CN103214009A - Synthesis ammonia decarburization technology - Google Patents

Synthesis ammonia decarburization technology Download PDF

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CN103214009A
CN103214009A CN2013100952880A CN201310095288A CN103214009A CN 103214009 A CN103214009 A CN 103214009A CN 2013100952880 A CN2013100952880 A CN 2013100952880A CN 201310095288 A CN201310095288 A CN 201310095288A CN 103214009 A CN103214009 A CN 103214009A
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tower
solution
gas
flash
section
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CN103214009B (en
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吴婷婷
陈建华
顾英
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Sinopec Engineering Group Co Ltd
Sinopec Ningbo Engineering Co Ltd
Sinopec Ningbo Technology Research Institute
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Sinopec Engineering Group Co Ltd
Sinopec Ningbo Engineering Co Ltd
Sinopec Ningbo Technology Research Institute
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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
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Abstract

The present invention relates to a synthesis ammonia decarbonization process, comprising the steps of: sending a converting gas from upstream process after heat exchanging into a CO2 absorber, countercurrent contacting with a barren solution and a semi-barren solution into the CO2 absorber to remove carbon dioxide, outputting purified gas which is subjected to gas-liquid separation and then fed into a demethanation furnace, feeding a pregnant solution out of the tower bottom of the CO2 absorber after heat exchanging into a pregnant solution flash tower for a first grade flash, flashing off most of H2 and CO, feeding the flashed pregnant solution from the pregnant solution flash tower into a flash section of a CO2 regeneration tower for second grade flash, discharging the gas phase from the top of the flash tower, feeding the liquid phase into a gas stripping section of the CO2 regeneration tower for further desorption and regeneration to form a semi-barren solution, feeding the semi-barren solution into a reboiler (2) at the CO2 regeneration tower bottom to exchange heat with the converting gas and boiling to form a barren solution, sending out from the bottom of the gas stripping section and feeding into the upper section of the CO2 absorber. Compared with the prior art, the decarburization technology is good in decarburization effects, the hydrogen content in the CO2 product is reduced to 0.5% or less, the heat in the process can be used fully, and the energy-saving and cost-reducing effects are good.

Description

A kind of synthetic ammonia decarbonization process
Technical field
The present invention relates to the chemical technique field, specifically refer to a kind of synthetic ammonia decarbonization process.
Background technology
Hot potassium carbonate technology (Hot potassium carbonate process) is widely used in the world a kind of carbon dioxide de eliminating method.In hot potassium carbonate technology, the reaction of solution of potassium carbonate absorbing carbon dioxide generates saleratus; CO 2Absorption process in wet chemical is a kind of reversible reaction.The regeneration of solution then is with the potassium bicarbonate solution thermal degradation of absorbing carbon dioxide, release of carbon dioxide regeneration salt of wormwood.Reaction equation is as follows:
CO 2+ K 2CO 3+ H 2O ← → 2KHCO 3+ Q formula (1)
Because this reaction is carried out very slowly, must add some material and as activator katalysis be played in reaction, increases substantially the receptivity of the rate of mass transfer and the solution of reaction process.Modal activator is an organic amine.Organic amine quickens hot potassium carbonate and absorbs CO 2Mechanism be:
At first, CO 2Form mixture with the organic amine reaction:
CO 2+ RR ˊ NH → RR ˊ NCOO -+ H +Formula (2)
The mixture hydrolysis that forms:
RR ˊ NHCOO -+ H 2O ← → HCO 3 -+ RR ˊ NH formula (3)
The ion transient equilibrium:
H ++ OH -← → H 2O formula (4)
In above reaction mechanism, the speed of reaction of formula (3) is the slowest, and in other words the controlled step of organic amine absorption CO2 reaction is the hydrolysis reaction of carbamate.The organic amine activator of early development, in the aqueous solution, form comparatively stable carbaminate because of it as diethanolamine with bicarbonate radical, its hydrolysis reaction (3) can not carry out rapidly, organic amine is consumed the generation carbaminate in closing on the reaction zone at interface, causes the decline of effective activator concentration and the reduction of katalysis.
Traditional hot potash method, actual according to operation for many years, the purified synthesis gas degree is not high, and solution regeneration degree is bad, improves and produces difficulty of load.At the existing device for modifying that needs, because the design capacity of key equipments such as absorption tower, regenerator column and tower bottom reboiler is little, then need the equipment that increases more if change the MDEA decarbonization process into, investment for trnasforming urban land is big, and be subjected to the restriction of existing installation, pipeline etc., change MDEA into after effect not obvious.
Summary of the invention
Technical problem to be solved by this invention is that the present situation at prior art provides a kind of CO 2The synthetic ammonia decarbonization process that receptivity is strong, solution absorption and mass-transfer efficiency height, energy efficient and degree of purification are high is with activator and decarbonization process.
The present invention solves the problems of the technologies described above the technical scheme that is adopted: this synthetic ammonia decarbonization process is characterized in that comprising the steps:
The conversion gas of 220～240 ℃ of sending here of upstream process, 2～3MPa cools after 170～180 ℃ through quenching water pump water spray, enters CO 2Solution heat exchange at the bottom of regenerator column tower bottom reboiler and the regenerator column is cooled to 125～135 ℃; Enter conversion gas/rich solution interchanger heat exchange and go out the rich solution on absorption tower, temperature is reduced to about 115～120 ℃, after conversion gas boiler feedwater heat exchange temperature is reduced to 70～80 ℃, enters the conversion gas separating device and isolates water of condensation, and gas phase partly enters CO 2Absorb at the bottom of the Tata, at CO 2In the absorption tower and from CO 2The absorption tower top of tower advance tower the 200～210t/h that is added with defoamer lean solution and from CO 2The semi lean solution counter current contact that 1150～1180t/h of tower is advanced at absorption Tata middle part removes carbonic acid gas, CO 2CO in the purified gas that the absorption tower tower top outlet is sent 2Volume content drops to below 0.1%, through CO 2Demethanization stove after the gas-liquid separation of absorption overhead separator;
From CO 2Pressure 2.4～the 2.8MpaG that comes out at the bottom of the absorption Tata, the rich solution that temperature is 110～120 ℃ are through the hydraulic turbine recovered energy, and pressure is reduced to 0.6～1.0MpaG; Enter and send into the rich solution flashing tower after conversion gas/rich solution interchanger heat exchange and carry out the one-level flash distillation, flash off the most of H that is dissolved in the rich solution 2And CO, flash steam enters flash steam washing tower warp from CO 218～the 22m at middle part, absorption tower 3The semi lean solution of/h washes away CO wherein 2After, send the gas ductwork utilization;
Rich solution after the flash distillation of sending from rich solution flashing tower bottom adds defoamer and enters CO 2The flash zone at regenerator column top carries out two-stage flash under 0.04～0.06MpaG pressure, flash off and contain CO 2With the flash steam of water vapour from CO 2The top of regenerator column is sent, through CO 2Enter return tank of top of the tower after the regenerator column condenser condenses, pass through CO again 2Reactor product cooler cooling and CO 2After the washing of washing tower, as CO 2Product is sent;
CO 2The solution that the flash zone on regenerator column top flashes off partly enters CO 2The further desorption and regeneration of the stripping section of regenerator column bottom forms semi lean solution, another part with from CO 2First part's lean solution of sending at the bottom of the regenerator column stripping stage tower is confluxed, and after the semi-leanpump supercharging, enters CO 2The stage casing on absorption tower;
200～210t/h solution enters CO 2Behind the stripping section of regenerator column, at CO 2Boiled the formation lean solution in the regenerator column tower bottom reboiler with after the heat exchange of described conversion gas, sent from the bottom of stripping stage;
Pressure 0.04～0.08MpaG, temperature are about 120 ℃ goes out CO 2The second section lean solution of regenerator column stripping stage through the lean pump pressurization, is cooled to after 68 ℃ through the lean solution water cooler after the cooling of lean solution oiler feed interchanger again, enters CO 2The absorption tower epimere;
From CO 2The first part's lean solution sent at the bottom of the regenerator column stripping stage tower and the throughput ratio of second section lean solution are 5～6:1.
Preferably, described CO 2The absorption tower comprises mutual placed in-line Shang Ta and Xia Ta, and the described tower diameter of going up tower is 2000～2500mm, and the filler in the last tower is divided into three sections, and the height of each section filler is respectively 4500～5000mm, and is provided with liquid distributor between the adjacent packing section; Each section filler comprises highly being epimere and the hypomere of 280～320mm again, and wherein the epimere filler is formed by the Pall ring of the thickness 0.80mm of the stainless steel heap that looses, and described hypomere be that diffusing heap of 50# Pall ring by carbon steel material forms;
Described CO 2The following Tata on absorption tower directly is 3300～3700mm, and the filler of being filled in the following tower also is divided into three sections, and every section packed height is 6500～6800mm, and is provided with liquid distributor between the adjacent packing section; Two sections fillers that are positioned at the top in the following tower are 50# carbon steel Pall ring, and the below packing section is a 50# stainless steel Pall ring.
The setting of filler and sparger can effectively improve flux, reduce pressure drop in the absorption tower, and improves mass-transfer efficiency, reduces CO in the purified gas 2Residual quantity.
Described CO 2Regenerator column is made up of mutual placed in-line Shang Ta and following tower, and wherein, described upward Tata directly is 3000～3300mm, and the filler in the last tower is divided into three sections, every section packed height 6800～7000mm, and be provided with liquid distributor between the adjacent segment; The packing section employing thickness that wherein is positioned at the top is the stainless steel JKB-250Y structured packing of 0.17mm, and the two packing section employing thickness that is positioned at the below is the polypropylene 50# cascade ring of 1.50mm.
CO 2The setting of filler can effectively improve flux, reduce pressure drop in the regenerator column, and improves mass-transfer efficiency, for volume increase creates conditions.
In order to improve the decarburization effect, contain 2.5～3.5wt% in the decarbonizing solution, bulky amine activator, described activator are the mixture of diethanolamine and bulky amine, both weight ratios are 3～5:1.Described decarbonizing liquid is employed washings in the whole flow process, according to the dissolved CO of institute wherein 2The difference of amount is divided into lean solution, semi lean solution and rich solution again.
Preferably, described bulky amine is a 2-amino-2-methyl-1-propanol.
Described structured packing is a metallurgic orifice corrugated packing.
Described liquid distributor is the slotted disc type gas-liquid distributor.The slotted disc type gas-liquid distributor is set between two sections packing layers, plays liquid collecting and the effect that distributes again.Use the dumped packing bracing or strutting arrangement every section filling batch bottom, so that the vapour-liquid convection flow.
Compared with prior art, technical process provided by the present invention has made full use of the heat that is produced in the system and has carried out heat exchange, by the optimization setting of whole network and the rich solution interchanger of setting up, can not only make to be dissolved into 50% above H in the rich solution 2, the CO flash distillation comes out, and utilize from the reboiler rich solution heat exchange that low changing air and absorption tower go out tower of coming out, reduce the load of low changing air oiler feed interchanger on the one hand, guarantee to enter gas temperature≤75 ℃ in the absorption tower, also improve the rich solution temperature on the other hand, helped the flash distillation and the regeneration of solution.The technical process that the application provided is compared to prior art, CO in the purified gas 2Residual quantity is reduced to below the 600ppm from 1000ppm, and the while is owing to the effect of flash distillation, CO 2Hydrogen content is reduced to below 0.5% in the product, and can make full use of the heat in the flow process, and energy conservation and consumption reduction effects is good.
Description of drawings
Fig. 1 is the schema of the embodiment of the invention.
Embodiment
Below in conjunction with Fig. 1 embodiment the present invention is described in further detail.
As shown in Figure 1, employed device structure in this synthetic ammonia decarbonization process under elder generation is introduced:
CO 2Absorption tower 6 comprises placed in-line mutually go up tower 61 and following tower 62, and the tower diameter of last tower is 2300mm, and the filler in the last tower is divided into three sections, and the height of each section filler is 4850mm, and is provided with the liquid distributor (not shown) between the adjacent packing section; Each section filler comprises highly for the epimere of 300mm again and highly is the hypomere of 4550mm; Wherein, the filler of epimere is formed by the Pall ring of the thickness 0.80mm of the stainless steel heap that looses, and the filler of hypomere be that diffusing heap of 50# Pall ring by carbon steel material forms.
CO 2The tower diameter of tower is 3500mm under the absorption tower, and the filler of being filled in the following tower also is divided into three sections, each section packed height be 6650mm, also be provided with the liquid distributor (not shown) between the adjacent packing section; Two sections fillers that are positioned at the top in the following tower are 50# carbon steel Pall ring, and the packing section of below is a 50# stainless steel Pall ring.
CO 2Regenerator column 11 is made up of with following tower 112 the mutual placed in-line tower 111 of going up, and wherein, described upward Tata directly is 3100mm, and the filler in the last tower is divided into three sections, the height 6900mm of each section filler, and be provided with liquid distributor between the adjacent segment; The packing section employing thickness that wherein is positioned at the top is the stainless steel JKB-250Y metal perforated plate corrugated regular filler of 0.17mm, and the two packing section employing thickness that is positioned at the below is the polypropylene 50# cascade ring of 1.50mm.
CO 2Absorption tower and CO 2Employed liquid distributor is the slotted disc type gas-liquid distributor in the regenerator column.
Present embodiment is provided with flashed vapour pressure indication/regulating loop at rich solution flashing tower cat head, and this loop comprises pressure unit, pressure regulator valve and pressure release valve.When tower top pressure reached 0.9MPa (G), pressure is high reported to the police, and opens the pressure release valve pressure release simultaneously; When pressure was 0.9MPa (G), pressure release valve cut out.
Be provided with the liquid level regulating loop at the bottom of the tower of rich solution flashing tower, by the Liquid level adjusting valve on the tower bottom tube line, the level stability at the bottom of the assurance tower.
After the normal operation of device, add activator in the decarbonizing liquid that is contained in advance in the device, the add-on of activator is the 3.wt% of decarbonizing solution weight.Activator in the present embodiment is the mixture of diethanolamine and 2-amino-2-methyl-1-propanol, and both weight ratios are 4:1.Along with the operation of device, decarbonizing liquid and activator all have certain consumption, can the concentration of activator in the decarbonizing liquid be detected, and in time add according to detected result.
Concrete technical process is as follows:
From 230.0 ℃ of low temperature shift converter, the conversion gas of 2.655Mpa G enters this operation, cools to 177 ℃ through quenching water pump 1 water spray, enters CO 2CO at the bottom of the absorption Tata 2Regenerator column reboiler 2 and CO 2Solution heat exchange at the bottom of the regenerator column is cooled to about 132 ℃;
Enter conversion gas/rich solution interchanger 3 heat exchange and go out the rich solution on absorption tower, temperature is reduced to about 118 ℃, reduces to 75 ℃ for water-to-water heat exchanger 4 temperature through the conversion gas boiler, enters CO again after conversion gas separating device 5 is isolated water of condensation 2At the bottom of 6 towers of absorption tower, the semi lean solution counter current contact of advancing the 1166t/h of tower at Ta Nei and the lean solution of the 205t/h that is added with defoamer of advancing tower from top of tower and tower middle part removes carbonic acid gas, makes CO in the tower top outlet purified gas 2Content drops to below 0.1%, through CO 2Demethanization stove after 7 gas-liquid separations of absorption overhead separator;
From CO 2The pressure 2.60MpaG that comes out at the bottom of 6 towers of absorption tower, the about 115 ℃ rich solution of temperature is through water conservancy turbine 8 recovered energies, and pressure is reduced to 0.8MpaG;
Through conversion gas/rich solution interchanger 3, enter rich solution flashing tower 9 and carry out the one-level flash distillation, flash off and be dissolved in the central most of H of rich solution 2And CO, flash steam enters flash steam washing tower 10 warps from CO 2The flow of the stripping tower of absorption tower hypomere is 20m 3The semi lean solution of/h washes away CO wherein 2After, send the gas ductwork utilization;
Rich solution after the flash distillation is delivered to CO after adding defoamer 2The flash zone 111 of regenerator column 11 carries out two-stage flash under 0.05MpaG pressure, flash off CO 2With the flash steam of water vapour from CO 2Regenerator column 11 tops are sent, and enter CO 2Enter return tank of top of the tower 13 after 12 condensations of regenerator column condenser and carry out gas-liquid separation, isolated gas phase enters CO 2Deliver to CO after reactor product cooler 14 coolings 2After washing tower 15 washs once more, as CO 2Product is sent.
CO 2The liquid phase that washing tower 15 bottoms are sent is through the 2nd CO 2 Regenerator reflux pump 16 is sent return tank of top of the tower 13 back to.
The liquid phase of sending from return tank of top of the tower 13 bottoms is through a CO 2Regenerator reflux pump 17CO 2Send into CO from the top of regenerator column 11 2Regenerator column recycles.
CO 2Be divided into two portions after the part solution that the regenerator column epimere flashes off goes out tower, a part enters CO 2The further desorption and regeneration of the stripping section of regenerator column hypomere forms semi lean solution; About 205t/h solution enters CO 2Behind the regenerator column 11 hypomere stripping sections, the liquid phase that flows at the bottom of the tower is introduced into CO 2Send after boiling the formation lean solution in the regenerator column reboiler 2.The lean solution that goes out stripping stage also is divided into first part and second section.
Another part semi lean solution that goes out flash zone can flow with first part's lean solution of sending from the stripping stage bottom, after semi-leanpump 18 superchargings, enters CO 2The stage casing on absorption tower 6;
Go out the about 120 ℃ second section lean solution of pressure 0.06MpaG, the temperature of stripping stage after 19 coolings of lean solution oiler feed interchanger,, be cooled to after 68 ℃ through lean solution water cooler 21 again, enter CO through lean pump 20 pressurizations 2The absorption tower epimere is as washings.
In the present embodiment, at CO 2The desalting pipe 22 that adds a DN40 on the washing tower washing water inlet pipe is at CO 2The washing tower moisturizing can moisturizing in technology in time, can also reduce the loss of activator in the decarbonizing liquid.
The control situation of several Control point is as follows in the technology:
A. go into absorption tower conversion temperature degree: 75 ℃, control by the water yield of adjusting low changing air oiler feed interchanger.
B. go into absorption tower lean solution temperature: 68 ℃, control by the quantity of circulating water of adjusting the lean solution water cooler.
C. go into absorption tower lean solution flow: 205t/h, adjust the lean pump rate of discharge by the variable valve group.
D. go into absorption tower semi lean solution flow: 1166t/h, adjust the pump discharge flow by the variable valve group.
E. flashing tower tower top pressure: 0.8MpaG adjusts the aperture of variable valve and controls by the pressure self-adjusting loop.
F. regenerator column tower top pressure: gauge pressure 0.05MpaG adjusts the aperture of variable valve and controls by the pressure self-adjusting loop.
G. the each point liquid level is by liquid level self-regulated loop control.
H. lean solution regeneration degree: fc=0.25 is by adjusting the heat of supplying with conversion gas boiling device at the bottom of the regenerator column, to guarantee solution regeneration quality.
I. salt of wormwood, activator, inhibiter are analyzed on time, quantitatively replenish according to analytical results.

Claims (7)

1. a synthetic ammonia decarbonization process is characterized in that comprising the steps:
The conversion gas of 220～240 ℃ of sending here of upstream process, 2～3MPa cools after 170～180 ℃ through quenching water pump (1) water spray, enters CO 2Regenerator column tower bottom reboiler (2) and solution heat exchange at the bottom of the regenerator column are cooled to 125～135 ℃; Enter conversion gas/rich solution interchanger (3) heat exchange and go out the rich solution on absorption tower, temperature is reduced to about 115～120 ℃, after the conversion gas boiler reduces to 70～80 ℃ for water-to-water heat exchanger (4) temperature, enter conversion gas separating device (5) and isolate water of condensation, gas phase partly enters CO 2At the bottom of the tower of absorption tower (6), at CO 2In the absorption tower and from CO 2The absorption tower top of tower advance tower the 200～210t/h that is added with defoamer lean solution and from CO 2The semi lean solution counter current contact that 1150～1180t/h of tower is advanced at absorption Tata middle part removes carbonic acid gas, CO 2CO in the purified gas that the absorption tower tower top outlet is sent 2Volume content drops to below 0.1%, through CO 2Demethanization stove after the gas-liquid separation of absorption overhead separator (7);
From CO 2The rich solution that the pressure 2.4～2.8MpaG that comes out at the bottom of the tower of absorption tower (6), temperature are 110～120 ℃ is through hydraulic turbine (8) recovered energy, and pressure is reduced to 0.6～1.0MpaG; Enter and send into rich solution flashing tower (9) after conversion gas/rich solution interchanger (3) heat exchange and carry out the one-level flash distillation, flash off the most of H that is dissolved in the rich solution 2And CO, flash steam enters flash steam washing tower (10) warp from CO 218～the 22m at middle part, absorption tower 3The semi lean solution of/h washes away CO wherein 2After, send the gas ductwork utilization;
Rich solution after the flash distillation of sending from rich solution flashing tower (9) bottom adds defoamer and enters CO 2The flash zone at regenerator column (11) top carries out two-stage flash under 0.04～0.06MpaG pressure, flash off and contain CO 2With the flash steam of water vapour from CO 2The top of regenerator column (11) is sent, through CO 2Enter return tank of top of the tower (13) after regenerator column condenser (12) condensation, pass through CO again 2Reactor product cooler (14) cooling and CO 2After the washing of washing tower (15), as CO 2Product is sent;
CO 2The solution that the flash zone on regenerator column (11) top flashes off partly enters CO 2The further desorption and regeneration of the stripping section of regenerator column (11) bottom forms semi lean solution, another part with from CO 2First part's lean solution of sending at the bottom of regenerator column (11) the stripping stage tower is confluxed, and after semi-leanpump (18) supercharging, enters CO 2The stage casing on absorption tower (6);
200～210t/h solution enters CO 2Behind the stripping section of regenerator column (12), at CO 2Boiled the formation lean solution in the regenerator column tower bottom reboiler (2) with after the heat exchange of described conversion gas, sent from the bottom of stripping stage;
Pressure 0.04～0.08MpaG, temperature are about 120 ℃ goes out CO 2The second section lean solution of regenerator column (11) stripping stage after lean solution oiler feed interchanger (21) cooling, through lean pump (22) pressurization, again through lean solution water cooler cold (23) but after 68 ℃, enter CO 2The absorption tower epimere;
From CO 2The first part's lean solution sent at the bottom of regenerator column (11) the stripping stage tower and the throughput ratio of second section lean solution are 5～6:1.
2. synthetic ammonia decarbonization process according to claim 1 is characterized in that: described CO 2The absorption tower comprises mutual placed in-line Shang Ta and Xia Ta, and the described tower diameter of going up tower is 2000～2500mm, and the filler in the last tower is divided into three sections, and the height of each section filler is respectively 4500～5000mm, and is provided with liquid distributor between the adjacent packing section; Each section filler comprises highly being epimere and the hypomere of 280～320mm again, and wherein the epimere filler is formed by the Pall ring of the thickness 0.80mm of the stainless steel heap that looses, and described hypomere be that diffusing heap of 50# Pall ring by carbon steel material forms;
Described CO 2The following Tata on absorption tower directly is 3300～3700mm, and the filler of being filled in the following tower also is divided into three sections, and every section packed height is 6500～6800mm, and is provided with liquid distributor between the adjacent packing section; Two sections fillers that are positioned at the top in the following tower are 50# carbon steel Pall ring, and the below packing section is a 50# stainless steel Pall ring.
3. synthetic ammonia decarbonization process according to claim 1 and 2 is characterized in that: described CO 2Regenerator column is made up of mutual placed in-line Shang Ta and following tower, and wherein, described upward Tata directly is 3000～3300mm, and the filler in the last tower is divided into three sections, every section packed height 6800～7000mm, and be provided with liquid distributor between the adjacent segment; The packing section employing thickness that wherein is positioned at the top is the stainless steel JKB-250Y structured packing of 0.17mm, and the two packing section employing thickness that is positioned at the below is the polypropylene 50# cascade ring of 1.50mm.
4. synthetic ammonia decarbonization process according to claim 3 is characterized in that: contain 2.5～3.5wt% in the decarbonizing solution, bulky amine activator, described activator are the mixture of diethanolamine and bulky amine, and both weight ratios are 3～5:1.
5. synthetic ammonia decarbonization process according to claim 4 is characterized in that: described bulky amine is a 2-amino-2-methyl-1-propanol.
6. the energy-saving benzene Fei Er of synthetic ammonia decarbonization device according to claim 5 decarbonization process is transformed, and it is characterized in that: described structured packing is a metallurgic orifice corrugated packing.
7. synthetic ammonia decarbonization process according to claim 5 is characterized in that: described liquid distributor is the slotted disc type gas-liquid distributor.
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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105477978A (en) * 2014-09-16 2016-04-13 中国石油化工股份有限公司 Method for enabling tail gas discharge of reaction circulation gas decarbonization to reach environmental protection index
CN107399778A (en) * 2017-08-30 2017-11-28 博能盛诺(北京)生物质能源科技有限公司 For separating the equipment and system of the carbon dioxide in Methane decarbonization liquid
CN109701360A (en) * 2017-10-26 2019-05-03 中国石油化工股份有限公司 In low-carbon alkene and acetic acid cooxidation product gas the removing of carbon dioxide with utilize apparatus and method
CN109999617A (en) * 2019-03-15 2019-07-12 中国天辰工程有限公司 The technique of CO concentration in a kind of reduction low-temperature methanol washing tail-gas

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5744009A (en) * 1995-07-07 1998-04-28 The M. W. Kellogg Company Method and apparatus for recovering condensables in vapor from a urea vacuum evaporator
CN101492616A (en) * 2008-12-12 2009-07-29 兖矿鲁南化肥厂 Desulfurization and decarburization integrated absorption process for polyglycol dimethyl ether
CN102642881A (en) * 2012-04-23 2012-08-22 神华集团有限责任公司 Device and method for steam stripping of condensate in water gas conversion process

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5744009A (en) * 1995-07-07 1998-04-28 The M. W. Kellogg Company Method and apparatus for recovering condensables in vapor from a urea vacuum evaporator
CN101492616A (en) * 2008-12-12 2009-07-29 兖矿鲁南化肥厂 Desulfurization and decarburization integrated absorption process for polyglycol dimethyl ether
CN102642881A (en) * 2012-04-23 2012-08-22 神华集团有限责任公司 Device and method for steam stripping of condensate in water gas conversion process

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105477978A (en) * 2014-09-16 2016-04-13 中国石油化工股份有限公司 Method for enabling tail gas discharge of reaction circulation gas decarbonization to reach environmental protection index
CN105477978B (en) * 2014-09-16 2018-09-25 中国石油化工股份有限公司 Reaction cycle gas decarbonization exhaust emissions reaches the method for environmental protection index
CN107399778A (en) * 2017-08-30 2017-11-28 博能盛诺(北京)生物质能源科技有限公司 For separating the equipment and system of the carbon dioxide in Methane decarbonization liquid
CN109701360A (en) * 2017-10-26 2019-05-03 中国石油化工股份有限公司 In low-carbon alkene and acetic acid cooxidation product gas the removing of carbon dioxide with utilize apparatus and method
CN109701360B (en) * 2017-10-26 2022-07-08 中国石油化工股份有限公司 Device and method for removing and utilizing carbon dioxide in low-carbon olefin and acetic acid co-oxidation product gas
CN109999617A (en) * 2019-03-15 2019-07-12 中国天辰工程有限公司 The technique of CO concentration in a kind of reduction low-temperature methanol washing tail-gas

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