CN110410761A - Waste heat recycles vaporization method processed - Google Patents
Waste heat recycles vaporization method processed Download PDFInfo
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- CN110410761A CN110410761A CN201910720087.2A CN201910720087A CN110410761A CN 110410761 A CN110410761 A CN 110410761A CN 201910720087 A CN201910720087 A CN 201910720087A CN 110410761 A CN110410761 A CN 110410761A
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- heat
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B1/00—Methods of steam generation characterised by form of heating method
- F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
- F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B30/00—Heat pumps
- F25B30/06—Heat pumps characterised by the source of low potential heat
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- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
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- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
The technical issues of waste heat of the invention recycles vaporization method processed, is related to coal chemical industry field of energy-saving technology, and discharge product heat cannot be efficiently used by solving the process for making of the prior art.Method includes the following steps: S1: the discharge product after methanol synthesizing process is delivered to evaporative component；S2: evaporative component absorbs the heat of discharge product, and processes to the heat, and the fluid in the evaporative component is caused to realize phase change transition.Function of the present invention to improve methanol synthesizing process meets the needs of people are to methanol synthesizing process system energy recycling and reusing.
Description
Technical field
The invention belongs to coal chemical industry field of energy-saving technology, in particular to a kind of waste heat recycles vaporization method processed.
Background technique
Methanol is important basic chemical industry raw material, and demand is being continuously increased, and can be made by coal or natural gas, modern
Technology section realizes the production scale of 10,000 tons up to a hundred, and nowadays, methanol synthesizing process is more and more paid attention to.Methanol closes
At in the process, the product gas come out from reactor contains a large amount of sensible heats and latent heat, sufficiently, economic this partial heat of recycling, is
One importance of device production.China's methanol synthesizing process typically directly uses 70-110 DEG C of product gas of heat at present
The cooling mode of air cooler, does not recycle this partial heat.
The inventors discovered that at least there is following technological deficiency in the prior art:
Manufacturing process in the prior art, is only to meet the needs of production technology, the discharge product in technical process
Temperature directlys adopt air cooler to being discharged after discharge product cooling, not to the partial heat up to 70-110 DEG C in the prior art
It is utilized, wastes mass energy.
In view of this, the present invention is specifically proposed.
Summary of the invention
In view of this, it is an object of the invention to overcome the deficiencies of the prior art and provide a kind of remaining heat recovery steam-making sides
Method overcomes the process for making of the prior art that cannot efficiently use the technical issues of product heat is discharged.The invention has
Many beneficial effects, narration as detailed below.
The technical solution adopted by the present invention to solve the technical problems is: a kind of waste heat recycling vaporization method processed is used for first
Alcohol synthesis technology, comprising the following steps:
S1: the discharge product after methanol synthesizing process is delivered to evaporative component；
S2: evaporative component absorbs the heat of discharge product, and processes to the heat, causes the stream in the evaporative component
Body realizes phase change transition.
In a preferred or optional scheme, the fluid phase change convert the step of are as follows:
A1: discharge product is cooled down through cooling device；
A2: by cooling device with the fluid conveying after the discharge product heat exchange to heating device, filled as heating
Set the driving heat of work.
In a preferred or optional scheme, cooling step in A1 are as follows:
B1: discharge product is delivered to heat exchanger and carries out the first cooling procedure；
B2: the first discharge product conveying heat taking and exchanging device after cooling carries out the second cooling procedure, takes hot heat exchange for described
Fluid conveying in device is to heating device；
B3: the second discharge product conveying water cooler after cooling completes third cooling procedure.
In a preferred or optional scheme, the heating device is two class heat pumps；
By the fluid conveying in the heat taking and exchanging device to the two classes heat pump, the two classes heat pump work is driven, and
The two classes heat pump is evaporated the liquid in pump, realizes the phase transformation by liquid to gas.
In a preferred or optional scheme, the two classes heat pump internal water system system is closed circle water system.
In a preferred or optional scheme, the water in the closed circle water system is desalted water.
In a preferred or optional scheme, the pressure of the heat taking and exchanging device is 6.0-8.0MPaA, the heat exchanger
85-110 DEG C of gas inlet temperature, 70-95 DEG C of temperature of the heat exchanger gas outlet.
The pipeline that product is delivered to the evaporative component of liquid is discharged in a preferred or optional scheme, in S1, it is in parallel
The pipeline of second heat taking and exchanging device is installed all the way.
In a preferred or optional scheme, the discharge product mixtures, mole composition: H2O < 1%, H2<
75%, CO < 10%, CO2< 2%, N2< 2%, Ar < 3%, CH4For < 1%, CH3OH < 10%.
The beneficial effects of the present invention are: the discharge product after methanol synthesizing process is sent to evaporative component, by evaporative component
Discharge product is utilized, the heat in discharge product is absorbed by evaporative component, and the heat by absorbing prepares steam,
Realize the phase change transition of liquid in evaporative component, the use as industrial other purposes, methanol-fueled CLC work in solution technology
The technical issues of wasting thermal energy is discharged after being directly over air cooler in skill discharge product, and energy recovery recycles, and realizes modern industry
Energy-saving target.
Detailed description of the invention
In order to more clearly explain the embodiment of the invention or the technical proposal in the existing technology, to embodiment or will show below
There is the required attached drawing used in technical description to be briefly described, it should be apparent that, the accompanying drawings in the following description is only this hair
Bright some embodiments for those of ordinary skill in the art without creative efforts, can be with root
Other attached drawings are obtained according to these attached drawings.
Fig. 1 is the structural schematic diagram that waste heat of the invention recycles vaporization method processed；
Wherein, in figure: 1. reactors；2. heat exchanger；3. heat taking and exchanging device；4. water cooler；5. two class heat pumps；6. enclosed is followed
Ring water system.
Specific embodiment
To make the purpose of the present invention, technical solution and advantage are clearer, will carry out below to technical solution of the present invention
Detailed description.Obviously, described embodiment is only invention a part of the embodiment, rather than comprehensive embodiment.It is based on
The embodiment of the present invention, those of ordinary skill in the art are obtained every other without making creative work
Embodiment belongs to the range that the present invention is protected.
Methanol is important Organic chemical products, and the production technology and domestic development of methanol are existing closely related, and methanol is one
Transparent, colourless, inflammable, the toxic liquid of kind, slightly alcohol smell, fusing point -97.8 are spent, and 64.8 degree of boiling point, 12.22 degree of flash-point,
470 degree of self-ignition point, relative density 0.7915, lower explosive limit 6%, the upper limit 36.5% can be with water, ethyl alcohol, ether, benzene, third
Ketone and most of organic solvents are miscible.It is important Organic Chemicals and high-grade fuel.Mainly for the manufacture of formaldehyde, vinegar
One of a variety of organic products such as acid, chloromethanes, first ammonia, dimethyl sulfate and pesticide, the important source material of medicine, it is prior
Be: also alternative to gasoline makees fuel use to methanol, and still, in the process of putting into production, there is still a need for energy conservation and energy recovery, this case skills
Scheme provided by art scheme is being utilized for energy recovery.
Waste heat as shown in Figure 1 recycles vaporization method processed, is used for methanol synthesizing process, comprising the following steps:
S1: the discharge product after methanol synthesizing process is delivered to evaporative component.Discharge product after methanol synthesizing process
The characteristics of be that pollution is small, impurity is few and thermal energy is high feature, it is therefore, general, discharge product is fed directly to evaporation group
Part, evaporative component, for example, thermal energy component or two class heat pump components, belong to the prior art, details are not described herein.
S2: evaporative component absorbs the heat of discharge product, and processes to heat, and the fluid in evaporative component is caused to realize phase
Become conversion.The thermal energy of product is discharged, is evaporated component and is utilized, to prepare steam, as used in other process flows, for example,
Heating.The characteristics of embodiment, resource recycling.
As optional embodiment, in thermal energy component the step of fluid phase change conversion are as follows:
A1: discharge product is cooled down through cooling device, the purpose for doing cooling treatment is: meeting the temperature of follow-up equipment
It is required that temperature is not excessively high easy to operate, equipment damage is avoided.Cooling device, for example, heat exchanger 2, e.g., shell-and-tube heat exchanger.
Product is discharged after heat exchanger 2, mole composition: H2O < 1%, H2< 75%, CO < 10%, CO2< 2%, N2< 2%,
Ar < 3%, CH4For < 1%, CH3OH < 10%, 85-110 DEG C of temperature, pressure 6.0-8.0MPaA.
A2: by cooling device with discharge product heat exchange after fluid conveying to heating device, as heating device work
The driving heat of work.
Further, step cooling in A1 are as follows:
B1: discharge product is delivered to heat exchanger and carries out the first cooling procedure；85-110 DEG C of temperature, pressure 6.0-8.0MPaA；
B2: the first discharge product conveying heat taking and exchanging device after cooling carries out the second cooling procedure, will be in heat taking and exchanging device
Fluid conveying to heating device.Heat taking and exchanging device makes heat be transmitted to cold fluid from hot fluid, is wanted with meeting defined technique
The device asked is a kind of industrial application of convective heat transfer and heat transfer.Dividing wall type, hybrid, storage can be divided by its operating process
Hot type (or back-heating type) three categories, this case mostly use the heat taking and exchanging device of dividing wall type, and effect is to make hot and cold two fluid by solid
Wall surface separates, and does not mix, and the exchange of heat is carried out by partition, being mixed into for impurity is effectively reduced, product will further be discharged
Temperature is cooled to 70-95 DEG C, meets the temperature requirement of follow-up equipment.
At this point, 65-85 DEG C of the hot water taking inlet temperature of heat taking and exchanging device 3, the aqueous solution in heat taking and exchanging device 3 is discharged production
After reaching 85-105 DEG C after object heating, to use it for anything else, for example, heating is used.
B3: the second discharge product conveying water cooler after cooling completes third cooling procedure, can be discharged, be discharged after the completion
Product drains into atmosphere after cooling down three times, greatly reduces pollution of the discharge product to environment.
Further, heating device is two class heat pumps 5.Two class heat pumps, as, second-kind absorption-type heat pump utilizes low product
Position heat source, realizes the circulatory system for pumping heat from low-temperature heat source to high temperature heat source, with energy saving, protection environment double
Recast is used, and the heat of low-temperature heat source is transferred to high-temperature medium using the two classes heat pump, can be realized the recycling of cryogenic energy.
Fluid in heat taking and exchanging device 3, for example, anaerobic water, is delivered to two class heat pumps 5 for the anaerobic water that temperature is 85-105 DEG C, drives
The work of two class heat pumps 5, and two class heat pumps 5 are evaporated the liquid in heat pump, realize the phase transformation by liquid to gas.Two classes
The preferable closed circle water system of heat pump 5, the water in closed circle water system is desalted water, and desalted water is to be easy to remove by contained
Strong electrolyte remove or be reduced to a degree of water, remaining salt content should avoid salts substances between 1~5 mg/litre
Loss to equipment improves service life of equipment.Two class heat pumps use deaerated water, 70-150 DEG C of deaerated water inlet temperature, pressure
0.15-0.65MPaA, the saturated vapor after two class heat pumps under the same pressure of output, water temperature on the recirculated water of two class heat pumps
30-35 DEG C of degree, 35-45 DEG C of recirculated water return water temperature.
The pipeline that product is delivered to the evaporative component of liquid is discharged as optional embodiment, in S1, parallel connection is pacified all the way
Pipeline equipped with the second heat taking and exchanging device.The effect of the structure, the using and the reserved, under special circumstances, for example, the maintenance of pipeline
When, by the way of traditional, it will be expelled directly out after discharge product neck cooling, as described in Figure 1.
Embodiment one:
1800000 tons/year of ammonia from coal projects, after heat exchanger 2, pressure is the outlet discharge product of reactor 1
7.34MPaA, temperature are 100.6 DEG C, and gas phase fraction is 97.76%, and product tolerance is discharged are as follows: 83979.34kmol/h, mole
Composition: H2O < 1%, H2< 75%, CO < 10%, CO2< 2%, N2< 2%, Ar < 3%, CH4For < 1%, CH3OH <
10%, such as H2O is 0.38%, H2For 68.92%, CO 5.3%, CO2For 1.32%, N2For 16.56%, Ar 2.45%,
CH4For 0.03%, CH3OH is 5.04%.After being cooled to 85 DEG C by heat taking and exchanging device 3,40 DEG C of rows are cooled to by water cooler 4
Out.3 hot water taking of heat taking and exchanging device is increased to 95 DEG C by 80 DEG C, hot water taking water 1255.6t/h.Hot water taking enters two class heat pumps 5
The saturated vapor 10.31t/h of 90 DEG C of deaerated water production pressure 0.4MPaG of heating, excess heat is by 32 DEG C of upper water, 37 DEG C of return water, stream
The recirculated water of amount 2600.72t/h is taken away.
The scheme of the prior art:
1800000 tons/year of ammonia from coal projects, after inlet outlet heat exchanger, pressure is the exported product gas of reactor 1
7.34MPaA, temperature are 100.6 DEG C, and gas phase fraction is 97.76%, and product tolerance is 83979.34kmol/h, mole composition:
H2O is 0.38%, H2For 68.92%, CO 5.3%, CO2For 1.32%, N2For 16.56%, Ar 2.45%, CH4For
0.03%, CH3OH is 5.04%, is discharged after being cooled to 40 DEG C by air cooler and water cooler, empty calory recycling.
Data comparison:
The saturated vapor 10.31t/h that can be made device negative pressure pressure 0.4MPaG using the method for the present invention, is recovered energy about
24487.68MJ/h。
MJ is million joules, and 1kwh=3600000 joules, the energy regenerating of 24487.68MJ/h can be used for multiple techniques
Process greatlys save electric energy.
Upper described, the only specific embodiment of the invention, but the protection scope of innovation and creation is not limited to
This, anyone skilled in the art can readily occur in variation or replace in the technical scope that innovation and creation disclose
It changes, should be covered by the protection scope of the present invention.Therefore, the protection scope of the invention should be with appended claims
Subject to protection scope.
Claims (10)
1. a kind of waste heat recycles vaporization method processed, it to be used for methanol synthesizing process, which comprises the following steps:
S1: the discharge product after methanol synthesizing process is delivered to evaporative component；
S2: evaporative component absorbs the heat of discharge product, and processes to the heat, causes the fluid in the evaporative component real
Existing phase change transition.
2. the method according to claim 1, wherein the step of fluid phase change is converted are as follows:
A1: discharge product is cooled down through cooling device；
A2: by cooling device with it is described discharge product heat exchange after fluid conveying to heating device, as heating device work
The driving heat of work.
3. according to the method described in claim 2, it is characterized in that, step cooling in A1 are as follows:
B1: discharge product is delivered to heat exchanger and carries out the first cooling procedure；
B2: the first discharge product conveying heat taking and exchanging device after cooling carries out the second cooling procedure, will be in the heat taking and exchanging device
Fluid conveying to heating device；
B3: the second discharge product conveying water cooler after cooling completes third cooling procedure.
4. according to the method described in claim 2, it is characterized in that, the heating device is two class heat pumps；
By the fluid conveying in the heat taking and exchanging device to the two classes heat pump, the two classes heat pump work is driven, and described
Two class heat pumps are evaporated the liquid solution in pump, realize the phase transformation by liquid to gas.
5. according to the method described in claim 4, it is characterized in that, two classes heat pump internal water system system is closed cycle water system
System.
6. according to the method described in claim 4, it is characterized in that, the heat of low-temperature heat source is shifted using the two classes heat pump
To high-temperature medium, the recycling of cryogenic energy can be realized.
7. according to the method described in claim 4, it is characterized in that, being recycled 30-35 DEG C of coolant-temperature gage on the recirculated water of two class heat pumps
35-45 DEG C of water return water temperature.
8. according to the method described in claim 4, it is characterized in that, the pressure of the heat taking and exchanging device is 6.0-8.0MPaA, institute
85-110 DEG C of inlet temperature of heat exchanger gas is stated, 70-95 DEG C of temperature of the heat exchanger gas outlet.
9. the method according to claim 1, wherein the pipe that product is delivered to the evaporative component of liquid is discharged in S1
Road, parallel connection are equipped with the pipeline of the second heat taking and exchanging device all the way.
10. the method according to claim 1, wherein the discharge product mixtures mole form: H2O < 1%,
H2< 75%, CO < 10%, CO2< 2%, N2< 2%, Ar < 3%, CH4For < 1%, CH3OH < 10%.
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| CN201910720087.2A CN110410761A (en) | 2019-08-06 | 2019-08-06 | Waste heat recycles vaporization method processed |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1056089A (en) * | 1991-05-25 | 1991-11-13 | 北京化工学院 | Utilize heat pump to reclaim the method for conversion process waste heat |
| WO2011142414A1 (en) * | 2010-05-14 | 2011-11-17 | 三浦工業株式会社 | Heat pump steam generating device |
| CN202928202U (en) * | 2012-11-22 | 2013-05-08 | 大连葆光节能空调设备厂 | Waste heat recovery type distributed energy and urban trunk sewage source heat pump coupling system |
| KR101593826B1 (en) * | 2014-09-24 | 2016-02-15 | 현대중공업 주식회사 | Combined cycle power generation system |
| CN206488677U (en) * | 2017-02-23 | 2017-09-12 | 内蒙古炬能热能技术有限责任公司 | Aluminium cell low temperature exhaust heat recycling system |
-
2019
- 2019-08-06 CN CN201910720087.2A patent/CN110410761A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1056089A (en) * | 1991-05-25 | 1991-11-13 | 北京化工学院 | Utilize heat pump to reclaim the method for conversion process waste heat |
| WO2011142414A1 (en) * | 2010-05-14 | 2011-11-17 | 三浦工業株式会社 | Heat pump steam generating device |
| CN202928202U (en) * | 2012-11-22 | 2013-05-08 | 大连葆光节能空调设备厂 | Waste heat recovery type distributed energy and urban trunk sewage source heat pump coupling system |
| KR101593826B1 (en) * | 2014-09-24 | 2016-02-15 | 현대중공업 주식회사 | Combined cycle power generation system |
| CN206488677U (en) * | 2017-02-23 | 2017-09-12 | 内蒙古炬能热能技术有限责任公司 | Aluminium cell low temperature exhaust heat recycling system |
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Application publication date: 20191105 |