CN104150508B - A kind of method that ammonia synthesis catalyst low pressure heats up - Google Patents
A kind of method that ammonia synthesis catalyst low pressure heats up Download PDFInfo
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- CN104150508B CN104150508B CN201410388751.5A CN201410388751A CN104150508B CN 104150508 B CN104150508 B CN 104150508B CN 201410388751 A CN201410388751 A CN 201410388751A CN 104150508 B CN104150508 B CN 104150508B
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- ammonia
- synthesis catalyst
- ammonia synthesis
- gas
- low pressure
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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
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Abstract
The invention discloses a kind of method that ammonia synthesis catalyst low pressure heats up, namely system pressure is supplemented to and is greater than 0.5MPa by synthesis system after being communicated with liquid ammonia storage tank, then gas is delivered to oil separator by open cycle compressor, deliver to synthetic tower after separating greasy dirt to heat up for ammonia synthesis catalyst, then through waste heat recoverer, heat exchanger, water cooler is sent to cool after water heater recovery waste heat, by Optimization Technology method, ammonia synthesis catalyst is heated up, do not need gas making, desulfurization, conversion, decarburization (or carbonization), compression, alcohol alkanisation system cloud gray model, liquid ammonia storage tank overbottom pressure is directly utilized to enter synthesis system, eliminate the process that above system repeats to drive, corresponding power consumption and coal consumption of having saved the compression of this system gas.
Description
Technical field
The invention belongs to chemical production technical field, particularly relate to a kind of method that ammonia synthesis catalyst low pressure heats up.
Background technology
The ammonia synthesis catalyst intensification technology that current industry generally adopts is after the whole production system of synthetic ammonia has been overhauled, gasification system first Gas-making Furnace temperature raising gas, after semi-water gas composition is qualified, open desulphurization system, compression system heats up for transformation system, transformation system heats up and terminates, pressure swing adsorption decarbonization (or carbonization) system is opened after conversion gas composition is qualified, alcohol alkanisation system is opened after unstripped gas composition is qualified, after alkane gas trace qualified after import synthesis system, synthesis system pressure is risen to 5.0MPa, then ammonia synthesis catalyst starts to heat up, ammonia synthesis catalyst temperature rise rate is generally 60 DEG C/h, maintenance terminates rear synthetic catalyst temperature and is generally 40 DEG C, 460 DEG C of ability need be warming up to normally produce, period approximately needs 7-8 hour, gas after alkane again could be supplemented Deng the qualified rear synthesis system of synthetic catalyst temperature index, gas making during this period, desulfurization, conversion, decarburization (or carbonization), compression, alcohol alkanisation system cloud gray model is a kind of waste, restarting after out of service is also a kind of waste.
The synthesis system of our company's prior art is through gas making, desulfurization, conversion, decarburization (or carbonization), compression, after alcohol alkanisation system cloud gray model, system pressure is supplemented to 5.0MPa, then gas is delivered to oil separator by open cycle compressor, deliver to synthetic tower after separating greasy dirt to heat up for ammonia synthesis catalyst, then through waste heat recoverer, heat is handed over, water cooler is sent to cool after water heater recovery waste heat, ammonia condenser is sent to lower the temperature further again after sending ammonia separator to separate part liquefied ammonia after cooling, then send cool exchanger to be separated liquefied ammonia and after reclaiming cold, return recycle compressor and carry out next one circulation, gas circulation is normally opened electric furnace afterwards and is suitably adjusted the electric current of electric furnace and voltage according to furnace temperature rising situation and reach the object that ammonia synthesis catalyst heats up, the liquefied ammonia separated send liquid ammonia storage tank.Ammonia synthesis catalyst heats up and carries out under gas making, desulfurization, conversion, decarburization (or carbonization), compression, alcohol alkanisation system operation too, causes the significant wastage of the energy.
Summary of the invention
The object of the invention is by optimized process flow, provide a kind of ammonia synthesis catalyst to heat up, do not need the method that the ammonia synthesis catalyst low pressure of carrying out under gas making, desulfurization, conversion, decarburization (or carbonization), compression, alcohol alkanisation system operation conditions heats up.
The object of the invention is to be achieved through the following technical solutions,
System pressure is supplemented to and is greater than 0.5MPa by synthesis system after being communicated with liquid ammonia storage tank, then gas is delivered to oil separator by open cycle compressor, deliver to synthetic tower after separating greasy dirt to heat up for ammonia synthesis catalyst, then through waste heat recoverer, heat is handed over, water cooler is sent to cool after water heater recovery waste heat, now suitably should control water cooler cooling temperature below 55 DEG C, ammonia condenser is sent to lower the temperature further again after sending ammonia separator to separate part liquefied ammonia after cooling, now suitably should control ammonia condenser cooling temperature below 55 DEG C, then send cool exchanger to be separated liquefied ammonia and after reclaiming cold, return recycle compressor and carry out next one circulation, gas circulation is normally opened electric furnace afterwards and is suitably adjusted the electric current of electric furnace and voltage according to furnace temperature rising situation and reach the object that ammonia synthesis catalyst heats up, the liquefied ammonia separated send liquid ammonia storage tank.
Preferably, system pressure is supplemented to 1.0-1.5MPa by synthesis system after being communicated with liquid ammonia storage tank.
Preferably, control water cooler cooling temperature 40-50 DEG C to be advisable.
Preferably, control ammonia condenser cooling temperature 40-50 DEG C to be advisable.
Beneficial effect of the present invention: by Optimization Technology method, ammonia synthesis catalyst is heated up, do not need gas making, desulfurization, conversion, decarburization (or carbonization), compression, alcohol alkanisation system cloud gray model, liquid ammonia storage tank overbottom pressure is directly utilized to enter synthesis system, eliminate the process that above system repeats to drive, save power consumption and the coal consumption of the compression of this system gas accordingly.
Accompanying drawing explanation
Fig. 1 is process flow sheet of the present invention
Fig. 2 is the process flow sheet of prior art.
Embodiment
As shown in Figure 1, after whole synthesis ammonia system has overhauled, according to gas making, desulfurization, conversion, decarburization (or carbonization), compression, the time of alcohol alkanisation system cloud gray model, synthesis system be communicated with liquid ammonia storage tank in advance, synthesis system pressure is supplemented to 1.0-1.5MPa, then gas is delivered to oil separator by open cycle compressor, deliver to synthetic tower after separating greasy dirt to heat up, then through waste heat recoverer for ammonia synthesis catalyst, heat is handed over, water cooler is sent to cool after water heater recovery waste heat, now suitably should control water cooler cooling temperature 40-50 DEG C, ammonia condenser is sent to lower the temperature further again after sending ammonia separator to separate part liquefied ammonia after cooling, now should suitably control ammonia condenser temperature 40-50 DEG C, then send cool exchanger to be separated liquefied ammonia and after reclaiming cold, return recycle compressor and carry out next one circulation, gas circulation is normally opened electric furnace afterwards and is suitably adjusted the electric current of electric furnace and voltage according to furnace temperature rising situation and reach the object that ammonia synthesis catalyst heats up, and makes the basic and gas making of ammonia synthesis catalyst heating-up time, desulfurization, conversion, decarburization (or carbonization), compression, the time of alcohol alkanisation system cloud gray model matches, and reaches whole synthesis ammonia system and once drives normally to run, energy-saving and cost-reducing object.
Claims (3)
1. the method for an ammonia synthesis catalyst low pressure intensification, it is characterized in that system pressure is supplemented to 1.0-1.5MPa by synthesis system after being communicated with liquid ammonia storage tank, then gas is delivered to oil separator by open cycle compressor, deliver to synthetic tower after separating greasy dirt to heat up for ammonia synthesis catalyst, then through waste heat recoverer, heat is handed over, water cooler is sent to cool after water heater recovery waste heat, now suitably should control water cooler cooling temperature below 55 DEG C, ammonia condenser is sent to lower the temperature further again after sending ammonia separator to separate part liquefied ammonia after cooling, now suitably should control ammonia condenser cooling temperature below 55 DEG C, then send cool exchanger to be separated liquefied ammonia and after reclaiming cold, return recycle compressor and carry out next one circulation, gas circulation is normally opened electric furnace afterwards and is suitably adjusted the electric current of electric furnace and voltage according to furnace temperature rising situation and reach the object that ammonia synthesis catalyst heats up, the liquefied ammonia separated send liquid ammonia storage tank.
2. the method for a kind of ammonia synthesis catalyst low pressure intensification according to claim 1, is characterized in that controlling water cooler cooling temperature 40-50 DEG C is advisable.
3. the method for a kind of ammonia synthesis catalyst low pressure intensification according to claim 1, is characterized in that controlling ammonia condenser cooling temperature 40-50 DEG C is advisable.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410388751.5A CN104150508B (en) | 2014-08-10 | 2014-08-10 | A kind of method that ammonia synthesis catalyst low pressure heats up |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201410388751.5A CN104150508B (en) | 2014-08-10 | 2014-08-10 | A kind of method that ammonia synthesis catalyst low pressure heats up |
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| CN104150508A CN104150508A (en) | 2014-11-19 |
| CN104150508B true CN104150508B (en) | 2016-02-24 |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1991009811A1 (en) * | 1990-01-04 | 1991-07-11 | Schwarzenbek Eugene F | Synthetic ammonia process |
| CN102557075A (en) * | 2010-12-07 | 2012-07-11 | 北京利达丰华科技有限公司 | Method for circularly utilizing cooling capacity and method for increasing yield of synthesis ammonia |
| CN203307064U (en) * | 2013-06-08 | 2013-11-27 | 浠水县福瑞德化工有限责任公司 | Ammonia synthesis system |
| CN103570039A (en) * | 2013-11-08 | 2014-02-12 | 安徽金禾实业股份有限公司 | Novel refrigeration method and novel refrigeration device in synthetic ammonia production process |
| CN203683104U (en) * | 2014-02-17 | 2014-07-02 | 孙经东 | Low-pressure heating device of synthetic tower of ammonia synthesizing device |
| CN203715291U (en) * | 2014-03-03 | 2014-07-16 | 四川隆桥化工集团有限公司 | Warming system with temperature regulating valve in synthetic ammonia reaction process |
-
2014
- 2014-08-10 CN CN201410388751.5A patent/CN104150508B/en not_active Expired - Fee Related
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1991009811A1 (en) * | 1990-01-04 | 1991-07-11 | Schwarzenbek Eugene F | Synthetic ammonia process |
| CN102557075A (en) * | 2010-12-07 | 2012-07-11 | 北京利达丰华科技有限公司 | Method for circularly utilizing cooling capacity and method for increasing yield of synthesis ammonia |
| CN203307064U (en) * | 2013-06-08 | 2013-11-27 | 浠水县福瑞德化工有限责任公司 | Ammonia synthesis system |
| CN103570039A (en) * | 2013-11-08 | 2014-02-12 | 安徽金禾实业股份有限公司 | Novel refrigeration method and novel refrigeration device in synthetic ammonia production process |
| CN203683104U (en) * | 2014-02-17 | 2014-07-02 | 孙经东 | Low-pressure heating device of synthetic tower of ammonia synthesizing device |
| CN203715291U (en) * | 2014-03-03 | 2014-07-16 | 四川隆桥化工集团有限公司 | Warming system with temperature regulating valve in synthetic ammonia reaction process |
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| CN104150508A (en) | 2014-11-19 |
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