CN104529820B - Energy-recuperation system and recovery method for the process for production of acrylonitrile section of feeding intake - Google Patents
Energy-recuperation system and recovery method for the process for production of acrylonitrile section of feeding intake Download PDFInfo
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- CN104529820B CN104529820B CN201410795928.3A CN201410795928A CN104529820B CN 104529820 B CN104529820 B CN 104529820B CN 201410795928 A CN201410795928 A CN 201410795928A CN 104529820 B CN104529820 B CN 104529820B
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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
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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
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Abstract
The invention discloses a kind of energy-recuperation system for the process for production of acrylonitrile section of feeding intake and recovery method, system includes: storage tank, the first working medium pump, condenser/evaporator, raw material working medium decompressor, superheater, reactor, the second working medium pump, expansion valve, vaporizer, generator, ejector and cycle fluid decompressor；Storage tank, the first working medium pump, condenser/evaporator, raw material working medium decompressor, superheater and described reactor are sequentially connected with；The injection entrance of the liquid-phase outlet of condenser/evaporator, the second working medium pump, expansion valve, vaporizer and ejector is sequentially connected with；The gas phase entrance of the second working medium pump, generator, ejector and condenser/evaporator is sequentially connected with；The gas phase entrance of generator, cycle fluid decompressor and condenser/evaporator is sequentially connected with.This system can overcome the shortcoming causing liquid material working medium cold energy and pressure to waste in the prior art process for production of acrylonitrile section of feeding intake.
Description
Technical field
The energy regenerating that the present invention relates to propylene ammmoxidation process production acrylonitrile process utilizes field, relates to especially
And a kind of energy-recuperation system for the process for production of acrylonitrile section of feeding intake and recovery method.
Background technology
Acrylonitrile is a kind of important industrial chemicals, has in fields such as synthetic fibers, synthetic rubber, plastics
Wide application prospect.
The production method of acrylonitrile has: 2-chloroethyl alcohol-sodium cyanide method, acetylene method, propylene ammmoxidation process.Propylene
The advantages such as it is cheap and easily-available that ammonia oxidation has raw material, and production cost is low, and production technology is simple, the current world
On acrylonitrile process more than 95% use propylene ammmoxidation process.
Current domestic process for production of acrylonitrile all use propylene ammmoxidation process, propylene liguid and liquefied ammonia respectively from
The spherical tank of raw material tank field after vaporization, enters superheater in working medium pump sends into propylene vaporizer and ammonia evaporator
After being superheated to about 66 DEG C, send into fluidized-bed reactor.
But the subject matter that this technological process exists is: it is anti-that raw material working medium enters in fluidized-bed reactor
Answering pressure relatively low, and the condition of storage of propylene liguid and liquefied ammonia is normal temperature high voltage, raw material working medium is through working medium
Pump pressure also can raise, and liquefied ammonia and propylene liguid vaporescence in vaporizer are reduction vaporization, this
Process can cause liquid material working medium cold energy and the waste of pressure energy.
The information being disclosed in this background section is merely intended to increase the reason of the general background to the present invention
Solve, and be not construed as recognizing or imply in any form that this information structure is for this area general technology
Prior art well known to personnel.
Summary of the invention
It is an object of the invention to provide a kind of energy regenerating system for the process for production of acrylonitrile section of feeding intake
System, thus overcome the shortcoming causing liquid material working medium cold energy and pressure to waste in prior art.
For achieving the above object, the invention provides a kind of energy for the process for production of acrylonitrile section of feeding intake
Recovery system, including: storage tank, the first working medium pump, condenser/evaporator, raw material working medium decompressor, overheated
Device, reactor, the second working medium pump, expansion valve, vaporizer, generator, ejector and cycle fluid
Decompressor；Described storage tank, described first working medium pump, described condenser/evaporator, described raw material working medium expand
Machine, described superheater and described reactor are sequentially connected with；The liquid-phase outlet of described condenser/evaporator, institute
The injection entrance stating the second working medium pump, described expansion valve, described vaporizer and described ejector connects successively
Connect；Described second working medium pump, described generator, described ejector and the gas phase of described condenser/evaporator
Entrance is sequentially connected with；Described generator, described cycle fluid decompressor and the gas of described condenser/evaporator
Phase entrance is sequentially connected with.
In technique scheme, described storage tank is spherical tank.
In technique scheme, described raw material working medium decompressor is scroll expander or screw expander.
In technique scheme, described reactor is fluidized-bed reactor.
In technique scheme, described expansion valve is electric expansion valve or heating power expansion valve.
In technique scheme, described cycle fluid decompressor is scroll expander or screw expander.
In technique scheme, described ejector is gas-gas ejector.
Another object of the present invention is to provide a kind of recovery method using above-mentioned energy-recuperation system, from
And overcome the shortcoming causing liquid material working medium cold energy and pressure to waste in prior art.
For achieving the above object, the invention provides a kind of recovery method using above-mentioned energy-recuperation system,
Comprise the following steps: 11) liquid material working medium from described storage tank through described first working medium pump send into described cold
Solidifying vaporizer vaporization forms gaseous feed working medium；12) described gaseous feed working medium is at described condenser/evaporator
The acting of described raw material working medium expander is entered after level pressure evaporation；13) the described gaseous feed after acting
Working medium enters the described superheater described reactor of overheated rear entrance and reacts.
It is still another object of the present invention to provide a kind of recovery method using above-mentioned energy-recuperation system, from
And overcome the shortcoming causing liquid material working medium cold energy and pressure to waste in prior art.
For achieving the above object, the invention provides a kind of recovery method using above-mentioned energy-recuperation system,
Comprising the following steps: 21) liquid circulation working medium enters described second work the most afterwards from described condenser/evaporator
Matter pump；22) being divided into two-way from described second working medium pump liquid circulation working medium out, a road is through described swollen
Enter the vaporization heat absorption of described vaporizer after swollen valve reducing pressure by regulating flow, form the first gaseous recycle working medium after heat absorption also
Entering described ejector as ejection gas to be compressed, another road enters the vaporization formation second of described generator
Gaseous recycle working medium；33) it is divided into two-way from described generator described second gaseous recycle working medium out,
One tunnel enters the compression of described ejector as pressurized working fluid and from the ejection gas of described vaporizer and mixes
Closing, another road enters the acting of described cycle fluid expander；34) through described ejector with described follow
Gaseous recycle working medium after ring working medium decompressor returns to described condenser/evaporator and is condensed into liquid.
Compared with prior art, there is advantages that
1, the present invention changes traditional decompression evaporator into condenser/evaporator, adds a set of cold energy and reclaims system
System (mainly includes generator, ejector, cycle fluid decompressor, the second working medium pump, expansion valve, steaming
Send out device), can fully recycle the cold energy of raw material working medium compared with conventional process flow, be used for freezing, with
Time cycle fluid decompressor reclaim mechanical energy can be used in acting generating.
2, compared with being evaporated under reduced pressure in decompression evaporator with conventional process flow, the present invention is at condensation evaporation
Level pressure evaporation in device, the available loss of energy is little.
3, compared with conventional process flow, the present invention adds raw material working medium after condenser/evaporator and expands
Machine, the pressure energy of recoverable raw material working medium, improves energy regenerating utilization rate further.
Accompanying drawing explanation
Fig. 1 is the structural representation of the energy-recuperation system according to the present invention.
Fig. 2 is the method flow diagram reclaiming raw material power pressure energy according to the present invention.
Fig. 3 is the method flow diagram reclaiming raw material working medium cold energy according to the present invention.
Fig. 4 is the T-S figure of the raw material working medium according to the present invention.
Fig. 5 is according to the T-S figure of cycle fluid in the first embodiment of the present invention.
Fig. 6 is the T-S figure of middle according to the second embodiment of the present invention cycle fluid.
T in Fig. 4-60Refer to ambient temperature.
Main Reference Numerals illustrates:
1-storage tank, 2-the first working medium pump, 3-condenser/evaporator, 4-raw material working medium decompressor, 5-superheater,
6-reactor, 7-the second working medium pump, 8-expansion valve, 9-vaporizer, 10-generator, 11-ejector, 12-
Cycle fluid decompressor, 13-thermal source, 14-low-temperature receiver.
Detailed description of the invention
Below in conjunction with the accompanying drawings, the detailed description of the invention of the present invention is described in detail, it is to be understood that this
The protection domain of invention is not limited by detailed description of the invention.
Explicitly indicate that unless otherwise other, otherwise in entire disclosure and claims, term " bag
Include " or its conversion as " comprising " or " including " etc. will be understood to comprise stated element or
Ingredient, and do not get rid of other elements or other ingredients.
As it is shown in figure 1, feed intake for process for production of acrylonitrile according to the one of the specific embodiment of the invention
The energy-recuperation system of section, including: storage tank the 1, first working medium pump 2, condenser/evaporator 3, raw material working medium
Decompressor 4, superheater 5, reactor the 6, second working medium pump 7, expansion valve 8, vaporizer 9, generator
10, ejector 11 and cycle fluid decompressor 12；Storage tank the 1, first working medium pump 2, condenser/evaporator
3, raw material working medium decompressor 4, superheater 5 and reactor 6 are sequentially connected with；The liquid of condenser/evaporator 3
The injection entrance of outlet, the second working medium pump 7, expansion valve 12, vaporizer 9 and ejector 11 is successively mutually
Connect；The gas phase entrance of the second working medium pump 7, generator 10, ejector 11 and condenser/evaporator 3 depends on
Secondary connection；The gas phase entrance of generator 10, cycle fluid decompressor 12 and condenser/evaporator 3 connects successively
Connect.
In this embodiment, storage tank 1 is spherical tank, for storing liquid raw material working medium, it is preferred to use for often
Temperature pressure reservoir.First working medium pump 2 is for boosting the liquid material working medium being stored in storage tank and send into
Condenser/evaporator.Condenser/evaporator 3 for make to vaporize from the liquid material working medium of storage tank and liquefy from
Ejector and the gaseous recycle working medium in decompressor.Raw material working medium decompressor 4 is scroll expander or screw rod
Decompressor, for reclaiming the pressure energy of gaseous feed working medium.Superheater 5 is for by pre-for gaseous feed working medium
Heat is to about 66 DEG C.Reactor 6 is fluidized-bed reactor, generates third as propylene, ammonia with oxygen reaction
The device of alkene nitrile.Second working medium pump 7 is for conveyance fluid, and the cryogenic liquid of autocondensation vaporizer divides in the future
Song Ru generator and vaporizer.Expansion valve 8 is electric expansion valve or heating power expansion valve, is a kind of throttling
Mechanism, for realizing the reducing pressure by regulating flow expansion process of liquid circulation working medium and regulating the flow of cycle fluid.
Vaporizer 9 vaporizes, to low temperature cold source 14 when being used for the liquid circulation working medium making low-temp low-pressure by vaporizer
Heat absorption reaches purpose of freezing.The effect of generator 10 is that remaining (giving up) heat of industry utilizing thermal source 13 makes liquid
State cycle fluid vaporizes and produces certain degree of superheat.Ejector 11 is gas-gas ejector, and effect is to utilize
From the low-temp low-pressure gaseous recycle working medium compression of the high temperature and high pressure gas flash-pot in the future of generator, phase
When in compressor.Cycle fluid decompressor 12 is scroll expander or screw expander, act as generation machine
Tool can be used for generating or other purposes.
For making to know more about the embodiment of the present invention, the side to the energy-recuperation system utilized in this embodiment below
Method is described in detail, and wherein, the method is probably divided into two parts, and Part I is in liquid material work
Matter carries out pressure recovery energy after level pressure evaporation, and Part II is to use after the cold energy recovery of liquid material working medium
In refrigeration and generation mechanical energy；
As shown in fig. 2, pressure recovery energy after level pressure evaporation is carried out for liquid material working medium, including following step
Rapid:
Step S100: liquid material working medium sends into condenser/evaporator 3 vapour from storage tank 1 through the first working medium pump 2
Change and form gaseous feed working medium；
Step S102: gaseous feed working medium enters raw material working medium after condenser/evaporator 3 level pressure is evaporated and expands
Machine 4 expansion work；
In this step, producing pressure energy after raw material working medium decompressor 4 expansion work, this pressure energy can
For generating electricity.
Step S104: the gaseous feed working medium after acting enters the overheated rear reactor 6 that enters of superheater 5 and enters
Row reaction.
Wherein, the figure of the T-S from Fig. 4 is it can be seen that the variations in temperature of raw material working medium.
As shown in 3 figures, for being used for freezing and producing mechanical energy after being reclaimed by the cold energy of liquid material working medium,
Comprise the following steps:
Step S200: liquid circulation working medium autocondensation vaporizer 3 enters the second working medium pump 7 the most afterwards；
Step S202: be divided into two-way from the second working medium pump liquid circulation working medium out, an expanded valve in road
Enter vaporizer 9 vaporization heat absorption after 8 reducing pressure by regulating flows, form the first gaseous recycle working medium after heat absorption and as drawing
It is to be compressed that body of emanating enters ejector 11, and another road enters generator 10 vaporization and forms the second gaseous recycle
Working medium；
In this step, enter vaporizer 9 vaporization after liquid circulation working medium expanded valve 8 reducing pressure by regulating flow to inhale
Thermogenetic cold energy can reclaim and freeze, and its mode reclaimed is multiple, such as, by cold energy according to temperature
Degree needs to be stored in water or in saline.
Step S204: being divided into two-way from generator 10 the second gaseous recycle working medium out, a road is as height
Pressure working fluid enters ejector 11 compression to be carried out the ejection gas of flash-pot 9 and mixes, and another road enters
Cycle fluid decompressor 12 expansion work；
In this step, the second gaseous recycle working medium enters what cycle fluid decompressor 12 expansion work produced
Mechanical energy can be used to generate electricity.
Step S206: the gaseous recycle working medium after ejector 11 and cycle fluid decompressor 12 returns to cold
Solidifying vaporizer 3 is condensed into liquid.
In this step, gaseous recycle working medium returns to condenser/evaporator 3 and is condensed into the cold energy that liquid is used
The cold energy produced when pervaporation step for condenser/evaporator 3 in above-mentioned steps S100.
The embodiment of the present invention changes traditional decompression evaporator into condenser/evaporator, adds a set of cold energy and returns
Receipts system (mainly include generator, ejector, cycle fluid decompressor, the second working medium pump, expansion valve,
Vaporizer), can fully recycle the cold energy of raw material working medium compared with conventional process flow, be used for freezing,
The mechanical energy that cycle fluid decompressor reclaims simultaneously can be used in acting generating.And after condenser/evaporator
Add raw material working medium decompressor, the pressure energy of recoverable raw material working medium, improve energy further and return
Receive utilization rate.
It is given below two and utilizes the specific embodiment of energy-recuperation system in the present embodiment:
Embodiment 1:
In this embodiment, liquid material working medium is propylene liguid, and cycle fluid is propane, and cycle fluid is
Master stream body.Reaction raw materials working medium propylene liguid sends into condenser/evaporator 3 from spherical tank 1 through the first working medium pump 2
After level pressure vaporizes and be overheated, in this embodiment, the pressure for vaporization in condenser/evaporator 3 is 1.3MPa；
Saturated propylene steam enters raw material working medium decompressor 4 reclaiming by swelling pressure energy, from raw material working medium decompressor 4
Out pressure be about 0.35MPa two-phase fluid enter superheater 5, overheated after propylene enter reactor
6 participate in reaction.The second working medium pump 7 is entered, from the second working medium from condenser/evaporator 3 liquid petroleum gas (liquid propane gas) out
Pump 7 liquid petroleum gas (liquid propane gas) out is divided into two-way, enters vaporizer 9 vapour after road expanded valve 8 reducing pressure by regulating flow
Changing heat absorption, another road enters generator 10 and utilizes the 0.4MPa saturated vapor of by-product in acrylonitrile process
(corresponding saturation temperature is 143.6 DEG C) heating propane makes it vaporize, and in this embodiment, propane is occurring
Pressure for vaporization in device 10 is 2.6MPa, and the degree of superheat is 5 DEG C；Make from vaporizer 9 gaseous propane out
Enter gas-gas ejector 11 for driving fluid to be compressed；Divide from generator 10 High Temperature High Pressure propane out
For two-way, a road enters gas-gas ejector 11 compression as pressurized working fluid and carrys out the injection of flash-pot 9
Gas also mixes, and another road enters cycle fluid decompressor 12 expansion work；From gas-gas ejector 11 He
The overheated gaseous propane that cycle fluid decompressor 12 pressure out is 1.3MPa, temperature is about 40 DEG C
It is condensed into liquid petroleum gas (liquid propane gas) in condenser/evaporator 3.Wherein, it can be seen that cycle fluid third from Fig. 5
The variations in temperature of alkane.
Embodiment 2:
In this embodiment, liquid material working medium is liquefied ammonia, and cycle fluid is ammonia, and cycle fluid is wet fluid.
Reaction raw materials working medium liquefied ammonia sends into the vaporization of condenser/evaporator 3 level pressure from spherical tank 1 through the first working medium pump 2,
In this embodiment, liquefied ammonia pressure for vaporization in condenser/evaporator 3 is 1.2MPa；Saturated ammonia after vaporization
Gas enters raw material working medium decompressor 4 reclaiming by swelling pressure energy, from raw material working medium decompressor 4 out pressure is
The two-phase fluid of about 0.3MPa enters superheater 5, overheated after ammonia enter reactor 6 and participate in reaction.
Enter the second working medium pump 7 from condenser/evaporator 3 liquefied ammonia out, divide from the second working medium pump 7 liquefied ammonia out
For two-way, entering vaporizer 9 vaporization heat absorption after road expanded valve 8 reducing pressure by regulating flow, another road enters to be sent out
Raw device 10 utilizes the saturated vapor heating liquefied ammonia of the 0.4MPa of by-product in acrylonitrile process to make it vaporize,
In this embodiment, liquefied ammonia pressure for vaporization in generator 10 is 3.3MPa, and the degree of superheat is 8 DEG C；From
Vaporizer 9 ammonia out enters gas-gas ejector 11 as driving fluid and is compressed；From generator 10
High Temperature High Pressure ammonia out is divided into two-way, and a road enters gas-gas ejector 11 as pressurized working fluid
Compression carrys out the ejection gas of flash-pot 9 and mixes, and another road enters cycle fluid decompressor 12 expansion and does
Merit；The quilt condenser/evaporator 3 from gas-gas ejector 11 and cycle fluid decompressor 12 ammonia out
It is condensed into liquefied ammonia.Wherein, it can be seen that the variations in temperature of cycle fluid liquefied ammonia from Fig. 6.
What deserves to be explained is, the cycle fluid in embodiment 1 or 2 is not limited to the working medium such as propane, ammonia.
The aforementioned description to the specific illustrative embodiment of the present invention illustrates that and the purpose of illustration.
These descriptions are not wishing to limit the invention to disclosed precise forms, and it will be apparent that according to above-mentioned
Teaching, can much change and change.The purpose selected exemplary embodiment and describe exists
In explaining the certain principles of the present invention and actual application thereof, so that those skilled in the art can be real
Now and utilize the various different exemplary of the present invention and various different selection and change.
The scope of the present invention is intended to be limited by claims and equivalents thereof.
Claims (8)
1. for an energy recycle device for the process for production of acrylonitrile section of feeding intake, including: storage tank (1),
First working medium pump (2), condenser/evaporator (3), raw material working medium decompressor (4), superheater (5), anti-
Answer device (6), the second working medium pump (7), expansion valve (8), vaporizer (9), generator (10), injection
Device (11) and cycle fluid decompressor (12)；
It is characterized in that:
Described storage tank (1), the first working medium pump (2), the liquid phase entrance of condenser/evaporator (3) are sequentially connected with,
The gaseous phase outlet of described condenser/evaporator (3), raw material working medium decompressor (4), superheater (5) and
Reactor (6) is sequentially connected with；Liquid material working medium condensed vaporizer (3) vapour from storage tank (1)
Raw material working medium decompressor (4) expansion work pressure recovery energy is entered, subsequently into superheater (5) after change
Enter reactor (6) after preheating, prepare acrylonitrile；Liquid material working medium is liquid ethylene or liquefied ammonia；
The liquid-phase outlet of described condenser/evaporator (3) and the entrance of the second working medium pump (7) connect, and second
The outlet of working medium pump (7) divides two-way, a road and described expansion valve (8), vaporizer (9) and described
The injection entrance of ejector (11) is sequentially connected with, and another road is connected with the entrance of described generator (10)；
The outlet of described generator (10) divides two-way, and a road is steamed with described condensation through described ejector (11)
Send out device (3) gas phase entrance connect, another road through described cycle fluid decompressor (12) also with described
The gas phase entrance of condenser/evaporator (3) connects；
Described second working medium pump (7) is for the liquid circulation working medium difference of autocondensation vaporizer (3) in the future
Send into vaporizer (9) and generator (10)；Cycle fluid is propane or ammonia；
Described vaporizer (9) is used for gasification of liquid cycle fluid, forms the first gaseous recycle working medium and reclaims
Cold energy；
Described generator (10), for liquid circulation working medium being vaporized, forms the second gaseous recycle working medium,
Divide two-way to respectively enter ejector (11) to be reclaimed by compression and cycle fluid decompressor (12) expansion work
Mechanical energy.
Energy recycle device the most according to claim 1, it is characterised in that described storage tank (1) is
Spherical tank.
Energy recycle device the most according to claim 1, it is characterised in that described raw material working medium is swollen
Swollen machine (4) is scroll expander or screw expander.
Energy recycle device the most according to claim 1, it is characterised in that described reactor (6)
For fluidized-bed reactor.
Energy recycle device the most according to claim 1, it is characterised in that described expansion valve (8)
For electric expansion valve or heating power expansion valve.
Energy recycle device the most according to claim 1, it is characterised in that described cycle fluid is swollen
Swollen machine (12) is scroll expander or screw expander.
Energy recycle device the most according to claim 1, it is characterised in that described ejector (11)
For gas-gas ejector.
8. using the method that the energy recycle device described in claim 1 recovers energy, its feature exists
In, comprise the following steps:
(a-1) liquid material working medium is sent into described from described storage tank (1) through described first working medium pump (2)
Condenser/evaporator (3) vaporization forms gaseous feed working medium；Described liquid material working medium is propylene liguid or liquid
Ammonia；
(a-2) described gaseous feed working medium enters described raw material work the most afterwards from described condenser/evaporator (3)
Matter decompressor (4) expansion work, pressure recovery energy；
(a-3) the described gaseous feed working medium after acting enters described in the overheated rear entrance of described superheater (5)
Reactor (6) participates in reaction, prepares acrylonitrile；
(b-1) liquid circulation working medium enters described second working medium pump the most afterwards from described condenser/evaporator (3)
(7)；Described cycle fluid is propane or ammonia；
(b-2) being divided into two-way from described second working medium pump (7) liquid circulation working medium out, a road is through institute
Enter described vaporizer (9) heat absorption vaporization after stating expansion valve (8) reducing pressure by regulating flow, form the first gaseous state and follow
Ring working medium is the most to be compressed as the ejection gas described ejector of entrance (11), and reclaims because inhaling thermogenetic
Cold energy；Another road enters described generator (10) vaporization and forms the second gaseous recycle working medium；
(b-3) it is divided into two-way from described generator (10) described second gaseous recycle working medium out, one
Road enters described ejector (11) compression injection from described vaporizer (9) as pressurized working fluid
Gas also mixes, and another road enters described cycle fluid decompressor (12) expansion work, reclaims mechanical energy；
(b-4) gaseous recycle after described ejector (11) and described cycle fluid decompressor (12)
Working medium returns to described condenser/evaporator (3) and is condensed into liquid.
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| CN201410795928.3A CN104529820B (en) | 2014-12-19 | 2014-12-19 | Energy-recuperation system and recovery method for the process for production of acrylonitrile section of feeding intake |
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| CN201410795928.3A CN104529820B (en) | 2014-12-19 | 2014-12-19 | Energy-recuperation system and recovery method for the process for production of acrylonitrile section of feeding intake |
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| CN1786622A (en) * | 2005-10-27 | 2006-06-14 | 王锦胜 | Multi-step combined energy exchanger and method of energy exchanging |
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| CN1786622A (en) * | 2005-10-27 | 2006-06-14 | 王锦胜 | Multi-step combined energy exchanger and method of energy exchanging |
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| Title |
|---|
| 丙烯腈装置节能改造与流化床反应器模拟分析;张沛存;《中国优秀博硕士学位论文全文数据库 (硕士) 工程科技Ⅰ辑（季刊 ）2003 年》;20030615(第 02 期);B016-43 * |
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