CN201476995U - Vacuum sampling system - Google Patents
Vacuum sampling system Download PDFInfo
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- CN201476995U CN201476995U CN2009202329107U CN200920232910U CN201476995U CN 201476995 U CN201476995 U CN 201476995U CN 2009202329107 U CN2009202329107 U CN 2009202329107U CN 200920232910 U CN200920232910 U CN 200920232910U CN 201476995 U CN201476995 U CN 201476995U
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- sampling
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- sampling bottle
- vacuum pump
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Abstract
The utility model discloses a vacuum sampling system which comprises the following components: a group of sampling openings, gas purging inlets corresponding with the group of the sampling openings, a cooling device, a sampling bottle, a sampling opening and a vacuum pump. The group of sampling opening are connected with the sampling bottle through the cooling device. One end of the sampling bottle is connected with the vacuum pump. Furthermore an air purging outlet is provided between the sampling bottle and the vacuum pump. The other end of the sampling bottle is connected with the sampling opening. The vacuum sampling system can analyze the reaction product composition, conversion rate and water-oil ratio in the reaction process. In the early period of device operation, the catalyst performance and the condition of device reactor and triple device can be accurately reflected. In the late period of the device operation, the operation inactivating of the catalyst can be accurately determined so the operator can replace the catalyst in time.
Description
Technical field
The utility model relates to a kind of sampling system, specifically a kind of vacuum sampling system that is used for the production of styrene method.
Background technology
At present, cinnamic in the world production method mainly contains styrene/propylene oxide co-production method and ethylbenzene dehydrogenation method.
Styrene/propylene oxide co-production method (SM/PO method) claims conjugated oxidation again, is succeeded in developing by Halcon company, and realizes industrialization in 1973 in Spain.Course of reaction is: under 130-160 ℃, 0.3-0.5MPa, ethylbenzene generates the ethylbenzene superoxide with dioxygen oxidation earlier in Liquid-phase reactor, the ethylbenzene superoxide that generates densely enters epoxidation process after to 17% through carrying, in temperature of reaction is that 110 ℃, pressure are under the 4.05MPa condition, becomes epoxypropane and phenylethyl alcohol with propylene initial ring oxidation reaction.Phenylethyl alcohol dehydration under 260 ℃, condition of normal pressure generates styrene, and the mass ratio of styrene and epoxypropane is 2.5: 1 in the reaction product.The manufacturer who has at present this method patent power of alienation in the world mainly contains Lyondell company and Shell company etc.This method technological process is long, equipment investment expense height, and ethylbenzene unit consumption and plant energy consumption etc. all will be higher than ethylbenzene dehydrogenation method technology.But the epoxypropane price of institute's coproduction is than styrene height, and the overall manufacturing cost is lower than the adabatic dehydrogenation method slightly.This method is produced cinnamic output and is accounted for about 10% of Gross World Product, and application seldom.
The ethylbenzene dehydrogenation method: ethylbenzene catalytic dehydrogenation is the cinnamic traditional handicraft of industrial production, is succeeded in developing first by U.S. Dow chemical company, and this method is produced cinnamic output and accounted for about 90% of Gross World Product.At present, the typical process of dehydrogenation of ethylbenzene to styrene mainly contains Fina/Badger technology, Lummus/UOP technology and BASF technology etc.The ultimate principle unanimity is former section with ethylbenzene promptly, and under ferrous oxide or Zinc oxide catalytic effect, dehydrogenation generates styrene under about 600 ℃ of gas phase states.Ethylbenzene dehydrogenation is an endothermic process, must adopt the mode of heat exchange that energy is provided, and the direct heat exchange mode of industrial main employing hyperthermia and superheating steam, reactor pattern then have isotherm formula fixed bed reactors and heat-insulating fixed bed reactors two big classes.Technology flow process, reactor, catalyzer and energy-saving and cost-reducing aspect characteristics are respectively arranged.
The styrene units working system is that what to adopt domestic-developed is raw material with ethylbenzene, negative pressure adabatic dehydrogenation preparation of styrene technology.
The technological process of styrene units working system mainly comprises ethylbenzene dehydrogenation, phenyl ethylene rectification.Ethyl benzene dehydrogenation system is by ethylbenzene evaporation and dehydrogenation reaction, the processing of technology lime set and stripping, tail gas compression and absorb three parts and form.Ethylbenzene evaporation and dehydrogenation reactor system are the cores of styrene units.
Fig. 1 is a styrene units working system process chart.Among the figure, F-301 is that steam superheater, R-301 are that first reactor, R-302 are that second reactor, E-301 are that superheater, E-302 are that Low Pressure Waste Heat Boiler, E-303 are Low Pressure Waste Heat Boiler.Ethylbenzene evaporation and dehydrogenation reactor system are made of units such as the dehydrogenation reactor (wherein an Intermediate Heat Exchanger is established at the second dehydrogenation reactor top) of two series connection, steam superheater, three heat interchanger, ethylbenzene evaporators.The function of this system is material ethylbenzene to be finished join vapour, evaporation and overheated, mix with hyperthermia and superheating water vapour then, obtain heat, be raised to temperature of reaction from steam superheater, enter the reactor catalyst bed, under negative pressure and adiabatic condition, dehydrogenation reaction takes place.The high-temperature gas product that reactor is discharged reclaims heat through cooling condensation step by step, and the technology lime set (dehydrogenation liquid and water) that enters the downstream handles and two systems of vent gas treatment further process.
Summary of the invention
For each material in the styrene units working system is taken a sample, the purpose of this utility model provides a kind of vacuum sampling system, can analyze reaction product composition, conversion ratio, water-oil factor in the course of reaction by this vacuum sampling system; At the device driving initial stage, can accurately reflect quality, the device reaction device of the performance of catalyzer, the situation of three equipment operations.Can judge accurately that catalyzer moves the situation of inactivation latter stage in the device operation, make operating personnel prepare the problem that catalyzer is changed early.
The purpose of this utility model is achieved through the following technical solutions:
A kind of vacuum sampling system, it is characterized in that: this vacuum sampling system comprise one group of sample tap, with one group of gas purging inlet, cooling device, sampling bottle, sample tap and vacuum pump that sample tap is corresponding, one group of sample tap is connected with sampling bottle by cooling device; One end of sampling bottle is connected with vacuum pump, and is provided with the gas purging outlet between sampling bottle and vacuum pump; The other end of sampling bottle is connected with sample tap.
In the utility model, described cooling device comprises refrigeratory and cooling bath, is equipped with cooling liquid inlet and cooling liquid outlet on refrigeratory and cooling bath; Between refrigeratory and cooling bath, be provided with thermometer.
For taking a sample conveniently, sampling bottle described in the utility model and sample tap are two groups of parallel connections, and two groups of sampling bottles all are connected with cooling device with vacuum pump.
The utility model is provided with sample platform below sample tap.
The utility model is provided with drain between sampling bottle and vacuum pump.
In the utility model, one group of sample tap is six, and the gas purging inlet corresponding with the hexad sample tap also is six, and is arranged on the sample tap top.Gas in the gas purging inlet can be nitrogen.
In the styrene units working system, because this reactive system is a negative-pressure operation, generally about 0.045MPaA, temperature of reaction is higher, reaches as high as 594 ℃.This sampling spot pressure lowest part is 0.030MPaA, must adopt the vacuum sampling system could realize the sampling of this reactive system.
The utility model has 6 sampling spots.Be respectively: the import and export of 2 first dehydrogenation reactors, 2 second dehydrogenation reactors are imported and exported 1 ethylbenzene evaporator outlet, 1 three heat exchanger exit.In the operational process of whole device, by the sampling of these six points being carried out the analysis of reaction product composition, conversion ratio, water-oil factor.At the device driving initial stage, can accurately reflect the quality of the performance of catalyzer; The situation of device reaction device, three equipment operations.Can accurately judge the situation of catalyzer operation inactivation latter stage in the device operation.Make operating personnel prepare the problem that catalyzer is changed early.
The utility model is easy to operate, can accurately judge the situation of device operation by sample analysis.
Description of drawings
Fig. 1 is a styrene units working system process chart;
Fig. 2 is the utility model structural representation;
Fig. 3 is that the A of Fig. 2 is to view.
Embodiment
A kind of vacuum sampling system described in the utility model is seen Fig. 2 and Fig. 3.This vacuum sampling system comprises hexad sample tap 1, hexad gas purging inlet 2, cooling device 3, sampling bottle 4, sample tap 5 and the vacuum pump 6 corresponding with hexad sample tap 1.Six sample taps are respectively: the import and export of 2 first dehydrogenation reactors, 2 second dehydrogenation reactors are imported and exported 1 ethylbenzene evaporator outlet, 1 three heat exchanger exit.Sample tap 5 is connected with sampling bottle 4 by cooling device 3.Sampling bottle 4 and sample tap 5 are two groups of parallel connections, and an end of sampling bottle 4 is connected with vacuum pump 6, and are provided with gas purging outlet 7 and drain 9 between sampling bottle 4 and vacuum pump 6; The other end of sampling bottle 4 is connected with sample tap 5.Gas in the gas purging inlet 2 adopts nitrogen.
Cooling device 3 comprises refrigeratory 31 and cooling bath 32, is equipped with cooling liquid inlet and cooling liquid outlet on refrigeratory 31 and cooling bath 32; Between refrigeratory 31 and cooling bath 32, be provided with thermometer 33.For taking a sample conveniently, below sample tap 5, be provided with sample platform 8.
The utility model is provided with operation valve 10 at pipeline enclosure.Between cooling device 3 and sampling bottle 4, be provided with vacuum meter 11 and probe temperature meter 12.
In styrene units working system process, by the sampling of these six points being carried out the analysis of reaction product composition, conversion ratio, water-oil factor.At the driving initial stage, can accurately reflect the quality of the performance of catalyzer; The situation of reactor, three equipment operations.Can accurately judge the situation of catalyzer operation inactivation latter stage in operation.Make operating personnel prepare the problem that catalyzer is changed early.
Claims (6)
1. vacuum sampling system, it is characterized in that: this vacuum sampling system comprises one group of sample tap (1), the gas purging corresponding with one group of sample tap (1) inlet (2), cooling device (3), sampling bottle (4), sample tap (5) and vacuum pump (6), and one group of sample tap (1) passes through cooling device (3) and is connected with sampling bottle (4); One end of sampling bottle (4) is connected with vacuum pump (6), and is provided with gas purging outlet (7) between sampling bottle (4) and vacuum pump (6); The other end of sampling bottle (4) is connected with sample tap (5).
2. vacuum sampling system according to claim 1 is characterized in that: described cooling device (3) comprises refrigeratory (31) and cooling bath (32), is equipped with cooling liquid inlet and cooling liquid outlet on refrigeratory (31) and cooling bath (32); Between refrigeratory (31) and cooling bath (32), be provided with thermometer (33).
3. vacuum sampling system according to claim 1 is characterized in that: described sampling bottle (4) and sample tap (5) are two groups of parallel connections.
4. vacuum sampling system according to claim 1 is characterized in that: be provided with sample platform (8) in sample tap (5) below.
5. vacuum sampling system according to claim 1 is characterized in that: be provided with drain (9) between sampling bottle (4) and vacuum pump (6).
6. vacuum sampling system according to claim 1 is characterized in that: one group of sample tap (1) is six, and the gas purging inlet (2) corresponding with hexad sample tap (1) also is six, and is arranged on sample tap (1) top.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202329107U CN201476995U (en) | 2009-07-24 | 2009-07-24 | Vacuum sampling system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202329107U CN201476995U (en) | 2009-07-24 | 2009-07-24 | Vacuum sampling system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201476995U true CN201476995U (en) | 2010-05-19 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009202329107U Expired - Lifetime CN201476995U (en) | 2009-07-24 | 2009-07-24 | Vacuum sampling system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201476995U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101846663A (en) * | 2010-05-28 | 2010-09-29 | 浙江大学 | Rapid on-line diagnosis method for deactivation condition of SCR (selective catalytic reduction) denitration catalyst |
| CN103969403A (en) * | 2014-05-09 | 2014-08-06 | 哈尔滨工程大学 | Method for measuring uniformity of ammonia gas concentration in SCR (silicon controller rectifier) system pipeline |
| CN106353140A (en) * | 2016-08-26 | 2017-01-25 | 江苏信泰机械有限公司 | Vacuum sampling system |
-
2009
- 2009-07-24 CN CN2009202329107U patent/CN201476995U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101846663A (en) * | 2010-05-28 | 2010-09-29 | 浙江大学 | Rapid on-line diagnosis method for deactivation condition of SCR (selective catalytic reduction) denitration catalyst |
| CN103969403A (en) * | 2014-05-09 | 2014-08-06 | 哈尔滨工程大学 | Method for measuring uniformity of ammonia gas concentration in SCR (silicon controller rectifier) system pipeline |
| CN103969403B (en) * | 2014-05-09 | 2015-07-22 | 哈尔滨工程大学 | Method for measuring uniformity of ammonia gas concentration in SCR (silicon controller rectifier) system pipeline |
| CN106353140A (en) * | 2016-08-26 | 2017-01-25 | 江苏信泰机械有限公司 | Vacuum sampling system |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20151127 Address after: 221200 Jiangsu Province, Xuzhou city Suining County Industrial Park, North Ring Road No. 66 Gang Patentee after: JIANGSU XINTAI MACHINERY CO., LTD. Address before: Jiangning District of Nanjing City, Jiangsu Province on the 211103 Industrial Road Run Qi Fang Takahashi Patentee before: Nanjing Hangda Precision Machinery Co., Ltd. |
|
| C56 | Change in the name or address of the patentee | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 221200 Jiangsu Province, Xuzhou city Suining County Industrial Park, North Ring Road No. 66 Gang Patentee after: Jiangsu Xintai Chemical Equipment Co., Ltd. Address before: 221200 Jiangsu Province, Xuzhou city Suining County Industrial Park, North Ring Road No. 66 Gang Patentee before: JIANGSU XINTAI MACHINERY CO., LTD. |
|
| CX01 | Expiry of patent term |
Granted publication date: 20100519 |
|
| CX01 | Expiry of patent term |