CN104128131A - Regeneration gas cycle recovery apparatus and method thereof - Google Patents
Regeneration gas cycle recovery apparatus and method thereof Download PDFInfo
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- CN104128131A CN104128131A CN201410310572.XA CN201410310572A CN104128131A CN 104128131 A CN104128131 A CN 104128131A CN 201410310572 A CN201410310572 A CN 201410310572A CN 104128131 A CN104128131 A CN 104128131A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Abstract
The invention discloses a regeneration gas cycle recovery apparatus and a method thereof, the method is characterized in that the regeneration gas in a regeneration gas inlet pipeline and a catalyst in the reactor are reacted to increase the activity of the catalyst, the reacted regeneration gas exhaust gas is output from a collection end of the reactor and then is carried out heat exchange through a heat exchanger, then the reacted regeneration gas exhaust gas is introduced in a separation pot, flash evaporation is carried out on the regeneration gas exhaust gas by the separation pot, the gas phase regeneration gas exhaust gas is output from the top of the separation pot, then passes through a gas phase output pipeline and is divided into two flows through a first gas phase output sub pipeline and a second gas phase output sub pipeline, flow in the first gas phase output sub pipeline is used for cycle recovery, flow in the second gas phase output sub pipeline is discharged or combusted; a flow controller calculates according to flow amount in the second gas phase output sub pipeline collected by the first flow transmitter and the proportion of key ingredients in the regeneration gas exhaust gas collected by a gas discharge analyzer, the proportion of the newly introduced regeneration gas to the cycle regeneration gas exhaust gas can be adjusted by a control valve after calculating, so that the key ingredient of the regeneration gas in the reactor is a preset concentration value.
Description
Technical field
The present invention relates to catalyst regeneration field, the device and method reclaiming for the regeneration gas circulation of MTP (Methanol To Propylene, preparing propylene from methanol) device reaction device in particular to one.
Background technology
In existing apparatus, reactor need to carry out regenerative operation conventionally.When these equipment that need to regenerate are switched to regeneration operating mode by normal operating operating mode, the step that conventionally will pass through the material returned, pressure release, displacement, purging, regeneration.In the step of displacement, purging and regeneration, conventionally use regeneration gas to process the catalyst in equipment or drier.The regeneration gas of access arrangement is conventionally used fresh inert gas or does not affect the gas of equipment inner catalyst performance.Behind regeneration gas access arrangement inside, react with the carbon deposit/impurity of catalyst surface, or carry the foreign gas of catalyst or drier desorption, finally discharge reactor.The regeneration gas of device for transferring, if contain fuel gas, employing is directly discharged into the way that flare system is burnt conventionally, if regeneration gas does not contain flammable or poisonous gas, conventionally can adopt the way that is directly discharged into atmosphere.Typical fixed bed reactors regeneration schematic flow sheet is shown in Fig. 1.
In existing regenerative response process, the first valve group 234 is opened, the 8th valve 1061 cuts out, the 9th valve 241 and the 6th valve 251 are closed, the 7th valve 1051 is opened, regeneration gas is entered by regeneration gas feeding line 107, first through superheater, 102 heating reach after regeneration temperature, enter reactor 101 inlet ends, during by beds, after regeneration there is variation in the component of gas, discharge in reactor 101 bottoms, reclaim after heat through heat exchanger 103, separate by knockout drum 104, then be directly discharged into atmosphere or enter flare system burning from toxic emission pipeline 105.In whole flow process, disposable atmosphere or the flare system of being all discharged to of regeneration gas, discharge capacity is larger, waste regeneration gas.
In regenerative process due to reactor, from the regeneration initial stage to regenerating latter stage, the component of regeneration gas changes always.Especially regenerate latter stage, the impurity content in catalyst or drier is remaining less, and regeneration gas is not directly passed equipment through any reaction conventionally, outside device for transferring, causes the utilization rate of regeneration gas lower.
Improvement is in the past the recovery of considering regeneration gas from the discharge of regeneration gas, regeneration gas is entered to the air inlet of the firing equipment such as incinerator or pyrolysis furnace, wishes that the burning of regeneration gas can provide portion of energy, then carries out energy recovery by the heat exchanger tube of heating furnace.But because regeneration gas is after reactor regeneration, oxygen wherein consumes, and what it was main consists of a large amount of nitrogen and carbon dioxide.If regeneration gas is discharged into heating furnace burner hearth, can reduce the thermal efficiency of heating furnace.
Therefore, in the urgent need to the existing regeneration gas circulatory system is improved.
Summary of the invention
The invention provides the device and method that a kind of regeneration gas circulation is reclaimed, in order to the utilization rate from improving regeneration gas, reduce the discharge capacity of regeneration gas in the unit interval, improve the utilization ratio of regeneration gas, to solve the problem of regeneration gas waste.
For achieving the above object, the invention provides a kind of regeneration gas and loop back receiving apparatus, comprise that the first valve group, second valve group, filter, superheater, compressor, heat exchanger, surge tank, the first cooler, gas discharging analyzer, flow controller, first flow transmitter, toxic emission controller, second transmitter, reactor, knockout drum, regeneration gas feeding line, reaction export pipeline, gas phase export pipeline, the first gas phase are exported sub-pipeline, the second gas phase is exported sub-pipeline, the 3rd valve, check-valves, the 4th valve, wherein:
On described regeneration gas feeding line, be provided with successively described the first valve group, described superheater, described second transmitter, described regeneration gas feeding line is finally connected with described reactor inlet end; Catalyst reaction when the described regeneration gas being flowed into by described regeneration gas feeding line is passed through the beds in described reactor and on described beds, described catalyst activity is improved, and reacted regeneration gas waste gas is exported from described reactor production end;
Described reactor production end is connected with described knockout drum by described reaction export pipeline, and described reaction export pipeline is provided with described heat exchanger; The regeneration gas waste gas of described reactor production end output enters described knockout drum after described heat exchanger heat exchange, and described knockout drum carries out after flash distillation described regeneration gas waste gas, and the described regeneration gas waste gas of gas phase is exported from described knockout drum top;
Described gas phase export pipeline is connected with described knockout drum top, and described gas phase export pipeline is finally divided into that described the first gas phase is exported sub-pipeline and described the second gas phase is exported sub-pipeline; From the described regeneration gas waste gas of the gas phase of described knockout drum top output by described gas phase export pipeline and exported sub-pipeline and described the second gas phase by described the first gas phase and export sub-pipeline and be divided into two plumes, described the first gas phase is exported plume in sub-pipeline for the recovery that circulates, and the plume that described the second gas phase is exported in sub-pipeline is discharged into atmosphere or burned;
The switching degree of described the first valve group and described second valve group is controlled respectively by described regeneration gas feeding line newly to enter regeneration gas and be discharged into atmosphere or burned described the second gas phase is exported the flow of the plume in sub-pipeline;
Described the first gas phase is exported and on sub-pipeline, is provided with successively described the 3rd valve, described filter, described the first cooler, described surge tank, described compressor, described check-valves, described the 4th valve, and is finally connected between the above first valve group of described regeneration gas feeding line and described superheater and locates; The plume that described the first gas phase is exported in sub-pipeline flows into described filter by described the 3rd valve, through described filter elimination part solid particle, and after described the first cooler is cooled to described suction port of compressor temperature required, remove liquid phase by described buffer, enter again described compressor compresses pressurization, after described check-valves and described the 4th valve, mix with the regeneration gas of newly entering in described regeneration gas feeding line;
Described the second gas phase is exported and on sub-pipeline, is provided with successively described gas discharging analyzer, described first flow transmitter and described second valve group; Wherein, described gas discharging analyzer is for analyzing the concentration ratio of described regeneration gas waste gas key component in described regeneration gas waste gas, and described first flow transmitter gathers described the second gas phase exports the flow of the plume of sub-pipeline;
Described toxic emission controller is connected with described first flow transmitter and described second valve group signal, described flow controller and described toxic emission controller, described second transmitter, described gas discharging analyzer and described the first valve group signal connect, the flow that described first flow transmitter is exported described the second gas phase the plume of sub-pipeline passes to described flow controller through described toxic emission controller, described second transmitter by enter described reactor described regeneration gas pass traffic give described flow controller, the ratio of key component in described regeneration gas waste gas in described regeneration gas waste gas passed to described flow controller by described gas discharging analyzer, described flow controller is calculated as and reaches default, what the concentration value of the key component of the described regeneration gas that described reactor needs was required newly enters regeneration gas and the ratio of exporting sub-pipeline by described the second gas phase and be discharged into atmosphere or burned described regeneration gas waste gas plume by described regeneration gas feeding line, and according to the first valve group described in result of calculation control and the switching degree by second valve group described in the control of described toxic emission controller to regulate respectively described regeneration gas feeding line and the second gas phase to export the plume size of sub-pipeline, thereby the concentration value that ensures the key component of the described regeneration gas that enters described reactor is default concentration value.
Wherein, anti-surge by-pass line, the 3rd flow transmitter and the 5th valve, wherein, described the 3rd flow transmitter and the 5th valve are located on described anti-surge by-pass line, described the 3rd flow transmitter is located at described first gas phase at described compressor outlet place and exports on sub-pipeline, for detection of the flow of described compressor; One end of described anti-surge by-pass line is connected to after described the first gas phase exports described the 3rd flow transmitter on sub-pipeline, the other end is connected to described the first gas phase and exports between the described filter and described the first cooler on sub-pipeline, for preventing described compressor surge.
Wherein, described compressor is split-compressor, wherein between two sections of one section of this split-compressor and this split-compressors, is connected the second cooler, for by the gas cooled after one section of pressurization of described compressor to two sections of entrance allowable temperatures of described compressor.
In addition, the present invention also provides a kind of regeneration gas circulation recovery method that utilizes described regeneration gas to loop back receiving apparatus, comprises the following steps:
Catalyst reaction when the described regeneration gas being flowed into by described regeneration gas feeding line is passed through the beds in described reactor and on described beds, described catalyst activity is improved, and reacted regeneration gas waste gas is exported from described reactor production end;
The regeneration gas waste gas of described reactor production end output enters described knockout drum after described heat exchanger heat exchange, and described knockout drum carries out after flash distillation described regeneration gas waste gas, and the described regeneration gas waste gas of gas phase is exported from described knockout drum top;
From the described regeneration gas waste gas of the gas phase of described knockout drum top output by described gas phase export pipeline and exported sub-pipeline and described the second gas phase by described the first gas phase and export sub-pipeline and be divided into two plumes, described the first gas phase is exported plume in sub-pipeline for the recovery that circulates, and the plume that described the second gas phase is exported in sub-pipeline is discharged into atmosphere or burned;
The plume that described the first gas phase is exported in sub-pipeline flows into described filter by described the 3rd valve, through described filter elimination part solid particle, and after described the first cooler is cooled to described suction port of compressor temperature required, remove liquid phase by described buffer, enter again described compressor compresses pressurization, after described check-valves and described the 4th valve, mix with the regeneration gas of newly entering in described regeneration gas feeding line;
The flow that described first flow transmitter is exported described the second gas phase the plume of sub-pipeline passes to described flow controller through described toxic emission controller, described second transmitter by enter described reactor described regeneration gas pass traffic give described flow controller, the ratio of key component in described regeneration gas waste gas in described regeneration gas waste gas passed to described flow controller by described gas discharging analyzer, the concentration value of the key component of the described regeneration gas that described flow controller needs according to default described reactor calculates, and according to the first valve group described in result of calculation control and by the switching degree of second valve group described in the control of described toxic emission controller, thereby the concentration value that ensures the key component of the described regeneration gas that enters described reactor is default concentration value.
Wherein, the ratio range of the key component in described regeneration gas waste gas and non-key component is 5%～100%.
Wherein, the described regeneration gas of newly entering is 0%～95% with the ratio of the described regeneration gas waste gas that circulation is reclaimed.
Compared with prior art, beneficial effect of the present invention is embodied in:
The device and method that regeneration gas provided by the invention circulation is reclaimed, the partial regeneration gas circulation in can realization response device inner catalyst regenerative process, thus reduce the regeneration gas flow that is discharged into down-stream system, save the energy; Meanwhile, in order to ensure total regeneration gas tolerance, remainder regeneration gas completes supplementing of fresh regenerated gas by controller, thereby control the concentration of regeneration gas key component, ensure the continued operation of regenerative process, reduced discharge, improved the circulation of inert gas and the utilization ratio of regeneration gas.
Brief description of the drawings
In order to be illustrated more clearly in the embodiment of the present invention or technical scheme of the prior art, to the accompanying drawing of required use in embodiment or description of the Prior Art be briefly described below, apparently, accompanying drawing in the following describes is only some embodiments of the present invention, for those of ordinary skill in the art, do not paying under the prerequisite of creative work, can also obtain according to these accompanying drawings other accompanying drawing.
Fig. 1 is that the regeneration gas of prior art is used and discharge schematic diagram;
Fig. 2 is the schematic diagram that the device that reclaims of the regeneration gas circulation of one embodiment of the invention and regeneration gas recycle.
Description of reference numerals: 101-reactor; 102-superheater; 103-heat exchanger; 104-knockout drum; 105-toxic emission pipeline; The normal feeding line of 106-; 107-regeneration gas feeding line; 108-reacts export pipeline; 109-second transmitter; 110-gas phase export pipeline; 111-the first gas phase is exported sub-pipeline; 112-the second gas phase is exported sub-pipeline; 201-second valve group; 202-first flow transmitter; 203-gas discharging analyzer; 206-the 3rd valve; 207-filter; 209-the first cooler; 210-surge tank; 215-compressor; 216-the second cooler; 221-the 5th valve; 222-the 3rd flow transmitter; 225-check-valves; 226-the 4th valve; 227-toxic emission controller; 228-flow controller; 232-regeneration gas feeding line; 234-the first valve group; 240-normal reaction product the first pipeline; 241-the 9th valve; 250-normal reaction product the second pipeline; 251-the 6th valve; 1051-the 7th valve; 1061-the 8th valve; 260-anti-surge by-pass line.
Detailed description of the invention
Below in conjunction with the accompanying drawing in the embodiment of the present invention, the technical scheme in the embodiment of the present invention is clearly and completely described, obviously, described embodiment is only the present invention's part embodiment, instead of whole embodiment.Based on the embodiment in the present invention, those of ordinary skill in the art, not paying the every other embodiment obtaining under creative work prerequisite, belong to the scope of protection of the invention.
Refer to Fig. 2, the schematic diagram that the device that the regeneration gas circulation that Fig. 2 is one embodiment of the invention is reclaimed and regeneration gas recycle.
As shown in Figure 2, when MTP device normally carries out preparing propylene from methanol reaction, the first valve group 234 is closed completely, the 8th valve 1061 is opened, methanol feedstock enters reactor 101 by normal feeding line 106, product enters reaction export pipeline 108 by reactor 101 bottoms, after heat exchanger 103 heat exchange that arrange on reaction export pipeline 108, enter knockout drum 104, now the 9th valve 241 and the 6th valve 251 are opened, the 7th valve 1051 cuts out, second valve group 201 and the 3rd valve 206 also should be closed, the product 1 of preparing propylene from methanol is exported from normal reaction product the second pipeline 250, product 2 is exported from normal reaction product the first pipeline 240.
The catalyst regeneration process that makes of prior art describes in detail in background technology, does not repeat them here, and what one embodiment of the invention was described below makes in catalyst regeneration process, how to recycle regeneration gas.
As shown in Figure 2, when catalyst regeneration, the first valve group 234 is opened, and the 8th valve 1061 cuts out, and the 9th valve 241, the 6th valve 251 and the 7th valve 1051 are all closed, and second valve group 201 and the 3rd valve 206 are opened.Regeneration gas is entered by regeneration gas feeding line 107, first through superheater, 102 heating reach after regeneration temperature, enter reactor 101 inlet ends, during by beds and catalyst reaction, there is variation in the component of reacted regeneration gas, referred to herein as regeneration gas waste gas, regeneration gas waste gas is discharged by reactor 101 bottoms, reclaim after heat through heat exchanger 103, separate by knockout drum 104, the regeneration gas waste gas of gas phase is exported from gas phase export pipeline 110.Because the 6th valve 251 and the 7th valve 1051 are all closed, second valve group 201 and the 3rd valve 206 are opened, regeneration gas waste gas in gas phase export pipeline 110 is split into two plumes and exports sub-pipeline 111 and the second gas phase is exported sub-pipeline 112 to the first gas phase, wherein, the plume that the first gas phase is exported in sub-pipeline 111 reclaims and re-uses for circulating, and the second gas phase is exported sub-pipeline 112 and is discharged into atmosphere or burned processing.
The plume that the first gas phase is exported in sub-pipeline 111 passes through the 3rd valve 206 inflow filters 207, wherein part solid particle of filter 207 eliminations, this plume is after the first cooler 209 is cooled to compressor 215 entrances temperature required afterwards, enter buffer 210 and remove liquid phase, enter again compressor 215 compression pressurizations from buffer 210 this plume out, after crossing check-valves 225 and the 4th valve 226, mix with the regeneration gas of newly entering in regeneration gas feeding line 107.Compressor 215 as required, comprises but is not limited to split-compressor.In one embodiment of the invention, compressor 215 is split-compressor, comprise two sections of one section of split-compressor and split-compressors, wherein between two sections of one section of this split-compressor and this compound compressors, be connected the second cooler 216, for by the gas cooled after one section of pressurization of described compressor to two sections of entrance allowable temperatures of described compressor.In another embodiment of the present invention, also comprise anti-surge by-pass line 260, the 3rd flowmeter 222 and the 5th valve 221, wherein, the 5th valve 221 is located on anti-surge by-pass line 260, one end of anti-surge by-pass line 260 is connected to the first gas phase and exports compressor 215 exits on sub-pipeline 111, the other end is connected to the first gas phase and exports between the filter 207 and the first cooler 209 on sub-pipeline 111, for preventing that compressor 215 from the normal work of surge impact occurring.Compressor 215 exits are also provided with the 3rd flowmeter 222, for detection of the flow of compressor 215, adjust valve 221 according to actual conditions, to ensure that compressor 215 normally works.
The second gas phase is exported and on sub-pipeline 112, is provided with successively gas discharging analyzer 203, first flow transmitter 202 and second valve group 201; Wherein, gas discharging analyzer 203 is for analyzing the concentration ratio of regeneration gas waste gas key component in regeneration gas waste gas, and first flow transmitter 202 gathers the second gas phase exports the flow of the plume of sub-pipeline 112.
The switching degree of the first valve group 234 and second valve group 201 is controlled respectively by regeneration gas feeding line 107 newly to enter regeneration gas and be discharged into atmosphere or the second burned gas phase is exported in sub-pipeline the flow of 112 plume.
As shown in Figure 2, toxic emission controller 227 is connected with first flow transmitter 202 and second valve group 201 signals, flow controller 228 and toxic emission controller 227, second transmitter 109, gas discharging analyzer 203 and the first valve group 234 signals connect, the flow that first flow transmitter 202 is exported the second gas phase the plume of sub-pipeline 112 passes to flow controller 228 through toxic emission controller 227, second transmitter 109 by the pass traffic of regeneration gas that enters reactor 101 to flow controller 228, the ratio of key component in regeneration gas waste gas in regeneration gas waste gas passed to flow controller 228 by gas discharging analyzer 203.When enforcement, flow controller 228 presets the concentration value of the key component of the regeneration gas that reactor 101 needs, and is preset with regeneration gas feeding line 107 and newly enters regeneration gas and export sub-pipeline 112 by the second gas phase to be discharged into atmosphere or the burned concentration ratio of regeneration gas waste gas plume and the mapping relations of the switching degree of the first valve group 234 and second valve group 201.Flow controller 228 is calculated as and reaches default, what the concentration value of the key component of the regeneration gas that reactor 101 needs was required newly enters regeneration gas and the concentration ratio of exporting sub-pipeline 112 by the second gas phase and be discharged into atmosphere or burned regeneration gas waste gas plume by regeneration gas feeding line 107, and according to this concentration ratio control first valve group 234 and the switching degree of controlling second valve group 201 by toxic emission controller 227 to regulate respectively regeneration gas feeding line 107 and the second gas phase to export the plume size of sub-pipeline 112, thereby the concentration value that ensures the key component of the regeneration gas that enters reactor 101 is default concentration value.In one embodiment of the invention, the requirement of the ratio range of the key component in regeneration gas waste gas and non-key component is 5%～100%.In another embodiment of the present invention, the regeneration gas of newly entering is 0%～95% with the ratio of the regeneration gas waste gas that circulation is reclaimed.
The form of the regeneration gas turnover reactor relating in above-mentioned steps, comprising top is inlet end, and bottom is production end, but does not limit to this kind of form, can be inlet end for bottom, and top is production end.
One of ordinary skill in the art will appreciate that: accompanying drawing is the schematic diagram of an embodiment, the module in accompanying drawing or flow process might not be that enforcement the present invention is necessary.
One of ordinary skill in the art will appreciate that: the module in the device in embodiment can be described and be distributed in the device of embodiment according to embodiment, also can carry out respective change and be arranged in the one or more devices that are different from the present embodiment.The module of above-described embodiment can be merged into a module, also can further split into multiple submodules.
Finally it should be noted that: above embodiment only, in order to technical scheme of the present invention to be described, is not intended to limit; Although the present invention is had been described in detail with reference to previous embodiment, those of ordinary skill in the art is to be understood that: its technical scheme that still can record previous embodiment is modified, or part technical characterictic is wherein equal to replacement; And these amendments or replacement do not make the essence of appropriate technical solution depart from the spirit and scope of embodiment of the present invention technical scheme.
Claims (6)
1. a regeneration gas loops back receiving apparatus, it is characterized in that, comprise that the first valve group, second valve group, filter, superheater, compressor, heat exchanger, surge tank, the first cooler, gas discharging analyzer, flow controller, first flow transmitter, toxic emission controller, second transmitter, reactor, knockout drum, regeneration gas feeding line, reaction export pipeline, gas phase export pipeline, the first gas phase are exported sub-pipeline, the second gas phase is exported sub-pipeline, the 3rd valve, check-valves, the 4th valve, wherein:
On described regeneration gas feeding line, be provided with successively described the first valve group, described superheater, described second transmitter, described regeneration gas feeding line is finally connected with described reactor inlet end; Catalyst reaction when the described regeneration gas being flowed into by described regeneration gas feeding line is passed through the beds in described reactor and on described beds, described catalyst activity is improved, and reacted regeneration gas waste gas is exported from described reactor production end;
Described reactor production end is connected with described knockout drum by described reaction export pipeline, and described reaction export pipeline is provided with described heat exchanger; The regeneration gas waste gas of described reactor production end output enters described knockout drum after described heat exchanger heat exchange, and described knockout drum carries out after flash distillation described regeneration gas waste gas, and the described regeneration gas waste gas of gas phase is exported from described knockout drum top;
Described gas phase export pipeline is connected with described knockout drum top, and described gas phase export pipeline is finally divided into that described the first gas phase is exported sub-pipeline and described the second gas phase is exported sub-pipeline; From the described regeneration gas waste gas of the gas phase of described knockout drum top output by described gas phase export pipeline and exported sub-pipeline and described the second gas phase by described the first gas phase and export sub-pipeline and be divided into two plumes, described the first gas phase is exported plume in sub-pipeline for the recovery that circulates, and the plume that described the second gas phase is exported in sub-pipeline is discharged into atmosphere or burned;
The switching degree of described the first valve group and described second valve group is controlled respectively by described regeneration gas feeding line newly to enter regeneration gas and be discharged into atmosphere or burned described the second gas phase is exported the flow of the plume in sub-pipeline;
Described the first gas phase is exported and on sub-pipeline, is provided with successively described the 3rd valve, described filter, described the first cooler, described surge tank, described compressor, described check-valves, described the 4th valve, and is finally connected between the above first valve group of described regeneration gas feeding line and described superheater and locates; The plume that described the first gas phase is exported in sub-pipeline flows into described filter by described the 3rd valve, through described filter elimination part solid particle, and after described the first cooler is cooled to described suction port of compressor temperature required, remove liquid phase by described buffer, enter again described compressor compresses pressurization, after described check-valves and described the 4th valve, mix with the regeneration gas of newly entering in described regeneration gas feeding line;
Described the second gas phase is exported and on sub-pipeline, is provided with successively described gas discharging analyzer, described first flow transmitter and described second valve group; Wherein, described gas discharging analyzer is for analyzing the concentration ratio of described regeneration gas waste gas key component in described regeneration gas waste gas, and described first flow transmitter gathers described the second gas phase exports the flow of the plume of sub-pipeline;
Described toxic emission controller is connected with described first flow transmitter and described second valve group signal, described flow controller and described toxic emission controller, described second transmitter, described gas discharging analyzer and described the first valve group signal connect, the flow that described first flow transmitter is exported described the second gas phase the plume of sub-pipeline passes to described flow controller through described toxic emission controller, described second transmitter by enter described reactor described regeneration gas pass traffic give described flow controller, the ratio of key component in described regeneration gas waste gas in described regeneration gas waste gas passed to described flow controller by described gas discharging analyzer, described flow controller is calculated as and reaches default, what the concentration value of the key component of the described regeneration gas that described reactor needs was required newly enters regeneration gas and the concentration ratio of exporting sub-pipeline by described the second gas phase and be discharged into atmosphere or burned described regeneration gas waste gas plume by described regeneration gas feeding line, and according to the first valve group described in the control of described concentration ratio and the switching degree by second valve group described in the control of described toxic emission controller to regulate respectively described regeneration gas feeding line and described the second gas phase to export the plume size of sub-pipeline, thereby the concentration value that ensures the key component of the described regeneration gas that enters described reactor is default concentration value.
2. regeneration gas according to claim 1 loops back receiving apparatus, it is characterized in that, also comprise anti-surge by-pass line, the 3rd flow transmitter and the 5th valve, wherein, described the 3rd flow transmitter and the 5th valve are located on described anti-surge by-pass line, described the 3rd flow transmitter is located at described first gas phase at described compressor outlet place and exports on sub-pipeline, for detection of the flow of described compressor; One end of described anti-surge by-pass line is connected to after described the first gas phase exports described the 3rd flow transmitter on sub-pipeline, the other end is connected to described the first gas phase and exports between the described filter and described the first cooler on sub-pipeline, for preventing described compressor surge.
3. regeneration gas according to claim 1 loops back receiving apparatus, it is characterized in that, described compressor is split-compressor, comprise two sections of one section of split-compressor and split-compressors, wherein between two sections of one section of this split-compressor and this split-compressors, be connected the second cooler, for by the gas cooled after one section of pressurization of described compressor to two sections of entrance allowable temperatures of described compressor.
4. utilize regeneration gas described in claim 1 to loop back a regeneration gas circulation recovery method for receiving apparatus, it is characterized in that, comprise the following steps:
Catalyst reaction when the described regeneration gas being flowed into by described regeneration gas feeding line is passed through the beds in described reactor and on described beds, described catalyst activity is improved, and reacted regeneration gas waste gas is exported from described reactor production end;
The regeneration gas waste gas of described reactor production end output enters described knockout drum after described heat exchanger heat exchange, and described knockout drum carries out after flash distillation described regeneration gas waste gas, and the described regeneration gas waste gas of gas phase is exported from described knockout drum top;
From the described regeneration gas waste gas of the gas phase of described knockout drum top output by described gas phase export pipeline and exported sub-pipeline and described the second gas phase by described the first gas phase and export sub-pipeline and be divided into two plumes, described the first gas phase is exported plume in sub-pipeline for the recovery that circulates, and the plume that described the second gas phase is exported in sub-pipeline is discharged into atmosphere or burned;
The plume that described the first gas phase is exported in sub-pipeline flows into described filter by described the 3rd valve, through described filter elimination part solid particle, and after described the first cooler is cooled to described suction port of compressor temperature required, remove liquid phase by described buffer, enter again described compressor compresses pressurization, after described check-valves and described the 4th valve, mix with the regeneration gas of newly entering in described regeneration gas feeding line;
The flow that described first flow transmitter is exported described the second gas phase the plume of sub-pipeline passes to described flow controller through described toxic emission controller, described second transmitter by enter described reactor described regeneration gas pass traffic give described flow controller, the ratio of key component in described regeneration gas waste gas in described regeneration gas waste gas passed to described flow controller by described gas discharging analyzer, the concentration value of the key component of the described regeneration gas that described flow controller needs according to default described reactor calculates, and according to the first valve group described in result of calculation control and by the switching degree of second valve group described in the control of described toxic emission controller, thereby the concentration value that ensures the key component of the described regeneration gas that enters described reactor is default concentration value.
5. regeneration gas circulation recovery method according to claim 4, is characterized in that, the key component in described regeneration gas waste gas and the ratio range of non-key component are 5%～100%.
6. regeneration gas circulation recovery method according to claim 4, is characterized in that, the described regeneration gas of newly entering is 0%～95% with the ratio of the described regeneration gas waste gas that circulation is reclaimed.
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| CN101035611A (en) * | 2004-12-10 | 2007-09-12 | 韦巴斯托股份公司 | Method for regenerating a reformer |
| US20100063337A1 (en) * | 2006-06-03 | 2010-03-11 | Lurgi Gmbh | Reactor for producing c2- to c8- olefins from a material flow containing oxygenate, water vapor and one or more hydrocarbons |
| CN103351272A (en) * | 2013-07-12 | 2013-10-16 | 黄河三角洲京博化工研究院有限公司 | MTP (Methanol to Propylene) and catalytic cracking combined technology and integrated unit |
| CN103611567A (en) * | 2013-12-04 | 2014-03-05 | 天津工业大学 | Regeneration method of methanol-to-olefin catalyst |
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2014
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101035611A (en) * | 2004-12-10 | 2007-09-12 | 韦巴斯托股份公司 | Method for regenerating a reformer |
| US20100063337A1 (en) * | 2006-06-03 | 2010-03-11 | Lurgi Gmbh | Reactor for producing c2- to c8- olefins from a material flow containing oxygenate, water vapor and one or more hydrocarbons |
| CN103351272A (en) * | 2013-07-12 | 2013-10-16 | 黄河三角洲京博化工研究院有限公司 | MTP (Methanol to Propylene) and catalytic cracking combined technology and integrated unit |
| CN103611567A (en) * | 2013-12-04 | 2014-03-05 | 天津工业大学 | Regeneration method of methanol-to-olefin catalyst |
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