CN105399112B - A kind of method and apparatus for synthesizing ammonia synthesis system Optimal improvements - Google Patents
A kind of method and apparatus for synthesizing ammonia synthesis system Optimal improvements Download PDFInfo
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- CN105399112B CN105399112B CN201510820309.XA CN201510820309A CN105399112B CN 105399112 B CN105399112 B CN 105399112B CN 201510820309 A CN201510820309 A CN 201510820309A CN 105399112 B CN105399112 B CN 105399112B
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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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- 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
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention discloses a kind of method and apparatus for synthesizing ammonia synthesis system Optimal improvements, belong to synthesis ammonia technical field.Method comprises the following steps：A, two outlets of synthetic tower carry out heat recovery through waste heat boiler, and the outlet through heat exchanger and synthetic tower carries out heat exchange to reaction gas again, and the reaction gas after heat exchange is cooled through soft water heater and water cooler successively；Reaction gas after b, cooling carries out heat exchange cooling through the gaseous mixture in cool exchanger and step c, then through ammonia separator separate section liquefied ammonia, the reaction gas of separation liquefied ammonia is condensed through ammonia condenser；After c, remaining reaction gas are mixed with unstripped gas, heat exchange heating is carried out with the reaction gas in step b again after separating liquefied ammonia through cool exchanger, the gaseous mixture after heating sends into synthetic tower by recycle compressor.Synthesis import ammonia content is down to 2.1% by original 2.7% within the system, and outlet ammonia content is slightly risen to 12.4% by original 11.5%.
Description
Technical field
The invention belongs to synthesize ammonia technical field, more particularly to a kind of method and dress for synthesizing ammonia synthesis system Optimal improvements
Put, more particularly to a kind of transformed on the basis of existing synthesis ammonia system and with good result synthesis ammonia method
And system.
Background technology
Ammonia, Ammonia, NH3, colourless gas have strong impulse smell；Density 0.7710, relative density
0.5971（Air=1.00）；Colourless liquid is easily liquefied as, pressurization at normal temperatures can make it liquefy（Critical-temperature 132.4
DEG C, 11.2 MPas of critical pressure, i.e. 112.2 atmospheric pressure）, -33.5 DEG C of boiling point, also easily be cured into snow shape solid, fusing point -
77.75℃；It is dissolved in water, ethanol and ether.Nitrogen and hydrogen can be resolved into high temperature, there is reduction；With the presence of catalyst
When can be oxidized to nitric oxide.For liquid nitrogen processed, ammoniacal liquor, nitric acid, ammonium salt and amine etc..It can directly be synthesized and made by nitrogen and hydrogen
.Energy skin ambustion, eyes, the mucous membrane of respiratory apparatus, people's suction are excessive, can cause lung swelling, so that it is dead.
Ammonia is used to manufacture ammoniacal liquor, nitrogenous fertilizer（Urea, carbon ammonium etc.）, compound fertilizer, nitric acid, ammonium salt, soda ash etc., be widely used in
The fields such as chemical industry, light industry, chemical fertilizer, pharmacy, synthetic fibers.It is inorganic salt containing nitrogen and orgnnic comopounds, sulfa drug, polyurethane, poly-
Nylon and nitrile rubber etc. are all needed directly using ammonia as raw material.In addition, liquefied ammonia is commonly used for refrigerant, ammonia is also used as biology
Fuel provides the energy.
Industrial ammonia is to pass through N with aber process2And H2In the presence of the catalyst at elevated temperature and pressure direct chemical combination and be made：
N2+3H2==HTHP catalyst===2NH3（Reversible reaction）
△rHθ =-92.4kJ/mol
Industry ammonia processed is mostly to be synthesized to be made by nitrogen and hydrogen in the presence of high pressure, high temperature and catalyst.Nitrogen
It is mainly derived from air；Hydrogen is mainly derived from hydrogeneous and carbon monoxide synthesis gas（Pure hydrogen also derives from the electrolysis of water）.By
The gaseous mixture of nitrogen and hydrogen composition is syngas for synthetic ammonia.
In the industrialized production of ammonia, generally synthesized using synthetic tower, behind synthetic tower setting heat recovery with it is cold
Concretio, for reclaiming heat in reaction gas and being liquefied ammonia by ammonia condensation, remaining gas circulation is used, and is re-fed into synthesis
In tower.Its basic process is：A, two outlets of synthetic tower are exchanged heat with waste heat boiler, soft water heater successively, and reaction gas is again
An outlet through heat exchanger and synthetic tower carries out heat exchange（Enter gas by two and be warming up to 130-145 DEG C）, the reaction gas after heat exchange
Water cooled but device is cooled；Reaction gas after b, cooling is through ammonia separator separate section liquefied ammonia（It is seldom a part of）, separating liquid
Reaction gas after ammonia carries out heat exchange cooling through the gaseous mixture in cool exchanger and step c, then is condensed through ammonia condenser；It is c, surplus
Remaining reaction gas carries out heat exchange heating, separating liquid with feeding cool exchanger after fresh gas mixing and the reaction gas in step b
Ammonia, the gaseous mixture after heating sends into synthetic tower by recycle compressor.
Certainly, also there are the different embodiments of above-mentioned technology in the prior art, but generally according to above-mentioned thinking.
Patent such as Application No. 201320331977.2 discloses a kind of synthesis ammonia system, including the cold friendship being sequentially connected
Parallel operation, circulator, heat exchanger, synthetic tower, center boiler, and ammonia separator and ammonia cooler, wherein cool exchanger also with ammonia
Separator and ammonia cooler are sequentially connected.The workflow of the present invention is as follows：From seven sections of next qualified refinery gas of compression, with passing through ammonia
Circulating air after cold is mixed into cool exchanger, separates and enters circulator after part liquefied ammonia and profit, then is come out from circulator
After oil, heated up into heat exchanger, enter in synthetic tower carry out ammonia synthesis reaction afterwards, gas exchanges heat through bottom
The interior water heat exchange generation steam that device is drawn into center boiler and center boiler enters main steam range, then comes out and passes through from center boiler
Synthesis tower bottom heat exchanger is exchanged heat, and synthetic tower is gone out after heat exchange and enters cool exchanger after over-heat-exchanger, water-cooled cooling again
Top heat exchanger, comes out into ammonia separator, separates and further cooled down into ammonia cooler after the liquefied ammonia of part in ammonia separator, cold
But the circulating air after enters cool exchanger, such iterative cycles, ammonia separator and cold exchange together with after fresh gas mixing
The liquefied ammonia that device is isolated send freezing ammonia storage tank.A part of storage tank carrys out liquefied ammonia and entered after ammonia cooler, evaporation to send freeze cycle to use.
Patent such as Application No. 201310548141.2 discloses the New Refrigerating in a kind of production of synthetic ammonia
Method, comprises the following steps：
A, go out the synthetic reaction gas of synthetic tower and be reduced to 106 DEG C after heat exchanger reclaims high level heat, reaction gas passes through again
Ammonia steams
The tube side of hair device is cooled down, and ammonia evaporator adds liquefied ammonia refrigerant from the shell side of bottom, and liquefied ammonia is in ammonia evaporator
Shell side top
2.1mpa, 80 DEG C of gas ammonia are evaporated, reaction gas temperature after the tube side of ammonia evaporator is reduced to 68 DEG C, Ran Houjin
Enter water-cooled
But device, reaction gas is reduced to 30 DEG C after water cooled but device cooling；
B, go out water cooler reaction gas enter cool exchanger after be cooled to 10 DEG C, enter back into ammonia condenser tube side carry out
Cooling, ammonia condenser adds liquefied ammonia refrigerant from the shell side of bottom, and liquefied ammonia evaporates 1.7mpa, 5 on ammonia condenser shell side top
DEG C gas ammonia, reaction gas by ammonia condenser tube side be reduced to -2 DEG C, subsequently into cool exchanger bottom ammoniacal liquor separate fill
Put, separate liquefied ammonia therein, deliver to liquid ammonia storage tank, remaining reaction gas removes circulator as circulating air, returns to synthetic tower；c、
2.1Mpa, ammonia of calming the anger in 80 DEG C are evaporated in ammonia evaporator and enters the jet chamber of ammonia injector, what ammonia condenser was evaporated
0.17Mpa, 5 DEG C of low pressure gas ammonia enter the suction chamber of ammonia injector, and mesolow gas ammonia mixing diffusion is extremely in injector
1.2Mpa, after 55 DEG C, it is condensed into evaporative condenser after 30 DEG C of liquefied ammonia, into ammonia storage tank.
Applicant has found following problem during prior art is realized：
1st, two outlets are synthesized in the prior art and are cooled to 190-200 DEG C through waste heat boiler heat exchange, then pass through soft water heater
165-175 DEG C is cooled to after heat exchange, partial heat, to pipe network, causes the hot gas of heat exchanger to go out by the hot water bank of soft water heater
Mouthful（The two of synthetic tower enter gas）Temperature is low（130-145 DEG C or so）, relative reduction system circulation amount.
2nd, because water cooler is using recirculated water closed cycle in synthesis ammonia, 32 DEG C or so of cooling water temperature causes water outlet
The temperature of circulating air after cooler is more than 36 DEG C, and the ammonia in circulating air there is no liquefaction, and ammonia separator there is no
Ammonia is separated, and synthetic cyclic gas is all separated in cool exchanger, so considerably increases the load of cool exchanger, synthesis
Tower import ammonia content is 2.7% or so.
2 points of the above causes the gas ammonia content height into synthetic tower, and system circulation amount diminishes, and ammonia synthesis positive reaction is suppressed,
Total conversion is reduced, and system pressure increases, power consumption rise.
The content of the invention
In order to solve the above problems, the embodiments of the invention provide it is a kind of synthesize ammonia synthesis system Optimal improvements method and
Device, is transformed using existing synthesis ammonia system, can effectively reduce the pressure and ammonia internal circulating load of whole system.The technology
Scheme is as follows：
On the one hand, the embodiments of the invention provide a kind of method for synthesizing ammonia synthesis system Optimal improvements, this method includes
Following steps：
A, synthetic tower two outlets through waste heat boiler carry out heat recovery, reaction gas again through heat exchanger and synthetic tower one
Outlet carries out heat exchange, and the reaction gas after heat exchange is cooled through soft water heater and water cooler successively；
Reaction gas after b, cooling carries out heat exchange cooling through the gaseous mixture in cool exchanger and step c, then through ammonia separator
Separate section liquefied ammonia, the reaction gas of separation liquefied ammonia is condensed through ammonia condenser；
After c, remaining reaction gas are mixed with unstripped gas, through cool exchanger separate liquefied ammonia after again with the reaction gas in step b
Heat exchange heating is carried out, the gaseous mixture after heating sends into synthetic tower by recycle compressor.
Further, the unstripped gas in the embodiment of the present invention is handled through cooler and oil eliminator.
Further, in the embodiment of the present invention recycle compressor output mixing pneumatic transmission synthetic tower one enter gas import or
Two enter gas import.
Specifically, it is provided in an embodiment of the present invention to comprise the following steps：
A, two outlets of synthetic tower carry out heat recovery through waste heat boiler and are cooled to 190-200 DEG C, and reaction gas is again through heat friendship
One outlet of parallel operation and synthetic tower carries out heat exchange and is cooled to 135-145 DEG C, and the reaction gas after heat exchange is successively through soft water heater
It is cooled to 112-118 DEG C and water cooler is cooled to 35-40 DEG C；
Reaction gas after b, cooling is cooled to less than 20 DEG C through the gaseous mixture progress heat exchange in cool exchanger and step c, then
Through ammonia separator separate section liquefied ammonia, the reaction gas of separation liquefied ammonia is condensed through ammonia condenser；
The mixing of c, remaining reaction gas and unstripped gas separate liquefied ammonia through cool exchanger after again with coming from water cooler in step b
Reaction gas carry out heat exchange heating, gaseous mixture after heating send the one of synthetic tower to enter gas import or two enters gas by recycle compressor
Import.
On the other hand, the embodiment of the present invention additionally provides a kind of synthesis ammonia synthesis system Optimal improvements device, including synthesis
Tower, waste heat boiler, heat exchanger, soft water heater, water cooler, cool exchanger, ammonia separator, ammonia condenser and circulation compression
Machine；Two exhaust outlets of the synthetic tower and the air inlet of waste heat boiler are connected, the gas outlet of the waste heat boiler and heat exchange
The hot air intake connection of device, cold air outlet and soft water heater, the water cooler of the heat exchanger are sequentially connected, and the heat is handed over
The cold air import of parallel operation heat and an exhaust outlets of synthetic tower are connected, and the heat outlet of the heat exchanger and the two of synthetic tower enter
Gas import is connected, and the hot air intake of the cool exchanger is connected with water cooler, cold air outlet and the ammonia point of the cool exchanger
It is sequentially connected from device, ammonia condenser, the cold air import of the cool exchanger is connected with ammonia condenser, the hot gas of the cool exchanger
Outlet, recycle compressor and synthetic tower are sequentially connected, and the liquid ammonia storage tank is connected with ammonia condenser and cool exchanger.
Wherein, the cold air import of the cool exchanger in the embodiment of the present invention is connected with the first oil eliminator, first oil
Feed gas chiller is provided between separator and unstripped gas air supply opening.
Wherein, the second oil eliminator is provided between the recycle compressor and synthetic tower in the embodiment of the present invention.
Wherein, in the embodiment of the present invention recycle compressor and the one of synthetic tower enters gas import and two and enters gas import connection.
The beneficial effect that technical scheme provided in an embodiment of the present invention is brought is：After synthesis technique transformation, waste heat boiler goes out
190-200 DEG C of circulating air of mouth can be improved to 165-175 directly into heat exchanger and synthesis two air inlets heat exchange, two intake air temperature
DEG C, the internal circulating load of 2 ammonia net values can be improved, while reducing into 10 DEG C or so of water cooler gas, the water cooled but device of circulating air
And after cool exchanger cooling, enter ammonia separator circulating air temperature and be down to less than 18 DEG C by former more than 36 DEG C, 40%-50% in circulating air
Ammonia is isolated in ammonia point, and 55% ammonia is further isolated in cool exchanger, and the ammonia content in synthetic cyclic gas can be down to
Less than 1.7%, hydrogen and nitrogen gas conversion ratio can improve 2 percentage points, and 1-2MPa can drop in the pressure of synthesis system, rule of thumb calculate ton
Ammonia can economize on electricity about 16 degree.
Brief description of the drawings
Fig. 1 is the structured flowchart of synthesis ammonia system of the prior art；
Fig. 2 is the structured flowchart of synthesis ammonia system provided in an embodiment of the present invention.
Embodiment
To make the object, technical solutions and advantages of the present invention clearer, the present invention is made into one below in conjunction with accompanying drawing
It is described in detail on step ground.
Embodiment 1
Referring to Fig. 2, ammonia synthesis system Optimal improvements device is synthesized the embodiments of the invention provide one kind, including synthetic tower 1,
Waste heat boiler 2, heat exchanger 3, soft water heater 4, water cooler 5, cool exchanger 6, ammonia separator 7, ammonia condenser 8 and circulation
Compressor 9 etc..Wherein, two exhaust outlets of synthetic tower 1 are connected with the air inlet of waste heat boiler 2, the gas outlet of waste heat boiler 2 with
The hot air intake connection of heat exchanger 3.The cold air outlet of heat exchanger 3 and soft water heater 4（It can be connected with waste heat boiler 2）、
Water cooler 5（Import）It is sequentially connected, the cold air import of heat exchanger heat 3 is connected with an exhaust outlets of synthetic tower 1, heat exchange
The heat outlet of device and the two of synthetic tower enter gas import connection.The hot air intake of cool exchanger 6 and water cooler 5（Outlet）Even
Connect, cold air outlet and ammonia separator 7, the ammonia condenser 8 of cool exchanger 6（Import）It is sequentially connected.The cold air import of cool exchanger 6
With ammonia condenser 8（Outlet）Connection, heat outlet, recycle compressor 9 and the synthetic tower 1 of cool exchanger 6 are sequentially connected.Liquefied ammonia is stored up
Tank（It is not shown）It is connected to collect liquefied ammonia with ammonia condenser 8 and cool exchanger 6.Wherein, waste heat boiler 2 is used to produce high temperature steaming
Vapour is incorporated in steam pipe system, and heat exchanger 3 is gas gas-heat exchanger, and the reaction gas for synthetic tower 1 to be come out goes out with synthetic tower 1
The outlet come is exchanged heat, and is not only reduced the temperature of reaction gas, is also improved two temperature for entering gas.Soft water heater 4 is
Common soft water heating arrangement, it is straightforward to provide hot water（Feeding conversion and Gas-making Process etc.）, or waste heat boiler 2 is carried
For the soft water after preheating, it is specifically as follows tubular heat exchanger.Water cooler 5 is specially cyclic spraying cooling structure.It is cold to exchange
Device 6 is gas-gas heat exchanger, and its bottom is used to separate liquefied ammonia provided with separator.Ammonia separator 7 is used to separate liquefied ammonia.Ammonia condenser 8
It is specific to be freezed using liquefied ammonia.Recycle compressor 9 is used to make reaction gas forced circulation and controls the pressure of whole system.
Wherein, referring to Fig. 2, system provided in an embodiment of the present invention also includes the first oil eliminator 10 and feed gas chiller
11, wherein, the cold air import of cool exchanger 6 is connected with the first oil eliminator 10, the first oil eliminator 10 and unstripped gas air supply opening
Between be provided with feed gas chiller 11（Specifically can be using liquefied ammonia refrigeration）.
Wherein, referring to Fig. 2, system provided in an embodiment of the present invention also include the second oil eliminator 12, recycle compressor 9 with
The second oil eliminator 12 is provided between synthetic tower 1.
Certainly, the system that the present invention is provided also includes other structures, is such as vented surge tank and other oil eliminators.
Wherein, referring to Fig. 2, the recycle compressor 9 in the embodiment of the present invention enters gas import and two with the one of synthetic tower 1 and enters gas
（Cold shock gas）Import is connected.
Wherein, each parameter of each structure of the invention and each structure of existing synthesis ammonia system is basically identical, such as water circulation
Amount, refrigerating capacity, exchange capability of heat etc., each structure can directly use the structure of original system, it is only necessary to wherein four structures of adjustment
Annexation, and the control parameter and ability of each structure are constant, and repacking cost is very low.
The present invention have exchanged heat exchanger and soft water heater, ammonia separator and cold friendship in existing synthesis ammonia system
The position of parallel operation, the exchange of two positions is indispensable, and the exchange of only any one position is all unable to reached purpose；In this hair
In bright, simple place-exchange can but reach very big effect, and its outstanding effect can not be embodied from single structure, but from
From the point of view of whole system, the pressure of whole system can be reduced, lowers the ammonia internal circulating load of system, power consumption is reduced.
Embodiment 2
Referring to Fig. 2, the embodiments of the invention provide the method that the device that a kind of Application Example 1 is provided synthesizes ammonia, including
Following steps：
A, two outlets of synthetic tower 1 carry out heat recovery through waste heat boiler 2 and are cooled to 200 DEG C, and reaction gas is again through heat exchange
Device 3 carries out heat exchange with an outlet of synthetic tower 1 and is cooled to 140 DEG C（Now, an outlet of synthetic tower 1 exchanges heat through heat exchanger 3
The two of feeding synthetic tower enter gas for 167 DEG C afterwards）, the reaction gas after heat exchange is cooled to 115 DEG C and water-cooled through soft water heater 4 successively
But device 5 is cooled to 37 DEG C.
B, cooled by water cooler 5 after reaction gas through the gaseous mixture in cool exchanger 6 and step c（From ammonia condenser 8
Residual gas mixed with unstripped gas）Carry out heat exchange and be cooled to 17 DEG C, now there is 45% or so liquefied ammonia condensation, then through ammonia separation
The reaction gas that device 7 separates after liquefied ammonia, separation liquefied ammonia is condensed through ammonia condenser 8.
C, condensed by ammonia condenser 8 after remaining reaction gas and unstripped gas（Through cooling and oil separation）After mixing, handed over through cold
The bottom of parallel operation 6 isolating construction separation liquefied ammonia after again with the reaction gas in step b（From water cooler 5）Heat exchange heating is carried out,
Gaseous mixture after heating sends into synthetic tower 1 by recycle compressor 9（The one of synthetic tower 1 is sent to enter gas import or two after oil separation
Enter gas import）.After synthesis transformation, synthesis two enters gas up to 167 DEG C, and heat exchanger 3 is worked off one's feeling vent one's spleen 140 DEG C, and soft water heater 4 is exported
115 DEG C, water cooler 5 exports 37 DEG C, and the inlet temperature of ammonia separator 7 is down to 17 DEG C, and part liquefied ammonia is separated from ammonia separator 7
The load of cool exchanger 6 is alleviated, synthesis import ammonia content is down to 2.1% by original 2.7%, and outlet ammonia content is by original
11.5% slightly rises to 12.4%, and synthesis circulator shortcut valve is fully closed, and cold shock by-pass open degree about 1 is enclosed, and synthetic reaction is good, system pressure
Power is reduced to 28.0MPa by original 29.2MPa, power consumption of compressor decline compared with the same period, daily 0.8 coefficient be 0.8 ×
3000=2400KWh, ton ammonia power consumption declines 20KWh.Rule of thumb calculating ton ammonia can economize on electricity 16 degree or so, produce benefit 30.72 ten thousand
Member, synthesis technique investment for trnasforming urban land is at 10.4 ten thousand yuan or so, and 16 × 4 × 0.48=30.72 of benefit ten thousand is produced in half a year recoverable investment per year
Member.
The foregoing is only presently preferred embodiments of the present invention, be not intended to limit the invention, it is all the present invention spirit and
Within principle, any modifications, equivalent substitutions and improvements made etc. should be included within the scope of the present invention.
Claims (6)
1. a kind of method for synthesizing ammonia synthesis system Optimal improvements, it is characterised in that comprise the following steps：
A, two outlets of synthetic tower carry out heat recovery through waste heat boiler and are cooled to 190-200 DEG C, and reaction gas is again through heat exchanger
Heat exchange is carried out with an outlet of synthetic tower and is cooled to 135-145 DEG C, and the reaction gas after heat exchange cools through soft water heater successively
35-40 DEG C is cooled to 112-118 DEG C and water cooler；
Reaction gas after b, cooling carries out heat exchange through the gaseous mixture in cool exchanger and step c and is cooled to less than 20 DEG C, then through ammonia
Separator separate section liquefied ammonia, the reaction gas of separation liquefied ammonia is condensed through ammonia condenser；
The mixing of c, remaining reaction gas and unstripped gas separate liquefied ammonia through cool exchanger after again with step b from the anti-of water cooler
Should gas carry out heat exchange heating, gaseous mixture after heating send the one of synthetic tower to enter gas import or two enter gas and enter by recycle compressor
Mouthful.
2. the method for synthesis ammonia synthesis system Optimal improvements according to claim 1, it is characterised in that the unstripped gas warp
Cooler and oil eliminator are handled.
3. one kind synthesis ammonia synthesis system Optimal improvements device, including synthetic tower, waste heat boiler, heat exchanger, soft water heater,
Water cooler, cool exchanger, ammonia separator, ammonia condenser and recycle compressor；Characterized in that,
Two exhaust outlets of the synthetic tower and the air inlet of waste heat boiler are connected, the gas outlet of the waste heat boiler and heat exchange
The hot air intake connection of device, cold air outlet and soft water heater, the water cooler of the heat exchanger are sequentially connected, and the heat is handed over
The cold air import of parallel operation heat and an exhaust outlets of synthetic tower are connected, and the heat outlet of the heat exchanger and the two of synthetic tower enter
Gas import is connected, and the hot air intake of the cool exchanger is connected with water cooler, cold air outlet and the ammonia point of the cool exchanger
It is sequentially connected from device, ammonia condenser, the cold air import of the cool exchanger is connected with ammonia condenser, the hot gas of the cool exchanger
Outlet, recycle compressor and synthetic tower are sequentially connected, and liquid ammonia storage tank is connected with ammonia condenser and cool exchanger.
4. synthesis ammonia synthesis system Optimal improvements device according to claim 3, it is characterised in that the cool exchanger
Cold air import is connected with the first oil eliminator, and raw material air cooling is provided between first oil eliminator and unstripped gas air supply opening
Device.
5. synthesis ammonia synthesis system Optimal improvements device according to claim 3, it is characterised in that the recycle compressor
The second oil eliminator is provided between synthetic tower.
6. synthesis ammonia synthesis system Optimal improvements device according to claim 3, it is characterised in that the recycle compressor
Enter gas import and two with the one of synthetic tower to enter gas import and be connected.
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| CN105883852B (en) * | 2016-04-29 | 2018-02-13 | 湖南安淳高新技术有限公司 | A kind of ammonia synthesis reaction system and ammonia synthesis reaction method |
| CN108178166B (en) * | 2017-12-29 | 2020-10-13 | 新奥泛能网络科技股份有限公司 | Method and system for separating synthetic ammonia |
| CN109516445B (en) * | 2018-12-05 | 2021-07-23 | 四川大学 | Closed circulation process for preparing nitric acid by combining electrolysis water and air separation |
| CN113666386B (en) * | 2021-08-26 | 2023-04-14 | 宁波中科远东催化工程技术有限公司 | Method for synthesizing ammonia from coke oven gas |
| CN115818665A (en) * | 2022-08-29 | 2023-03-21 | 贵州开阳化工有限公司 | Air tightness test method of ammonia synthesis high-pressure system |
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Denomination of invention: A Method and Device for Optimizing and Improving Synthetic Ammonia Synthesis System Effective date of registration: 20230731 Granted publication date: 20170718 Pledgee: Bank of China Limited Huanggang branch Pledgor: HUBEI XIANGYUN (Group) CHEMICAL Co.,Ltd. Registration number: Y2023420000318 |
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