CN209143713U - Synthesis ammonia system is dropped a hint middle gas ammonia and hydrogen retrieval system - Google Patents
Synthesis ammonia system is dropped a hint middle gas ammonia and hydrogen retrieval system Download PDFInfo
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- CN209143713U CN209143713U CN201821786021.0U CN201821786021U CN209143713U CN 209143713 U CN209143713 U CN 209143713U CN 201821786021 U CN201821786021 U CN 201821786021U CN 209143713 U CN209143713 U CN 209143713U
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- ammonia
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- ammonic washing
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- pressure ammonic
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Abstract
It drops a hint middle gas ammonia and hydrogen retrieval system the utility model discloses a kind of synthesis ammonia system, flash steam from liquid ammonia ball tank and ammonia vehicle enters from the lower inlet of low pressure Ammonic washing tower, the top desalination water inlet of low pressure Ammonic washing tower compresses and washes ammonia pump with height and is connected, periodic off-gases from synthesis system enter from the first high pressure Ammonic washing tower lower gas import, the top gas outlet of first high pressure Ammonic washing tower is connected with the gas feed of the second high pressure Ammonic washing tower lower part, the top desalination water inlet of second high pressure Ammonic washing tower compresses and washes ammonia pump with height and is connected, the tower bottom of second high pressure Ammonic washing tower washes ammonium hydroxide outlet and is connected with the top water inlet of the first high pressure Ammonic washing tower, the cold side import of feed gas chiller is connected with the cold side outlet port of ammonia cooler, the hot side outlet of feed gas chiller is connected with desalination water pot；The hot side import of ammonia cooler is connected with desalting pipe, and the cold side import of ammonia cooler is connected with liquefied ammonia pipeline；The bottom ammonium hydroxide of first high pressure Ammonic washing tower enters low pressure Ammonic washing tower by recirculation cooler.
Description
Technical field
It drops a hint middle gas ammonia and hydrogen retrieval system the utility model relates to a kind of synthesis ammonia system, belongs to Chemical Manufacture neck
Domain.
Background technique
Synthesis ammonia is the pillar industries of the national economy, and it is the first that yield occupies various chemical products, while being also that energy consumption is big
Family, about 10% energy is for synthesizing ammonia in the world.As the energy, environment Double jeopardy increasingly sharpen, synthesis ammonia dress
The energy-saving and emission-reduction set are imperative.
The hydrogen ammonia reclaiming process of the periodic off-gases of synthesis ammonia is to be carried out washing ammonia respectively to periodic off-gases with high pressure Ammonic washing tower at present, low
The ammonia flashed vapour that pressure Ammonic washing tower comes out liquid ammonia storage tank, liquefied ammonia letdown tank and liquid ammonia ball tank carries out washing ammonia, speeds to put after washing ammonia
Gas is entered cooler and is cooled down using recirculated water, and the saturated water and mist in periodic off-gases enter separator after supercooling and separate
Moisture preheats subsequently into preheater, finally enters H2/N2Membrane separator, the H2/N2The hydrogen that membrane separator is separated
Compressibility is removed, the nitrogen and hydrogen mixture not being completely separated removes fuel pipe network.
The concentration of the weak aqua ammonia come out from high pressure Ammonic washing tower is 7-9%, the concentration point for the weak aqua ammonia that low pressure Ammonic washing tower comes out
Not Wei 10% or so, weak aqua ammonia concentration is too low, can not directly take out.Current way is will to come out again from high pressure Ammonic washing tower
It weak aqua ammonia and it is sent into ammonia steaming system together from the weak aqua ammonia that low pressure Ammonic washing tower comes out is distilled to recover ammonia, the liquefied ammonia of recycling goes to store up
Slot, this needs to consume a large amount of steam, causes operating cost high, is unfavorable for energy-saving and emission-reduction.
We improve thus, and desalted water becomes weak aqua ammonia after washing the gas ammonia in periodic off-gases in high pressure Ammonic washing tower,
Weak aqua ammonia concentration is in 10-12% or so, and by entering the import of recirculation cooler after Liquid level adjusting valve, ammonium hydroxide passes through circulating cooling
Enter after device is cooling from the middle part of low pressure Ammonic washing tower, ammonium hydroxide continues to absorb the gas ammonia come from liquid ammonia ball tank and ammonia vehicle in tower, low
Ammonia concn in pressure Ammonic washing tower maintains 18-25% or so, and ammonium hydroxide is washed after coming out from the bottom of low pressure Ammonic washing tower into low pressure
Ammonia pump, ammonium hydroxide wash ammonia pump pressurization rear portion by low pressure and enter recirculation cooler and be recycled, and a part of ammonium hydroxide passes through
Ammonia vessel is sent to after flowmeter and flow control valve to be stored.A field sampling analysis is provided on ammonium hydroxide pipeline
Point, for being periodically sampled and analyzing to ammonia concn.
Find that the system still remains following problems in use:
(1), since the ammonium hydroxide that low pressure Ammonic washing tower comes out is taken out as product, so being wanted according to purchase producer
It asks, ammonia concn must be maintained at 20~21%, and ammonia concn < 20%, then ammonium hydroxide product can not be taken out.Normal production
In the case of, for the weak aqua ammonia concentration come out from high pressure Ammonic washing tower bottom 10~12% or so, weak aqua ammonia enters low pressure Ammonic washing tower again
Secondary to be washed with flashed vapour being discharged when filling ammonia from liquid ammonia ball tank and ammonia vehicle, the concentration of such weak aqua ammonia is entirely capable of reaching purchase
Buy the requirement of producer.But reduced if taking out liquefied ammonia, the flash distillation tolerance being discharged when filling ammonia from ammonia vehicle is greatly reduced, this just makes
The requirement of purchase producer is not achieved at the weak aqua ammonia concentration that low pressure Ammonic washing tower exports, weak aqua ammonia product design index is unqualified,
The reduction of income from sales is directly contributed, while also increasing the production cost of processing weak aqua ammonia.
(2), when high pressure Ammonic washing tower stops release, if the flashed vapour of spherical tank and ammonia vehicle also needs to be discharged into low pressure and washes ammonia at this time
Tower carries out washing absorption, the normal operation that must just maintain low pressure Ammonic washing tower to produce, and the operating pressure control of low pressure Ammonic washing tower exists
1.2MPa left and right.Due to the parking pressure release of high pressure Ammonic washing tower, cause in the ammonium hydroxide recharge to high pressure Ammonic washing tower in low pressure Ammonic washing tower, when
After being filled in high pressure Ammonic washing tower by ammonium hydroxide, ammonium hydroxide meeting overflow can damage H to subsequent handling when serious2/N2Film in membrane separator
Pipe, causes serious safety accident and production accident.
(3) when summer temperature is high, the upper coolant-temperature gage of recirculated water comes out at the top of high pressure Ammonic washing tower at 30 DEG C or so
Periodic off-gases temperature is at 28 DEG C or so, and at this moment periodic off-gases enter feed gas chiller, and the temperature of periodic off-gases not only cannot be by recirculated water
Cooling, is also heated by recirculated water, saturated water and mist in periodic off-gases is caused to be unable to get effective refrigerated separation, serious prestige
Coerce the operational safety of subsequent handling membrane separator.
Utility model content
In view of the above technical problems, the utility model is intended to provide a kind of synthesis ammonia system and drops a hint middle gas ammonia and hydrogen retrieval
System guarantees the continual and steady concentration for reaching customer requirement of ammonium hydroxide product, ammonium hydroxide is avoided to flow back to high pressure Ammonic washing tower, reduces life
To H in production2/N2It is endangered caused by membrane separator, solves the problems, such as the cooling of periodic off-gases.
For this purpose, middle gas ammonia and hydrogen retrieval the technology employed by the present utility model is a kind of synthesis ammonia system is dropped a hint
System, including high pressure Ammonic washing tower, low pressure Ammonic washing tower, feed gas chiller, periodic off-gases separator, raw material hot-air heater and H2/N2Film
Separator, the flash steam from liquid ammonia ball tank and ammonia vehicle enter from the lower inlet of low pressure Ammonic washing tower, the low pressure Ammonic washing tower
Desalination water inlet in top compresses and washes ammonia pump with height and is connected, it is characterised in that: the high pressure Ammonic washing tower include the first high pressure Ammonic washing tower and
Second high pressure Ammonic washing tower, the periodic off-gases from synthesis system enter from the first high pressure Ammonic washing tower lower gas import, and described first
The top gas outlet of high pressure Ammonic washing tower is connected with the gas feed of the second high pressure Ammonic washing tower lower part, the second high pressure Ammonic washing tower
Top desalination water inlet compress and wash ammonia pump with the height and be connected, the tower bottom of the second high pressure Ammonic washing tower washes ammonium hydroxide outlet and first
The top water inlet of high pressure Ammonic washing tower is connected, top gas outlet and the feed gas chiller of the second high pressure Ammonic washing tower
Hot side import be connected, the cold side outlet port of the feed gas chiller is connected with the periodic off-gases separator, the periodic off-gases divide
It is connected from the gas vent of device with the raw material hot-air heater, the gas vent and the H of the raw material hot-air heater2/N2Film point
It is connected from device, the cold side import of the feed gas chiller is connected with the cold side outlet port of ammonia cooler, the feed gas chiller
Hot side outlet be connected with desalination water pot；
The hot side import of the ammonia cooler is connected with desalting pipe, the cold side import and liquefied ammonia pipeline of the ammonia cooler
It is connected, the hot side outlet of the ammonia cooler connects gas ammonia pipeline；
The bottom ammonium hydroxide outlet line of the first high pressure Ammonic washing tower is connected with recirculation cooler, and first height compresses and washes ammonia
Liquid level adjusting valve and check-valves, the ammonium hydroxide outlet of the recirculation cooler and low pressure are provided on the bottom ammonium hydroxide outlet line of tower
The centre inlet of Ammonic washing tower is connected, and the bottom weak aqua ammonia outlet of the low pressure Ammonic washing tower washes ammonia pump with low pressure and is connected, the low pressure
Ammonia pump is washed to be connected with ammonia vessel and recirculation cooler.
Periodic off-gases from synthesis system initially enter the first high pressure Ammonic washing tower, with dilute ammonia from the second high pressure Ammonic washing tower
Water carries out counter current contacting washing in tower, and periodic off-gases enter the second height after coming out from the top of the first high pressure Ammonic washing tower and compress and wash ammonia
Tower, the desalted water for compressing and washing ammonia pump from height enter from the top of the second high pressure Ammonic washing tower, and desalted water and periodic off-gases carry out in tower
Counter current contacting washing, the periodic off-gases after washing twice are gone out at the top of the second high pressure Ammonic washing tower.Weak aqua ammonia is high from second
Pressure Ammonic washing tower bottom come out after be sent to the first high pressure Ammonic washing tower continue to periodic off-gases carry out washing absorption, weak aqua ammonia finally from
The bottom of first high pressure Ammonic washing tower come out after be sent to low pressure Ammonic washing tower continue using.
Cooling (cooling to 8-10 DEG C) is carried out to desalted water using liquefied ammonia, then desalted water after cooling is transported to unstripped gas
For cooler for cooling down periodic off-gases, periodic off-gases carry out water separation subsequently into periodic off-gases separator, the periodic off-gases after separating water into
Enter raw material hot-air heater to be heated, the periodic off-gases after heating enter H2/N2Membrane separator separates hydrogen.Hydrogen after separation returns
Compression set utilizes, and the gas after separating hydrogen goes fuel system to burn.
Desalination water pot is removed after the cooling periodic off-gases of desalted water.It is provided on the bottom ammonium hydroxide outlet line of first high pressure Ammonic washing tower
Liquid level adjusting valve and check-valves avoid the ammonium hydroxide in low pressure Ammonic washing tower from returning in high pressure Ammonic washing tower.
The ammonium hydroxide of first high pressure Ammonic washing tower enters after recirculation cooler is cooling from the middle part of low pressure Ammonic washing tower, and ammonium hydroxide exists
Continue to absorb the gas ammonia from the next flash steam of liquid ammonia ball tank and ammonia vehicle in tower, ammonium hydroxide enters after coming out from the bottom of low pressure Ammonic washing tower
Low pressure washes ammonia pump, and ammonium hydroxide, which by low pressure washes ammonia pump pressurization rear portion and enters recirculation cooler, to be recycled, a part of ammonia
Water is stored by being sent to Ammonia vessel after flowmeter and flow control valve.A field sampling is provided on ammonium hydroxide pipeline
Analysis site, for being periodically sampled and analyzing to ammonia concn.
Originally the ammonia concn come out from high pressure Ammonic washing tower washes ammonia stream 10~12% or so, by series connection is improved
Journey, the ammonia concn come out from the first high pressure Ammonic washing tower can be improved to 15~18% or so, even if in the reduction of ammonia vehicle flashed vapour
In the case of, the ammonia concn come out from low pressure Ammonic washing tower can also reach 20~21%, and meet purchase producer and requires, the product of ammonium hydroxide
Quality is guaranteed.
In above scheme: the tower bottom of the second high pressure Ammonic washing tower wash ammonium hydroxide outlet and the top of the first high pressure Ammonic washing tower into
Force (forcing) pump is provided on the connected pipeline in the mouth of a river.
In above scheme: the low pressure, which is washed on the pipeline that ammonia pump is connected with ammonia vessel, is provided with flowmeter and flow adjusting
Valve.
The utility model has the advantages that the ammonia concn that the improved system of the utility model can continue to guarantee that low pressure Ammonic washing tower comes out reaches
20~21%, meet the needs of client, the ammonium hydroxide in low pressure Ammonic washing tower is avoided to blow back into high pressure Ammonic washing tower, having prevented ammonium hydroxide may
It is endangered into membrane separator bring, the problem of summer of having determined can not cool down periodic off-gases due to circulating water temperature height.
Detailed description of the invention
Fig. 1 is the process flow chart of the utility model.
Specific embodiment
By way of example and in conjunction with the accompanying drawings, the utility model is described in further detail:
Embodiment 1, as shown in Figure 1, synthesis ammonia system is dropped a hint, middle gas ammonia and hydrogen retrieval system are by the first high pressure Ammonic washing tower
1, the second high pressure Ammonic washing tower 2, low pressure Ammonic washing tower 3, feed gas chiller 4, periodic off-gases separator 5, feed gas separator 6, H2/N2
Membrane separator 7, height compress and wash ammonia pump 8, desalination water pot 9, ammonia cooler 10, recirculation cooler 11, low pressure and wash ammonia pump 12, ammonia vessel
13, force (forcing) pump 14, Liquid level adjusting valve 16, flowmeter 16, flow control valve 17 and check-valves 18 form.
Periodic off-gases from synthesis system enter from the 1 lower gas import of the first high pressure Ammonic washing tower, the first high pressure Ammonic washing tower 1
Top gas outlet be connected with the gas feed of 2 lower part of the second high pressure Ammonic washing tower, the top desalted water of the second high pressure Ammonic washing tower 2
Import compresses and washes ammonia pump 8 with height and is connected, and the tower bottom of the second high pressure Ammonic washing tower 2 washes the top of ammonium hydroxide outlet and the first high pressure Ammonic washing tower 1
Water inlet is connected, and the tower bottom of the second high pressure Ammonic washing tower 2 washes what ammonium hydroxide outlet was connected with the top water inlet of the first high pressure Ammonic washing tower 1
Force (forcing) pump 14 is provided on pipeline.
The top gas outlet of second high pressure Ammonic washing tower 2 is connected with the hot side import of feed gas chiller 4, raw material air cooling
The cold side outlet port of device 4 is connected with periodic off-gases separator 5, and the gas vent of periodic off-gases separator 5 is connected with raw material hot-air heater 6,
The gas vent and H of raw material hot-air heater 62/N2Membrane separator 7 is connected, the cold side import and ammonia cooler of feed gas chiller 4
10 cold side outlet port is connected, and the hot side outlet of feed gas chiller 10 is connected with desalination water pot 9, and the water in desalination water pot 9 passes through
Height compresses and washes ammonia pump 8 and is extracted into the second high pressure Ammonic washing tower 2 and low pressure Ammonic washing tower 3.
The hot side import of ammonia cooler 10 is connected with desalting pipe, cold side import and the liquefied ammonia pipeline phase of ammonia cooler 10
Even, the hot side outlet of ammonia cooler 10 connects gas ammonia pipeline
The bottom ammonium hydroxide outlet line of first high pressure Ammonic washing tower 1 is connected with recirculation cooler 11, the first high pressure Ammonic washing tower 1
Liquid level adjusting valve 15 and check-valves 18 are provided on the ammonium hydroxide outlet line of bottom, the ammonium hydroxide outlet of recirculation cooler 11 is washed with low pressure
The centre inlet of ammonia tower 3 is connected, and the flash steam from liquid ammonia ball tank and ammonia vehicle enters from the lower inlet of low pressure Ammonic washing tower 3, low
The top desalination water inlet of pressure Ammonic washing tower 3 compresses and washes ammonia pump 8 with height and is connected, the bottom weak aqua ammonia outlet of low pressure Ammonic washing tower 3 and low pressure
It washes ammonia pump 12 to be connected, low pressure washes ammonia pump 12 and is connected with ammonia vessel 13 and recirculation cooler 11.Low pressure washes ammonia pump 12 and ammonia vessel 13
Flowmeter 16 and flow control valve 17 are provided on connected pipeline.
The utility model is not limited to the above embodiment, it will be understood by those skilled in the art that: do not departing from this
A variety of change, modification, replacement and modification, this reality can be carried out to these embodiments in the case where the principle and objective of utility model
It is defined by the claims and their equivalents with novel range.
Claims (3)
- Middle gas ammonia and hydrogen retrieval system 1. a kind of synthesis ammonia system is dropped a hint, including high pressure Ammonic washing tower, low pressure Ammonic washing tower, unstripped gas Cooler, periodic off-gases separator, raw material hot-air heater and H2/N2Membrane separator, the flash steam from liquid ammonia ball tank and ammonia vehicle is from low The lower inlet of Ammonic washing tower is pressed to enter, the top desalination water inlet of the low pressure Ammonic washing tower compresses and washes ammonia pump with height and is connected, feature Be: the high pressure Ammonic washing tower include the first high pressure Ammonic washing tower and the second high pressure Ammonic washing tower, the periodic off-gases from synthesis system from First high pressure Ammonic washing tower lower gas import enters, and ammonia is compressed and washed with the second height in the top gas outlet of the first high pressure Ammonic washing tower The gas feed of tower lower part is connected, and the top desalination water inlet of the second high pressure Ammonic washing tower compresses and washes ammonia pump with the height and is connected, The tower bottom of the second high pressure Ammonic washing tower washes ammonium hydroxide outlet and is connected with the top water inlet of the first high pressure Ammonic washing tower, and described second is high The top gas outlet of pressure Ammonic washing tower is connected with the hot side import of the feed gas chiller, the cold side of the feed gas chiller Outlet is connected with the periodic off-gases separator, and the gas vent of the periodic off-gases separator is connected with the raw material hot-air heater, The gas vent and the H of the raw material hot-air heater2/N2Membrane separator be connected, the cold side import of the feed gas chiller with The cold side outlet port of ammonia cooler is connected, and the hot side outlet of the feed gas chiller is connected with desalination water pot；The hot side import of the ammonia cooler is connected with desalting pipe, cold side import and the liquefied ammonia pipeline phase of the ammonia cooler Even, the hot side outlet of the ammonia cooler connects gas ammonia pipeline；The bottom ammonium hydroxide outlet line of the first high pressure Ammonic washing tower is connected with recirculation cooler, the first high pressure Ammonic washing tower Liquid level adjusting valve and check-valves are provided on the ammonium hydroxide outlet line of bottom, ammonia is washed with low pressure in the ammonium hydroxide outlet of the recirculation cooler The centre inlet of tower is connected, and the bottom weak aqua ammonia outlet of the low pressure Ammonic washing tower washes ammonia pump with low pressure and is connected, and the low pressure washes ammonia Pump is connected with ammonia vessel and recirculation cooler.
- 2. synthesis ammonia system is dropped a hint middle gas ammonia and hydrogen retrieval system according to claim 1, it is characterised in that: described second The tower bottom of high pressure Ammonic washing tower washes on the pipeline that ammonium hydroxide outlet is connected with the top water inlet of the first high pressure Ammonic washing tower and is provided with pressurization Pump.
- 3. any one of -2 synthesis ammonia systems are dropped a hint middle gas ammonia and hydrogen retrieval system according to claim 1, it is characterised in that: The low pressure washes on the pipeline that ammonia pump is connected with ammonia vessel and is provided with flowmeter and flow control valve.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201821786021.0U CN209143713U (en) | 2018-10-31 | 2018-10-31 | Synthesis ammonia system is dropped a hint middle gas ammonia and hydrogen retrieval system |
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| CN201821786021.0U CN209143713U (en) | 2018-10-31 | 2018-10-31 | Synthesis ammonia system is dropped a hint middle gas ammonia and hydrogen retrieval system |
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| CN209143713U true CN209143713U (en) | 2019-07-23 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113697772A (en) * | 2021-09-30 | 2021-11-26 | 杭州冰冷科技有限公司 | System and process method for recovering hydrogen and ammonia in synthetic ammonia purge gas |
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2018
- 2018-10-31 CN CN201821786021.0U patent/CN209143713U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113697772A (en) * | 2021-09-30 | 2021-11-26 | 杭州冰冷科技有限公司 | System and process method for recovering hydrogen and ammonia in synthetic ammonia purge gas |
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