The present invention relates to a process and to a plant of treating an ammonia and carbon dioxide containing wastewater stream so as to produce a concentrated aqueous ammonia solution containing at least 5% by weight of dissolved ammonia and at most 20% by weight of dissolved carbon dioxide and a purified wastewater stream containing at most 1.000 ppm dissolved ammonia, wherein the process comprises the following steps.

Ammonia and carbon dioxide containing wastewater streams are generated during a plurality of industrial process, such as during the production of biogas, for in- stance by anaerobic digestion of agricultural and municipal waste. Such processes gain more and more importance, since biogas is obtainable as valuable product and simultaneously agricultural and municipal waste is reduced at least partially. From anaerobic digestion, large volumes of wastewater are generated containing both, ammonia and carbon dioxide. An example for such a wastewater including ammonia and carbon dioxide is filtered fermentation broth or anaerobically digest- ed cattle manure effluent. These wastewaters need to be appropriately treated, which is, however, challenging, since the respective known processes are energy intensive and require expensive plants. Moreover, the valuable ammonia is not recovered.

For example, it is common practice to treat such wastewater streams by stripping in one step with dosage of caustic. It is desired that in the initial carbon dioxide stripping step the lowest amount possible of the ammonia contained in the wastewater stream is lost, i.e. removed from it together with the carbon dioxide. In addition, enough carbon dioxide must be removed in the initial carbon dioxide stripping step in order to reliably avoid precipitation of salts during the later treat- ment steps, such as the precipitation of ammonium carbonate. In addition, it is desired that the obtained purified water contains as low concentration as possible of ammonia. The known processes for treating an ammonia and carbon dioxide containing wastewater stream so as to produce a concentrated aqueous ammonia solution and a purified wastewater stream reliably avoiding a salt precipitation during the process and in the produced concentrated aqueous ammonia solution during usual storage temperature have the drawback of being very energy inten- sive and of requiring complex plants.

In view of this, the object underlying the present invention is to provide a plant and a process for treating an ammonia and carbon dioxide containing wastewater stream so as to produce a concentrated aqueous ammonia solution and a purified wastewater stream, which reliably avoids a salt precipitation during the process and in the produced concentrated aqueous ammonia solution at usual storage temperature, and which is in particular very energy and capital efficient, i.e. which requires a plant of low complexity and which is characterized by a low operational energy demand.

In accordance with the present invention this object is satisfied by providing a process of treating an ammonia and carbon dioxide containing wastewater stream so as to produce a concentrated aqueous ammonia solution containing at least 5% by weight of dissolved ammonia and at most 20% by weight of dissolved carbon dioxide and a purified wastewater stream containing at most 1.000 ppm dissolved ammonia, wherein the process comprises the following steps: a) feeding the wastewater stream into a carbon dioxide degasser column comprising at least one bed of one or more random packings, at least one bed of one or more structured packings or at least one tray, wherein i) a first portion of the wastewater stream is fed at a position above at least one bed of one or more random packings, above at least one bed of one or more structured packings or above at least one tray and ii) a second portion of the wastewater stream having a higher temperature than the first portion and/or a mixture of a second portion of the wastewater stream with a por- tion of a liquid carbon dioxide depleted stream being withdrawn as bottom fraction from the carbon dioxide degasser column having a higher tempera- ture than the first portion is fed at a position below at least one bed of one or more random packings, below at least one bed of one or more random packings structured packings or below at least one tray into the carbon di- oxide degasser column, wherein the bed of one or more random packings, the bed of one or more structured packings or the trays above which the first portion of the wastewater stream is fed is the same as or located above the bed of one or more random packings, the bed of one or more structured packings or the tray below which the second portion of the wastewater stream and/or the mixture of a second portion of the wastewater stream with a portion of a liquid carbon dioxide depleted stream is fed, wherein the mass flow ratio of the first portion of the wastewater stream to the total wastewater stream fed into the carbon dioxide degasser column is 0.01 to 0.6, b) withdrawing a gaseous carbon dioxide rich stream containing less than 10% by weight of the ammonia contained in the wastewater stream as overhead fraction and the liquid carbon dioxide depleted stream having a pH value of 9.0 or higher as bottom fraction from the carbon dioxide degasser column, c) feeding the liquid carbon dioxide depleted stream having a pH value of 9.0 or higher into an ammonia stripper column, d) withdrawing a gaseous ammonia rich stream as overhead fraction and the purified wastewater stream containing at most 1 .000 ppm dissolved ammo- nia as bottom fraction from the ammonia stripper column, wherein at least a portion of the liquid purified wastewater stream withdrawn from the ammo- nia stripper column is evaporated, wherein all or a portion of the evaporated portion is fed back into the ammonia stripper column, e) feeding the gaseous ammonia rich stream and separately therefrom water into a quencher column, withdrawing a gaseous vent gas stream as over- head fraction and withdrawing concentrated aqueous ammonia solution containing at least 5% by weight of dissolved ammonia and at most 20% by weight of dissolved carbon dioxide as bottom fraction from the quencher column.

This solution bases on the surprising finding that performing before the carbon dioxide removal from the ammonia and carbon dioxide containing wastewater feed stream a feed split into a first portion of feed being fed into the carbon dioxide degasser column at a position being above at least one bed of one or more ran- dom packings, at least one bed of one or more structured packings or at least one tray and into a second portion of feed (optionally admixed with a portion of a liquid carbon dioxide depleted stream being withdrawn as bottom fraction from the car- bon dioxide degasser column) having a higher temperature than the first portion of feed being fed into the carbon dioxide degasser column at a position being below at least one bed of one or more random packings, at least one bed of one or more structured packings or at least one tray into the carbon dioxide degasser column and being separated from the position, at which the first portion of feed is intro- duced into the carbon dioxide degasser column by at least one bed of one or more random packings, at least one bed of one or more structured packings or at least one tray, wherein the mass flow ratio of the first portion of the wastewater stream to the total wastewater stream fed into the carbon dioxide degasser column is 0.01 to 0.6, allows to separate in a carbon dioxide degasser column a required amount of carbon dioxide with a very low energy demand and with minimal ammonia loss of less than 1 %. The present invention bases furthermore on the finding that it is not required to remove all or essentially all of the carbon dioxide during step a), which would be associates with a high loss of ammonia, but that it is only neces- sary to remove a minimum amount of carbon dioxide, which is sufficient to avoid a salt precipitation during the further process steps and in the concentrated aqueous ammonia solution at the desired storage temperature. In other words, the present invention allows to remove in step a) comparable low amounts of carbon dioxide further decreasing the operational costs of the process in comparison to a com- plete removal of carbon dioxide. In particular, this is achieved without any need of using inert gas during the carbon dioxide stripping step and/or ammonia stripping step, which would be connected with a complex plant and increased operational costs, and also without any need of recycling large volumes of process streams from downstream steps to upstream steps, as required in most of the prior art processes. The process in accordance with the present invention allows to effi- ciently remove ammonia from the ammonia and carbon dioxide containing wastewater stream without need to adjust any base before or during the ammonia stripping step d), thus avoiding a complex pH value control as well as handling and dosage of caustic. Accordingly, the addition of acid and/or base to the feed and/or to the liquid carbon dioxide depleted stream is not at all necessary, which facili- tates the process as well as the plant, in which the process is performed. This is due to the fact that the liquid carbon dioxide depleted stream being withdrawn from the carbon dioxide degasser column as bottom fraction and being fed into the ammonia stripper column has a pH value of 9.0 or higher, thus having a pH value assuring that all or at least most of the ammonia is present in the liquid carbon dioxide depleted stream in non-dissociated from allowing to get stripped in the ammonia stripper column. As described in further detail below, the present inven- tion further allows to efficiently use heat of process streams generated during the process by heat integration. All in all, the present invention provides a plant and a process for treating an ammonia and carbon dioxide containing wastewater stream so as to produce a concentrated aqueous ammonia solution and a purified wastewater stream, which reliably avoids a salt precipitation during the process and in the produced concentrated aqueous ammonia solution during usual storage temperature, and which is in particular very energy and capital efficient, i.e. which requires a quite uncomplex plant and which is characterized by a low operational energy demand. Even if the present invention allows to remove in step a) compa- rable low amounts of carbon dioxide, the present invention also allows to remove all of the carbon dioxide contained in the wastewater stream and to produce a very pure ammonium hydroxide solution.

The term “dissolved” comprises in accordance with the present invention a physi- cal dissolution of a compound as well as a chemical dissolution of a compound. Thus, the term ammonia being dissolved in aqueous ammonia solution comprises ammonia molecules being physically dissolved in water as well as ammonium ions and hydroxide ions resulting from the chemical dissolution of ammonia in water. Likewise, the term carbon dioxide being dissolved in aqueous ammonia solution comprises carbon dioxide molecules being physically dissolved in water as well as aqueous carbonic acid, i.e. a mixture of carbonate ions, bicarbonate ions, carba- mate ions, ammonium ions and hydronium ions resulting from the chemical disso- lution of carbon dioxide in water.

In accordance with the present invention, in step b) a liquid carbon dioxide deplet- ed stream having a pH value of 9.0 or higher is withdrawn as bottom fraction from the carbon dioxide degasser column. This means that in the carbon dioxide de- gasser so much carbon dioxide is removed from the wastewater stream that in the resulting liquid carbon dioxide depleted stream a pH value of 9.0 or higher results. For instance, the conditions necessary therefore may be calculated with the statis- tical model described further below. Thus, even if, as set out above, in the process in accordance with the present invention not all or essentially all of the carbon dioxide is removed during step a), but only a minimal amount of carbon dioxide is removed, the removed minimal amount is high enough so as to assure a pH value of 9.0 or higher in the resulting liquid carbon dioxide depleted stream. Preferably, the liquid carbon dioxide depleted stream being withdrawn as bottom fraction from the carbon dioxide degasser column in step b) has a pH value of 10.0 or higher. Moreover, it is preferred that the liquid carbon dioxide depleted stream being with- drawn as bottom fraction from the carbon dioxide degasser column in step b) has a pH value of 13.0 or lower, preferably of 12.0 or lower and more preferably of 11 .0 or lower. Good results are in particular obtained, when the liquid carbon diox- ide depleted stream being withdrawn as bottom fraction from the carbon dioxide degasser column in step b) has a pH value of 9.0 to 11 .0 and most preferably of 10.0 to 11.0.

As set out above, the present patent application allows to remove only a minimum of the carbon dioxide from the concentrated aqueous ammonia solution, thus min- imizing the energy required for the process and minimizing the requires separation equipment for the plant. Thus, the concentrated aqueous ammonia solution may comprise carbon dioxide to a certain extend. However, it is preferred that the car- bon dioxide content of the concentrated aqueous ammonia solution is limited so that the produced concentrated aqueous ammonia solution does not form any precipitate and in particular no ammonium carbonate precipitate, when stored for at least 1 day at a temperature of 10°C.

In accordance with the present invention, a liquid carbon dioxide depleted stream having a pH value of 9.0 or higher is withdrawn in step b) as bottom fraction from the carbon dioxide degasser column and the liquid carbon dioxide depleted stream is fed in step c) into an ammonia stripper column. This means that the liquid car- bon dioxide depleted stream being withdrawn as bottom fraction from the carbon dioxide degasser column is fed directly into the ammonia stripper column, i.e. without any further process step between the withdrawal of the liquid carbon diox- ide depleted stream as bottom fraction from the carbon dioxide degasser column and the introduction of this liquid carbon dioxide depleted stream into the ammonia stripper column. In particular, no mixing and no phase separation is performed between the withdrawal of the liquid carbon dioxide depleted stream as bottom fraction from the carbon dioxide degasser column and its introduction into the ammonia stripper column.

According to a further particular preferred embodiment of the present invention, in step e) no inert gas is fed in addition to the gaseous ammonia rich stream and the water into the quencher column. Even more preferably, in the whole process no inert gas is fed into any of the columns, i.e. the carbon dioxide degasser column, the ammonia stripper column and the quencher column. This further reduces the required plant investment costs as well as the operational costs. Inert gas means in this context any gas which does not react with ammonia, such as for instance nitrogen, argon, helium, oxygen, air or coke oven gas.

In a further development of the idea of the present invention, it is suggested that no base and/or no acid is added to the wastewater stream or feed, respectively, before or during it is fed into the carbon dioxide degasser column, to the mixture contained in the carbon dioxide degasser column, to the liquid carbon dioxide depleted stream before or during it is fed into the ammonia stripper column or to the mixture contained in the ammonia stripper column. More preferably, in the whole process no base and/or no acid is added to any of the process streams. It is a further surprising finding of the present invention that - contrary to the ammonia stripping processes described in the prior art - an adjustment of the pH value of the liquid stream entering the ammonia stripper column and of the mixture con- tained in the ammonia stripper column is not necessary. This does not only facili- tate the process, but further reduces the operational costs.

Furthermore, it is preferred that the purified wastewater stream withdrawn in step d) of the process in accordance with the present invention from the ammonia stripper column is neither completely nor partially recycled to the carbon dioxide degasser column used in step a). In addition, it is preferred that in step a) no further stream is fed to the carbon dioxide degasser column in addition to i) the first portion of the wastewater stream and ii) the second portion of the wastewater stream and/or mixture of a second portion of the wastewater stream with a portion of a liquid carbon dioxide depleted stream being withdrawn as bottom fraction from the carbon dioxide degasser.

The present invention is not particularly limited concerning the kind of ammonia and carbon dioxide containing wastewater stream. For example, the wastewater stream may be filtered or centrifuged fermentation broth, an anaerobically digested cattle manure effluent or any effluent from a fermenter or from the production of biogas by anaerobic digestion of agricultural or municipal waste. Good results are in particular obtained, when the wastewater stream fed into step a) comprises more than 0.05 to 0.65% by weight of dissolved ammonia, 0.10 to 0.79% by weight of dissolved carbon dioxide and 0 to 1% by weight of organic solids. For instance, the content of organic solids may be more than 0 to 1% by weight, such as 0.10 to 1 .00% by weight, 0.20 to 1 .00% by weight or 0.50 to 1 .00% by weight. The organic solids may be sugar, protein, cell debris, decomposition molecules, biomass or the like. Further optional components of the wastewater may be meth- anol, ethanol, ethylacetate, acetic acid and salts being different from ammonia or carbonate salts.

In accordance with the present invention, i) a first portion of the wastewater stream is fed at a position above at least one bed of one or more random packings, above at least one bed of one or more structured packings or above at least one tray and ii) a second portion of the wastewater stream having a higher temperature than the first portion and/or a mixture of a second portion of the wastewater stream with a portion of a liquid carbon dioxide depleted stream being withdrawn as bottom fraction from the carbon dioxide degasser column having a higher temperature than the first portion is fed at a position below at least one bed of one or more random packings, below at least one bed of one or more structured packings or below at least one tray into the carbon dioxide degasser column, wherein the bed of one or more random packings, the bed of one or more structured packings or the tray above which the first portion of the wastewater stream is fed is the same as or located above the bed of one or more random packings, above the bed of one or more structured packings or above the tray below which the second portion of the wastewater stream and/or the mixture of a second portion of the wastewater stream with a portion of a liquid carbon dioxide depleted stream is fed. This means that the position at which the first portion of the wastewater stream is fed and the position at which the second portion of the wastewater stream is fed into the car- bon dioxide degasser column are separated by at least on bed of one or more random packings, bed of one or more structured packings or tray. For instance, if the carbon dioxide degasser column comprises five beds of one or more random packings, five beds of one or more structured packings or five trays, the first por- tion of the wastewater stream may be fed into the carbon dioxide degasser column above any of the first to fourth beds of one or more random packings, first to fourth beds of one or more structured packings or first to fourth trays seen from the top to the bottom of the carbon dioxide degasser column, whereas the second portion of the wastewater stream may be fed at a position being at least one bed of one or more random packings, at least one bed of one or more structured packings or at least one tray below that of the first portion of the wastewater stream.

The present invention is not particularly restricted concerning the number of beds comprising one or more random packings, the number of beds comprising one or more structured packings or the number of trays included in the carbon dioxide degasser column. For instance, the carbon dioxide degasser column may com- prise one bed of one or more random packings, one bed of one or more structured packings or one tray, wherein the first portion of the wastewater stream is fed above and the second portion of the wastewater stream and/or mixture of the second portion of the wastewater stream with a portion of a liquid carbon dioxide depleted stream is fed below the bed of one or more random packings, below the bed of one or more structured packings or below the tray into the carbon dioxide degasser column. Suitable examples for structured packings are cross-channel structured packings.

In accordance with an alternative embodiment of the present invention, the carbon dioxide degasser column comprises two beds of one or more random packings, two beds of one or more structured packings or two trays on top of each other, wherein the first portion of the wastewater stream is fed at a position above the uppermost and the second portion of the wastewater stream is fed at a position below the lowermost bed of one or more random packings, below the lowermost bed of one or more random packings structured packings or below the lowermost tray into the carbon dioxide degasser column.

In order to further reduce the operational costs of the process of the present inven- tion, it is suggested in a further development of the idea of the present invention that the second portion of the wastewater stream and/or the mixture of the second portion of the wastewater stream with a portion of a liquid carbon dioxide depleted stream being withdrawn as bottom fraction from the carbon dioxide degasser col- umn is heated, before being introduced into the carbon dioxide degasser column. As heating medium, one or more of a water rich condensate stream obtained from the gaseous ammonia rich stream withdrawn in step d) by partial condensation, of the purified wastewater stream withdrawn in step d) and of the liquid carbon diox- ide depleted stream or a portion of the liquid carbon dioxide depleted stream with- drawn in step b) may be used in the heat exchanger(s). If necessary, external heating medium may be used in addition to or instead of the aforementioned inter- nal process streams. The external heating medium may be for instance steam, hot oil or compressed hot water. For example, i) the second portion of the wastewater stream may be heated in a heat exchanger, before being fed into the carbon diox- ide degasser column, wherein a water rich condensate stream obtained from the gaseous ammonia rich stream withdrawn in step d) by partial condensation is used in the heat exchanger as heating medium, and/or ii) the second portion of the wastewater stream may be heated in a heat exchanger, before being fed into the carbon dioxide degasser column, wherein the purified wastewater stream with- drawn in step d) is used in the heat exchanger as heating medium, and/or iii) the second portion of the wastewater stream may be heated in a heat exchanger, before being fed into the carbon dioxide degasser column, wherein the liquid car- bon dioxide depleted stream or a portion of the liquid carbon dioxide depleted stream withdrawn in step b) is used in the heat exchanger as heating medium. The heat exchanger(s) may be for instance shell tube heat exchangers or plate and frame heat exchangers.

In accordance with a particular preferred embodiment of the present invention, i) the second portion of the wastewater stream is heated in a (first) heat exchanger, before being fed into the carbon dioxide degasser column, wherein a water rich condensate stream obtained from the gaseous ammonia rich stream withdrawn in step d) by partial condensation is used in the (first) heat exchanger as heating medium, and thereafter ii) the second portion of the wastewater stream is heated in a (second) heat exchanger, before being fed into the carbon dioxide degasser column, wherein the purified wastewater stream withdrawn in step d) is used in the (second) heat exchanger as heating medium. Good results are in particular ob- tained, when in this embodiment downstream of the (second) heat exchanger iii) the second portion of the wastewater stream and/or a mixture of the second por- tion of the wastewater stream with a portion of the liquid carbon dioxide depleted stream being withdrawn as bottom fraction from the carbon dioxide degasser col- umn is heated in a (third) heat exchanger, before being fed into the carbon dioxide degasser column, wherein the liquid carbon dioxide depleted stream or a portion of the liquid carbon dioxide depleted stream withdrawn in step b) is used in the heat exchanger as heating medium. Again, the heat exchanger(s) may be for instance shell tube heat exchangers or plate and frame heat exchangers. In particular, if more than the internal energy is necessary to heat/evaporate the second portion of the wastewater stream, the second portion of the wastewater stream or a mixture of the second portion of the wastewater stream with a portion of a liquid carbon dioxide depleted stream being withdrawn as bottom fraction from the carbon dioxide degasser column may be heated/evaporated, after optionally having been heated in one or more heat exchangers, such as the aforementioned heat exchangers, in an evaporator with an external heating medium, before the heated/evaporated second portion of the wastewater stream or mixture of the second portion of the wastewater stream with a portion of a liquid carbon dioxide depleted stream being withdrawn as bottom fraction from the carbon dioxide de- gasser column is fed into the carbon dioxide degasser column. The incorporation of an evaporated stream of the second portion of the wastewater stream or of a mixture of the second portion of the wastewater stream and with a portion of a liquid carbon dioxide depleted stream into the carbon dioxide degasser column has the advantage that the vapor fraction of this stream does not mix with the liquid and thus does not dilute the (liquid) bottom fraction of the carbon dioxide degasser column, but rises as vapor in the carbon dioxide degasser column up- wards.

As an alternative, instead of evaporating the second portion of the wastewater stream and/or the mixture of the second portion of the wastewater stream with a portion of a liquid carbon dioxide depleted stream being withdrawn as bottom fraction from the carbon dioxide degasser column in a heat exchanger, this stream can be supplied as liquid to the sump of the carbon dioxide degasser column and additionally, low pressure stripping steam is supplied to the sump of the same column.

As set out above, the second portion of the wastewater stream may be fed direct- ly, i.e. without addition of any substance, into the carbon dioxide degasser column. As set out above, however, in a further development of the idea of the present invention it is suggested that a portion of the liquid carbon dioxide depleted stream being withdrawn as bottom fraction from the carbon dioxide degasser column is mixed with the second portion of the wastewater stream, before the so obtained mixture is fed into the carbon dioxide degasser column. Thereby, due to the addi- tional heat of the admixed liquid carbon dioxide depleted stream being withdrawn as bottom fraction from the carbon dioxide degasser column, the second portion of the wastewater stream is efficiently heated/evaporated, before being introduced into the liquid carbon dioxide depleted stream.

Good results are in particular obtained, when the first portion of the wastewater stream being fed into the carbon dioxide degasser column has a temperature of 10 to 50°C and preferably of 30 to 40°C, whereas preferably the second portion of the wastewater stream being fed into the carbon dioxide degasser column has a tem- perature of 70 to 160°C and more preferably of 100 to 130°C at the inlet of the carbon dioxide degasser column.

As set out above, the mass flow ratio of the first portion of the wastewater stream to the total wastewater stream fed into the carbon dioxide degasser column is 0.01 to 0.6. The sum of the first portion of the wastewater stream and of the second portion of the wastewater stream is the total wastewater stream. For instance, the mass flow ratio of the first portion of the wastewater stream to the total wastewater stream fed into the carbon dioxide degasser column is more than 0.1 to 0.6, such as more than 0.1 to 0.5, more than 0.1 to 0.4, more than 0.1 to 0.3 or more than 0.1 to 0.2.

Good results are in particular obtained, when the pressure within the carbon diox- ide degasser column during step a) is at least essentially atmospheric, such as between 0.095 and 0.1013 MPa, or atmospheric, i.e. 0.1013 MPa. However, it has been found in the present invention that the ammonia loss is minimized in step a), if the pressure in the carbon dioxide degasser column is above atmospheric pres- sure. Therefore, it is more preferred that the pressure within the carbon dioxide degasser column during step a) is more than 0.1013 to 0.6 MPa, still more prefer- ably more than 0.1013 to 0.4 MPa, yet more preferably 0.15 to 0.3 MPa and most preferably 0.15 to 0.25 MPa.

The carbon dioxide depletion ratio obtained in the carbon dioxide degasser column during step a), i.e. the ratio of the carbon dioxide amount removed with the gase- ous carbon dioxide rich stream in step a) divided by the carbon dioxide amount contained in the ammonia and carbon dioxide containing wastewater stream, is preferably adjusted to be at least 20%, more preferably at least 50% and most preferably at least 70%. Moreover, it is preferred that the ammonia loss in the carbon dioxide degasser column during step a), i.e. the ratio of the ammonia amount removed with the gaseous carbon dioxide rich stream in step a) divided by the ammonia amount contained in the ammonia and carbon dioxide containing wastewater stream, is preferably adjusted to be at most 5% and most preferably at least 1%.

Preferably, the gaseous carbon dioxide rich stream being withdrawing in step b) contains less than 5% by weight, more preferably less than 1% by weight and most preferably less than 0.1% by weight of the ammonia contained in the wastewater stream.

The liquid carbon dioxide depleted stream being withdrawn in step b) preferably contains less than 0.5% by weight of dissolved carbon dioxide and 0 to 2% by weight of dissolved ammonia and has a temperature of 100 to 130°C. It has been found in the present invention that the sump temperature of the carbon dioxide degasser column should not exceed 150°C. In accordance with a further preferred embodiment of the present invention, during step c) the pressure is adjusted within the ammonia stripper column to be 0.09 to 0.13 MPa and the temperature is adjusted within the ammonia stripper column to be 90 to 120°C.

In accordance with a further preferred embodiment of the present invention, the operational parameters in the carbon dioxide degasser column in step a) may be optimized by the following statistical model. The statistical model allows to calcu- late the optimal value of the operation parameters column pressure and feed split ratio related to the CO ₂ -degasser column. The statistical model is in particular reliable for an ammonia and carbon dioxide containing wastewater stream fed into step a) comprising more than 0.05 to 0.65% by weight of dissolved ammonia and 0.10 to 0.79% by weight of dissolved carbon dioxide, wherein the intended storage temperature of the obtained concentrated aqueous ammonia solution is 5 to 30°C, wherein during the storage no precipitate shall form in the concentrated aqueous ammonia solution.

To select the optimal process configuration, decision variables are defined, where- in the decision variables are defined as follows:

(equation 1 ) wherein the parameters pij, qjk and rk are given in the following tables: and wherein the variables are defined as follows: f _bA - decision variable A,

T _s - storage temperature (of final product), c _CO2 - carbon dioxide concentration in feed, c _NH3 - ammonia concentration in feed, i,j,k - summation indices also used as exponent.

The decision for the optimal process configuration is based on the calculation results.

If f _bA °, then the optimal process comprises three of the aforementioned heat exchange steps i) to iii), i.e. i) the second portion of the wastewater stream is heated in a heat exchanger, before being fed into the carbon dioxide degasser column, wherein a water rich condensate stream obtained from the gaseous am- monia rich stream withdrawn in step d) by partial condensation is used in the (first) heat exchanger as heating medium, ii) the second portion of the wastewater stream is heated in a heat exchanger, before being fed into the carbon dioxide degasser column, wherein the purified wastewater stream withdrawn in step d) is used in the heat exchanger as heating medium and iii) the second portion of the wastewater stream and/or a mixture of the second portion of the wastewater stream with a portion of the liquid carbon dioxide depleted stream being withdrawn as bottom fraction from the carbon dioxide degasser column is heated in a heat exchanger, before being fed into the carbon dioxide degasser column, wherein the liquid carbon dioxide depleted stream or a portion of the liquid carbon dioxide depleted stream withdrawn in step b) is used in the heat exchanger as heating medium. In this case, the feed split ratio and the column pressure have to be cal- culated with the below equations 2 and 3.

If f _biA > o, then the optimal process comprises two of the aforementioned heat exchange steps i) to iii). In this case, the feed split ratio has to be calculated with the below equation 2 and the column pressure is 101 ,000 Pa.

The optimal feed split ratio and the optimal column pressure are calculated ac- cording to the following equations 2 and 3:

(equation 2)

(equation 3), wherein f _cs - f _f and p _Col = f _p and the model parameters aijk and bijk are given in the following table: and wherein the variables are defined as follows: f _cs - feed split ratio, p _col - column top pressure, - decision variable C,

T _s - storage temperature (of final product), ^c co2 - carbon dioxide concentration in feed, - ammonia concentration in feed, i,j ,k - summation indices also used as exponent.

In order to obtain a high separation efficiency, it is suggested in a further develop- ment of the idea of the present invention that the ammonia stripper column com- prises one or more beds being constituted by one or more random packings, one or more beds being constituted by one or more structured packings or by one or more trays. Particular good results are obtained, when the ammonia stripper col- umn comprises at least two beds comprising one or more random packings, at least two beds comprising one or more structured packings or at least two trays, wherein the at least two beds or trays are arranged on top of each other, wherein the liquid carbon dioxide depleted stream is fed into the ammonia stripper column at a position between two adjacent beds of one or more random packings, be- tween two adjacent beds of one or more structured packings or between two adja- cent trays, and wherein in step d) the evaporated liquid purified wastewater stream is fed back into the ammonia stripper column below the at least two beds of one or more random packings, below the at least two beds of one or more structured packings or below the at least two trays. For instance, the ammonia stripper col- umn comprises in the aforementioned embodiment exactly two such beds or trays being arranged on top of each other. As set out further above, it is preferred that no inert gas stream is fed into the ammonia stripper column.

It is preferred that the purified wastewater stream being withdrawn in step d) con- tains at most 1.000 ppm, more preferably at most 500 ppm, even more preferably at most 250 ppm, yet more preferably at most 150 ppm, still more preferably less than 50 ppm and most preferably less than 10 ppm of dissolved ammonia.

Moreover, it is preferred that the portion of the evaporated purified wastewater stream, which is fed back into the ammonia stripper column in step d), has a tem- perature of 100 to 120°C.

In accordance with a further particular preferred embodiment of the present inven- tion, the gaseous ammonia rich stream, which is withdrawn in step d) from the ammonia stripper column, is led through a compressor, which is preferably a multi- stage turbofan compressor, so as to compress and heat the gaseous ammonia rich stream to a temperature of 110 to 130°C, wherein the compressed and heated gaseous ammonia rich stream is then led through a heat exchanger, in which it heats and evaporates the liquid purified wastewater stream to be evaporated in step d), whereupon the compressed and heated gaseous ammonia rich stream partially condenses, wherein the condensed portion thereof is separated and led optionally via a heat exchanger back into the ammonia stripper column, whereas the non-condensed portion thereof is fed in step e) as gaseous ammonia rich stream into the quencher column. The condensed portion of the heated gaseous ammonia rich stream may be led through a head exchanger for heating the sec- ond portion of the of the wastewater stream as described above.

In the aforementioned preferred embodiment, according to which the ammonia stripper column comprises at least two beds comprising one or more random packings, at least two beds comprising one or more structured packings or at least two trays, it is particularly preferred that the condensed portion of the compressed and heated gaseous ammonia rich stream is led back into the ammonia stripper column at a position above the at least two beds of one or more random packings, at least two beds of one or more structured packings or at least two trays.

In view of a good separation efficiency, it is further preferred that the quencher column comprises at least two beds comprising one or more random packings, at least two beds comprising one or more structured packings or at least trays, wherein the at least two beds or trays are arranged on top of each other, wherein the water is fed into the quencher column at a position above the uppermost of the at least two beds of one or more random packings, uppermost of the at least two beds of one or more structured packings or uppermost of the tray and the gaseous ammonia rich stream is fed into the quencher column at a position below the low- ermost of the at least two beds of one or more random packings, lowermost of the at least two beds of one or more structured packings or lowermost of the at least two trays. In a further development of the idea of the present invention, it is proposed that a portion of the concentrated aqueous ammonia solution being withdrawn from the bottom of the quencher column in step e) is led back into the quencher column and preferably at a position between two adjacent beds of one or more random packings, two adjacent beds of one or more random structured packings or two adjacent trays.

Preferably, the concentrated aqueous ammonia solution being withdrawn from the quencher column in step e) contains at least 10% by weight, more preferably at least 15% by weight, still more preferably at least 20% by weight and most prefer- ably at least 25% by weight of dissolved ammonia. The vent gas stream being withdrawn as overhead fraction form the quencher column contains less than 10 ppm ammonia.

In accordance with another aspect, the present invention relates to a plant for treating an ammonia and carbon dioxide containing wastewater stream so as to produce a concentrated aqueous ammonia solution containing at least 5% by weight of dissolved ammonia and at most 20% by weight of dissolved carbon dioxide and a purified wastewater stream containing at most 1 .000 ppm dissolved ammonia, wherein the plant comprises: i) a carbon dioxide degasser column comprising at least one bed of one or more random packings, at least one bed of one or more structured packings or at least one tray, a first feed inlet line entering the carbon dioxide degas- ser column at a position above at least one bed of one or more random packings, above at least one bed of one or more structured packings or above at least one tray, a second inlet line for feed or a mixture of feed and a liquid carbon dioxide depleted stream entering the carbon dioxide degas- ser column at a position below at least one bed of one or more random packings, below at least one bed of one or more structured packings or be- low at least one tray, wherein the bed of one or more random packings, the bed of one or more structured packings or the tray above which the first feed inlet line enters the carbon dioxide degasser column is the same as or located above the bed of one or more random packings, above the bed of one or more structured packings or above the tray below which the second inlet line for feed or a mixture of feed and a liquid carbon dioxide depleted stream enters the carbon dioxide degasser column, an overheads outlet line for a gaseous carbon dioxide rich stream and a bottom outlet line for a liquid carbon dioxide depleted stream, ii) an ammonia stripper column comprising an inlet line being directly connect- ed with the bottom outlet line of the carbon dioxide degasser column, an overhead outlet line for a gaseous ammonia rich stream, a bottom outlet line for a purified wastewater stream and a return line being connected with the bottom outlet line, wherein the bottom outlet line and/or the return line leads through an evaporator, and iii) a quencher column comprising an inlet line being directly or indirectly con- nected with the overhead outlet line of the ammonia stripper column, an in- let line for water and an outlet line for concentrated aqueous ammonia solu- tion.

Ammonia stripper column comprising an inlet line being directly connected with the bottom outlet line of the carbon dioxide degasser column means that between the bottom outlet line and the inlet line to the ammonia stripper column no further device is arranged, such as in particular no mixer and/or no phase separator or settler, respectively. Moreover, no base and/or acid dosing line is combined with any of the bottom outlet line and the inlet line to the ammonia stripper column.

The plant may comprise a (central) feed line, which splits into the first feed inlet line and into the second inlet line for feed or a mixture of feed and a liquid carbon dioxide depleted stream. Alternatively, the (central) feed line splits into the first feed inlet line and into a second feed line, wherein the second feed line leads into the second inlet line for feed or a mixture of feed. In the last mentioned alternative, the second feed line preferably combines with a recycle line for liquid carbon diox- ide depleted stream, thus forming the second inlet line for a mixture of feed, wherein the recycle line splits off from the bottom outlet line for liquid carbon diox- ide depleted stream of the carbon dioxide degasser column.

The present invention is not particularly restricted concerning the number of beds comprising one or more random packings, the number of beds comprising one or more structured packings or the number of trays included in the carbon dioxide degasser column. For instance, the carbon dioxide degasser column may com- prise one bed of one or more random packings, one bed of one or more structured packings or one tray, wherein the first portion of the wastewater stream is fed above and the second portion of the wastewater stream is fed below the bed of one or more random packings, the bed of one or more structured packings or the tray into the carbon dioxide degasser column. Suitable examples for structured packings are cross-channel structured packings.

In accordance with an alternative embodiment of the present invention, the carbon dioxide degasser column comprises two beds of one or more random packings, two beds of one or more structured packings or two trays on top of each other, wherein the first feed inlet line enters the carbon dioxide degasser column at a position above the upper bed of one or more random packings, above the upper bed of one or more structured packings or above the upper tray and the second inlet line for feed or a mixture of feed and a liquid carbon dioxide depleted stream enters the carbon dioxide degasser column at a position below the lower bed of one or more random packings, below the lower bed of one or more structured packings or below the lower tray.

In a further development of the idea of the present invention, it is suggested that the plant further comprises i) a heat exchanger, through which a) the second feed line or second inlet line and b) a condensate line being connected with the over- head outlet line for gaseous ammonia rich stream are led, and/or ii) a heat ex- changer, through which c) the second feed line or the second inlet line and d) the bottom outlet line for the purified wastewater stream of the ammonia stripper col- umn are led and/or iii) a heat exchanger, through which e) the second feed line or the second inlet line and f) the bottom outlet line for the liquid carbon dioxide de- pleted stream of the carbon dioxide degasser column are led.

Preferably, the plant comprises i) a heat exchanger, through which the second feed line and a condensate line being connected with the overhead outlet line for gaseous ammonia rich stream are led, and downstream thereof ii) a heat ex- changer, through which the second feed line and the bottom outlet line for the purified wastewater stream of the ammonia stripper column are led.

Good results are in particular obtained, if the plant further comprises downstream of the heat exchanger ii) a iii) heat exchanger, through which the second feed line and the bottom outlet line for the liquid carbon dioxide depleted stream of the car- bon dioxide degasser column are led.

The plant may further comprise, optionally downstream of one or more of the aforementioned heat exchangers, an evaporator comprising an inlet and outlet line for external heating medium as well as an inlet and outlet for the second inlet line for feed or a mixture of feed and a liquid carbon dioxide depleted stream.

In accordance with a further particularly preferred embodiment of the present in- vention, the ammonia stripper column comprises at least two beds of one or more random packings, at least two beds of one or more structured packings or at least two trays arranged on top of each other, wherein the inlet line being connected with the bottom outlet line of the carbon dioxide degasser column enters the am- monia stripper column at a position between two adjacent beds of one or more random packings, between two adjacent beds of one or more structured packings or between two adjacent trays, and wherein a return line enters the ammonia stripper column at a position below the at least two beds of one or more random packings, below the at least two beds of one or more structured packings or below the at least two trays and optionally another return line enters the ammonia strip- per column at a position above the at least two beds of either random packing, structured packing or trays.

The plant may further comprise a compressor, which is preferably a multi-stage turbofan compressor, being connected with the overhead outlet line for the gase- ous ammonia rich stream of the ammonia stripper column and an outlet line. Downstream of the compressor preferably a heat exchanger is arranged, to which the outlet line of the compressor and the bottom outlet line for a purified wastewater stream of the ammonia stripper column are led, wherein the evapora- tor is connected with the inlet line of the quencher column.

In a further development of the idea of the present invention, it is proposed that the aforementioned evaporator is also connected with a second line, which is prefera- bly the return line to the ammonia stripper column. Preferably, the second line or return line, respectively, is connected with the ammonia stripper column at a posi- tion above the at least two beds of random packing and/or structured packing.

In accordance with yet a further particularly preferred embodiment of the present invention, the quencher column of the plant comprises at least two beds of one or more random packings, at least two beds of one or more structured packings or at least two trays arranged on top of each other, wherein the inlet line for water en- ters the quencher column at a position above the uppermost of the at least two beds of one or more random packings, of the at least two beds of one or more structured packings or of the at least two trays and the vapor inlet line being direct- ly or indirectly connected with the overhead outlet line of the ammonia stripper column enters the quencher column at a position below the lowermost of the at least two beds of one or more random packings, of the at least two beds of one or more structured packings or of the at least two trays.

Preferably, the plant further comprises a return line, which is connected with the outlet line for concentrated aqueous ammonia solution of the quencher column and which leads back into the quencher column.

It is further preferred that the return line enters the quencher column at a position between two adjacent beds of one or more random packings, two adjacent beds of one or more structured packings or two adjacent trays.

Subsequently, the present invention is described by means of illustrative, but not limiting figures, in which:

Fig. 1 shows a schematic view of the plant in accordance with one exem- plary embodiment of the present invention.

Fig. 2 shows a schematic view of the plant in accordance with another exemplary embodiment of the present invention.

The plant 10 for treating an ammonia and carbon dioxide containing wastewater stream so as to produce a concentrated aqueous ammonia solution containing at least 5% by weight of dissolved ammonia and at most 20% by weight of dissolved carbon dioxide and a purified wastewater stream containing at most 1 .000 ppm dissolved ammonia shown in fig. 1 comprises a carbon dioxide degasser column 12, an ammonia stripper column 14 and a quencher column 16. The carbon diox- ide degasser column 12 comprises a first feed inlet line 18, a second feed inlet line 20 for a mixture of feed and a liquid carbon dioxide depleted stream and a bed 22 of structured packing, wherein the first feed inlet line 18 enters the carbon dioxide degasser column 12 at a position above the bed 22 of structured packing and the second feed inlet line 20 enters the carbon dioxide degasser column 12 at a posi- tion below the bed 22 of structured packing. The plant further comprises a central feed inlet line 24, which splits into the first feed inlet line 18 and into a second feed line 25, wherein the second feed line 25 leads into the second feed inlet line 20 for a mixture of feed and a liquid carbon dioxide depleted stream. More specifically, the second feed line 25 leads, seen from the central feed inlet line 24 in down- stream direction, through a first heat exchanger 26 and through a second heat exchanger 28 and then leads into the second feed inlet line 20, which leads through an evaporator (reboiler) 30, so that the second portion of the feed in the second feed line 25 and the mixture of feed and liquid carbon dioxide depleted stream in the second feed inlet line 20 are heated and evaporated, before the evaporated mixture of feed and liquid carbon dioxide depleted stream enters the carbon dioxide degasser column 12. The carbon dioxide degasser column 12 further comprises an overheads outlet line 32 for a gaseous carbon dioxide rich stream and a bottom outlet line 34 for liquid carbon dioxide depleted stream. The bottom outlet line 34 for liquid carbon dioxide depleted stream splits into a recycle line 35 and into the inlet line 36 to the ammonia stripper column 14, wherein the recycle line 35 combines with the second feed line 25 to the second feed inlet line 20 for the mixture of feed and liquid carbon dioxide depleted stream.

The ammonia stripper column 14 comprises two beds 38, 38’ of structured packing arranged on top of each other, wherein the inlet line 36 being connected with the bottom outlet line 34 of the carbon dioxide degasser column 12 enters the ammo- nia stripper column 14 at a position between the two adjacent beds 38, 38’ of structured packing. The ammonia stripper column 14 further comprises an over- head outlet line 40 for gaseous ammonia rich stream, a bottom outlet line 42 for purified wastewater stream and a return line 44 being connected with the bottom outlet line 42 for withdrawing a portion of the purified wastewater stream and re- turning it into the ammonia stripper column 14. The return line 44 splits from the bottom outlet line 42 and leads through an evaporator (reboiler) 46 and then en- ters the ammonia stripper column 14 at a position below the lower bed 38’ of struc- tured packing. The bottom outlet line 42 leads through the heat exchanger 28 and then out of the plant 10. The plant 10 further comprises a compressor 48, which is preferably a multi-stage turbofan compressor, which is connected with the over- head outlet line 40 for the gaseous ammonia rich stream of the ammonia stripper column 14 and further with a line 50, which connects the compressor 48 with the evaporator (reboiler) 46. The evaporator (reboiler) 46 has two outlets, one of which being connected to a vapor inlet line 54 of the quencher column 16 and the other one being connected to a condensate return line 56 to the ammonia stripper col- umn 14, which leads through the heat exchanger 26 and which enters the ammo- nia stripper column 14 at a position above the upper bed 38 of structured packing.

Also the quencher column 16 comprises two beds 58, 58’ of structured packing arranged on top of each other. Furthermore, the quencher column 16 comprises an inlet line 60 for water, which enters the quencher column 16 at a position above the uppermost of the two beds 58 of structured packing, whereas the inlet line 54 being indirectly connected with the overhead outlet line 40 of the ammonia stripper column 14 enters the quencher column 16 at a position below the lowermost of the two beds 58’ of structured packing. In addition, the quencher column 16 comprises an outlet line 62 for concentrated aqueous ammonia solution leading through heat exchanger 66. Downstream of the heat exchanger 66, line 62 splits into leading back into the quencher column 16 at a position between the two adjacent beds 58, 58’ of structured packing and a line to outside battery limits, in which the product ammonia solution is obtained. Finally, the quencher column 16 comprises an out- let line 68 for withdrawing vent gas from the quencher column 16.

The plant 10 for treating an ammonia and carbon dioxide containing wastewater stream shown in figure 2 is the same as that shown in figure 1 except that it addi- tionally comprises a further heat exchanger 70, through which the inlet line 36 of the ammonia stripper column 14 being connected with the bottom outlet line 34 of the carbon dioxide degasser column 12 and through which the second feed line 25 lead in order to heat the second portion of the feed led through the second feed line 25.

During the operation of the plants 10 shown in figures 1 and 2, an ammonia and carbon dioxide containing wastewater stream, such as filtered fermentation broth or an anaerobically digested cattle manure effluent, is led as feed into the plant via the central feed inlet line 24. The feed is split into a first portion of the wastewater stream, which is introduced via the first feed inlet line 18 into the carbon dioxide degasser column 12 above the structured packing 22, and into a second portion of the wastewater stream. In accordance with the present invention, the mass flow ratio of the first portion of the wastewater stream is adjusted so as to be 0.01 to 0.6 based on the total wastewater stream fed into the carbon dioxide degasser column.

The second portion of the wastewater stream is fed via the second feed line 25 through heat exchangers 26, 28 in the embodiment of figure 1 and through evapo- rators 26, 28, 70 in the embodiment of figure 2, in order to heat the second portion of the wastewater stream. While the second portion of the wastewater stream is heated in heat exchanger 26 by the condensed liquid stream withdrawn from the ammonia stripper column 14 as overheads fraction via lines 40, 50, 56, the wastewater stream is heated in heat exchanger 28 by the purified wastewater stream withdrawn as bottom fraction from the ammonia stripper column 14 via line 42 and the wastewater stream is heated in heat exchanger 70 of the embodiment of figure 2 by a portion of the liquid carbon dioxide depleted stream being with- drawn as bottom fraction from the carbon dioxide degasser column 12 via lines 34, 36. Downstream thereof, the heated second portion of the wastewater stream is combined at the entrance of line 20 with a portion of the liquid carbon dioxide depleted stream being withdrawn as bottom fraction from the carbon dioxide de- gasser column 12 via lines 34, 35, wherein the so obtained mixture is evaporated in the evaporator (reboiler) 30 by means of an external heating medium. The evaporated mixture of the second portion of the wastewater stream with the por- tion of the carbon dioxide depleted stream is introduced into the carbon dioxide degasser column 12 below the structured packing 22 and rises in the carbon diox- ide degasser column 12 upwards, whereas the colder first portion of the wastewater stream being fed to the top of the carbon dioxide degasser column 12 trickles in the carbon dioxide degasser column 12 downwards. On account of the heat and mass transfer between the two phases being increased by the structured packing 22, enriched pure gaseous carbon dioxide with water and a low fraction of ammonia is separated from the liquid phase and is withdrawn as overheads frac- tion through line 32 from the carbon dioxide degasser column 12. The liquid frac- tion, in turn, is depleted from carbon dioxide and the liquid carbon dioxide depleted stream is withdrawn from the carbon dioxide degasser column 12 as bottom frac- tion through line 34.

The liquid carbon dioxide depleted stream is led in the embodiment of figure 1 through line 36 directly into the ammonia stripper column 14 and in the embodi- ment of figure 2 first through the heat exchanger 70 and then through line 36 into the ammonia stripper column 14. A portion of the bottoms fraction being withdrawn from the ammonia stripper column 14 through line 42 is evaporated in the heat exchanger (reboiler) 46 and fed back through the return line 44 into the ammonia stripper column 14. On account of the heat and mass transfer between the two phases being increased by the structured packings 38, 38’ enriched gaseous am- monia together with the remaining carbon dioxide and some water is separated from the liquid phase and is withdrawn as overheads fraction through line 40 from the ammonia stripper column 14. The purified liquid wastewater stream, in turn, is depleted from ammonia and carbon dioxide and is withdrawn from the ammonia stripper column 14 as bottom fraction through line 42. While the purified liquid wastewater stream is withdrawn from the plant 10, the gaseous ammonia rich stream is sent through lines 40, 50, 56 after having been led through the compres- sor 48, sent through line 50 and through the heat exchanger (reboiler) 46, from which the non-condensed fraction is sent vial line 54 into the bottom part of the quencher column 16. The gaseous ammonia rich stream is contacted in the quencher column 16 with the liquid water having been introduced into the upper part of the quencher column 16 through line 60 and with the concentrated aqueous ammonia solution being withdrawn from the ammonia stripper column 14 via line 62 and being partly returned into the section between the two beds 58, 58’ of the quencher column 16 through line 64, whereas the other part is drawn as product ammonia solution to outside battery limits. On account of the heat and mass trans- fer between the vapor phase and the liquid phase being increased by the struc- tured packings 58, 58’ the ammonia and a fraction of the residual carbon dioxide dissolve in the water forming the concentrated aqueous ammonia solution contain- ing at least 5% by weight of dissolved ammonia and at most 20% by weight of dissolved carbon dioxide, which is withdrawn from the quencher column 16 as bottom fraction, whereas the remaining gases including gaseous carbon dioxide is withdrawn as overheads fraction from the quencher column 16 through the outlet line 68.

Reference numerals

10 Plant

12 Carbon dioxide degasser column

14 Ammonia stripper column

16 Quencher column

18 First feed inlet line into the carbon dioxide degasser column

20 Second feed inlet line into the carbon dioxide degasser column

22 Bed of structured packing of carbon dioxide degasser column

24 Central feed inlet line

25 Second feed line

26 Heat exchanger

28 Heat exchanger

30 Evaporator (reboiler) of the carbon dioxide degasser column

32 Overheads outlet line of the carbon dioxide degasser column

34 Bottom outlet line of the carbon dioxide degasser column

35 Recycle line

36 Inlet line to ammonia stripper column

38, 38’ Bed of structured packing of carbon dioxide ammonia stripper col- umn

40 Overhead outlet line of the ammonia stripper column

42 Bottom outlet line of the ammonia stripper column

44 Return line of the ammonia stripper column

46 Evaporator (reboiler) of the ammonia stripper column

48 Compressor

50 Connection line

54 Inlet line to quencher column

56 Return line to ammonia stripper column 58, 58’ Bed of structured packing of quencher column

60 Water inlet line

62 Outlet line for concentrated aqueous ammonia solution

64 Return line to quencher column 66 Heat exchanger

68 Outlet line

70 Heat exchanger