CN203890265U - Light benzene hydrogenation unit - Google Patents
Light benzene hydrogenation unit Download PDFInfo
- Publication number
- CN203890265U CN203890265U CN201420341665.4U CN201420341665U CN203890265U CN 203890265 U CN203890265 U CN 203890265U CN 201420341665 U CN201420341665 U CN 201420341665U CN 203890265 U CN203890265 U CN 203890265U
- Authority
- CN
- China
- Prior art keywords
- tower
- interchanger
- outlet
- heat exchanger
- shell side
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model relates to a light benzene hydrogenation unit which comprises a first heat exchanger, a tower evaporator, a second heat exchanger, a pre-reaction tower, a third heat exchanger, a main hydrogenation tower, a condenser and a high-pressure separator, wherein a tube side outlet of the first heat exchanger is connected with the evaporator; a gas outlet of the evaporator is connected with a tube side inlet of the second heat exchanger; a tube side outlet of the second heat exchanger and a gas inlet of the pre-reaction tower are connected with a heat-conducting oil heater; a gas outlet of the pre-reaction tower is connected with a tube side inlet of the third heat exchanger; an electric heater is connected between the third heat exchanger and main hydrogenation tower; a gas outlet of the main hydrogenation tower is connected with a shell side inlet of the third heat exchanger; a shell side outlet of the third heat exchanger is connected with a shell side inlet of the second heat exchanger; a shell side outlet of the second heat exchanger is connected with a shell side inlet of the first heat exchanger; a shell side outlet of the first heat exchanger is connected with the condenser; and the condenser is connected with the high-pressure separator. The light benzene hydrogenation unit is simple in equipment and process and convenient to control, and has the advantages of high heat utilization ratio and favorable effects of desulfurization, denitrification and deoxidation.
Description
Technical field
The utility model relates to crude benzene refining field, specifically a kind of light benzene hydrogenation unit.
Background technology
Benzene, toluene and dimethylbenzene are all very important industrial chemicals, its industrial be by crude benzol through purifying separated and obtaining, so-called crude benzol is purified and the separated crude benzene refining technique that refers to.Current crude benzene refining technique mainly contains three classes: acid wash, hydrofining method, extractive distillation method, wherein acid wash is because environmental pollution is seriously eliminated, in conjunction with hydrofining and extractive distillation, the applicant provides a kind of new process for refining, it comprise take off in advance heavy, crude benzol is separated into heavy benzol and light benzene, in light benzene, hydrogenation carries out desulfurization under the effect of catalyzer again, denitrogenation and deoxygenation, obtain benzene, toluene and dimethylbenzene and other light component, again by de-light processing, light component in said mixture and reaction impurities (hydrogen sulfide etc.) are removed, thereby obtain work in-process BTXS(benzene, toluene, dimethylbenzene and C8, the mixtures such as non-aromatics, be referred to as again dehydrogenated oil mixture), again by pre-rectification process, work in-process BTXS is separated into BT(benzene, toluene, the mixture of non-aromatics) and XS(dimethylbenzene, the mixture of C8 etc.), BT is passed in extraction plant, thereby obtain product non-aromatics, the mixture of benzene and toluene is through in purified petroleum benzin tower apparatus, thereby benzene is separated with toluene, obtain the finished product benzene, toluene, treatment process by XS through benzenol hydrorefining, isolate the finished product dimethylbenzene and C8.
Do not have at present ready-made equipment can realize above-mentioned technical process, thereby a covering device need to be set separately.The utility model designs mainly for light benzene hydrogenation process, because the temperature of hydrogen benzene hydrogenation catalytic desulfurization, denitrogenation and deoxygenation is higher, current equipment cannot be realized heat on this procedure and effectively control and efficient utilization, has the problem of resource and energy wastage.
Utility model content
The technical problems to be solved in the utility model be to provide a kind of equipment flowsheet simple, control convenient, heat utilization ratio is high and desulfurization, denitrogenation, light benzene hydrogenation unit that deoxidation effect is good.
For solving the problems of the technologies described above, the constructional feature of the utility model light benzene hydrogenation unit is to comprise First Heat Exchanger, tower evaporator, the second interchanger, pre-reaction tower, the 3rd interchanger, main hydrogenation tower, condenser and high-pressure separator, the tube side import of First Heat Exchanger bottom is connected with the outlet of light benzene storage tank, the tube side outlet at top is connected with the opening for feed of vaporizer, the bottom of vaporizer be communicated with one by thermal oil the vaporizer reboiler as heating medium, the air outlet at vaporizer top is connected with the tube side import at the second interchanger top, between the tube side outlet of the second interchanger and the inlet mouth of pre-reaction tower bottom, be connected with hotline heater, the air outlet of pre-reaction top of tower is connected with the tube side import at the 3rd interchanger top, between the tube side outlet of the 3rd interchanger bottom and the inlet mouth of main hydrogenation top of tower, is connected electric heater, hydrogen inlet is offered at the middle part of main hydrogenation tower, the air outlet of main hydrogenation tower bottom is connected with the shell side import of the 3rd interchanger, the shell side outlet of the 3rd interchanger is connected with the shell side import of the second interchanger, the shell side outlet of the second interchanger is connected with the shell side import of First Heat Exchanger, the shell side outlet of First Heat Exchanger is connected with the inlet mouth of condenser, the liquid outlet of condenser is connected with the opening for feed of high-pressure separator, the outlet of product liquid is offered in the bottom of high-pressure separator, the top of high-pressure separator offers circulation gas outlet, the bottom of vaporizer reboiler offers the circulation gas import being connected by circulation line with above-mentioned circulation gas outlet, gas compressor is installed on circulation line.
Adopt said structure, stock oil gasifies to vaporizer after First Heat Exchanger preheating, when hotline heater intensification reaches temperature of reaction, enter pre-reaction tower again and carry out desulfurization, denitrogenation, deoxygenation, from pre-reaction tower gas mixture out, through the laggard hydrogenation tower of becoming owner of of electric heater heating, carry out deep desulfuration, denitrogenation, deoxygenation, each interchanger that gas product enters in system again uses as heating medium, finally by condenser condenses and enter and carry out gas-oil separation in high-pressure separator, from gaseous constituent out in high-pressure separator, again by vaporizer reboiler, entering vaporizer internal recycle reacts.Visible, whole system flow process is simple, it is convenient to control, through a plurality of interchanger, repeatedly utilize system thermal, make the heat utilization ratio of system high, simultaneously, utilize hotline heater and electric heater progressively to promote temperature of reaction, and carry out two step desulfurization, denitrogenation and deoxygenation through pre-reaction tower and main hydrogenation tower, and reaction effect is good, and product purity is high.
On described circulation line, be also connected with circulation gas interchanger, the tube side of this circulation gas interchanger is communicated with circulation line, and the shell side of this circulation gas interchanger is serially connected between the shell side outlet and the shell side import of First Heat Exchanger of the second interchanger.Owing to can containing a large amount of hydrogen in the gaseous constituent in high-pressure separator, for fear of waste, this gas is sent back in system and re-used by circulation line, and circulation gas interchanger is set can be preheated this portion gas, simultaneously also recycle the heat of system.
Heat exchange structure in interchanger comprises upper tubesheet, lower tubesheet and is connected to many heat transfer tubes between upper and lower tube sheet, between upper and lower tube sheet, also interval arranges polylith and is connected to the traverse baffle on equipment inner wall, and traverse baffle cross arrangement is on the inwall of equipment two opposite sides.The heat exchange structure of each interchanger is the structure of this kind of shell-and-tube, and so-called tube side refers to the passage that each heat transfer tube is communicated with, and shell side is the space in housing, and tube side and shell side are offered import and outlet respectively, utilize the tube wall of heat transfer tube to carry out heat exchange.
Described pre-reaction tower bottom has been horizontally set with screen, the bottom of screen is pre-reaction tower inlet chamber, on pre-reaction tower inlet mouth, be connected with the air inlet extension tube that extends to inlet chamber middle part, the inner extending end of this air inlet extension tube is installed air distribution plate to lower opening and on opening, screen top catalyst filling filler forms catalyst layer, offers pre-reaction tower catalyzer unload mouth on pre-reaction tower in the bottom of catalyst filling layer.
In described main hydrogenation tower, by Stainless Steel Cloth, be separated into successively from the bottom to top outlet chamber, lower floor's catalyzer chamber, hydrogen gas chamber, catalyzer chamber, upper strata and unstripped gas inlet chamber, on main hydrogenation tower, offer the hydrogen inlet being communicated with hydrogen gas chamber, on the inherent hydrogen inlet of main hydrogenation tower, be connected with hydrogen extension tube, the inner extending end of extension tube is installed hydrogen gas pipe, main hydrogenation tower inlet mouth is opened in tower body top and unstripped gas gas pipe is installed on inlet mouth, main hydrogenation tower air outlet is opened on Qie air outlet, tower body bottom installs collector box, the bottom in catalyzer Qiang He lower floor's catalyzer chamber, main hydrogenation tower upper strata is respectively offered a main hydrogenation tower catalyzer and is unloaded mouth.
Described condenser is air cooled condenser.
In sum, the utility model equipment flowsheet simple, control convenient, heat utilization ratio is high and desulfurization, denitrogenation, deoxidation effect are good.
Accompanying drawing explanation
Below in conjunction with the drawings and specific embodiments, the utility model is described in further detail:
Fig. 1 is the Structure and Process schematic diagram of wherein a kind of embodiment of the present utility model;
Fig. 2 is the Structure and Process schematic diagram of another kind of embodiment of the present utility model;
Fig. 3 is the structural representation of interchanger in the utility model;
Fig. 4 is the structural representation of main hydrogenation tower in the utility model;
Fig. 5 is the structural representation of pre-reaction tower in the utility model;
Fig. 6 is the structural representation of vaporizer in the utility model;
Fig. 7 is the structural representation of vaporizer reboiler in the utility model;
Fig. 8 is the structural representation of hotline heater in the utility model;
Fig. 9 is the structural representation of the utility model mesohigh separator.
Embodiment
With reference to accompanying drawing, a kind of embodiment of the utility model light benzene hydrogenation unit is for comprising First Heat Exchanger 1, tower evaporator 2, the second interchanger 3, pre-reaction tower 4, the 3rd interchanger 5, main hydrogenation tower 6, condenser 7 and high-pressure separator 8, the tube side import of First Heat Exchanger 1 bottom is connected with the outlet of light benzene storage tank, the outlet of the tube side at top is connected with the opening for feed of vaporizer 2, the bottom of vaporizer 2 be communicated with one by thermal oil the vaporizer reboiler 9 as heating medium, the air outlet at vaporizer 2 tops is connected with the tube side import at the second interchanger 3 tops, between the tube side outlet of the second interchanger 3 and the inlet mouth of pre-reaction tower 4 bottoms, be connected with hotline heater 10, the air outlet at pre-reaction tower 4 tops is connected with the tube side import at the 3rd interchanger 5 tops, between the inlet mouth at the outlet of the tube side of the 3rd interchanger 5 bottoms and main hydrogenation tower 6 tops, is connected electric heater 11, the air outlet of main hydrogenation tower 6 bottoms is connected with the shell side import of the 3rd interchanger 5, the shell side outlet of the 3rd interchanger 5 is connected with the shell side import of the second interchanger 3, the shell side outlet of the second interchanger 3 is connected with the shell side import of First Heat Exchanger 1, the shell side outlet of First Heat Exchanger 1 is connected with the inlet mouth of condenser 7, the liquid outlet of condenser 7 is connected with the opening for feed of high-pressure separator 8, product liquid outlet 8-03 is offered in the bottom of high-pressure separator 8, the top of high-pressure separator 8 offers circulation gas outlet 81, the bottom of vaporizer reboiler 9 offers the circulation gas import 9-01 being connected by circulation line 89 with above-mentioned circulation gas outlet 8-01, gas compressor 891 is installed on circulation line 89.Wherein, the effect of condenser 7 is by the condensation of High Temperature Gas liquid mixture, and it can adopt water-cooled or air-cooled structure, and the utility model is preferably the latter.
In Fig. 2, illustrated another kind of embodiment of the present utility model, this embodiment is from the different of Fig. 1, on circulation line 89, be also connected with circulation gas interchanger 892, the tube side of this circulation gas interchanger 892 is communicated with circulation line 89, and the shell side of this circulation gas interchanger 892 is serially connected between the shell side outlet and the shell side import of First Heat Exchanger 1 of the second interchanger 3.Owing to can containing a large amount of hydrogen in the gaseous constituent in high-pressure separator 8, for fear of waste, this gas is sent back in system and re-used by circulation line 89, and circulation gas interchanger 892 is set can be preheated this portion gas, simultaneously also recycle the heat of system.
In said structure, stock oil gasifies to vaporizer 2 after First Heat Exchanger 1 preheating, when hotline heater 10 intensifications reach temperature of reaction, enter pre-reaction tower 4 again and carry out desulfurization, denitrogenation, deoxygenation, from pre-reaction tower 4 gas mixture out, through the laggard hydrogenation tower 6 of becoming owner of of electric heater 11 heating, carry out deep desulfuration, denitrogenation, deoxygenation, each interchanger that gas product enters in system again uses as heating medium, finally by condenser 7 condensations and enter and carry out gas-oil separation in high-pressure separator 8, from gaseous constituent out in high-pressure separator 8, again by vaporizer reboiler 9, entering vaporizer 5 internal recycle reacts.Visible, whole system flow process is simple, it is convenient to control, through a plurality of interchanger, repeatedly utilize system thermal, make the heat utilization ratio of system high, simultaneously, utilize hotline heater and electric heater progressively to promote temperature of reaction, and carry out two step desulfurization, denitrogenation and deoxygenation through pre-reaction tower and main hydrogenation tower, and reaction effect is good, and product purity is high.
First, second, and third interchanger and circulation gas interchanger in the utility model, have been used, heat exchange structure in these four interchanger is identical, the First Heat Exchanger of take in an embodiment describes as example, as shown in Figure 3, heat exchange structure comprises upper tubesheet 12, lower tubesheet 13 and is connected to the many heat transfer tubes 14 between upper and lower tube sheet, between upper and lower tube sheet, also interval arranges polylith and is connected to the traverse baffle 15 on equipment inner wall, and traverse baffle 15 cross arrangement are on the inwall of equipment two opposite sides.Adopt the structure of this kind of shell-and-tube, so-called tube side refers to the passage that each heat transfer tube is communicated with, and shell side is the space in housing, and tube side and shell side are offered import and outlet respectively, utilize the tube wall of heat transfer tube 14 to carry out heat exchange.In Fig. 3, what in the tube side of First Heat Exchanger 1, enter is stock oil liquid, therefore, tube side import 1-02 under, tube side outlet 1-01 is upper, what in shell side, enter is reacted high-temperature gas, offers shell side import 1-03 and shell side outlet 1-04 on interchanger.
Wherein, from Fig. 7 and Fig. 8, heat exchange structure and the heat exchange structure in interchanger in vaporizer reboiler 9 and hotline heater 10 are similar, in the shell side of vaporizer reboiler 9 and hotline heater 10, pass into thermal oil, utilize heat-conducting oil heating.In Fig. 7, on vaporizer reboiler 9, offer reboiler liquid-inlet 9-03, reboiler liquid exit 9-02, reboiler heat conductive oil inlet 9-04, reboiler thermal oil outlet 9-05 and circulation gas import 9-01.In Fig. 8, on hotline heater 10, offer well heater import 10-01, heater outlet 10-02, well heater heat conductive oil inlet 10-04 and well heater thermal oil outlet 10-03.
As shown in Figure 4, in main hydrogenation tower 6, by Stainless Steel Cloth, be separated into successively from the bottom to top outlet chamber 61, lower floor's catalyzer chamber 62, hydrogen gas chamber 63, catalyzer chamber, upper strata 64 and unstripped gas inlet chamber 65, on main hydrogenation tower 6, offer the hydrogen inlet 6-01 being communicated with hydrogen gas chamber 63, on the inherent hydrogen inlet 6-01 of main hydrogenation tower 6, be connected with hydrogen extension tube 66, the inner extending end of extension tube 66 is installed hydrogen gas pipe 67, main hydrogenation tower inlet mouth 6-02 is opened in tower body top and unstripped gas gas pipe 68 is installed on inlet mouth, main hydrogenation tower air outlet 6-03 is opened on Qie air outlet, tower body bottom collector box 69 is installed, the bottom in main hydrogenation tower 6 catalyzer Qiang64He lower floor catalyzer chambeies, upper strata 62 is respectively offered a main hydrogenation tower catalyzer and is unloaded a mouthful 6-04.
As shown in Figure 5, on pre-reaction tower, offer pre-reaction tower inlet mouth 4-01, pre-reaction tower air outlet 4-02, pre-reaction tower 4 bottoms have been horizontally set with screen 41, the bottom of screen 41 is pre-reaction tower inlet chamber, on pre-reaction tower inlet mouth, be connected with the air inlet extension tube 42 that extends to inlet chamber middle part, the inner extending end of this air inlet extension tube 42 is installed air distribution plate 43 to lower opening and on opening, screen 42 top catalyst filling fillers form catalyst layer 44, offer pre-reaction tower catalyzer unload a mouthful 4-03 on pre-reaction tower 4 in the bottom of catalyst filling layer.
In Fig. 9, illustrated the structure of high-pressure separator 8, in high-pressure separator 8, offer separator import 8-02, product liquid outlet 8-03 and circulation gas outlet 8-01, the bottom of high-pressure separator 8 arranges intercepting basin 81, and the bottom of intercepting basin 81 is opened separator and established sewage draining exit 8-04.Separator import 8-02 is opened in the top of high-pressure separator 8 and extension tube 82 is installed in import, and extension tube 82 extends downward near separator diapire, and erosion control baffle plate 83 is also installed on extension tube 82 sides.
Wherein, on each tank body in the utility model, offer as required the conventional openings such as evacuation port, sewage draining exit and liquidometer installing port, pressure transmitter installing port, level meters installing port, those skilled in the art arrange according to the needs of equipment flowsheet, for prior art, do not repeat them here.
In sum, the utility model is not limited to above-mentioned embodiment.Those skilled in the art, not departing under the prerequisite of spirit and scope of the present utility model, can do some changes and modification.Protection domain of the present utility model should be as the criterion with claim of the present utility model.
Claims (6)
1. a light benzene hydrogenation unit, is characterized in that comprising First Heat Exchanger (1), tower evaporator (2), the second interchanger (3), pre-reaction tower (4), the 3rd interchanger (5), main hydrogenation tower (6), condenser (7) and high-pressure separator (8), the tube side import of First Heat Exchanger (1) bottom is connected with the outlet of light benzene storage tank, the tube side outlet at top is connected with the opening for feed of vaporizer (2), the bottom of vaporizer (2) be communicated with one by thermal oil the vaporizer reboiler (9) as heating medium, the air outlet at vaporizer (2) top is connected with the tube side import at the second interchanger (3) top, between the tube side outlet of the second interchanger (3) and the inlet mouth of pre-reaction tower (4) bottom, be connected with hotline heater (10), the air outlet at pre-reaction tower (4) top is connected with the tube side import at the 3rd interchanger (5) top, between the tube side outlet of the 3rd interchanger (5) bottom and the inlet mouth at main hydrogenation tower (6) top, is connected electric heater (11), hydrogen inlet (6-01) is offered at the middle part of main hydrogenation tower (6), the air outlet of main hydrogenation tower (6) bottom is connected with the shell side import of the 3rd interchanger (5), the shell side outlet of the 3rd interchanger (5) is connected with the shell side import of the second interchanger (3), the shell side outlet of the second interchanger (3) is connected with the shell side import of First Heat Exchanger (1), the shell side outlet of First Heat Exchanger (1) is connected with the inlet mouth of condenser (7), the liquid outlet of condenser (7) is connected with the opening for feed of high-pressure separator (8), product liquid outlet (8-03) is offered in the bottom of high-pressure separator (8), the top of high-pressure separator (8) offers circulation gas outlet (81), the bottom of vaporizer reboiler (9) offers the circulation gas import (9-01) being connected by circulation line (89) with above-mentioned circulation gas outlet (8-01), gas compressor (891) is installed on circulation line (89).
2. light benzene hydrogenation unit as claimed in claim 1, it is characterized in that being also connected with on described circulation line (89) circulation gas interchanger (892), the tube side of this circulation gas interchanger (892) is communicated with circulation line (89), and the shell side of this circulation gas interchanger (892) is serially connected between the shell side outlet and the shell side import of First Heat Exchanger (1) of the second interchanger (3).
3. light benzene hydrogenation unit as claimed in claim 2, it is characterized in that the heat exchange structure in interchanger comprises upper tubesheet (12), lower tubesheet (13) and is connected to the many heat transfer tubes (14) between upper and lower tube sheet, between upper and lower tube sheet, also interval arranges polylith and is connected to the traverse baffle (15) on equipment inner wall, and traverse baffle (15) cross arrangement is on the inwall of equipment two opposite sides.
4. light benzene hydrogenation unit as claimed in claim 1, it is characterized in that described pre-reaction tower (4) bottom has been horizontally set with screen (41), the bottom of screen (41) is pre-reaction tower inlet chamber, on pre-reaction tower inlet mouth, be connected with the air inlet extension tube (42) that extends to inlet chamber middle part, the inner extending end of this air inlet extension tube (42) is installed air distribution plate (43) to lower opening and on opening, screen (42) top catalyst filling filler forms catalyst layer (44), and the upper pre-reaction tower catalyzer of offering in the bottom of catalyst filling layer of pre-reaction tower (4) unloads mouthful (4-03).
5. light benzene hydrogenation unit as claimed in claim 1, it is characterized in that by Stainless Steel Cloth, being separated into successively from the bottom to top outlet chamber (61) in described main hydrogenation tower (6), lower floor's catalyzer chamber (62), hydrogen gas chamber (63), catalyzer chamber, upper strata (64) and unstripped gas inlet chamber (65), on main hydrogenation tower (6), offer the hydrogen inlet (6-01) being communicated with hydrogen gas chamber (63), on the inherent hydrogen inlet of main hydrogenation tower (6) (6-01), be connected with hydrogen extension tube (66), the inner extending end of extension tube (66) is installed hydrogen gas pipe (67), main hydrogenation tower inlet mouth (6-02) is opened in tower body top and unstripped gas gas pipe (68) is installed on inlet mouth, main hydrogenation tower air outlet (6-03) is opened in collector box (69) is installed on Qie air outlet, tower body bottom, the bottom in catalyzer chamber, main hydrogenation tower (6) upper strata (64) and lower floor's catalyzer chamber (62) is respectively offered a main hydrogenation tower catalyzer and is unloaded mouthful (6-04).
6. the light benzene hydrogenation unit as described in any one in claim 1-5, is characterized in that described condenser (7) is air cooled condenser.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420341665.4U CN203890265U (en) | 2014-06-25 | 2014-06-25 | Light benzene hydrogenation unit |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420341665.4U CN203890265U (en) | 2014-06-25 | 2014-06-25 | Light benzene hydrogenation unit |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203890265U true CN203890265U (en) | 2014-10-22 |
Family
ID=51716693
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420341665.4U Expired - Fee Related CN203890265U (en) | 2014-06-25 | 2014-06-25 | Light benzene hydrogenation unit |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203890265U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114534278A (en) * | 2020-11-10 | 2022-05-27 | 宝武碳业科技股份有限公司 | Benzene hydrogenation pre-evaporation system with online cleaning function, process and application |
-
2014
- 2014-06-25 CN CN201420341665.4U patent/CN203890265U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114534278A (en) * | 2020-11-10 | 2022-05-27 | 宝武碳业科技股份有限公司 | Benzene hydrogenation pre-evaporation system with online cleaning function, process and application |
| CN114534278B (en) * | 2020-11-10 | 2024-03-15 | 宝武碳业科技股份有限公司 | Benzene hydrogenation pre-evaporation system with online cleaning function, process and application |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104560132B (en) | A kind of Continuous Liquid Phase wax oil hydrogenation processing method | |
| AU2002226329B2 (en) | Improved hydroprocessing process and method of retrofitting existing hydroprocessing reactors | |
| CN102766021B (en) | Production system and production method for continuously producing ethanol by ethyl acetate through using hydrogenation | |
| CN106608805B (en) | A kind of method of liquid phase selective hydrogenation of C 3 hydrocarbons | |
| CN102039104B (en) | Reactor and liquid-phase hydrogenation processing method | |
| CN109053355B (en) | Method for purifying biphenyl by continuous rectification | |
| CN203923054U (en) | A kind of device of being produced benzene, toluene and dimethylbenzene by crude benzol | |
| CN103785332A (en) | A two-phase hydrogenation reactor and applications thereof | |
| CN106477792A (en) | A kind of method and device for stripping process petrochemical industry sour water nothing side line single column negative pressure | |
| CN100429194C (en) | Method for utilizing reaction heat in process of producing methane chloride and purifying mixture | |
| CN106147830B (en) | The piece-rate system and separation method of hydrogenation reaction effluent | |
| CN203890265U (en) | Light benzene hydrogenation unit | |
| CN203174041U (en) | Steam stripping tower | |
| CN108587684A (en) | A kind of joint aromatics production line CONTINUOUS REFORMER unit | |
| CN201537408U (en) | Purification treatment tower for producing hydrogen with natural gas | |
| CN210595940U (en) | Heat conduction oil processing device | |
| JP4348657B2 (en) | Hydrocarbon conversion process by treatment in distillation zone including withdrawal of stabilized distillate combined with reaction zone and its use in benzene hydrogenation | |
| CN111018021B (en) | Hydrogen sulfide acidic water purification method based on side line and tower kettle reflux ratio control | |
| KR101173907B1 (en) | A fractional distillation device of ternary separation with internally heat-integrated distillation column | |
| CN209702624U (en) | The parallel methanol synthesis reaction system of double-reactor | |
| CN103789006A (en) | A two-phase hydrogenation reactor and a two-phase hydrogenation method | |
| CN203558986U (en) | Device for refining and machining aromatic hydrocarbons by using liquefied gas | |
| CN203878115U (en) | Combined type oil product hydrogenation device | |
| CN204111689U (en) | Selective hydrogenation device | |
| CN103183577A (en) | Heat exchange system and heat exchange method for carbon five extractive distillation |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20141022 Termination date: 20160625 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |