CN108383309B - Ammonia extraction system and ammonia extraction process for coal chemical industry conversion of acidic condensate - Google Patents
Ammonia extraction system and ammonia extraction process for coal chemical industry conversion of acidic condensate Download PDFInfo
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- CN108383309B CN108383309B CN201810175058.8A CN201810175058A CN108383309B CN 108383309 B CN108383309 B CN 108383309B CN 201810175058 A CN201810175058 A CN 201810175058A CN 108383309 B CN108383309 B CN 108383309B
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/024—Purification
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- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/10—Separation of ammonia from ammonia liquors, e.g. gas liquors
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F1/02—Treatment of water, waste water, or sewage by heating
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Abstract
The invention discloses an ammonia extraction system and an ammonia extraction process for converting acidic condensate in coal chemical industry, wherein the ammonia extraction system comprises CO2Separating tower, ammonia desorption tower and ammonia rectification tower, wherein the ammonia-containing acidic condensate passes through an ammonia-containing condensate pump and CO2The separation columns are communicated, and the CO is2The tower bottom of knockout tower is connected with the ammonia stripping tower, the top of the tower of ammonia stripping tower is connected with ammonia rectifying column through the condensation subassembly, the top of the tower of ammonia rectifying column is connected with sulphur adsorber, ammonia compressor, ammonia condenser and liquid ammonia buffer tank in proper order. Aiming at the thermodynamic characteristics of the conversion condensate, the invention separately arranges CO2The separation tower and the ammonia desorption tower separate CO from the condensate by means of pressure change in sections and according to the thermodynamic characteristics of the system and by means of equilibrium separation principle and different pressures2、H2S and NH3The method effectively solves a series of problems that the extraction composition of the existing single-tower side-stream extraction technology is unstable, the liquid ammonia yield is low, the quality of liquid ammonia products is poor, and the operation is influenced due to the serious sulfur corrosion of equipment.
Description
Technical Field
The invention belongs to the technical field of ammonia-containing acidic condensate treatment and environmental protection, and particularly relates to an ammonia extraction system and an ammonia extraction process for converting acidic condensate in coal chemical industry.
Background
Aiming at the treatment and ammonia extraction of the conversion acid condensate, the reference of H contained in a refinery is generally adopted at home at present2S，NH3(low CO2 content) side-draw technology for acidic water treatment, but the shift acidic condensate contains a large amount of CO2，CO2/NH3High proportion, if the stripping side-draw technology is adopted, CO in the side-draw gas2Relatively high, great difficulty in follow-up ammonia extraction, large circulation amount, unstable operation and poor quality of liquid ammonia products.
Disclosure of Invention
The invention aims to: aiming at the existing problems, the ammonia extraction system and the ammonia extraction process for the coal chemical industry conversion acidic condensate are provided, which have the advantages of reasonable process flow, stable operation and good quality of liquid ammonia products, and can effectively solve the problem of sulfur corrosion.
The technical scheme of the invention is realized as follows: the utility model provides a coal chemical industry changes acidic condensate and carries ammonia system which characterized in that: comprising CO2Separating tower, ammonia desorption tower and ammonia rectification tower, wherein the ammonia-containing acidic condensate passes through an ammonia-containing condensate pump and CO2The separation columns are communicated, and the CO is2The tower bottom of knockout tower is connected with the ammonia stripping tower, the top of the tower of ammonia stripping tower is connected with ammonia rectifying column through the condensation subassembly, the top of the tower of ammonia rectifying column is connected with sulphur adsorber, ammonia compressor, ammonia condenser and liquid ammonia buffer tank in proper order.
The invention relates to a system for extracting ammonia by converting acidic condensate in coal chemical industry, wherein CO is obtained2Passing CO through the top of the separation column2The condenser of the separation tower is connected with a sulfur recovery system, and the tower bottom of the ammonia desorption tower is connected with CO2The separation tower is connected, and the tower bottom of the ammonia rectification tower is connected with CO through a circulating reflux tank and a circulating pump2The separation tower is connected.
The ammonia-containing acid condensate liquid is divided into two parts after passing through an ammonia-containing condensate liquid pump, wherein one part and CO are separated2The upper part of the separation tower is connected with the other part of the separation tower through an ammonia-containing condensate preheater and CO2The middle parts of the separation towers are connected.
The condensation component of the system for extracting ammonia from the coal chemical industry conversion acid condensate comprises a desorption tower condenser and a second-stage condenser, wherein the top of the ammonia desorption tower sequentially passes through the desorption tower condenser and the second-stage condenser and then is connected with an ammonia rectification tower, the condensate of the desorption tower condenser returns to the ammonia desorption tower, the condensate of the second-stage condenser returns to CO through a circulating pump2A separation tower.
The ammonia extraction process of the coal chemical industry conversion acidic condensate ammonia extraction system is characterized in that: after the ammonia-containing acidic condensate is pressurized by an ammonia-containing condensate pump, cold and hot materials are fed into CO2Upper and middle part of the separation column, CO2CO contained in the separated gas at the top of the separation tower2、H2S andNH3the mixed gas enters CO2A water washing section of the separation tower, NH is washed by low-temperature condensate and water3Washed off, CO2High concentration CO is obtained at the top of the separation tower2、H2S acid gas, said CO2The dilute ammonia water at the bottom of the separation tower is sent to an ammonia desorption tower for desorption and separation of NH3And CO2The washing liquid at the bottom of the ammonia desorption tower is sent out after heat recovery, most of the desorbed gas at the top of the ammonia desorption tower is condensed and returned to the ammonia desorption tower by the condenser of the desorption tower, the rest ammonia-containing gas is desorbed and condensed by the second-stage condenser connected in series, and the condensate liquid from the second-stage condenser returns to CO2Separating in a separating tower, feeding ammonia gas from the top of the separating tower to an ammonia rectifying tower, and rectifying, desulfurizing, compressing and condensing the ammonia gas to obtain high-purity liquid ammonia product.
According to the ammonia extraction process of the coal chemical industry conversion acid condensate ammonia extraction system, the ammonia-containing acid condensate is pressurized by the ammonia-containing condensate pump, and the pressure of the ammonia-containing acid condensate is 8-20 BAR, CO2CO separated from the top of the separation tower2、H2S and NH3The operating pressure of the mixed gas is 8-20 BAR, and the CO is2The temperature of the washing water adopted at the top of the separation tower is 40-50 ℃.
The ammonia extraction process of the coal chemical industry conversion acid condensate ammonia extraction system has the advantage that the operating pressure of the ammonia desorption tower is 2-6 BAR.
Aiming at the thermodynamic characteristics of the conversion condensate, the invention separately arranges CO2The separation tower and the ammonia desorption tower separate CO from the condensate by means of pressure change in sections and according to the thermodynamic characteristics of the system and by means of equilibrium separation principle and different pressures2、H2S and NH3The method effectively solves a series of problems that the extraction composition of the existing single-tower side-stream extraction technology is unstable, the liquid ammonia yield is low, the quality of liquid ammonia products is poor, and the operation is influenced due to the serious sulfur corrosion of equipment.
Drawings
FIG. 1 is a process flow diagram of the present invention.
The labels in the figure are: 1 is CO2A separation tower, 2 is an ammonia desorption tower, 3 isAn ammonia rectifying tower, 4 an ammonia-containing condensate pump, and 5 CO2The system comprises a separation tower condenser, a sulfur recovery system 6, a sulfur absorber 7, an ammonia compressor 8, an ammonia condenser 9, a liquid ammonia buffer tank 10, a circulation reflux tank 11, a circulation pump 12, an ammonia-containing condensate preheater 13, a desorption tower condenser 14 and a second-stage condenser 15.
Detailed Description
The present invention will be described in detail below with reference to the accompanying drawings.
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is described in further detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
As shown in figure 1, the ammonia extraction system for the acid condensate in the conversion of the coal chemical industry comprises CO2A separation tower 1, an ammonia desorption tower 2 and an ammonia rectification tower 3, wherein the ammonia-containing acid condensate passes through an ammonia-containing condensate pump 4 and CO2The separation columns 1 are communicated, and the CO is2The top of the separation column 1 is passed over CO2The separator condenser 5 is connected to a sulfur recovery system 6, and the CO is recovered2The tower bottom of the separation tower 1 is connected with an ammonia desorption tower 2, the tower top of the ammonia desorption tower 2 is connected with an ammonia rectification tower 3 through a condensation component, and the tower bottom of the ammonia desorption tower 2 is connected with CO2The separation tower 1 is connected, and the bottom of the ammonia rectification tower 3 is connected with CO through a circulating reflux tank 11 and a circulating pump 122The separation tower 1 is connected, and the top of the ammonia rectifying tower 3 is connected with a sulfur absorber 7, an ammonia compressor 8, an ammonia condenser 9 and a liquid ammonia buffer tank 10 in sequence.
Wherein the ammonia-containing acidic condensate is divided into two parts after passing through an ammonia-containing condensate pump 4, wherein one part is separated from CO2The upper part of the separation column 1 is connected with the other part of the separation column through an ammonia-containing condensate preheater 13 and CO2The middle part of the separation tower 1 is connected, the condensing component comprises a desorption tower condenser 14 and a second-stage condenser 15, the top of the ammonia desorption tower 2 sequentially passes through the desorption tower condenser 14 and the second-stage condenser 15 and then is connected with the ammonia rectification tower 3, the condensate of the desorption tower condenser 14 returns to the ammonia desorption tower 2, and the condensate of the second-stage condenser 15CO is returned via the circulation pump 122A separation column 1.
An ammonia extraction process of an ammonia extraction system for coal chemical industry conversion acidic condensate, which mainly aims at separating CO from ammonia-containing acidic condensate in a coal chemical industry conversion process2To achieve the recovery of pure NH3The method of (1). The condensate is NH-containing3、CO2、H2S and H2Quaternary system of O, thermodynamic and phase diagram Characteristics (CO) according to this composition2High content of H2S), the invention utilizes the equilibrium separation principle and adopts different pressures to separate CO from condensate in sections2And ammonia extraction, and a series of problems of unstable extraction composition, low liquid ammonia yield, poor quality, serious sulfur corrosion of equipment to influence operation and the like of the existing single-tower side-stream extraction technology are improved and solved.
The invention provides a process technology for setting CO2CO separation by pressure swing in separation tower and ammonia desorption tower2And NH3The raw material adopted by the invention is acidic condensate generated in the conversion, and the typical component concentrations are respectively as follows: NH (NH)3：1％～2％，CO2：2％～5％，H2S: 0.07-0.2 WT% of mixture, at 30-40 deg.C and 3-4 BAR, although the concentration range of the treatment can be wider, such as ammonia concentration of 10-20%, CO concentration2The concentration is within the range of 10-20%. After the ammonia-containing acidic condensate is pressurized by an ammonia-containing condensate pump, the pressure is increased to 8-20 BAR, and cold and hot materials are fed into CO2The upper part and the middle part of the separation tower have operating pressure of 8-20 BAR, and a reboiler at the bottom of the tower provides heat, CO2CO contained in the separated gas at the top of the separation tower2、H2S and NH3The mixed gas enters CO2The water washing section of the separation tower can also be independently provided with a water washing tower, and NH is washed by low-temperature condensate at the top of the tower and water3Washing, wherein the temperature of the washing water is 40-50 ℃ to avoid crystallization possibly occurring under abnormal working conditions, further reduce the ammonia concentration, and simultaneously avoid the acid gas from entering an ammonium bicarbonate crystallization area and CO2High concentration CO is obtained at the top of the separation tower2、H2S acid gas (containing very small amount)NH of (2)3) Where the column can separate most of the CO2And H2S, CO of tower top gas passing through tower top2The condenser of the separation tower is condensed and refluxed and only contains a small amount of NH3From CO2The acid gas may be sent to a sulfur recovery system from the separator condenser. The CO is2Dilute ammonia water (containing small amount of H) at bottom of separation tower2S) is sent to an ammonia desorption tower to carry out desorption and separate NH3And CO2The operating pressure of the ammonia desorption tower is 2-6 BAR, heat is provided through a reboiler at the bottom of the ammonia desorption tower, washing liquid at the bottom of the ammonia desorption tower is sent out after heat recovery, most of desorbed gas at the top of the ammonia desorption tower is condensed by a condenser of the desorption tower and flows back to the ammonia desorption tower, and condensate (containing H) from condensers of all stages is desorbed and condensed by other ammonia-containing gas through a second-stage or multi-stage condenser connected in series2S) return to CO2The separation tower is used for separating H2S，H2S is not circularly accumulated in the system, so that the problem of sulfur corrosion is effectively solved, ammonia gas at the top of the S is sent to an ammonia rectifying tower, and the ammonia gas comes out from the top of the ammonia rectifying tower and is removed with residual H through a sulfur absorber2And S, simultaneously obtaining high-purity ammonia gas, and finally obtaining a pure liquid ammonia product after compression and condensation. Into CO2The condensate at the bottom of the separation tower can be preheated by using the condensate at the bottom of the ammonia desorption tower so as to recover heat and reduce consumption.
The technical process provided by the invention has the advantages of reasonable arrangement, stable operation, high liquid ammonia yield, optimized heat recovery and reduced consumption, and the H is set2And the obtained liquid ammonia product has high purity and good quality, and ammonia in the converted acid condensate is recovered and used as a byproduct, so that the treatment value of the acid condensate is improved.
The specific embodiment is as follows: example 1
The raw materials and compositions described in this example are as follows (WT%)
NH3 1％；
CO2 2.6％；
H2S 0.03％；
The balance of water;
temperature: 40 ℃;
pressure: 4 BAR.
The operating conditions of this example: CO22Separation column operating pressure: 17 BAR; operating pressure of ammonia desorption tower: 3 BAR.
The specific process flow is as follows: containing NH3、CO2、H2S and H2Pressurizing the condensate of O to 8-20 BAR by an ammonia-containing condensate pump, separating cold and hot materials, preheating part of the materials by an ammonia-containing condensate preheater, and introducing the preheated materials into CO2Separation column for CO2And H2Separation of S, the column operating at a pressure of 1.7MPaA, CO being separated off2Gas coming out from the top of the tower for preventing NH3With CO2Condensed to form crystals, CO2Washing water is added into the top of the separation tower, and CO is added2Washing in the water washing section of the separation column to remove NH from the overhead gas3The content is very low, the condensate at the bottom of the tower is diluted ammonia water, and the diluted ammonia water enters an ammonia desorption tower.
The ammonia desorption tower adopts low-pressure steam of 0.4MPaA as a heat source of a reboiler of the desorption tower, the ammonia in the condensate is desorbed in the tower, the desorbed gas at a top outlet of the ammonia desorption tower is gaseous ammonia containing water and a small amount of sulfur, the gaseous ammonia passes through a desorption tower condenser and a second-stage condenser and enters an ammonia rectification tower, the operating pressure of the tower is 0.3MPaA, and the operating pressure can be adjusted within +/-0.1 MPa or within a wider range according to the grade of the low-pressure steam during normal operation according to the load change of the ammonia desorption tower.
Wherein, the ammonia gas at the outlet of the ammonia desorption tower top is cooled to 120 ℃ by a desorption tower condenser, the condensate liquid returns to the ammonia desorption tower, the uncondensed ammonia gas continuously enters a second-stage condenser to carry out fractional condensation, the temperature is reduced to 35 ℃, the uncondensed ammonia gas enters an ammonia rectifying tower, and NH in the ammonia gas at the outlet of the ammonia rectifying tower3Not less than 99.8 percent. Gas ammonia coming out of the top of the ammonia rectifying tower enters a sulfur absorber, a desulfurizing agent is filled in the sulfur absorber, the sulfur content of the gas ammonia coming out of the sulfur absorber is less than 5mg/l, the desulfurized gas ammonia enters an ammonia compressor and is boosted to 1.7MPaA, the gas ammonia coming out of the ammonia compressor is condensed by an ammonia condenser to prepare liquid ammonia, the liquid ammonia enters a liquid ammonia buffer tank, a liquid ammonia product at the outlet of the buffer tank is sent to a boundary area user, and a gas phase (normal no flow) outlet of the buffer tank returns to a front-end system for recycling, so that waste gas emission is avoided.
Collecting sulfur-containing ammonia water at the outlet of the second-stage condenser and the ammonia rectifying tower into a circulating reflux tank, and returning the sulfur-containing ammonia water to CO through a circulating pump2Separation of residual CO in a separation column2And H2S。
Example 2
The process flow described in this example is the same as in example 1. The condensate consisted of:
NH3 1.65％；
CO2 4.05％；
H2S 0.17％；
the balance of water;
temperature: 40 ℃;
pressure: 4 BAR.
The operating conditions of this example: CO22Separation column operating pressure: 17 BAR; operating pressure of ammonia desorption tower: 3 BAR.
Example 3
The process flow described in this example is the same as in example 1. The condensate consisted of:
NH3 8.7％；
H2S 0.6％；
the balance of water;
temperature: 85 ℃;
pressure: 4 BAR.
The operating conditions of this example: CO22Separation column operating pressure: 17 BAR; operating pressure of ammonia desorption tower: 3 BAR.
Steam consumption test of examples and comparative examples:
to test the steam consumption of the present invention, the amount of steam consumed in the example and comparative examples to treat the shift condensate from the shift condensate was calculated and is listed in the following table:
table 1: treatment of shift acid condensate steam consumption (reduced value)
From the above table, it can be seen that:
1. the data in the comparative examples are derived from the side draw technique in the similar literature data. Condensate composition in comparative example: NH (NH)3：1.5％；H2S: 0.5%, CO not considered2And the balance of water.
2. Comparative example raw material liquid without considering CO2Content of, therefore, CO is not considered either2And NH3The heat of decomposition of the ammonium carbonate formed is combined, and therefore the steam consumption will be lower, as the CO is taken into account in the actual composition2The content and the steam consumption (according to the treatment capacity per ton) can be increased, and the liquid ammonia yield under the working condition is lower, and the steam consumption per ton of liquid ammonia is higher than the process technology provided by the invention.
3. The steam consumption per ton of ammonia production decreases substantially as the ammonia and carbon dioxide concentration of the condensate increases.
It is to be understood that the above examples are only illustrative and not limiting of the process flow. Therefore, any modification and replacement of the raw material condensate composition, the operation parameters, the process combination mode, and the like within the principle of the present invention should be included in the protection scope of the present invention.
Claims (5)
1. The utility model provides a coal chemical industry changes acidic condensate and carries ammonia system which characterized in that: comprising CO2A separation tower (1), an ammonia desorption tower (2) and an ammonia rectification tower (3), wherein the ammonia-containing acidic condensate passes through an ammonia-containing condensate pump (4) and CO2The separation tower (1) is communicated, the ammonia-containing acid condensate is pressurized by an ammonia-containing condensate pump (4), the pressure is increased to 8-20 BAR, the ammonia-containing acid condensate is divided into two parts by the ammonia-containing condensate pump (4), wherein one part and CO are respectively2The upper part of the separation tower (1) is connected, and the other part is connected with CO through an ammonia-containing condensate preheater (13)2The middle part of the separation tower (1) is connected, and the operation pressure is also 8-20 BAR, the CO2The tower bottom of knockout tower (1) is connected with ammonia stripper (2), the operating pressure of ammonia stripper (2) is 2 ~ 6BAR, the top of the tower of ammonia stripper (2) is passed through the condensation subassembly and is connected with ammonia rectifying column (3), the top of the tower of ammonia rectifying column (3) is connected with sulphur adsorber (7), ammonia compressor (8), ammonia condenser (9) and liquid ammonia buffer tank (10) in proper order, and desorption gas major part at the top of ammonia stripper (2) is through stripper condenser (14) condensation reflux ammonia stripper (2), and remaining ammonia-containing gas is behind second level condenser (15) or the multistage condenser desorption condensation of establishing ties, and the condensate that each level of condenser came out returns CO, and the condensate that each level of condenser came out is desorbed and is condensed2Separation H is carried out by the separation tower (1)2S，H2S is not accumulated cyclically in the system.
2. The system for extracting ammonia from coal chemical industry conversion acid condensate as claimed in claim 1, wherein: the CO is2The top of the separation column (1) is passed through CO2The separation tower condenser (5) is connected with a sulfur recovery system (6), and the tower bottom of the ammonia desorption tower (2) is connected with CO2The separation tower (1) is connected, the bottom of the ammonia rectification tower (3) is connected with CO through a circulating reflux tank (11) and a circulating pump (12)2The separation tower (1) is connected.
3. The system for extracting ammonia from coal chemical industry conversion acid condensate as claimed in claim 1, wherein: the condensation subassembly includes desorber condenser (14) and second level condenser (15), the top of the tower of ammonia desorber (2) is connected with ammonia rectifying column (3) after desorber condenser (14) and second level condenser (15) in proper order, the condensate of desorber condenser (14) returns ammonia desorber (2), the condensate of second level condenser (15) returns CO through circulating pump (12) and returns2A separation column (1).
4. The ammonia extraction process of the coal chemical industry conversion acid condensate ammonia extraction system according to any one of claims 1 to 3, characterized in that: after the ammonia-containing acidic condensate is pressurized by an ammonia-containing condensate pump, the pressure is increased to 8-20 BAR, and cold and hot materials are fed into CO2The operating pressure of the upper part and the middle part of the separation tower is also 8-20 BAR, CO2Separation towerCO-containing gas separated from the top of the column2、H2S and NH3The mixed gas enters CO2Water washing section of the separation column, CO2CO separated from the top of the separation tower2、H2S and NH3The operating pressure of the mixed gas is 8-20 BAR, and NH is washed by low-temperature condensate and water3Washed off, CO2High concentration CO is obtained at the top of the separation tower2、H2S acid gas, said CO2The dilute ammonia water at the bottom of the separation tower is sent to an ammonia desorption tower for desorption and separation of NH3And CO2The operation pressure of the ammonia desorption tower is 2-6 BAR, washing liquid at the bottom of the ammonia desorption tower is sent out after heat recovery, most of desorbed gas at the top of the ammonia desorption tower is condensed by a desorption tower condenser and flows back to the ammonia desorption tower, the rest ammonia-containing gas is desorbed and condensed by a second-stage condenser connected in series, and condensate liquid from the second-stage condenser returns to CO2Separating in a separating tower, feeding ammonia gas from the top of the separating tower to an ammonia rectifying tower, and rectifying, desulfurizing, compressing and condensing the ammonia gas to obtain high-purity liquid ammonia product.
5. The ammonia extraction process of the coal chemical conversion acid condensate ammonia extraction system according to claim 4, characterized in that: the CO is2The temperature of the washing water adopted at the top of the separation tower is 40-50 ℃.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| EP0088478A1 (en) * | 1982-03-05 | 1983-09-14 | Stamicarbon B.V. | Process for the separation of ammonia and carbon dioxide from mixtures containing ammonia, carbon dioxide and water |
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| DE102008058143B4 (en) * | 2008-11-20 | 2012-04-12 | Lurgi Gmbh | Process and plant for recovering NH3 from a mixture containing NH3 and sour gases |
| CN201439518U (en) * | 2009-06-12 | 2010-04-21 | 北京新峰泰克工程技术有限公司 | System for purifying crude synthetic gas with low-temperature methanol |
| CN101874967B (en) * | 2009-12-18 | 2012-07-04 | 中国五环工程有限公司 | Process for removing acid gas with low-temperature methanol solution |
| CN101885993B (en) * | 2010-07-12 | 2013-05-29 | 赛鼎工程有限公司 | Purification process for removing sulphur and carbon dioxide in gas by using two-step method |
| CN104495965A (en) * | 2014-12-30 | 2015-04-08 | 中国天辰工程有限公司 | Process for treating low-temperature condensate at conversion section |
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| EP0088478A1 (en) * | 1982-03-05 | 1983-09-14 | Stamicarbon B.V. | Process for the separation of ammonia and carbon dioxide from mixtures containing ammonia, carbon dioxide and water |
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