CN105271304B - Energy saving apparatus for emptying methane gas in ammonia synthesis circulation gas - Google Patents
Energy saving apparatus for emptying methane gas in ammonia synthesis circulation gas Download PDFInfo
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- CN105271304B CN105271304B CN201510616687.6A CN201510616687A CN105271304B CN 105271304 B CN105271304 B CN 105271304B CN 201510616687 A CN201510616687 A CN 201510616687A CN 105271304 B CN105271304 B CN 105271304B
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Abstract
The invention discloses an energy saving apparatus for emptying a methane gas in an ammonia synthesis circulation gas, and belongs to the field of synthesis process ammonia preparation in order to solve the problems of resource and energy waste and unit product cost rising caused by loss of 80% or above of effective nitrogen and hydrogen with the emptied gas in the ammonia gas production process in the prior art. The energy saving apparatus for emptying the methane gas in the ammonia synthesis circulation gas comprises an ammonia synthesis tower, a pipeline into the tower, a pipeline out of the tower, and a synthetic gas cooler arranged on the pipeline out of the tower, the pipeline out of the tower is provided with a pipeline I paralleling to the synthetic gas cooler, the pipeline I is provided with an ammonia cooling recoverer, and a sampling valve I and an emptying valve are arranged behind the ammonia cooling recoverer on the pipeline I. The apparatus can substantially reduce the loss rate of the effective gas in air, and is economic.
Description
Technical field
The invention belongs to synthesize legal system ammonia field, specifically, it is related to a kind of ammonia synthesizing methane gas emptying energy saver.
Background technology
Synthesized in the production process of ammonia by nitrogen hydrogen, the control of the gas content such as methane in ammonia synthesis system circulating air,
It is one of key factor of available nitrogen hydrogen utilization ratio height in Ammonia Production, is the energy resource that nitrogen hydrogen prepares synthesis ammonia
One of important means for the technology of utilizing is saved, is to reduce one of important measures of production cost.
In production, in ammonia synthesis system circulating air, methane content is mainly derived from unstripped gas preparation process and brings into, Yi Jiwei
Amount CO+CO2Generate in the system and accumulate, although methane itself is harmless to producing, but realizes economical operation, in ammonia synthesis circulating air
Methane content will be controlled within certain index, too high levels, and nitrogen hydrogen resources utilization rate is just relatively high, but too high be will result in
The power consumption of whole production system rises, and cost increases；The low then power consumption of content declines, but the nitrogen hydrogen resources of preciousness are wasted
Seriously, also result in cost rising.How to accomplish neither to waste nitrogen hydrogen resources, and do not increase power consumption, ammonia synthesis is followed
In ring gas, the control of methane content plays very important effect to final products cost.
Control to methane content in ammonia synthesis circulating air, conventional method is to supplement fresh nitrogen hydrogen to enter ammonia synthesis
Methane gas emptying is set after mixing with the recyclegas for having separated ammonia after system, is entered tower circulating air and is dropped a hint middle methane content
18-20%, the gas for having more than 80% are lost with emptying gas for effective nitrogen hydrogen, cause energy resource to waste,
Unit cost is raised, and market competitiveness of enterprises is low.
The content of the invention
For solving the above problems, the present invention provides one kind and ammonia synthesis operation can kept to enter tower recyclegas methane content not
On the premise of change, raising drop a hint middle methane-gas scale, reduce methane and drop a hint the ammonia of the available nitrogen hydrogen content taken away
Methane gas emptying energy saver in synthetic cyclic gas, which can improve available gas utilization rate, increase yield in unit time, drop
Low production cost.
In ammonia synthesis circulating air of the present invention, methane gas emptying energy saver, including ammonia convertor, enters tower tube line
With go out tower tube line, and the syngas cooler being arranged on out on tower tube line, go out tower tube line be provided with and forming gas cooling
The parallel pipeline I of device, pipeline I are provided with ammonia cooling withdrawer, sampling valve I and atmospheric valve.
The pipeline I parallel with syngas cooler that the present invention is arranged, and the ammonia cooling recovery arranged on pipeline I
Device, atmospheric valve, after atmospheric valve to be arranged on ammonia cooling withdrawer for which, uncooled ammonia cooling in can dropping a hint is reclaimed,
And then the content of middle methane of dropping a hint is improved, methane content can improve 10%, the raising of middle methane content of dropping a hint, Neng Gouyou
The nitrogen hydrogen that avoids of effect is vented the loss for causing because of methane, it is possible to increase nitrogen hydrogen resources utilization rate, reduces cost, while the effect
The acquirement of fruit does not change the composition into tower circulating air.
Further, the go out tower tube line parallel with pipeline I is provided with gas-liquid separator, and the gas-liquid separator is arranged on conjunction
Into after gas cooler.
Further, pipeline II, pipeline are connected with the pipeline between the syngas cooler and gas-liquid separator
II is provided with QI invigorating valve.
Further, go out after tower being provided between ammonia convertor and syngas cooler on tower tube line pre- heat regenerator and change
Hot device, is sequentially connected circulator, oil water separator, heat exchanger and ammonia convertor by pipeline after gas-liquid separator.
Further, heat exchanger is arranged on after tower after pre- heat regenerator, the pipeline between oil water separator and heat exchanger
Heat exchanger entrance valve and sampling valve II is provided with, sampling valve II is arranged near oil water separator, and heat exchanger entrance valve is close
Heat exchanger is arranged.
Further, enter tower tube line to be provided with into tower main valve at the top of ammonia convertor, bottom of ammonia enters and sets on tower tube line
Have into tower pair valve.Enter the gas of tower main valve entrance, into the annular space cooling tower wall between the staving of ammonia convertor and internals, make tower
Temperature is not higher than operating temperature, and such as 120 DEG C, which is entered after the gas mixing that tower pair valve is entered, in tower in catalysis with bottom of towe
Produce ammonia in the presence of agent, reacted gas by tower bottom out.
Cool from ammonia convertor bottom of towe synthesis gas out withdrawer preheated first, further drop by heat exchanger
Temperature, from heat exchanger gas out in syngas cooler by point ammonia for the first time, the gas after being condensed and by pipeline II
The gas for filling into together in gas-liquid separator carries out time condensation and divides ammonia, the gas after secondary point of ammonia to enter circulator, go out
The circulating air of circulator is entered in heat exchanger Jing after oil water separator oil-water separation and is heated up, and is carried out in then passing to ammonia convertor
Ammonia synthesis.And the ammonia cooling withdrawer arranged on the pipeline I parallel with syngas cooler and gas-liquid separator, have separation concurrently
The effect of device, is vented after ammonia cold recovery, and methane content is raised, so emptying amount is reduced, hydrogen, nitrogen losses are few, while entrainment
Ammonia it is few.
Compared with prior art, the invention has the beneficial effects as follows：Device of the present invention, methane emptying in the unit interval
Gas flow is little, and available nitrogen hydrogen utilization rate is high, and device resource utilization of the present invention is high, good economical benefit, if enter tower
Gases methane content be 20%, before improvement (i.e. supplement fresh nitrogen hydrogen into after ammonia synthesis system with separated following for ammonia
Methane gas emptying is set after ring gas mixing) middle methane content 20% of dropping a hint, dropping a hint middle methane content after improvement can
25-28% is brought up to, ammonia average 26% is calculated, improve front 100,000 tons of scales, methane emptying amount is 2250m3/ h, is vented after improvement
Methane content 19-20% or so in gas, emptying total amount can be reduced to 1731mm3/ h, saves nitrogen hydrogen 519m per hour3/ h,
Liquefied ammonia 197kg/h can be increased production, day increases production 4.7 tons, by 2200 yuan/ton of the market price, 1.04 ten thousand yuan of value is saved daily, with 100,000
Ton scale is calculated, and year produces 330 days, can be saved nitrogen hydrogen volume increase 1551 tons of ammonia of synthesis, is worth 3,430,000 yuan.
Description of the drawings
Fig. 1 is apparatus structure schematic diagram of the present invention；
Wherein, 1- QI invigorating valve；2- gas-liquid separators；3- circulators；4- oil water separators；5- atmospheric valves；6- heat exchangers；
7- ammonia convertors；Pre- heat regenerator after 8- towers；9- syngas coolers；10- heat exchanger entrance valves；11- enters tower pair valve；
12- enters tower main valve；13- ammonia cools down withdrawer；14- sampling valves I；15- sampling valves II；16- pipelines I；17- pipelines II.
Specific embodiment
Below in conjunction with the accompanying drawings the present invention is further explained.
As shown in figure 1, methane gas emptying energy saver in a kind of ammonia synthesis circulating air, including ammonia convertor 7, enters tower tube
Line, go out tower tube line, and be sequentially arranged pre- heat regenerator 8, heat exchanger 6, syngas cooler 9 after the tower on tower tube line is gone out
With gas-liquid separator 2, gas-liquid separator 2 is sequentially connected with circulator 3, oil water separator 4, heat exchanger 6 and ammonia synthesis by pipeline
Tower 7, carries out heat exchange by the gaseous mixture for going out the carrying of tower tube line with the gas Jing after oil water separator is separated in heat exchanger 6.
Go out tower tube line and be provided with the pipeline I 16 parallel with syngas cooler 9 and gas-liquid separator 2, pipeline I 16 is provided with ammonia cooling
Withdrawer 13, sampling valve I 14 and atmospheric valve 5.Connecting pipeline on pipeline in the middle of syngas cooler 9 and gas-liquid separator 2
II 17, pipeline II 17 is provided with QI invigorating valve 1, and the pipeline between oil water separator 4 and heat exchanger 6 is provided with sampling valve II 15 and changes
Hot device inlet valve 10, sampling valve II 15 are arranged near oil water separator 4, and heat exchanger entrance valve 10 is arranged near heat exchanger 6,
Sampling valve II 15 be used for detection from oil water separator 4 out, into the inlet tower gas body of ammonia convertor 7.
Heretofore described forward and backward position relationship, to be vented the flow direction of gaseous mixture in energy saver as ginseng
Examine, before the equipment that the equipment that gaseous mixture is first flowed through is flowed through after.
Device of the present invention is explained with reference to a specific production process：
Fresh supplemented gas, Jing after QI invigorating valve 1 is mixed with 9 exit gas of syngas cooler, into gas-liquid separation
Device 2 carries out gas-liquid separation, and gas is forced into 18.0MPa into circulator 3, is separated in gas by oil water separator 4 and is carried secretly
Profit, enter heat exchanger 6 by heat exchanger entrance valve 10,6 are changed with 7 exit gas of ammonia convertor in the heat exchanger
Inlet tower gas temperature is brought up to 100 degree by heat, and Jing enters tower main valve 12 into annular space between 7 cylinder of ammonia convertor and internals all the way
Cooling tower wall, makes not higher than 120 degree of tower temperature, its 7 bottom of ammonia convertor with converge from the gas for entering the secondary entrance of valve 11 of tower, it is laggard
Enter in tower and produce ammonia in the presence of catalyst；Reacted gas by ammonia convertor 7 bottom of towe out, 300～330 after reaction
DEG C gas enter tower after 8 1～1.3MPa of by-product of pre- heat regenerator steam, 205～215 DEG C of gas pre- heat regenerators from after tower
8 outlets out enter heat exchanger 6 afterwards, and temperature is down to 38 DEG C or so in the heat exchanger 6, enters subsequently into syngas cooler 9
One step is condensed, the liquefied ammonia of condensation syngas cooler 9 bottom segregation section by first separation, the gas temperature once divided after ammonia
Degree is down to -10 DEG C or so and converges into gas-liquid separator 2 and carry out secondary point of ammonia with gas is supplemented, and the gas after secondary point of ammonia is entered and followed
Next circulation is entered after ring machine 3.On the pipeline I 16 parallel with syngas cooler 9, gas-liquid separator 2, the cooling of Jing ammonia
After withdrawer 13, it is vented by atmospheric valve 5, while middle gas content of dropping a hint, I 16 gas of pipeline can be detected by sampling valve I 14
Amount is little, and ammonia cooling withdrawer 13 has the effect of separator concurrently.Methane gas after emptying is entered and carries hydrogen production device, hydrogen reuse, methane
Burning byproduct steam is carried out into combustion furnace, tail gas is up to standard to be applied.
Atmospheric valve 5 is arranged such, and is vented compared with after heat exchanger 6, before syngas cooler 9, can reduce and drop a hint
The ammonia of middle entrainment, often produces 1 ton of ammonia and can reduce ammonia loss 16kg.
Claims (7)
1. methane gas emptying energy saver in a kind of ammonia synthesis circulating air, including ammonia convertor (7), enters tower tube line and goes out tower tube
Line, and the syngas cooler (9) being arranged on out on tower tube line, it is characterised in that it is described go out tower tube line be arranged on ammino
Into tower (7) bottom, it is described enter tower tube line include that top enters tower tube line and bottom enters tower tube line；Go out tower tube line to be provided with and synthesis gas
The parallel pipeline I (16) of body cooler (9), pipeline I (16) are provided with ammonia cooling withdrawer (13), sampling valve I (14) and emptying
Valve (5), the go out tower tube line parallel with pipeline I are provided with gas-liquid separator (2)；Go out ammonia convertor (7) and synthesis gas on tower tube line
Pre- heat regenerator (8) and heat exchanger (6) after tower is provided between body cooler (9), and gas-liquid separator (2) is connected successively by pipeline afterwards
Circulator (3), oil water separator (4), heat exchanger (6) is connect, heat exchanger (6) is respectively communicated to ammonia convertor (7) by pipeline
Top enters tower tube line and bottom enters tower tube line.
2. in ammonia synthesis circulating air according to claim 1, methane gas is vented energy saver, it is characterised in that the gas
After liquid/gas separator (2) is arranged on syngas cooler (9).
3. in ammonia synthesis circulating air according to claim 1 and 2, methane gas is vented energy saver, it is characterised in that institute
State and on the pipeline between syngas cooler (9) and gas-liquid separator (2), be connected with pipeline II (17), set on pipeline II (17)
There is QI invigorating valve (1).
4. in ammonia synthesis circulating air according to claim 1 and 2, methane gas is vented energy saver, it is characterised in that change
Hot device (6) are arranged on after tower after pre- heat regenerator (8).
5. in ammonia synthesis circulating air according to claim 1 and 2, methane gas is vented energy saver, it is characterised in that oil
Pipeline between water separator (4) and heat exchanger (6) is provided with heat exchanger entrance valve (10) and sampling valve II (15).
6. in ammonia synthesis circulating air according to claim 1 and 2, methane gas is vented energy saver, it is characterised in that take
Sample valve II (15) is arranged near oil water separator (4), and heat exchanger entrance valve (10) is arranged near heat exchanger (6).
7. in ammonia synthesis circulating air according to claim 1 and 2, methane gas is vented energy saver, it is characterised in that ammonia
Enter tower tube line to be provided with into tower main valve (12) at the top of synthetic tower (7), ammonia convertor (7) bottom enters tower tube line and is provided with into tower pair valve
(11)。
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510616687.6A CN105271304B (en) | 2015-09-24 | 2015-09-24 | Energy saving apparatus for emptying methane gas in ammonia synthesis circulation gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510616687.6A CN105271304B (en) | 2015-09-24 | 2015-09-24 | Energy saving apparatus for emptying methane gas in ammonia synthesis circulation gas |
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| Publication Number | Publication Date |
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| CN105271304A CN105271304A (en) | 2016-01-27 |
| CN105271304B true CN105271304B (en) | 2017-03-22 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201510616687.6A Active CN105271304B (en) | 2015-09-24 | 2015-09-24 | Energy saving apparatus for emptying methane gas in ammonia synthesis circulation gas |
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Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| RU2261225C2 (en) * | 2000-03-03 | 2005-09-27 | Проусесс Менеджмент Энтерпрайсиз Лтд. | Method of ammonia synthesis and an installation used for the purpose |
| CN102502704B (en) * | 2011-09-30 | 2013-06-05 | 刘军 | Recovery method of ammonia from vent gas during ammonia synthesis |
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Denomination of invention: Energy saving device for venting methane gas in ammonia synthesis circulating gas Effective date of registration: 20211201 Granted publication date: 20170322 Pledgee: Linshu sub branch of Linshang Bank Co.,Ltd. Pledgor: SHANDONG JINYIMENG ECOLOGICAL FERTILIZER Co.,Ltd. Registration number: Y2021980013601 |
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