CN208814667U - A kind of de- hydrocarbon device of carbon dioxide catalysis oxidation - Google Patents
A kind of de- hydrocarbon device of carbon dioxide catalysis oxidation Download PDFInfo
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- CN208814667U CN208814667U CN201821132905.4U CN201821132905U CN208814667U CN 208814667 U CN208814667 U CN 208814667U CN 201821132905 U CN201821132905 U CN 201821132905U CN 208814667 U CN208814667 U CN 208814667U
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- preheater
- hydrocarbon
- pipeline
- carbon dioxide
- gas
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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
- Y02P20/10—Process efficiency
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Abstract
The utility model provides a kind of de- hydrocarbon device of carbon dioxide catalysis oxidation, including compressor, cooler, separator, first preheater, second preheater, circulating fan, heater, de- hydrocarbon reactor, the compressor, cooler, separator, first preheater, circulating fan, second preheater, heater, de- hydrocarbon reactor is sequentially connected according to unstripped gas circulating direction, the compressor also passes through pipeline and connect with the first preheater, the utility model makes the room temperature pipeline of script be warming up to 110 DEG C with the heat of compression by carbon-dioxide gas compressor bypass line, take full advantage of original energy, by warm-up time and heat energy saving 20%；In addition, the older system of energy consumption reduces 90% when preheating whole system by circulating fan preheating, warm-up time can be made to save 30%；And it is adequately protected catalyst when shutting down cooling using the cooling displacement moisture of dry carbon dioxide, has substantially prolonged catalyst service life, reach save the cost, energy-saving purpose.
Description
Technical field
The utility model relates to a kind of chemical equipment technical field, especially a kind of carbon dioxide catalysis oxidation takes off hydrocarbon dress
It sets.
Background technique
Carbon dioxide catalysis oxidation de-hydrocarbon system is the important component of carbon dioxide recovering apparatus, using hydro carbons in height
Hydrocarbon reaction is fallen to be used for carbon dioxide gas purification by the characteristics of can reacting with oxygen under warm catalyst action.
Currently, carbon dioxide catalysis oxidation take off hydrocarbon use room temperature unstrpped gas, initially enter preheater and reaction gas into
After row heat exchange, enter electric furnace later and heat, enters de- hydrocarbon reactor later and reacted, the gas after reaction returns to preheating
Room temperature is cooled to through water cooler after device recycling heat and goes out catalytic oxidation system after separator separates free water.
Original system is heated to 350 DEG C of reaction temperature or more by room temperature and needs more than 24 hour time, too fast heating speed
Not only waste of energy also results in thermal stress and excessively concentrates and damage equipment.The entire carbon dioxide system in this heating time section
System is in high energy consumption operating status always, but can not produce qualified food-grade carbon-dioxide, and carbon dioxide system is caused to open
Dynamic cost is very high.And in equipment downtime, in unstripped gas, remaining moisture will lead to catalyst softening, and long-time service can make to be catalyzed
The easy dusting of agent.
Summary of the invention
In view of the deficiencies of the prior art, the utility model provides a kind of de- hydrocarbon device of carbon dioxide catalysis oxidation, solves to add
Catalyst softens problem when high energy consumption runs and shuts down in thermal process.
The technical solution of the utility model are as follows: a kind of de- hydrocarbon device of carbon dioxide catalysis oxidation, including compressor, cooling
Device, separator, the first preheater, the second preheater, circulating fan, heater, de- hydrocarbon reactor, the compressor pass through pipe
Road is connect with cooler, and the cooler is connect by pipeline with separator, and the separator is pre- by pipeline and first
First air inlet of hot device connects；
The compressor also passes through pipeline and connect with the first air inlet of the first preheater, first preheater
First gas outlet is connect by pipeline with the first air inlet of the second preheater, wherein the temperature of compressor output gas is 110
DEG C, the unstripped gas temperature of first the first gas outlet of preheater output is 200 DEG C；
Be additionally provided with circulating fan between first preheater and the second preheater, the circulating fan import with
Second gas outlet of the second preheater connects, and the air outlet of the circulating fan is connect with the first air inlet of the second preheater,
Internal system circulation is realized by circulating fan, to be further reduced device preheating time；
First gas outlet of second preheater is connected by the air inlet of pipeline and heater, and the heater goes out
Port is connect by pipeline with the air inlet of de- hydrocarbon reactor, is placed with de- hydrocarbon catalyst in the de- hydrocarbon reactor, wherein
The temperature of the unstripped gas of the first gas outlet output of second preheater is 350 DEG C, the gas outlet output of the heater
The temperature of unstripped gas is 380-400 DEG C；
The gas outlet of the de- hydrocarbon reactor is connect by pipeline with the second air inlet of the second preheater, and described second is pre-
Second gas outlet of hot device is connect by pipeline with the second air inlet of the first preheater, the second air inlet of first preheater
Mouth is also connected by pipeline with carbon dioxide storage tank, and the unstripped gas after de- hydrocarbon passes through after the second preheater and the first preheater
Output channel output, wherein the temperature of the gas after the de- hydrocarbon of the gas outlet output of the de- hydrocarbon reactor is 500 DEG C, the
The temperature of gas after the de- hydrocarbon of the second gas outlet output of two preheaters is 300 DEG C, and the second gas outlet of the first preheater is defeated
The temperature of the gas after de- hydrocarbon out is 150-200 DEG C.
Further, check valve a is provided on the pipeline between the compressor and cooler.
Further, check valve b is provided on the pipeline between the compressor and the first air inlet of the first preheater
With check valve c.
Further, check valve d is provided on the pipeline between the separator and the first air inlet of the first preheater
With check valve e.
Further, it is additionally provided on the pipeline between the second air inlet and carbon dioxide storage tank of first preheater
Check valve f.
Further, the first preheater lower end is additionally provided with blow valve, when shutdown, by opening blow valve, and
Open check valve f, so that dry carbon dioxide is shut down after device moisture is replaced into dry gas.
Further, check valve g is additionally provided on the output channel.
Further, the de- hydrocarbon reactor lower end is provided with blowdown valve.
When carbon takes off hydrocarbon, it is first shut off check valve e, check valve f and check valve g, and opens the first preheater, the second preheating
Device, heater, circulating fan, de- hydrocarbon reactor, it is pre- to the first preheater, the second preheater, de- hydrocarbon reactor by heater
Heat, and circulation in system is realized by circulating fan, preheating time is further decreased, after the completion of preheating, open check valve b, list
To valve c, check valve e, the unstripped gas for being mixed with certain oxygen is entered in compressor by admission line, after compressor compresses,
The temperature of unstripped gas is 110 DEG C, and then compressed unstripped gas is directly inputted into first through check valve b, check valve c, check valve e
Preheater is tentatively preheated, so that unstripped gas is preheated to 200 DEG C, subsequently into carrying out being preheated to 350 in the second preheater
DEG C, it subsequently into being heated to 380-400 DEG C in heater, is finally delivered in de- hydrocarbon reactor and reacts, after the reaction was completed, pass through
The gas outlet of de- hydrocarbon reactor lower end, which inputs the gas after de- hydrocarbon in the second preheater and the first preheater, to be cooled down, and is passed through
Second preheater and the first preheater recycle extra heat, are then exported the gas after de- hydrocarbon by output channel, reaction
After stopping, by open check valve f and blow valve, the drying carbon dioxide in carbon dioxide storage tank is input in system,
So that dry carbon dioxide is shut down after the moisture in system is replaced into dry gas.
The utility model has the following beneficial effects: compressing the room temperature pipeline of script by the bypass line of compressor end
Heat is warming up to 110 DEG C, takes full advantage of original energy, by warm-up time and heats energy saving 20%；
In addition, the older system of energy consumption reduces 90% when preheating whole system by circulating fan preheating, can make to heat
Saving of time 30%, and greatly reduce system preparation time；
Also, it is adequately protected catalyst, has been greatly prolonged using the cooling displacement moisture of dry carbon dioxide when shutting down cooling
Catalyst service life, reaches save the cost, energy-saving purpose.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of the utility model；
In figure, 1- compressor, 2- cooler, 3- separator, the first preheater of 4-, the second preheater of 5-, 6- circulating fan,
7- heater, 8- take off hydrocarbon reactor, 9- carbon dioxide storage tank, and 10- check valve a, 11- check valve b, 12- check valve c, 13- is unidirectional
Valve d, 14- check valve e, 15- check valve f, 16- blow valve.
Specific embodiment
Specific embodiment of the present utility model is described further with reference to the accompanying drawing:
As shown in Figure 1, a kind of carbon dioxide catalysis oxidation takes off hydrocarbon device, including compressor 1, cooler 2, separator 3, the
One preheater 4, the second preheater 5, circulating fan 6, heater 7, de- hydrocarbon reactor 8, the compressor 1 by pipeline with it is cold
But device 2 connects, and is provided with check valve a10 on the pipeline；
The cooler 2 is connect by pipeline with separator 3, and the separator 3 passes through pipeline and the first preheater 4
The connection of the first air inlet, be provided with check valve d13 and check valve e14 on the pipeline；
The compressor 1 is also connect by pipeline with the first air inlet of the first preheater 4, is additionally provided on the pipeline
Check valve b11 and check valve c12；
First gas outlet of first preheater 4 is connect by pipeline with the first air inlet of the second preheater 5,
In, the temperature of 1 output gas of compressor is 110 DEG C, and the unstripped gas temperature of the first gas outlet output of the first preheater 4 is 200
℃；
Be additionally provided with circulating fan 6 between first preheater 4 and the second preheater 5, the circulating fan 6 into
Mouth is connect with the second gas outlet of the second preheater 5, the first air inlet of the air outlet of the circulating fan 6 and the second preheater 5
Mouth connection realizes internal system circulation by circulating fan 6, to be further reduced the preheating time of device；
First gas outlet of second preheater 5 is connect by pipeline with the air inlet of heater 7, the heater 7
Gas outlet connect with the air inlet of de- hydrocarbon reactor 8 by pipeline, de- hydrocarbon is placed in the de- hydrocarbon reactor 8 and is catalyzed
Agent, wherein the temperature of the unstripped gas of the first gas outlet output of second preheater 5 is 350 DEG C, and the heater 7 goes out
The temperature of the unstripped gas of port output is 380-400 DEG C；
The gas outlet of the de- hydrocarbon reactor 8 is connect by pipeline with the second air inlet of the second preheater 5, and described second
Second gas outlet of preheater 5 is connect by pipeline with the second air inlet of the first preheater 5, and the of first preheater 5
Two air inlets also pass through pipeline and are connected with carbon dioxide storage tank 9, and check valve f15 is additionally provided on the pipeline；
Unstripped gas after de- hydrocarbon is exported after the second preheater 5 and the first preheater 4 by output channel, wherein described
De- hydrocarbon reactor 8 gas outlet output de- hydrocarbon after gas temperature be 500 DEG C, the second gas outlet of the second preheater 5
The temperature of gas after the de- hydrocarbon of output is 300 DEG C, the temperature of the gas after the de- hydrocarbon of the second gas outlet output of the first preheater 4
Degree is 150-200 DEG C.
Further, 4 lower end of the first preheater is additionally provided with blow valve 16, when shutdown, passes through and opens blow valve
16, and open check valve f15, so that dry carbon dioxide is shut down after device moisture is replaced into dry gas.
Further, check valve g is additionally provided on the output channel.
Further, 8 lower end of de- hydrocarbon reactor is provided with blowdown valve.
When carbon takes off hydrocarbon, it is first shut off check valve e14, check valve f15 and check valve g, and open the first preheater 4, second
Preheater 5, heater 7, circulating fan 6, de- hydrocarbon reactor 8 are given the first preheater 4 by heater 7, the second preheater 5, are taken off
Hydrocarbon reactor 8 preheats, and realizes circulation in system by circulating fan 6, further decreases preheating time, after the completion of preheating, opens
Check valve b11, check valve c12, check valve e14 are opened, the unstripped gas for being mixed with certain oxygen is entered into compressor 1 by admission line
In, after the compression of compressor 1, the temperature of unstripped gas is 110 DEG C, and then compressed unstripped gas is through check valve b11, check valve
C12, check valve e14 are directly inputted into the first preheater 4 and are tentatively preheated, so that unstripped gas is preheated to 200 DEG C, then into
Enter and carry out being preheated to 350 DEG C in the second preheater 5, subsequently into being heated to 380-400 DEG C in heater 7, is finally delivered to de-
It is reacted in hydrocarbon reactor 8, it is after the reaction was completed, by the gas outlet for taking off 8 lower end of hydrocarbon reactor that the gas after 500 DEG C of de- hydrocarbon is defeated
Enter and cooled down in the second preheater 5 and the first preheater 4, extra heat is recycled by the second preheater 5 and the first preheater 4
Then gas after de- hydrocarbon is exported by output channel, after reaction stops, passing through open check valve f15 and blow valve by amount
16, the drying carbon dioxide in carbon dioxide storage tank 9 is input in system, so that drying carbon dioxide for the moisture in system
It is shut down after being replaced into dry gas.
The description of the embodiments and the specification only illustrate the principle of the present utility model and most preferred embodiment, is not taking off
Under the premise of from the spirit and scope of the utility model, the utility model also has various changes and improvements, these changes and improvements
It falls within the scope of the claimed invention.
Claims (8)
1. a kind of carbon dioxide catalysis oxidation takes off hydrocarbon device, including compressor, cooler, separator, the first preheater, second are in advance
Hot device, circulating fan, heater, de- hydrocarbon reactor, the compressor are connect by pipeline with cooler, the cooler
It is connect by pipeline with separator, the separator is connect by pipeline with the first air inlet of the first preheater；
It is connect it is characterized by: the compressor also passes through pipeline with the first air inlet of the first preheater, described first
First gas outlet of preheater is connect by pipeline with the first air inlet of the second preheater, wherein compressor output gas
Temperature is 110 DEG C, and the unstripped gas temperature of first the first gas outlet of preheater output is 200 DEG C；
Circulating fan, the circulating fan import and second are additionally provided between first preheater and the second preheater
Second gas outlet of preheater connects, and the air outlet of the circulating fan connect with the first air inlet of the second preheater, passes through
Circulating fan realizes internal system circulation；
First gas outlet of second preheater is connected by the air inlet of pipeline and heater, the gas outlet of the heater
It is connect by pipeline with the air inlet of de- hydrocarbon reactor, is placed with de- hydrocarbon catalyst in the de- hydrocarbon reactor, wherein described
The temperature of the unstripped gas of the first gas outlet output of second preheater is 350 DEG C, the raw material of the gas outlet output of the heater
The temperature of gas is 380-400 DEG C；
The gas outlet of the de- hydrocarbon reactor is connect by pipeline with the second air inlet of the second preheater, second preheater
The second gas outlet connect with the second air inlet of the first preheater by pipeline, the second air inlet of first preheater is also
It is connected by pipeline with carbon dioxide storage tank, the unstripped gas after de- hydrocarbon passes through output after the second preheater and the first preheater
Pipeline output, wherein the temperature of the gas after the de- hydrocarbon of the gas outlet output of the de- hydrocarbon reactor is 500 DEG C, and second is pre-
The temperature of gas after the de- hydrocarbon of the second gas outlet output of hot device is 300 DEG C, the second gas outlet output of the first preheater
The temperature of gas after de- hydrocarbon is 150-200 DEG C.
2. a kind of carbon dioxide catalysis oxidation according to claim 1 takes off hydrocarbon device, it is characterised in that: the compressor with
Check valve a is provided on pipeline between cooler.
3. a kind of carbon dioxide catalysis oxidation according to claim 1 takes off hydrocarbon device, it is characterised in that: the compressor with
Check valve b and check valve c are provided on pipeline between first air inlet of the first preheater.
4. a kind of carbon dioxide catalysis oxidation according to claim 1 takes off hydrocarbon device, it is characterised in that: the separator with
Check valve d and check valve e are provided on pipeline between first air inlet of the first preheater.
5. a kind of carbon dioxide catalysis oxidation according to claim 1 takes off hydrocarbon device, it is characterised in that: first preheating
Check valve f is additionally provided on pipeline between the second air inlet and carbon dioxide storage tank of device.
6. a kind of carbon dioxide catalysis oxidation according to claim 1 takes off hydrocarbon device, it is characterised in that: described first is pre-
Hot device lower end is additionally provided with blow valve, when shutdown, by opening blow valve and check valve f, so that dry carbon dioxide will
Device moisture is shut down after being replaced into dry gas.
7. a kind of carbon dioxide catalysis oxidation according to claim 1 takes off hydrocarbon device, it is characterised in that: the efferent duct
Check valve g is additionally provided on road.
8. a kind of carbon dioxide catalysis oxidation according to claim 1 takes off hydrocarbon device, it is characterised in that: the de- hydrocarbon is anti-
Device lower end is answered to be provided with blowdown valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821132905.4U CN208814667U (en) | 2018-07-17 | 2018-07-17 | A kind of de- hydrocarbon device of carbon dioxide catalysis oxidation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821132905.4U CN208814667U (en) | 2018-07-17 | 2018-07-17 | A kind of de- hydrocarbon device of carbon dioxide catalysis oxidation |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN208814667U true CN208814667U (en) | 2019-05-03 |
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ID=66270957
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201821132905.4U Active CN208814667U (en) | 2018-07-17 | 2018-07-17 | A kind of de- hydrocarbon device of carbon dioxide catalysis oxidation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN208814667U (en) |
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2018
- 2018-07-17 CN CN201821132905.4U patent/CN208814667U/en active Active
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