialization of activation three phases, improve the efficiency of catalyst performance evaluation, realize urging
The performance evaluation of agent, high degree of automation saves test period, and using effect is good.
The utility model is described in further detail with reference to the accompanying drawings and examples.
Brief description of the drawings
Fig. 1 is the structural representation of the preparing propylene by dehydrogenating propane catalyst performance evaluation device of the utility model embodiment 1.
Fig. 2 is the structural representation of the preparing propylene by dehydrogenating propane catalyst performance evaluation device of the utility model embodiment 2.
Fig. 3 is the utility model embodiment 1 and the computer controls part control principle block diagram of embodiment 2.
When Fig. 4 is that the utility model embodiment 1 tests the first reaction tube tail gas, tail gas switching six-way valve, chromatogram sampling six
The connection status schematic diagram of port valve and gas chromatograph.
When Fig. 5 is that the utility model embodiment 1 tests the second reaction tube tail gas, tail gas switching six-way valve, chromatogram sampling six
The connection status schematic diagram of port valve and gas chromatograph.
When Fig. 6 is that the utility model embodiment 2 tests the first reaction tube tail gas, tail gas switching six-way valve, chromatogram sampling six
The connection status schematic diagram of port valve and gas chromatograph.
When Fig. 7 is that the utility model embodiment 2 tests the second reaction tube tail gas, tail gas switching six-way valve, chromatogram sampling six
The connection status schematic diagram of port valve and gas chromatograph.
When Fig. 8 is that the utility model embodiment 2 tests the 3rd reaction tube tail gas, tail gas switching six-way valve, chromatogram sampling six
The connection status schematic diagram of port valve and gas chromatograph.
When Fig. 9 is that the utility model embodiment 2 tests the 4th reaction tube tail gas, tail gas switching six-way valve, chromatogram sampling six
The connection status schematic diagram of port valve and gas chromatograph.
Description of reference numerals:
1-gas bottle；2-mass flowmenter；3-check valve；
4-electric heating multi-stage oven；5-1-the first reaction tube；5-2-the second reaction tube；
The reaction tubes of 5-2-the 3rd；The reaction tubes of 5-3-the 4th；6-1-the first catalyst；
6-2-the second catalyst；The catalyst of 6-3-the 3rd；The catalyst of 6-4-the 4th；
7-tail gas switches six-way valve；7A-the first tail gas switches six-way valve；7B-the second tail gas switches six-way valve；
The tail gas of 7C-the 3rd switches six-way valve；8-chromatogram sampling six-way valve；9-first pressure table；
10-second pressure table；11-electronic counterbalance valve；12-1-PLC module；
The RS232 serial communication modulars of 12-2-the；The RS232 serial communication modulars of 12-3-the 2nd；
13-computer；14-gas chromatograph.
Specific embodiment
Structure of the present utility model is described by embodiment 1 and embodiment 2.
Embodiment 1
As shown in figures 1 and 3, the device for evaluating performance of the present embodiment preparing propylene by dehydrogenating propane catalyst includes：Calculate
Reactive moieties that machine control section, air path part are connected with the air path part and the analysis inspection being connected with the reactive moieties
Survey part；
The air path part includes four gas pipings being in parallel, four gas pipings be respectively nitrogen pipeline,
Propane pipeline, hydrogen pipeline and air pipe line, are provided with gas bottle 1, the mass flowmenter 2 being in series on every gas piping
With check valve 3；
The reactive moieties include being provided with the electric heating multi-stage oven 4 of high temperature section, middle-temperature section and low-temperature zone, the electric heating multi-stage oven
Penetration type is fitted with reaction tube in 4, and the porch of the reaction tube is provided with boost gauge 9, the exit of the reaction tube
It is provided with outlet pressure table 10 and electronic counterbalance valve 11；
The analysis detection part includes that the tail gas installed in the output end of electronic counterbalance valve 11 switches six-way valve 7, is arranged on
The gas-chromatography of the chromatogram sampling six-way valve 8 of the tail gas switching output end of six-way valve 7 and the output end of six-way valve 8 of being sampled installed in chromatogram
Instrument 14；
The computer controls part includes computer 13 and the electric wire for real-time control connected with computer 13
Road plate, is integrated with PLC module 12-1, a RS232 serial communication modulars 12-2 and the 2nd RS232 strings on the electronic circuit board
Port communications module 12-3, the PLC module 12-1 are carried out two-way by a RS232 serial communication modulars 12-2 with computer 13
Communication, the PLC module 12-1 carries out bi-directional data friendship by the 2nd RS232 serial communication modulars 12-3 with gas chromatograph 14
Change.
In the present embodiment, the high temperature section temperature of the electric heating multi-stage oven 4 is 550 DEG C~700 DEG C, the electric heating multi-stage oven 4
Middle-temperature section temperature be 350 DEG C~500 DEG C, the low-temperature zone temperature of the electric heating multi-stage oven 4 is 50 DEG C~120 DEG C.
In the present embodiment, the model D07-19C of the mass flowmenter 2, the range of the mass flowmenter 2 is
300mL/min。
In the present embodiment, the tail gas switching six-way valve 7 and chromatogram sampling six-way valve 8 are electronic six-way valve.
The reaction tube is preferably quartz ampoule, and its quantity is preferably 1~8.As shown in figure 1, described in the present embodiment
The quantity of reaction tube is 2, and 2 reaction tubes are respectively the first reaction tube 5-1 and the second reaction tube 5-2；First reaction tube
5-1 and the second reaction tube 5-2 are quartz ampoule, and the internal diameter of the first reaction tube 5-1 and the second reaction tube 5-2 is 6mm~9mm,
External diameter is 8mm~11mm, and length is all higher than 1m, can the volume of loading catalyst be 1mL~8mL；First reaction tube
5-1 and the second reaction tube 5-2 are independently connected a set of air path part；In the present embodiment, because the quantity of the reaction tube is 2
Individual, accordingly, the quantity of the tail gas switching six-way valve 7 is 1, and as shown in the 7A in Fig. 1, Fig. 4 and Fig. 5, the tail gas is cut
Change six-way valve and possess six paths, represented with A1, A2, A3, A4, A5 and A6 respectively.
Embodiment 2
As shown in Figures 2 and 3, the device for evaluating performance of the present embodiment preparing propylene by dehydrogenating propane catalyst includes：Calculate
Reactive moieties that machine control section, air path part are connected with the air path part and the analysis inspection being connected with the reactive moieties
Survey part；
The air path part includes four gas pipings being in parallel, four gas pipings be respectively nitrogen pipeline,
Propane pipeline, hydrogen pipeline and air pipe line, are provided with gas bottle 1, the mass flowmenter 2 being in series on every gas piping
With check valve 3；
The reactive moieties include being provided with the electric heating multi-stage oven 4 of high temperature section, middle-temperature section and low-temperature zone, the electric heating multi-stage oven
Penetration type is fitted with reaction tube in 4, and the porch of the reaction tube is provided with boost gauge 9, the exit of the reaction tube
It is provided with outlet pressure table 10 and electronic counterbalance valve 11；
The analysis detection part includes that the tail gas installed in the output end of electronic counterbalance valve 11 switches six-way valve 7, is arranged on
The gas-chromatography of the chromatogram sampling six-way valve 8 of the tail gas switching output end of six-way valve 7 and the output end of six-way valve 8 of being sampled installed in chromatogram
Instrument 14；
The computer controls part includes computer 13 and the electric wire for real-time control connected with computer 13
Road plate, is integrated with PLC module 12-1, a RS232 serial communication modulars 12-2 and the 2nd RS232 strings on the electronic circuit board
Port communications module 12-3, the PLC module 12-1 are carried out two-way by a RS232 serial communication modulars 12-2 with computer 13
Communication, the PLC module 12-1 carries out bi-directional data friendship by the 2nd RS232 serial communication modulars 12-3 with gas chromatograph 14
Change.
In the present embodiment, the high temperature section temperature of the electric heating multi-stage oven 4 is 550 DEG C~700 DEG C, the electric heating multi-stage oven 4
Middle-temperature section temperature be 350 DEG C~500 DEG C, the low-temperature zone temperature of the electric heating multi-stage oven 4 is 50 DEG C~120 DEG C.
In the present embodiment, the model D07-19C of the mass flowmenter 2, the range of the mass flowmenter 2 is
300mL/min。
In the present embodiment, the tail gas switching six-way valve 7 and chromatogram sampling six-way valve 8 are electronic six-way valve.
The reaction tube is preferably quartz ampoule, and its quantity is preferably 1~8.In the present embodiment, the quantity of reaction tube is
4 (as shown in Figure 2), 4 reaction tubes are respectively the first reaction tube 5-1, the second reaction tube 5-2, the 3rd reaction tube 5-3 and the 4th
Reaction tube 5-4, the first reaction tube 5-1, the second reaction tube 5-2, the 3rd reaction tube 5-3 and the 4th reaction tube 5-4 are stone
Ying Guan, internal diameter is 6mm~9mm, and external diameter is 8mm~11mm, and length is all higher than 1m, can the volume of loading catalyst be
1mL~8mL.The second reaction tubes of first reaction tube 5-1 5-2, the 3rd reaction tube 5-3 and the 4th reaction tube 5-4 independently connect
Connect a set of air path part；In the present embodiment, because the quantity of the reaction tube is 4, accordingly, the tail gas switching six is led to
The quantity of valve 7 is 3, respectively：First tail gas switching six-way valve 7A, the second tail gas switching six-way valve 7B and the switching of the 3rd tail gas
Six-way valve 7C；As shown in 7A, 7B and 7C in Fig. 2 and Fig. 6 to 9, each tail gas switching six-way valve is provided with six paths, point
Yong not A1, A2, A3, A4, A5, A6；B1、B2、B3、B4、B5、B6；C1, C2, C3, C4, C5, C6 are represented.
Application method of the present utility model is described by embodiment 3 to 6.
Embodiment 3
The present embodiment is using method of the device to the performance evaluation of preparing propylene by dehydrogenating propane catalyst as described in Example 1
Including two stages, the first stage is that the performance of active catalyst is evaluated；Second stage is when active catalyst is because of length
After phase causes activity decrease or inactivation using factors such as, carbon distributions, the catalyst is regenerated, and to the performance of regenerated catalyst
Evaluated.With reference to Fig. 1 and Fig. 3, the present embodiment catalyst performance evaluation method specifically includes following steps：
First stage, the performance to active catalyst are evaluated, and detailed process is：
Step one, pretreatment：By the preparing propylene by dehydrogenating propane catalyst filling of activity in reaction tube, then will be described
Reaction tube is inserted into electric heating multi-stage oven 4, and the catalyst in reaction tube is located at the low-temperature zone (low-temperature zone of electric heating multi-stage oven 4
Temperature be 50 DEG C~120 DEG C), the backward reaction tube in be passed through nitrogen displacement inner air tube, then stop to it is described instead
Nitrogen is passed through in should managing, is changed to be passed through hydrogen to catalyst pretreatment；
The quantity of reaction tube is two, respectively the first reaction tube 5-1 and the second reaction tube 5-2 in the present embodiment；This reality
It is two kinds, respectively the first catalyst 6-1 and the second catalyst 6-2 to apply the species of the catalyst selected in example；During concrete operations,
First catalyst 6-1 is filled in the first reaction tube 5-1, and the second catalyst 6-2 is filled in the second reaction tube 5-2；Described
One catalyst 6-1 with diameter 1.3mm~1.4mm, aperture 19nm macroporous aluminium oxide as carrier, Pt in the first catalyst 6-1
Mass content is the mass content of 0.4%, Na for the mass content that the mass content of 1.5%, K is 0.4%, Ca is 1.1%, Sn
Mass content be 0.5%, the mass content of aluminum oxide is 96.1%；The second catalyst 6-2 with diameter 1.3mm~
1.4mm, the macroporous aluminium oxide of aperture 21nm are carrier, and the mass content of Pt is the quality of 0.4%, Na in the first catalyst 6-1
Content be the mass content of 0.7%, K for the mass content of 1%, Ca is the mass content of 0.2%, Sn for 0.8%, aluminum oxide
Mass content is 96.9%；
In the present embodiment, the temperature of low-temperature zone residing for the first reaction tube 5-1 is 50 DEG C, to being passed through in the first reaction tube 5-1
The flow of nitrogen is 5mL/min, and the retention time is 5min, and after stopping is passed through nitrogen, is changed to be passed through hydrogen, hydrogen flowing quantity is
30mL/min, pretreatment time is 2h；The temperature of low-temperature zone residing for second reaction tube 5-2 is 80 DEG C, in the second reaction tube 5-2
The flow of nitrogen is passed through for 5mL/min, the retention time is 5min, stopping is passed through nitrogen, be changed to be passed through hydrogen after, hydrogen flowing quantity is
30mL/min, pretreatment time is 4h；
Step 2, propane catalytic dehydrogenation：It is continually fed under conditions of hydrogen in each reaction tube, it is first slow mobile described
Reaction tube, until catalyst in reaction tube is located at the high temperature section of electric heating multi-stage oven 4, then to being passed through third in the reaction tube
Alkane, (reaction pressure is reflected by the reading of outlet pressure table 10 to control electronic counterbalance valve 11 to adjust reaction pressure by PLC module
Out), so as to carry out propane catalytic dehydrogenating reaction；
In the present embodiment, the propane catalytic dehydrogenating reaction of the first catalyst 6-1 is：Continue in the first reaction tube 5-1
It is passed through hydrogen and keeps hydrogen flowing quantity under conditions of 30mL/min, first slowly movement first is reacted with the operating rate of 0.2m/h
Pipe 5-1 makes the first catalyst 6-1 gradually many to electric heating by the middle-temperature section (temperature of middle-temperature section is 450 DEG C) of electric heating multi-stage oven 4
The high temperature section (temperature of high temperature section is 600 DEG C) of section stove 4, is then passed through propane and hydrogen simultaneously in the first reaction tube 5-1, leads to
Cross PLC module and control electronic counterbalance valve 11, make the reading of outlet pressure table 10 for 0.02MPa, now maintain the catalyst in electricity
The flow-rate ratio of the high temperature section of hot multi-stage oven 4, propane and hydrogen is 1:Under conditions of 1, it is de- that the first catalyst 6-1 starts propane catalysis
Hydrogen reacts, and record tests the time started for 0min, and sustained response time 410h.The propane catalytic dehydrogenation of the second catalyst 6-2
React and be：Be continually fed into the second reaction tube 5-2 hydrogen and keep hydrogen flowing quantity be 30mL/min under conditions of, first with
Slowly mobile second reaction tube 5-2 makes the second catalyst 6-2 by the middle-temperature section of electric heating multi-stage oven 4 to the operating rate of 0.2m/h
(temperature of middle-temperature section be 400 DEG C) gradually arrive the high temperature section (temperature of high temperature section is 600 DEG C) of electric heating multi-stage oven 4, then, to the
Propane and hydrogen are passed through simultaneously in two reaction tube 5-2, electronic counterbalance valve 11 is controlled by PLC module 12-1, make outlet pressure table
10 reading is 0.1MPa, now maintains the catalyst in the high temperature section of electric heating multi-stage oven 4, and the flow-rate ratio of propane and hydrogen is 1:
Under conditions of 1, and when the reaction time of the first reaction tube 5-1 being 30min, the second catalyst 6-2 is set to start propane catalysis de-
Hydrogen reacts, and sustained response time 440h；
Step 3, detection：Continuous on-line detection is carried out to the reacted gas of dehydrogenating propane using gas chromatograph 14, from
And the conversion ratio and the selectivity of propylene of propane on catalyst in whole course of reaction are calculated, thus to the dehydrogenating propane of activity
Propylene processed is evaluated with the performance of catalyst；Detailed process is：
Step 301, when the first reaction tube 5-1 reaction time be 0~30min when, as shown in figure 4, by the first tail gas switching
Six-way valve 7A switches to the state of the tail gas for surveying the first reaction tube 5-1, and the tail gas of the first reaction tube 5-1 switches by the first tail gas
In the quantitative loop that six-way valve 7A samples six-way valve 8 to chromatogram, during 1min, chromatogram sampling six-way valve 8 is rotated, and chromatogram nitrogen will be quantitative
The tail gas sample of the first reaction tube 5-1 in ring completes detection in blowing to gas chromatograph 14；
Preferably, after the Tail gas measuring of the first reaction tube 5-1 is completed in gas chromatograph 14, sampling six-way valve 8 goes back to
Original position, continues to make the tail gas of the first reaction tube 5-1 to enter in quantitative loop, can be completed once in the every 10min of gas chromatograph 14
The test of sample in quantitative loop, therefore by PLC module 12-1 control chromatogram sampling six-way valves 8 in 11min, 12min, 21min,
Rotated respectively once during 22min, 3 sample tests can be completed in 30min, you can draw what 3 the first reaction tube 5-1 reacted
Result of the test；
Step 302, when the first reaction tube 5-1 reaction time being 30min, as shown in figure 5, the switching of the first tail gas six is led to
Valve 7A switches to the state of the tail gas for surveying the second reaction tube 5-2, and now, the tail gas of the second reaction tube 5-2 is cut by the first tail gas
Change in the quantitative loop that six-way valve 7A reaches chromatogram sampling six-way valve 8, chromatogram sampling six-way valve 8 is rotated, and chromatogram nitrogen is by quantitative loop
In the tail gas sample of the second reaction tube 5-2 blow to detection completed in gas chromatograph 14；
Preferably, after the Tail gas measuring of the second reaction tube 5-2 is completed in gas chromatograph 14, chromatogram sampling six-way valve 8
Original position is gone back to, continues to make the tail gas of the second reaction tube 5-2 to enter in quantitative loop, can complete once quantitative in the every 10min of chromatogram
The test of sample in ring, therefore six-way valve 8 is sampled in 41min, 42min, 51min, 52min by PLC module 12-1 control chromatograms
When rotate respectively once, 3 sample tests can be completed in 30min, you can draw 3 second reaction tube reaction experiment knots
Really；
Step 303, when the first reaction tube 5-1 reaction time be 60min when, repeat step 301, as the first reaction tube 5-1
When reaction time is 90min, repeat step 302, so circulation, tail gas switching six-way valve are rotated once per 30min；
According to the result that gas chromatograph 14 is detected, when the activity for confirming catalyst indeed declines or inactivates, then enter
Second stage；
Second stage：After active catalyst causes activity decrease or inactivation because of factors such as long-term use, carbon distributions, this is urged
Agent is regenerated, and performance to regenerated catalyst is evaluated, and detailed process is：
Step a, regeneration：Stop to propane and hydrogen is passed through in the reaction tube, be changed to be passed through nitrogen, slow mobile response
Pipe, until catalyst in making pipe is located at the middle-temperature section of electric heating multi-stage oven 4, then stops entering to being passed through nitrogen in the reaction tube
Row gas displacement, is changed to be passed through air, afterwards slow mobile response pipe, until the catalyst in making pipe is located at electric heating multi-stage oven 4
Low-temperature zone regenerated, the catalyst for being regenerated；
In the present embodiment, when the first catalyst 6-1 activity decreases or inactivation need to regenerate, stop first to the first reaction tube
Propane and hydrogen are passed through in 5-1, are changed to be passed through nitrogen, with the slow mobile first reaction tube 5-1 of the operating rate of 0.2m/h, make the
One catalyst 6-1 is located at the middle-temperature section (temperature of middle-temperature section is 450 DEG C) of electric heating multi-stage oven 4, then leads to in the first catalyst 6-1
Enter air, keep 2h, with the slow mobile first reaction tube 5-1 of the operating rate of 0.2m/h, the first catalyst 6-1 is located at electric heating
The low-temperature zone (temperature of low-temperature zone is 50 DEG C) of multi-stage oven 4, keeps 2h to carry out regeneration treatment, the first catalyst 6- for being regenerated
1；When the second catalyst 6-2 activity decrease or inactivation need to regenerate when, stop first to be passed through in the second reaction tube 5-2 propane and
Hydrogen, is changed to be passed through nitrogen, with the slow mobile second reaction tube 5-2 of the operating rate of 0.2m/h, is located at the second catalyst 6-2
The middle-temperature section (temperature of middle-temperature section is 450 DEG C) of electric heating multi-stage oven 4, then to air is passed through in the second catalyst 6-2,4h is kept,
With the operating rate of 0.2m/h, slowly mobile second reaction tube 5-2 makes the second catalyst 6-2 be located at the low-temperature zone of electric heating multi-stage oven 4
(temperature of low-temperature zone is 50 DEG C), keeps 4h to carry out regeneration treatment, the second catalyst 6-2 for being regenerated；
Step b, evaluation：According to the pretreatment described in method I steps one, the propane catalytic dehydrogenation described in step 2 and
Characterization processes described in step 3, calculate the choosing of the conversion ratio and propylene of propane in regenerated catalyst in whole course of reaction
Selecting property, thus the performance to regenerated catalyst evaluate.
The performance test results of the present embodiment catalyst are shown in Table 1.
Embodiment 4
The present embodiment catalyst performance evaluation method only exists the difference of technological parameter selection, the present embodiment with embodiment 3
The technological parameters different from embodiment 3 are shown in Table 1.The performance test results of the present embodiment catalyst are shown in Table 1.
Embodiment 5
The present embodiment catalyst performance evaluation method only exists the difference of technological parameter selection, the present embodiment with embodiment 3
The technological parameters different from embodiment 3 are shown in Table 1.The performance test results of the present embodiment catalyst are shown in Table 1.
Performance test results of the utilization described device of embodiment 1 of table 1 to the catalyst of embodiment 3 to 5
Embodiment 6
The present embodiment is using method of the device to the performance evaluation of preparing propylene by dehydrogenating propane catalyst as described in Example 2
Including two stages, the first stage is the performance of active catalyst to be evaluated (i.e. method I)；Second stage is when activity is urged
After agent causes activity decrease or inactivation because of factors such as long-term use, carbon distributions, the catalyst is regenerated, and to regeneration catalyzing
The performance of agent is evaluated (i.e. method II).With reference to Fig. 2 and Fig. 3, the present embodiment catalyst performance evaluation method specifically include with
Lower step：
First stage, the performance to active catalyst are evaluated, and detailed process is：
Step one, pretreatment：By the preparing propylene by dehydrogenating propane catalyst filling of activity in reaction tube, then will be described
Reaction tube is inserted into electric heating multi-stage oven 4, and the catalyst in reaction tube is located at the low-temperature zone of electric heating multi-stage oven 4, backward
Nitrogen displacement inner air tube is passed through in the reaction tube, then stops being passed through nitrogen in the reaction tube, be changed to be passed through hydrogen,
Pre-processed with to catalyst；
In the present embodiment, the temperature of low-temperature zone residing for the first reaction tube 5-1 is 60 DEG C, to being passed through in the first reaction tube 5-1
The flow of nitrogen is 5mL/min, and the retention time is 5min, and after stopping is passed through nitrogen, is changed to be passed through hydrogen, hydrogen flowing quantity is
30mL/min, pretreatment time is 2h；The temperature of low-temperature zone residing for second reaction tube 5-2 is 80 DEG C, in the second reaction tube 5-2
The flow of nitrogen is passed through for 5mL/min, the retention time is 5min, stopping is passed through nitrogen, be changed to be passed through hydrogen after, hydrogen flowing quantity is
30mL/min, pretreatment time is 4h；The temperature of low-temperature zone residing for 3rd reaction tube 5-3 is 60 DEG C, in the 3rd reaction tube 5-3
The flow of nitrogen is passed through for 50mL/min, the retention time is 5min, stopping is passed through nitrogen, be changed to be passed through hydrogen after, hydrogen flowing quantity
It is 60mL/min, pretreatment time is 2h；The temperature of low-temperature zone residing for 4th reaction tube 5-4 is 90 DEG C, to the 4th reaction tube 5-4
The flow of nitrogen is inside passed through for 100mL/min, the retention time is 5min, stopping is passed through nitrogen, be changed to be passed through hydrogen after, hydrogen stream
It is 80mL/min to measure, and pretreatment time is 4h；
The quantity of reaction tube is four in the present embodiment, respectively the first reaction tube 5-1, the second reaction tube 5-2, the 3rd anti-
Should pipe 5-3 and the 4th reaction tube 5-4；The species of the catalyst selected in the present embodiment is four kinds, respectively the first catalyst 6-
1st, the second catalyst 6-2, the 3rd catalyst 6-3 and the 4th catalyst 6-4；During concrete operations, the first catalyst 6-1 is filled in
In one reaction tube 5-1, the second catalyst 6-2 is filled in the second reaction tube 5-2, and the 3rd catalyst 6-3 is filled in the 3rd reaction
In pipe 5-3, the 4th catalyst 6-4 is filled in the 4th reaction tube 5-4；The first catalyst 6-1 with diameter 1.3mm~
1.4mm, the macroporous aluminium oxide of aperture 19nm are carrier, and the mass content of Pt is the quality of 0.4%, Na in the first catalyst 6-1
Content is the mass content of 1.5%, K for the mass content that the mass content of 0.4%, Ca is 1.1%, Sn is 0.5%, aluminum oxide
Mass content be 96.1%；The second catalyst 6-2 is with the macroporous aluminium oxide of diameter 1.3mm~1.4mm, aperture 21nm
Carrier, the mass content of Pt is that the mass content that the mass content of 0.4%, Na is 0.7%, K is 1% in the first catalyst 6-1,
The mass content of Ca is 0.8% for the mass content of 0.2%, Sn, and the mass content of aluminum oxide is 96.9%；3rd catalysis
Agent 6-3 with diameter 1.3mm~1.4mm, aperture 15nm macroporous aluminium oxide as carrier, the quality of Pt contains in the 3rd catalyst 6-3
Measure be 0.4%, Na mass content for 0.9%, K mass content for 0.4%, Ca mass content for 0.4%, Sn quality
Content is 1.2%, and the mass content of aluminum oxide is 96.7%；The 4th catalyst 6-4 is with diameter 1.3mm~1.4mm, aperture
The macroporous aluminium oxide of 29nm is carrier, and the mass content of Pt is that the mass content of 0.5%, Na is in the 4th catalyst 6-4
The mass content of 1.1%, K is 1.5%, the quality of aluminum oxide for the mass content that the mass content of 0.4%, Ca is 0.1%, Sn
Content is 96.4%；
Step 2, propane catalytic dehydrogenation：It is continually fed under conditions of hydrogen in each reaction tube, it is first slow mobile described
Reaction tube, until catalyst in reaction tube is located at the high temperature section of electric heating multi-stage oven 4, then to being passed through third in the reaction tube
Alkane, controls electronic counterbalance valve 11 to adjust reaction pressure, so as to carry out propane catalytic dehydrogenating reaction by PLC module；
In the present embodiment, the propane catalytic dehydrogenating reaction of the first catalyst 6-1 is：Continue in the first reaction tube 5-1
It is passed through hydrogen and keeps hydrogen flowing quantity under conditions of 30mL/min, first slowly movement first is reacted with the operating rate of 0.3m/h
Pipe 5-1 makes the first catalyst 6-1 gradually many to electric heating by the middle-temperature section (temperature of middle-temperature section is 450 DEG C) of electric heating multi-stage oven 4
The high temperature section (temperature of high temperature section is 600 DEG C) of section stove 4, is then passed through propane and hydrogen simultaneously in the first reaction tube 5-1, leads to
Cross PLC module and control electronic counterbalance valve 11, make the reading of outlet pressure table 10 for 0.02MPa, now maintain the catalyst in electricity
The flow-rate ratio of the high temperature section of hot multi-stage oven 4, propane and hydrogen is 1:Under conditions of 1, it is de- that the first catalyst 6-1 starts propane catalysis
Hydrogen reacts, and record tests the time started for 0min, and sustained response time 410h.The propane catalytic dehydrogenation of the second catalyst 6-2
React and be：Be continually fed into the second reaction tube 5-2 hydrogen and keep hydrogen flowing quantity be 30mL/min under conditions of, first with
Slowly mobile second reaction tube 5-2 makes the second catalyst 6-2 by the middle-temperature section of electric heating multi-stage oven 4 to the operating rate of 0.3m/h
(temperature of middle-temperature section be 450 DEG C) gradually arrive the high temperature section (temperature of high temperature section is 600 DEG C) of electric heating multi-stage oven 4, then, to the
Propane and hydrogen are passed through simultaneously in two reaction tube 5-2, electronic counterbalance valve 11 is controlled by PLC module 12-1, make outlet pressure table
10 reading is 0.1MPa, now maintains the catalyst in the high temperature section of electric heating multi-stage oven 4, and the flow-rate ratio of propane and hydrogen is 1:
Under conditions of 1, and when the reaction time of the first reaction tube 5-1 being 30min, the second catalyst 6-2 is set to start propane catalysis de-
Hydrogen reacts, and sustained response time 440h.The propane catalytic dehydrogenating reaction of the 3rd catalyst 6-3 is：To the 3rd reaction tube 5-3
Under conditions of being inside continually fed into hydrogen and keeping hydrogen flowing quantity to be 30mL/min, first with the operating rate of 0.3m/h slowly mobile the
Three reaction tube 5-3 make the 3rd catalyst 6-3 gradually be arrived by the middle-temperature section (temperature of middle-temperature section is 450 DEG C) of electric heating multi-stage oven 4
The high temperature section (temperature of high temperature section be 550 DEG C) of electric heating multi-stage oven 4, then, to be passed through simultaneously in the 3rd reaction tube 5-3 propane and
Hydrogen, electronic counterbalance valve 11 is controlled by PLC module 12-1, makes the reading of outlet pressure table 10 for 0.1MPa, now keeps urging
The flow-rate ratio of high temperature section of the agent in electric heating multi-stage oven 4, propane and hydrogen is 1:Under conditions of 1, and as the first reaction tube 5-1
Reaction time be 60min when, the 3rd catalyst 6-3 is started propane catalytic dehydrogenating reaction, and sustained response time 470h.The
The propane catalytic dehydrogenating reaction of four catalyst 6-4 is：Hydrogen is continually fed into the 4th reaction tube 5-4 and hydrogen flowing quantity is kept
Under conditions of 30mL/min, first with the operating rate of 0.3m/h, slowly mobile 4th reaction tube 5-4 passes through the 4th catalyst 6-4
Cross electric heating multi-stage oven 4 middle-temperature section (temperature of middle-temperature section be 500 DEG C) gradually arrive electric heating multi-stage oven 4 high temperature section (high temperature section
Temperature is 600 DEG C), then, propane and hydrogen are passed through simultaneously in the 4th reaction tube 5-4, controlled by PLC module 12-1 electronic
Counterbalance valve 11, makes the reading of outlet pressure table 10 for 0.3MPa, now maintains the catalyst in the high temperature section of electric heating multi-stage oven 4,
The flow-rate ratio of propane and hydrogen is 1:Under conditions of 1, and when the reaction time of the first reaction tube 5-1 being 90min, the 4th is set to urge
Agent 6-4 starts propane catalytic dehydrogenating reaction, and sustained response time 340h；
Step 3, detection：Continuous on-line detection is carried out to the reacted gas of dehydrogenating propane using gas chromatograph 14, from
And the conversion ratio and the selectivity of propylene of propane on catalyst in whole course of reaction are calculated, thus to the dehydrogenating propane of activity
Propylene processed is evaluated with the performance of catalyst；Detailed process is：
Step 301, when the first reaction tube 5-1 reaction time be 0~30min when, as shown in fig. 6, by the first tail gas switching
Six-way valve 7A switches to the state of the tail gas for surveying the first reaction tube 5-1, and the tail gas of the first reaction tube 5-1 switches by the first tail gas
Six-way valve 7A and the 3rd tail gas switch in the quantitative loop that six-way valve 7C samples six-way valve 8 to chromatogram, and during 1min, chromatogram sampling six is led to
Valve 8 is rotated, and chromatogram nitrogen is detected during the tail gas sample of the first reaction tube 5-1 to be blown to the quantitative loop of gas chromatograph 14,
Now, the tail gas of the second reaction tube 5-2 is emptied by the first tail gas switching six-way valve 7A, and the tail gas of the 3rd reaction tube 5-3 passes through
Second tail gas switches six-way valve 7B and the switching six-way valve 7C emptyings of the 3rd tail gas, and the tail gas of the 4th reaction tube 5-4 is by the second tail
Autogenous cutting changes six-way valve 7B emptyings；
Step 302, when the first reaction tube 5-1 reaction time being 30min, as shown in fig. 7, the switching of the first tail gas six is led to
Valve 7A switches to the state of the tail gas for surveying the second reaction tube 5-2, and similarly, the tail gas of the second reaction tube 5-2 is cut by the first tail gas
Change in the quantitative loop that six-way valve 7A and the 3rd tail gas switching six-way valve 7C sample six-way valve 8 to chromatogram, during 31min, chromatogram sampling
Six-way valve 8 is rotated, and detection is completed during the tail gas sample of the second reaction tube 5-2 in quantitative loop is blown into gas chromatograph 14, now,
The tail gas of the first reaction tube 5-1 is emptied by the first tail gas switching six-way valve 7A, and the tail gas of the 3rd reaction tube 5-3 is by the second tail
Autogenous cutting changes six-way valve 7B and the switching six-way valve 7C emptyings of the 3rd tail gas, and the tail gas of the 4th reaction tube 5-4 switches by the second tail gas
Six-way valve 7B is emptied；
Step 303, when the first reaction tube 5-1 reaction time being 60min, as shown in figure 8, the switching of the second tail gas six is led to
Valve 7B switches to the state of the tail gas for surveying the 3rd reaction tube 5-3, and the tail gas of the 3rd reaction tube 5-3 leads to by the second tail gas switching six
Valve 7B and the 3rd tail gas switch in the quantitative loop that six-way valve 7C samples six-way valve 8 to chromatogram, during 61min, chromatogram sampling six-way valve 8
Rotate, chromatogram nitrogen is detected during the tail gas sample of the 3rd reaction tube 5-3 to be blown to the quantitative loop of gas chromatograph 14, this
When, the tail gas of the first reaction tube 5-1 switches six-way valve 7A by the first tail gas and the 3rd tail gas switching six-way valve 7C is emptied, and second
The tail gas of reaction tube 5-2 is emptied by the first tail gas switching six-way valve 7A, and the tail gas of the 4th reaction tube 5-4 is cut by the second tail gas
Change six-way valve 7B emptyings；
Step 304, when the first reaction tube 5-1 reaction time being 90min, as shown in figure 9, the switching of the second tail gas six is led to
Valve 7B switches to the state of the tail gas for surveying the 4th reaction tube 5-4, and the tail gas of the 4th reaction tube 5-4 leads to by the second tail gas switching six
Valve 7B and the 3rd tail gas switch in the quantitative loop that six-way valve 7C samples six-way valve 8 to chromatogram, during 91min, chromatogram sampling six-way valve 8
Rotate, chromatogram nitrogen is detected during the tail gas sample of the 4th reaction tube 5-4 to be blown to the quantitative loop of gas chromatograph 14, this
When, the tail gas of the first reaction tube 5-1 switches six-way valve 7A by the first tail gas and the 3rd tail gas switching six-way valve 7C is emptied, and second
The tail gas of reaction tube 5-2 is emptied by the first tail gas switching six-way valve 7A, and the tail gas of the 3rd reaction tube 5-3 is cut by the second tail gas
Change six-way valve 7B emptyings；
According to the result that gas chromatograph 14 is detected, when the activity decrease or inactivation of catalyst, then into second stage；
Second stage：After active catalyst causes activity decrease or inactivation because of factors such as long-term use, carbon distributions, this is urged
Agent is regenerated, and performance to regenerated catalyst is evaluated, and detailed process is：
Step a, regeneration：Stop to propane and hydrogen is passed through in the reaction tube, be changed to be passed through nitrogen, slow mobile response
Pipe, until catalyst in making pipe is located at the middle-temperature section of electric heating multi-stage oven 4, then stops entering to being passed through nitrogen in the reaction tube
Row gas displacement, is changed to be passed through air, afterwards slow mobile response pipe, until the catalyst in making pipe is located at electric heating multi-stage oven 4
Low-temperature zone regenerated, the catalyst for being regenerated；
In the present embodiment, when the first catalyst 6-1 activity decreases or inactivation need to regenerate, stop first to the first reaction tube
Propane and hydrogen are passed through in 5-1, are changed to be passed through nitrogen, with the slow mobile first reaction tube 5-1 of the operating rate of 0.2m/h, make the
One catalyst 6-1 is located at the middle-temperature section (temperature of middle-temperature section is 450 DEG C) of electric heating multi-stage oven 4, then leads to in the first catalyst 6-1
Enter air, keep 2h, with the slow mobile first reaction tube 5-1 of the operating rate of 0.2m/h, the first catalyst 6-1 is located at electric heating
The low-temperature zone (temperature of low-temperature zone is 50 DEG C) of multi-stage oven 4, keeps 2h to carry out regeneration treatment, the first catalyst 6- for being regenerated
1；When the second catalyst 6-2 activity decrease or inactivation need to regenerate when, stop first to be passed through in the second reaction tube 5-2 propane and
Hydrogen, is changed to be passed through nitrogen, with the slow mobile second reaction tube 5-2 of the operating rate of 0.2m/h, is located at the second catalyst 6-2
The middle-temperature section (temperature of middle-temperature section is 450 DEG C) of electric heating multi-stage oven 4, then to air is passed through in the second catalyst 6-2,4h is kept,
With the operating rate of 0.2m/h, slowly mobile second reaction tube 5-2 makes the second catalyst 6-2 be located at the low-temperature zone of electric heating multi-stage oven 4
(temperature of low-temperature zone is 50 DEG C), keeps 4h to carry out regeneration treatment, the second catalyst 6-2 for being regenerated；When the 3rd catalyst
When the activity decrease or inactivation of 6-3 need to regenerate, stop being passed through propane and hydrogen in the 3rd reaction tube 5-3 first, be changed to be passed through
Nitrogen, with the slow mobile 3rd reaction tube 5-3 of the operating rate of 0.2m/h, makes the 3rd catalyst 6-3 be located at electric heating multi-stage oven 4
Middle-temperature section (temperature of middle-temperature section is 450 DEG C), then to air is passed through in the 3rd catalyst 6-3,4h is kept, with the operation of 0.2m/h
Slowly mobile 3rd reaction tube 5-3 makes the 3rd catalyst 6-3 be located at the low-temperature zone (temperature of low-temperature zone of electric heating multi-stage oven 4 to speed
It is 50 DEG C), keep 4h to carry out regeneration treatment, the 3rd catalyst 6-3 for being regenerated；When the activity decrease of the 4th catalyst 6-4
Or inactivation stops being passed through propane and hydrogen in the 4th reaction tube 5-4 first when need to regenerate, and is changed to be passed through nitrogen, with 0.2m/h
The slow mobile 4th reaction tube 5-4 of operating rate, the 4th catalyst 6-4 is located at the middle-temperature section (middle-temperature section of electric heating multi-stage oven 4
Temperature be 450 DEG C), then to air is passed through in the 4th catalyst 6-4, keep 4h, slowly moved with the operating rate of 0.2m/h
4th reaction tube 5-4 makes the 4th catalyst 6-4 be located at the low-temperature zone (temperature of low-temperature zone is 50 DEG C) of electric heating multi-stage oven 4, keeps
4h carries out regeneration treatment, the 4th catalyst 6-4 for being regenerated；
Step b, evaluation：According to the pretreatment described in method I steps one, the propane catalytic dehydrogenation described in step 2 and
Characterization processes described in step 3, calculate the choosing of the conversion ratio and propylene of propane in regenerated catalyst in whole course of reaction
Selecting property, thus the performance to regenerated catalyst evaluate.
The performance test results of the present embodiment catalyst are shown in Table 2.
Performance test results of the utilization described device of embodiment 2 of table 2 to the catalyst of embodiment 6
It follows that the utility model simple structure, reasonable in design, disclosure satisfy that catalytic reaction and catalyst regeneration will
Ask, realize catalyst reaction, regeneration and the serialization of activation three phases, improve the efficiency of catalyst performance evaluation, the device
The reaction for doing preparing propylene by dehydrogenating propane is not only suitable, but also can be adapted to do hydrogenation, dehydrogenation, oxidation, the cracking of other alkane
Or the reaction such as isomerization.
The above, is only preferred embodiment of the present utility model, and not the utility model is imposed any restrictions.Every
Any simple modification, change and equivalence change factually substantially made to above example with new technique, still fall within this
In the protection domain of utility model technical scheme.
Claims (5)
1. a kind of device for evaluating performance of preparing propylene by dehydrogenating propane catalyst, it is characterised in that including computer controls part,
Reactive moieties that air path part is connected with the air path part and the analysis detection part being connected with the reactive moieties；
The air path part includes four gas pipings being in parallel, and four gas pipings are respectively nitrogen pipeline, propane
Pipeline, hydrogen pipeline and air pipe line, are provided with gas bottle (1), the mass flowmenter (2) being in series on every gas piping
With check valve (3)；
The reactive moieties include being provided with the electric heating multi-stage oven (4) of high temperature section, middle-temperature section and low-temperature zone, the electric heating multi-stage oven
(4) interior penetration type is fitted with reaction tube, the porch of the reaction tube is provided with boost gauge (9), and the reaction tube goes out
Outlet pressure table (10) and electronic counterbalance valve (11) are provided with mouthful；
It is described analysis detection part include be connected with the electronic counterbalance valve (11) tail gas switching six-way valve (7), installed in tail
Autogenous cutting changes chromatogram sampling six-way valve (8) of six-way valve (7) output end and the gas phase of six-way valve (8) output end of being sampled installed in chromatogram
Chromatograph (14)；
The computer controls part includes computer (13) and the electric wire for real-time control connected with computer (13)
Road plate, is integrated with PLC module (12-1), a RS232 serial communication modulars (12-2) and second on the electronic circuit board
RS232 serial communication modulars (12-3), the PLC module (12-1) is by a RS232 serial communication modulars (12-2) and meter
Calculation machine (13) carries out two-way communication, and the PLC module (12-1) is by the 2nd RS232 serial communication modulars (12-3) and gas phase color
Spectrometer (14) carries out bidirectional data exchange.
2. the device for evaluating performance of a kind of preparing propylene by dehydrogenating propane catalyst according to claim 1, it is characterised in that
The quantity of the reaction tube is 1~8, and the reaction tube is quartz ampoule.
3. the device for evaluating performance of a kind of preparing propylene by dehydrogenating propane catalyst according to claim 1, it is characterised in that
The high temperature section temperature of the electric heating multi-stage oven (4) is 550 DEG C~700 DEG C, and the middle-temperature section temperature of the electric heating multi-stage oven (4) is
350 DEG C~500 DEG C, the low-temperature zone temperature of the electric heating multi-stage oven (4) is 50 DEG C~120 DEG C.
4. the device for evaluating performance of a kind of preparing propylene by dehydrogenating propane catalyst according to claim 1, it is characterised in that
The model D07-19C of the mass flowmenter (2), the range of the mass flowmenter (2) is 300mL/min.
5. the device for evaluating performance of a kind of preparing propylene by dehydrogenating propane catalyst according to claim 1, it is characterised in that
The tail gas switches six-way valve (7) and chromatogram sampling six-way valve (8) is electronic six-way valve.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106483242A (en) * | 2016-12-16 | 2017-03-08 | 西安凯立新材料股份有限公司 | A kind of device for evaluating performance of preparing propylene by dehydrogenating propane catalyst and evaluation method |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106483242A (en) * | 2016-12-16 | 2017-03-08 | 西安凯立新材料股份有限公司 | A kind of device for evaluating performance of preparing propylene by dehydrogenating propane catalyst and evaluation method |
| CN106483242B (en) * | 2016-12-16 | 2018-10-30 | 西安凯立新材料股份有限公司 | A kind of method of evaluating performance of preparing propylene by dehydrogenating propane catalyst |
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