CN107758616A - A kind of heat exchange of energy-conserving and environment-protective and condenser system - Google Patents
A kind of heat exchange of energy-conserving and environment-protective and condenser system Download PDFInfo
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- CN107758616A CN107758616A CN201610664030.1A CN201610664030A CN107758616A CN 107758616 A CN107758616 A CN 107758616A CN 201610664030 A CN201610664030 A CN 201610664030A CN 107758616 A CN107758616 A CN 107758616A
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- 239000007788 liquid Substances 0.000 claims abstract description 74
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 42
- 239000002994 raw material Substances 0.000 claims abstract description 26
- 238000005516 engineering process Methods 0.000 claims abstract description 14
- 239000006200 vaporizer Substances 0.000 claims abstract description 6
- 239000000463 material Substances 0.000 claims description 26
- 238000006243 chemical reaction Methods 0.000 claims description 22
- 230000008016 vaporization Effects 0.000 claims description 15
- 238000001816 cooling Methods 0.000 claims description 13
- 238000009834 vaporization Methods 0.000 claims description 9
- 230000008676 import Effects 0.000 claims 7
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims 3
- 235000011941 Tilia x europaea Nutrition 0.000 claims 3
- 239000004571 lime Substances 0.000 claims 3
- 239000007789 gas Substances 0.000 abstract description 37
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 abstract description 17
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 16
- 239000001257 hydrogen Substances 0.000 abstract description 16
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 14
- 238000012546 transfer Methods 0.000 abstract description 8
- 238000004519 manufacturing process Methods 0.000 abstract description 6
- 238000011084 recovery Methods 0.000 abstract description 4
- 239000000126 substance Substances 0.000 abstract description 4
- 230000007613 environmental effect Effects 0.000 abstract description 3
- 238000010438 heat treatment Methods 0.000 abstract description 3
- -1 converter Substances 0.000 abstract description 2
- 238000000354 decomposition reaction Methods 0.000 abstract description 2
- 239000012530 fluid Substances 0.000 abstract description 2
- 238000000926 separation method Methods 0.000 abstract description 2
- 239000000498 cooling water Substances 0.000 description 12
- 238000000034 method Methods 0.000 description 7
- 239000012071 phase Substances 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- 239000002826 coolant Substances 0.000 description 3
- 238000005984 hydrogenation reaction Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 238000005868 electrolysis reaction Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- 230000005514 two-phase flow Effects 0.000 description 2
- 238000003723 Smelting Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- PYKYMHQGRFAEBM-UHFFFAOYSA-N anthraquinone Natural products CCC(=O)c1c(O)c2C(=O)C3C(C=CC=C3O)C(=O)c2cc1CC(=O)OC PYKYMHQGRFAEBM-UHFFFAOYSA-N 0.000 description 1
- 150000004056 anthraquinones Chemical class 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000112 cooling gas Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 239000010931 gold Substances 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000011835 investigation Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- ULSIYEODSMZIPX-UHFFFAOYSA-N phenylethanolamine Chemical compound NCC(O)C1=CC=CC=C1 ULSIYEODSMZIPX-UHFFFAOYSA-N 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
-
- 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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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Health & Medical Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
A kind of heat exchange of energy-conserving and environment-protective and condenser system, belong to power-saving technology and environmental protection equipment field, be related to gas converting heat technology, suitable for there are all condenser systems caused by condensate liquid, suitable for all chemical industries, especially methanol decomposition hydrogen manufacturing industry.The present invention is formed by connecting by equipment such as raw material flow container, preheater, heat exchanger, vaporizer, converter, water cooler and Liquid level adjusting valves by pipeline, the system is by changing gas inlet and outlet direction and improving fluid passage, the separation of gas and condensate liquid is realized well, improve the coefficient of heat transfer, reduce the heating load of whole system, reduce circulation water consumption, reduce heat exchange area, utility is reclaimed, it is incomplete to solve heat recovery in Chemical Manufacture, the problem of energy expenditure is excessive, the purpose of energy-conserving and environment-protective is reached.
Description
Technical field
This project belongs to power-saving technology and environmental protection equipment field, belongs to energy-conserving and environment-protective technology and product, is related to gas converting heat
Technology, suitable for there is all condenser systems caused by condensate liquid, suitable for all chemical industries, especially methanol decomposition hydrogen manufacturing row
Industry.
Background technology
From the point of view of present circumstances, China's water resource and the energy are all at full stretch, and energy-conservation is known as water, coal, oil, natural
" the 5th energy " outside gas, and the energy waste phenomenon being related at present in all kinds of chemical industry engineerings and equipment is extremely serious,
Energy recovery is incomplete, and cooling water demand is big, and cooling water is directly discharged with water can cause thermal pollution, economy and the wasting of resources,
Save water and energy turns into urgent problem.
The main function of heat exchange and condenser system is to reclaim the heat in hot fluid, while the medium for needing to cool down is obtained
Cooling.The heat energy of GOOD TASTE will be reclaimed wherein heat energy by the cold medium with needing to heat in usual heat source gas, low product
Position thermal source is then that cooling agent takes away heat by water or air, realizes the cooling of heat source gas.
Heat exchanger is the big and various in style product of an amount, and the investigation to external condenser system market shows, shell-and-tube
Condenser system market still accounts for 64%.Although the competitiveness of various board-like condenser systems is rising, shell-and-tube condenser system bears height
There is great advantage in terms of pressure and High Pressure Difference, leading position will be occupied.
Hydrogen industrially has extensive purposes.In recent years, due to fine chemistry industry, anthraquinone producing hydrogen peroxide, powder smelting
Gold, oil hydrogenation, forestry product and agriculture product hydrogenation, bioengineering, petroleum refining hydrogenation and hydrogen fuel cleaning vehicle etc. it is rapid
Development, rapidly increases pure hydrogen demand.To not facilitating the area of hydrogen source, if used traditional with petroleum-type, natural gas
Or coal be raw material gas making come separating and preparing hydrogen need it is huge investment-- " equivalent to half synthesis ammonia ", be only applicable to large-scale consumer.
Hydrogen can be conveniently made in middle-size and small-size user's electrolysis water, but energy consumption is very big, and every cubic metre of hydrogen power consumption reaches 6 degree, and hydrogen is pure
Spend undesirable, impurity is more, while scale is also restrained, therefore many originals are carried out one after another with the producer of water electrolysis hydrogen production in recent years
Technological transformation, use the new process route of preparing hydrogen by methanol vapour transformation instead.
Nowadays, schizolysis hydrogen production plant with methanol is widely used, and its basic skills is：First alcohol and water is mixed according to a certain percentage
Close, after being pressurizeed with pump, exchanged heat through heat exchanger, then enter converter after vaporizing, being superheated to the temperature needed for reaction, turning
Change in device in the presence of catalyst, methanol resolves into hydrogen, carbon monoxide first, and carbon monoxide generates hydrogen with steam reaction again
Gas, carbon dioxide etc. convert gas, and conversion gas carries in heat exchanger with entering after condensed device cools down again after material benzenemethanol, water heat exchange
Pure process carries out purification processes；In the flow, about 230 DEG C or so of the conversion temperature degree reflected, in heat exchanger with original
Material first alcohol and water carries out after heat exchange cooling that condensed device is cooled to less than 40 DEG C by recirculated cooling water again, is converting air cooling process
In, gas phase water vapour is constantly condensed out, and is formed biphase gas and liquid flow with gas, is influenceed condenser thermal transfer coefficient, temperature is not easy
Lower, when typically entering condenser, convert the temperature of gas at 130 DEG C or so, and required heat exchange area is big, cost of investment
Height, heat recovery is not ideal enough, and required cooling water amount is big.
The content of the invention
The defects of present invention exists for above-mentioned background technology provides heat exchange and the condenser system of a kind of energy-conserving and environment-protective, should
System establishes new technological process, realization is changed by changing original heat exchange and the number of devices and device structure of condenser system
Gas-liquid separation in hot systems, the heat transfer coefficient of medium is improved, thermal source is entered into the medium temperature of water cooling system as far as possible
Ground will be low, maximumlly reclaims heat therein, reduces the heating load of vaporization superheater, reduces the cooling water of water cooling system
Dosage, total heat exchange area of whole system is reduced, save equipment investment.
To reach this purpose, the invention discloses a kind of heat exchange of energy-conserving and environment-protective and condenser system, it is by passing through pipeline
The equipment such as connected raw material flow container, preheater, heat exchanger, vaporizer, converter, water cooler and Liquid level adjusting valve form.
Material liquid is entered preheater shell side after buffered, inhaled in preheater by out-of-bounds entering raw material flow container by pipeline
Receive conversion gas heat to be preheated, enter back into after heat exchanger shell pass carries out second of heat exchange with conversion gas and enter vaporization overheat
Device, cracked being vaporized and being superheated to needed for reaction in vaporizing superheater into converter after temperature and conversion reaction,
The conversion gas of high temperature is generated, reaction cracking needs to absorb heat, and conversion reaction can discharge heat, vaporize needed for superheater and converter
Heat is by out-of-bounds heat supply；Conversion gas is exchanged heat into heat exchanger tube pass after being come out from converter with material liquid, cooling, now
The generation of partial condensation liquid is had, two phase flow is produced to avoid gas from being mixed with condensate liquid, heat transfer efficiency is influenceed, in heat exchanger tube pass
The port of export shunts to gas-liquid, and condensate liquid is drawn through into Liquid level adjusting valve from exchanger base returns to raw material flow container, by it
The unreacted material and heat carried all directly returns to raw material flow container, is no longer participate in the cooling of next step, gas is then from heat exchange
Go out to enter preheater tube side at the top of device, exchanged heat again with material liquid, the condensate liquid being now condensed out from gas phase is again
The secondary Liquid level adjusting valve that is drawn through returns to raw material flow container, and gas enters water cooler shell side after preheater Base top contact, until
Go out system to out-of-bounds after being cooled to normal temperature, now temperature difference is big, and a large amount of unreacted material liquids are condensed, directly from shell side
Liquid level adjusting valve is discharged to below and returns to raw material flow container, and the condensate liquid drawn from preheater, heat exchanger and water cooler passes through；Water
Cooling medium is recirculated cooling water or chilled brine.
In summary, the system has following characteristics：
In preheater, heat exchanger and water cooler, gas is discharged from heat exchanger top exit, and condensate liquid is from exchanger base
Discharge, gas phase and liquid phase shunting are realized, gas-liquid two-phase is avoided the formation of, improves the coefficient of heat transfer, enhance exchange capability of heat.
Condensate liquid is no longer participate in cooling procedure below, passes through pipeline after preheater, heat exchanger, water cooler, bottom discharge
Raw material flow container is directly returned, heat has directly been taken back to material liquid system, has reclaimed condensate heat.
Condensate liquid returns to raw material flow container by pipeline, directly reclaimed after preheater, heat exchanger, water cooler, bottom discharge
Unreacted material, realizes the zero-emission of condensate liquid, has good environmental protection effect.
Water cooler walks tube side using cooling water, and gas phase walks the mode of shell side, in time by condensate liquid from heat exchanger shell pass bottom
Discharge, improve heat transfer coefficient.
One air chamber is set at the top of heat exchanger, there are enough vaporization spaces after being raised so as to material liquid temperature.
Condensate liquid is to a Liquid level adjusting valve is mounted with the pipeline of raw material flow container, to convert gas when ensureing and being arranged outside condensate liquid
It will not discharge.
Brief description of the drawings
Figure of description Fig. 1 is the flow chart of patent of the present invention, and 1 enters raw material flow container for out-of-bounds material liquid in figure（101）Pipe
Road, 2 be connection raw material flow container（101）With preheater（102）Pipeline, 3 for connection preheater（102）With heat exchanger（103）'s
Material liquid pipeline, 4 be connection heat exchanger（103）With vaporizer（104）Material liquid pipeline, 5 for connection vaporizer（104）With turning
Change device（105）Unstrpped gas pipeline, 6 be connection converter and heat exchanger（103）Conversion feed channel, 7 for connection heat exchanger
（103）With preheater（102）Conversion feed channel, 8 for connection preheater（102）With water cooler（106）Conversion feed channel, 9
To export to the conversion feed channel outside battery limit (BL) from water cooler, 10 be heat exchanger（103）To the condensate liquid pipeline of Liquid level adjusting valve, 11
For preheater（102）It is water cooler to the condensate liquid pipeline of Liquid level adjusting valve, 12（106）To the condensate line of Liquid level adjusting valve
Road, 13 be into the heat conducting oil pipe for vaporizing superheater, and 14 is vaporize superheater to the heat conducting oil pipe of converter, and 15 be converter
The heat conducting oil pipe of outlet, 16 be the recirculated cooling water inlet channel of water cooler, and 17 be the circulating cooling water outlet pipe of water cooler
Road.
Embodiment
For the feature of patent of the present invention, technological means and the specific purposes reached, function can be further appreciated that, with reference to attached
Patent of the present invention is described in further detail with embodiment for figure.
Accompanying drawing 1 is referred to, the device is the heat recovery and utilization and conversion gas of a set of 6000Nm3/h hydrogen production units by carbinol
Cooling system, the operating pressure are 1.8MPa, and material liquid is by first alcohol and water each 50%（w/w）Composition, water is excessive, vaporization temperature
Spend for 170 DEG C.
The device is by the raw material flow container that is connected by pipeline（101）, preheater（102）, heat exchanger（103）, vaporizer
（104）, converter（105）, water cooler（106）And Liquid level adjusting valve V1 is formed, the connection between each part is all connected using pipeline,
Its technical process is as follows：
Material liquid from the external world passes through pipeline（1）Into raw material flow container（101）After buffering, pass through pipeline（2）Into preheater
（102）Shell side, in preheater（102）In with conversion gas carry out heat exchange carry out tentatively preheat after pass through pipeline（3）Into heat exchange
Device（103）After shell side carries out second of heat exchange heating with conversion gas, then pass through pipeline（4）Into vaporization superheater（104）,
In vaporization superheater（104）In be vaporized and be superheated to needed for reaction and pass through pipeline after temperature（5）Into converter（105）Enter
Row cracking and conversion reaction, the conversion gas of high temperature is generated, convert gas from converter（105）Through pipeline after out（6）Into heat exchange
Device（103）Tube side is exchanged heat with material liquid, cooling, the generation of partial condensation liquid is now had, to avoid gas from being mixed with condensate liquid
Close and produce two phase flow, heat transfer efficiency is influenceed, in heat exchanger（103）The tube side port of export shunts to gas-liquid, by condensate liquid from changing
Hot device bottom is drawn through pipeline（10）And Liquid level adjusting valve（V1）Raw material flow container (101) is returned to, what is carried is unreacted
Material and heat all directly return to raw material flow container（101）, the cooling of next step is no longer participate in, gas is then from heat exchanger（103）Top
Go out to pass through pipeline in portion（8）Into preheater（102）Tube side, exchanged heat with material liquid, be now condensed from gas phase again
The condensate liquid gone out passes through pipeline（11）It is drawn through Liquid level adjusting valve and returns to raw material flow container（101）, gas is from preheater（102）Top
Portion is drawn through pipeline（9）Into water cooler（106）Shell side, pass through pipeline after being cooled to normal temperature（9）Discharge system is to boundary
Outside, now temperature difference is big, and a large amount of unreacted material liquids are condensed, directly from water cooler（106）Shell side is below by pipe
Road（12）And Liquid level adjusting valve（V1）Return to raw material flow container (101), water cooler（106）Cooling medium be recirculated cooling water；
In this technological process, the heat required for vaporizing superheater and converter is supplied by the conduction oil out-of-bounds to come.
After heat exchange and condenser system by a kind of energy-conserving and environment-protective of patent of the present invention, experimental data is ideal, main body
Present the following aspects：
Conversion gas enters water cooler（106）Temperature fall below less than 80 DEG C, and conventional heat transfer systems can only drop to 110 DEG C.
Heat required for material liquid vaporization is 2,410,000 kilocalories, and the heat required for the vaporization of conventional system material liquid is
2660000 kilocalories.
Total heat exchange area is 338 ㎡, and conventional condenser heat exchange area is up to 520 ㎡.
24.7 tons of cooling water amount of condenser, and routine consumes cooling water up to 38 tons.
Example described above only expresses a kind of embodiment of patent of the present invention, and its description is more specific and detailed, but
Therefore the limitation to the scope of the claims of the present invention can not be interpreted as.It should be pointed out that the ordinary skill people for this area
For member, on the premise of inventional idea of the present invention is not departed from, various modifications and improvements can be made, these belong to this hair
The protection domain of bright patent.Therefore, the protection domain of patent of the present invention should be determined by the appended claims.
Claims (8)
1. heat exchange and the condenser system of a kind of energy-conserving and environment-protective, including raw material flow container, preheater, heat exchanger, vaporizer, converter,
The equipment such as water cooler and Liquid level adjusting valve, feed conduit（1）With raw material flow container（101）Import is connected；Raw material flow container（101）Outlet
Pass through pipeline（2）With preheater（102）Material liquid import is connected；Preheater（102）Material liquid exports and heat exchanger（103）It is former
Liquor inlet passes through pipeline（3）It is connected；Heat exchanger（103）Material liquid outlet passes through pipeline（4）With vaporizing superheater（104）Material
Entrance point is connected；Vaporize superheater（104）Material vaporization brings out mouth and passes through pipeline（5）With converter（105）Import is connected, conversion
Device（105）Outlet passes through pipeline（6）With heat exchanger（103）The import of hot side end is connected, heat exchanger（103）Hot side brings out mouth and passes through pipe
Road（7）With preheater（102）The import of hot side end is connected, preheater（102）The hot side end port of export passes through pipeline（8）With water cooler
（106）Hot side import end is connected, from water cooler（106）Hot side brings out mouth and passes through pipeline（9）Reacting gas after cooling is conveyed
To out-of-bounds；Heat exchanger（103）Tube side condensate liquid outlet passes through pipeline（10）With Liquid level adjusting valve（V1）It is connected；Preheater
（102）Tube side condensate liquid outlet passes through pipeline（11）With Liquid level adjusting valve（V1）It is connected；Water cooler（106）Shell side condensate liquid is arranged
Outlet passes through pipeline（12）With Liquid level adjusting valve（V1）It is connected；Liquid level adjusting valve（V1）Liquid import is returned by pipeline and raw material flow container
It is connected；Conduction oil passes through pipeline（13）With vaporizing superheater（104）Heat conductive oil inlet end connects；Vaporize superheater（104）Heat conduction
Oil export passes through pipeline（14）With converter（105）Heat conductive oil inlet end is connected, converter（105）Conduction oil outlet end passes through pipe
Road（15）By conduction oil conveying output out-of-bounds.
2. according to the heat exchange new technology of the energy-conserving and environment-protective described in claim 1, it is characterised in that：Heat exchanger（103）Tube side gas
Discharged respectively from the different mouths of pipe from condensate liquid, gas is discharged from heat exchanger top, and condensate liquid is from heat exchanger（103）Discharge bottom.
3. according to the heat exchange new technology of the energy-conserving and environment-protective described in claim 1, it is characterised in that：Preheater（102）Tube side gas
Discharged respectively from the different mouths of pipe from condensate liquid, gas is discharged from preheater top, and condensate liquid is from preheater（102）Discharge bottom.
4. according to the heat exchange new technology of the energy-conserving and environment-protective described in claim 1, it is characterised in that：Water cooler（106）Middle circulation is cold
But water walks tube side, and shell side is made in conversion leave with rage.
5. according to the heat exchange new technology of the energy-conserving and environment-protective described in claim 1, it is characterised in that：Heat exchanger（103）That discharges is cold
Lime set passes through Liquid level adjusting valve（V1）It is discharged into raw material flow container（101）.
6. according to the heat exchange new technology of the energy-conserving and environment-protective described in claim 1, it is characterised in that：Preheater（102）That discharges is cold
Lime set passes through Liquid level adjusting valve（V1）It is discharged into raw material flow container（101）.
7. according to the heat exchange new technology of the energy-conserving and environment-protective described in claim 1, it is characterised in that：Water cooler（106）That discharges is cold
Lime set passes through Liquid level adjusting valve（V1）It is discharged into raw material flow container（101）.
8. according to the heat exchange new technology of the energy-conserving and environment-protective described in claim 1, it is characterised in that：Heat exchanger（103）Top is set
One steam chest.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610664030.1A CN107758616A (en) | 2016-08-15 | 2016-08-15 | A kind of heat exchange of energy-conserving and environment-protective and condenser system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610664030.1A CN107758616A (en) | 2016-08-15 | 2016-08-15 | A kind of heat exchange of energy-conserving and environment-protective and condenser system |
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| Publication Number | Publication Date |
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| CN107758616A true CN107758616A (en) | 2018-03-06 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201610664030.1A Pending CN107758616A (en) | 2016-08-15 | 2016-08-15 | A kind of heat exchange of energy-conserving and environment-protective and condenser system |
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103910329A (en) * | 2013-12-30 | 2014-07-09 | 成都科特瑞兴科技有限公司 | High-efficiency energy-saving heat exchange novel technology |
| RU144911U1 (en) * | 2014-03-11 | 2014-09-10 | Федеральное государственное бюджетное образовательное учреждение высшего профессионального образования "Казанский государственный энергетический университет" (ФГБОУ ВПО "КГЭУ") | HEAT ELECTRIC STATION |
| CN104555922A (en) * | 2015-01-23 | 2015-04-29 | 成都科特瑞兴科技有限公司 | New technology for producing hydrogen by conversion of methyl alcohol and water vapor |
| CN105037109A (en) * | 2015-08-11 | 2015-11-11 | 鹤壁宝发能源科技股份有限公司 | Mid temperature-low temperature cascaded dimethyl ether production method |
| CN105517682A (en) * | 2013-09-06 | 2016-04-20 | 株式会社大赛璐 | Method and plant for using recompressed vapor |
| CN105713113A (en) * | 2014-12-05 | 2016-06-29 | 中国石油天然气股份有限公司 | Method for recovering heat of gas-phase material in condensation kettle |
| CN206069360U (en) * | 2016-08-15 | 2017-04-05 | 成都科特瑞兴科技有限公司 | A kind of heat exchange of energy-conserving and environment-protective and condenser system |
-
2016
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Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105517682A (en) * | 2013-09-06 | 2016-04-20 | 株式会社大赛璐 | Method and plant for using recompressed vapor |
| CN103910329A (en) * | 2013-12-30 | 2014-07-09 | 成都科特瑞兴科技有限公司 | High-efficiency energy-saving heat exchange novel technology |
| RU144911U1 (en) * | 2014-03-11 | 2014-09-10 | Федеральное государственное бюджетное образовательное учреждение высшего профессионального образования "Казанский государственный энергетический университет" (ФГБОУ ВПО "КГЭУ") | HEAT ELECTRIC STATION |
| CN105713113A (en) * | 2014-12-05 | 2016-06-29 | 中国石油天然气股份有限公司 | Method for recovering heat of gas-phase material in condensation kettle |
| CN104555922A (en) * | 2015-01-23 | 2015-04-29 | 成都科特瑞兴科技有限公司 | New technology for producing hydrogen by conversion of methyl alcohol and water vapor |
| CN105037109A (en) * | 2015-08-11 | 2015-11-11 | 鹤壁宝发能源科技股份有限公司 | Mid temperature-low temperature cascaded dimethyl ether production method |
| CN206069360U (en) * | 2016-08-15 | 2017-04-05 | 成都科特瑞兴科技有限公司 | A kind of heat exchange of energy-conserving and environment-protective and condenser system |
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