The method of processing gas containing methane and at least one higher hydrocarbon and water

 

(57) Abstract:

The invention relates to a method for processing natural gas to remove water and/or extraction of impurities higher hydrocarbons. Pre-processed gas is divided into two volumes, each of which passes at least one stage of cooling. One of the fractions of the aqueous phase obtained after cooling, condensation and separation, is brought into contact with the treated gas inside the contact zone. The aqueous phase includes a solvent that is partially miscible with water. As a result, the portion of the processed gas is saturated with solvent. Upholding separate the cleaned gas from the aqueous phase and liquid phase hydrocarbons. The liquid phase and the solvent re-use in the process of gas purification. The technical result is to reduce capital and energy costs in the dehydration of natural gas with simultaneous separation of impurities higher hydrocarbons. 12 C. p. F.-ly, 4 Il.

The invention concerns a method of processing gas containing methane and at least one higher hydrocarbon and water to remove water and extraction of higher hydrocarbons (higher hydrocarbons).

The method according to the invention allow the part of the condensed hydrocarbons, contained in natural gas, through a streamlined and integrated way.

Petroleum products and, in particular, natural gas, and other containing hydrocarbon gas, such as gases from refineries, contain products that are undesirable for their transportation and/or manipulation.

Of such products removed one of the main component is water, which is a promoter hydrate and promote corrosion, especially when the oil contains acid components, such as H2S and/or CO2. Hydrates can cause driving the transporting pipelines, and the corrosive effect of the acid gases contained in natural gas, leads to bad piping, processing equipment and impairment of natural gas to consumers.

These two phenomena are accompanied by extremely adverse consequences that may interrupt the process of production of hydrocarbons.

The processing gas may further include a stage of extraction of higher hydrocarbons, for example, liquid natural gas (LGN), containing fraction GPL and gasoline.wow fraction (C5

There are various methods of processing natural gas.

In French patent FR-B-2605241 described processing method using physical chilled solvent, allowing complex operations to natural gas processing: dehydration, separate or in combination with the extraction of higher hydrocarbons and/or deoxidation of the specified gas in the case of a content of acid components.

In French patent FR-B-2636857 it is shown that if the process stage of separation of higher hydrocarbons (LGN) recovery of the solvent can be more effective through the use stage of leaching liquid hydrocarbons water formed in the dehydration process gas.

Applications of such methods are described, for example, in the publication "IFPEXOL for Environmentally Sound Gas Processing" (EFFEXOR for environmentally friendly gas technology), J. Lara, A., Minkkinen and S. Patel, presented at the 71st Conference "GPA" in March 1992 Anagama, California, USA.

In the publication "Integrated Natural Gas Treatment: Gained Industrial Experience with IFPEXOL Process" (Full processing of natural gas: increased experience on CR 95 in Cannes (France) in November 1995, describes, in particular, the method of water washing liquid hydrocarbon phase to remove at least part of the contained solvent.

In Fig. 1 shows an illustration of the method described in the above sources prior art regarding the processing gas containing methane, water, at least one condensed hydrocarbons and possibly acidic components. The method is as follows.

Processed natural gas is delivered by pipeline 1. Part or all of this gas quantity is put in contact in the zone of contact G1 formed, for example, a nozzle, with a mixture of solvent and water is supplied through pipe 2.

Solvent used may be selected from the set consisting of methanol, ethanol, propanol, methylpropional ether, ethylpropyl ether, dipropylamine, ether methyltricyclo butyl, dimethoxymethane, dimethoxyethane and methoxyethanol. Preferably the solvent used is methanol.

Solvent gas phase is removed at the head of the pipeline 3. In the lower part of the pipe 4 is devoting substantially freed from solvent aqueous phase.The gas phase head part containing water and a solvent, most often, is in the saturation state. It is cooled in the heat exchanger E1 refrigerant so as to allow condensation of the aqueous phase of a solvent and a liquid hydrocarbon phase. Indicated that the amount of solvent entrained in the aqueous phase at the exit of the contact zone GI, may be sufficient to prevent the difficulties associated with the formation of hydrates at the cooling stage E1. Pipeline 5 in the process can be entered Supplement to make up for losses of solvent in the treated gas, liquid hydrocarbon fraction (LGN) and possibly in the water discharged through the pipeline 19. On the same pipe 19 can be made descent flow, Chibis gas and liquid phase is withdrawn from heat exchanger E1 via the pipeline 6. Both liquid phase and gaseous phase are separated in the vessel B1.

Dehydrated treated gas is withdrawn from the listed capacity on the pipeline 7. Both the liquid phase resulting from the condensation are separated by settling in the tank B1.

The aqueous phase formed mainly of water and solvent, is withdrawn from the vessel B1 via the pipeline 8. Pump P1 allows the re-injection of the indicated aqueous phase through the pipeline 9 in the pipe 2, then in the contact zone G1.

The hydrocarbon phase formed mainly condensed hydrocarbons natural gas (C3+) (containing possibly dissolved ethane and methane) and the solvent can be discharged through the pipeline 10 in the path of stabilization and washing. This redistribution can be carried out heat exchange between the gas received from the contact zone G1, and the hydrocarbon phase is withdrawn through pipeline 10. In Fig. 1 it is not shown. Pump P2 provides a supply of liquid hydrocarbons by pipeline 11 in column S1 stabilization. The purpose of this operation is to separate from the named liquid hydrocarbon phase is the most volatile component (C1and C2drawn from the process which I pipeline 13 in the area of water washing G2 in order to remove the contained solvent.

The aqueous phase derived from the contact zone G1 in line 4 and purified at least in part on the solvent enters the pump P3. Part of this aqueous phase with a controlled flow is directed into the contact zone G2 through the pipeline 14. The other part is discharged through line 19.

In the specified contact zone G2 part of the aqueous phase, received on line 14, allows the washing of the hydrocarbon phase. The solvent is characterized by a great affinity with water than with the hydrocarbon phase, is captured at least partially in the aqueous phase at the end of this stage.

Liquid hydrocarbon phase, purified from the greater part of the solvent contained in it at the entrance to the contact area G2, is discharged through pipe 15.

Solvent liquid phase is removed from the contact zone G2 through the pipeline 16. This phase enters the pump P4 and served in the contact zone G1. Depending on the concentration of solvent specified phase is served either in the contact zone G1 through the pipeline 17, or in the pipeline 2 for mixing with the aqueous phase coming from the containers B1 through the pipeline 9.

Compared to previously used techniques this method to herbarium and weight equipment, what is particularly optimal in the context of the production of hydrocarbons at sea. In addition, the separation of water and solvent in contact with the treated gas eliminates the separation by distillation.

The objective of the invention is to develop a method in order to reduce capital investment, size and weight, and manufacturing costs of processing gas.

The problem is solved by the method and installation according to the invention, which are primarily designed for the dehydration of a gas, e.g., natural gas containing water and at least one higher hydrocarbon, and to provide at least partial separation of condensed hydrocarbons.

The principle of the method according to the invention is that the treated gas is separated into at least two parts (1) and (2):

- volume (1) is cooled in the absence of solvent to a temperature close to the temperature of hydrate formation, but exceeding it, which results in the destruction of a significant part of the condensed fractions and

- volume (2) is brought into contact with an aqueous phase containing a solvent and formed in the second stage, cooling the aqueous phase, cleansed at least partially from the solvent, and, on the other hand, the gas phase containing solvent, which allows to cool the gas to a temperature below the temperature of the cooling gas volume (1) at the first stage of cooling and to comply with the relevant requirements gas requirements.

The method according to the invention differs in that it provides for the following stages:

(a) the processed gas is divided into two parts (1) and (2);

b) volume of gas (1) is cooled, resulting in the condensation of the aqueous liquid phase and the liquid phase of higher hydrocarbons;

C) separate phases formed during cooling (b);

g) the specified volume (2) processed gas formed under division (a) bring into contact with water containing solvent phase within the contact zone, while contained in the aqueous phase of the solvent extracted gas, which at the end of this stage (g) contaminated solvent, and water purified at least in part on the solvent, the aqueous phase is given in base contact zone;

d) in the introduced additive solvent;

d) cool the volume of gas formed at stages (C) and (d), and in prisutstviye solvent containing aqueous phase and a liquid hydrocarbon phase;

g) share of processed gas from which at least partially removed water and higher hydrocarbons, aqueous phase and a liquid hydrocarbon phase formed during cooling (e);

C) at least partially serves the aqueous phase with a solvent content after stage (f) through (g).

The method according to the invention is explained in more detail in Fig. 1-4, which show:

Fig. 1 - the method according to the prior art;

Fig. 2-4 are examples of the method according to the invention.

The example implementation shown in Fig. 2

The processed gas is divided into two volumes supplied through the pipes 51 and 52.

The first volume of gas flowing through the pipeline 52 is cooled by the heat exchanger E51. At the outlet of this heat exchanger, the gas temperature approaches the temperature of hydrate formation in the treated gas, but exceeds it. Used in this heat exchanger the cooling medium may be a cooling installation environment, such as air or water, or the entire amount or only a portion of the treated gas coming from the tank B1 to line 7 and through the heat exchanger E52. Thus obtained partially condensed environment Poduene E51, are separated by settling in the tank B51. It should be noted that these two frameworks do not contain solvent. Liquid hydrocarbon fraction is removed from the process through pipe 57 for either recycling or re-submission in the head part of the heat exchanger E52, as shown by the dashed line. The resulting aqueous phase, not containing solvent, is removed from the process through pipe 58. Preferably, it was then used as a phase for washing liquid hydrocarbon phase, contaminated solvent, as described in the example implementation shown in Fig. 4.

The second volume of gas supplied through the pipe 51, enters the base contact zone G50 ensures that the extraction of at least part of the solvent contained in the aqueous phase is supplied through pipe 53 in the head part of the contact zone G50. At least partially purified from solvent aqueous phase is given in base contact zone G50 pipeline 55, and the gas content of the solvent is given in the head part of the contact zone G50 pipeline 54.

Coming through the pipe 59 from the three-phase capacity B51 gas mixes with containing the I additional a quantity of solvent. The amount of such additives is controlled in order to obtain the gas concentration such that the RSC which eliminates any risk of hydrate formation at later stages of cooling, thus compensating the loss of solvent in the treated gas and liquid fractions.

Thus obtained gas mixture with a solvent content is supplied by pipeline 60 to the heat exchanger E52, in which it is cooled in the heat exchange with the treated gas. Cooling continues then in the heat exchanger E1 via a refrigerant to provide the condensation of water and hydrocarbon fractions, corresponding to the requirements of the process.

Gas and liquid phase emerging from the heat exchanger E1 via pipeline 63, are separated by settling in the tank B1.

Dehydrated processed gas is discharged through line 7. The liquid hydrocarbon phase is removed from the process through pipe 64. It can be used at the stages of stabilization and/or washing, as disclosed in the example implementation shown in Fig. 4. Aqueous liquid phase containing the solvent is drained from the tank B1 via the pipeline 8 and is fed by pump P1 through the pipeline 53 goals in who may use the area between the aqueous phase containing solvent and a volume of gas for the extraction solvent in the contact column is dramatically reduced size, this uses only a reduced portion of the processed gas component, typically less than 50%, but can be, for example, less than 30%.

Used in the method according to the invention the solvent is at least partially miscible with water in order to exert an inhibitory influence on the formation of ice and/or hydrates. To enable its smooth extraction of the aqueous solution in contact with the treated gas to its boiling point should be low, preferably below the boiling point of water, or he must form a water azeotrope mixture with a low boiling point.

This solution can be, for example, alcohols, namely methanol, ethanol or propanol, an ether, in particular methylpropyloxy ether, DIPROPYLENE ether, methyl ether-triple-butyl, ketone or, for example, dimethoxymethane, dimethoxyethane or methoxyethanol, this list is attached as an unlimited example.

The temperature at the end of stage (e) in the method according to the invention is typically from -5 to -100oC. lower Than the specified temperature, the greater must be the concentration of the solvent in podnasepsni the invention is, typically, from 40 to 90 weight. %.

Volume (2) gas can flow through the contact area on the stage (d) is preferably from 10 to 50% of the total number of processed gas.

On stage (W) may be a cooling gas or by external cooling loop, or as a result of expansion when passing through the valve or turbine.

The temperature at the end of stage (b) cooling is preferably from +5 to +30oC. This stage cooling can be provided, for example, or by heat exchange with the treated gas, or as a result of heat exchange with an external refrigerant, such as water or air or, if necessary, as a result of heat exchange with the refrigerant circulating through the external circuit.

Volume (2) gas received in the contact area on the stage (g), can be preheated in order to simplify the extraction of the solvent from the aqueous phase received in the head part of the contact zone at the stage (g). You can act according to the scheme in Fig. 3.

Of the doses received in the contact area G50 pipeline 51, pre-heated in the heat exchanger E53 by leaving the contact zone G50 gas, then calobra at the end of this heating stage may be, for example, from 80 to 150oC. This method is particularly preferred in the case when the applied solvent is heavier than methanol, for example, when using ethanol.

The aqueous phase obtained at the end of stage (C) of the process can be optimally used for washing liquid collected at the end of stage (f) process hydrocarbon phase containing methanol. Applied in this case, the implementation shown in Fig. 4.

The processed gas is distributed in two volumes (1) and (2). Volume (2), bypass pipeline 101, is fed into the base contact zone G100. An aqueous solution containing the solvent flows through the pipe 103 to the head of a specified surface area, as part of an aqueous solution with a solvent content generated in washing condensate, flows through the pipe 119 on the side of the column. A specified part of an aqueous solution is used in an amount, by which the flow of an aqueous solution with a very low solvent content, extracted from the lower part of the contact zone through the pipeline 105, approximately corresponds to the amount of water to be removed from the treated gas.

Circulating through the pipeline 102 segosa when washing condensates and supplied through pipelines 118 and 120. The mixture enters the heat exchanger E101, in which she is brought to a temperature close to the temperature of hydrate formation, but exceeding it.

The mixture is partially condensed in and out of the heat exchanger through the pipeline 106, is directed to a container B51 three-phase separation. Aqueous phase and a liquid hydrocarbon phase, condensed on the cooling stage E101, are separated by settling in the tank B51. The aqueous phase with a low content of solvent received from the tank B51 pipeline 108, is sent to a static mixer M100, providing washing liquid hydrocarbon phase containing solvent. Gas, abstracted from the three-phase capacity B51 pipeline 109, mixed with the solvent gas received by pipeline 104 from the contact zone.

Received from the three-phase capacity B51 liquid hydrocarbon phase is withdrawn from the process through pipe 107A and goes on the stage of stabilization. It can also be used in the process and submitted by pipeline 107B in the upper part of the heat exchanger E102.

Thus obtained in the pipe 111, the mixture is directed into the heat exchanger E102, in which it is cooled in the th is m calculation to cause condensation of water fraction and a liquid hydrocarbon fraction.

Liquid and gas phase which is withdrawn from heat exchanger E1 via pipeline 113, are separated in the vessel B1.

The processed gas is diverted from the listed capacity on the pipeline 7. As shown in Fig. 4, the said gas may be used as a refrigerant in heat exchangers E102 and E101 before it is removed from the process. Both the liquid phase formed by condensation in the heat exchanger E1, separated by settling in the tank B1. The condensed liquid hydrocarbon phase that is derived from the capacity of B1 pipeline 114, is stable. The purpose of this activity is to separate from the hydrocarbon phase is the most volatile component (C1and C2drawn from the process pipeline 115. The liquid hydrocarbon phase containing greater than C2components, is supplied by pipeline 116 in the mixer M100, in which it is brought into contact with an aqueous phase with a low content of solvent received from the separation vessel B51 pipeline 108. A large part of the solvent, preferably water-soluble, at this stage goes from the hydrocarbon phase is about after settling discharged by pipeline 121 washed and stabilized liquid hydrocarbon phase, reusable and pipeline 118 - solvent aqueous phase. This aqueous phase partially to the head portion of the heat exchanger E101 pipeline 120 and partially fed through pipe 119 to the staging area surface area G1OO. The relative flow when passing through the pipes 119 and 120 is set so as to maintain constant the amount of water and solvent circulating in the process.

You can apply other link is not beyond the bounds of the present invention.

In particular, it is possible to direct the aqueous phase, formed during the washing liquid hydrocarbon phase, a fully or partially in the second stage of cooling in the upper part, as shown in Fig. 4, illustrating by dotted lines the pipeline 122 allows you to direct the aqueous phase from the tank B100 on the area located above the heat exchanger E102.

Rinsing liquid hydrocarbon phase by the aqueous phase can be performed in a single mixer with behind the sump. It can also be carried out in countercurrent column, which can be, for example, the Packed column. Can PR is adiya's (g) between the amount (2) processed gas and aqueous phase can also be carried out in different columns, for example, in tray or Packed column. When using Packed columns can be used in structured packings.

Used in this method, the heat exchangers can be of different types, for example, either pipe or calender, or heat exchanger, e.g. welded aluminum plate heat exchanger.

Advantages of the method according to the invention, described with reference to Fig. 2, are illustrated by example 1. Example 2 allows you to specify the conditions of application of the method in the case of washing liquid hydrocarbon phase. The description of this example is shown with reference to Fig. 4.

Example 1

Natural gas at the place of its receipt, the pressure is 5 MPa, temperature - 67oC (composition see below), gas vodonosen (water content at the input of the process is about 6000 ppm/mol). Its consumption is 380 t/h, which corresponds to approximately 10 Mm3a day.

Composition Weight. %

N2- 0,8

CO2- 7,6

Methane - 62,7

Ethane - 10,5

Propane - 5,6

Bhutan - 3,3

Pentane - 6,8

C6+ - 2,7

In this example, the solvent used is methanol.

90% of the produced gas is sent through a pipe 52 to the heat exchanger E51. On CLASS="ptx2">

From the separation vessel B51 out the following three phases:

- 335,60 t/h of gas with a residual moisture content of 560 ppm/mol,

by 1.68 t/h of water, which can either withdraw from the process, or use repeated washing condensed hydrocarbon phase received from the tank B1. This number represents approximately 80% of the water contained in the treated gas,

-6,60 t/h condensed hydrocarbon phase (LGN) containing methanol, which can be stabilized prior to their removal from the process for disposal or which can be re-submitted to the process on the area above the heat exchanger E52.

The remaining volume of the produced gas (10%) is supplied to the contact zone G50 pipeline 51. Contactor G50 contains structured nozzle. Recycled aqueous solution of methanol is supplied to the head portion of the contactor on the pipe 53 at a temperature of -35oC. At the end of stage contact depleted solvent content water solution is removed from the contactor through the pipeline 55. This solution contains 136 ppm. weight. the solvent. The total amount of the aqueous phase, exhaust piping 58 and 55 (about 2 t/h) approximates krolowej part of the nozzle on the pipe 54, as a result of contact with an aqueous solution contaminated solvent. Its content in the gas is 1.20 weight. %. This gas mixes with the gas flowing from the tank B51, and receive a Supplement of methanol at a rate of 175 kg/h before you enter exchangers E52 and E1. This additive is selected so as to avoid any risk of hydrate formation.

At the exit of the heat exchanger E1, the temperature is 350oC. Capacity B1 allows a division into the following three phases:

- 315 t/h of treated gas with a residual moisture content 5,13 ppm/mol. This gas may, if desired, be used as a refrigerant in the heat exchanger E22 and E21 before you enter into the distribution network;

- 1 t/h of the aqueous phase with the solvent supplied to the contact zone G50;

- 52,6 t/h condensed hydrocarbon phase, which may optionally be stabilized, and then before disposing washed to remove solvent (2,5 weight. %).

This example shows that the application of the method according to the invention allows to obtain performance equivalent to the performance of the method-analogue, in which the volume of gas R is Due to this size, the weight and cost of the contactor, which is the crucial method of this type, therefore reduced.

Example 2

Natural gas at the place of its reception, its pressure, temperature, flow rate and composition corresponds to example 1. In this example, the solvent used is methanol.

65% of the produced gas is mixed in the pipe 102 with a portion of the aqueous phase containing the solvent in the washing condensates, and to divert the pipeline 118. The mixture is fed into the heat exchanger E101. At the outlet of this heat exchanger in the pipeline 106, the temperature of the partially condensed gas is 20oC. From the tank B51 split out the following three phases:

- 242,40 t/h of gas with a residual moisture content of 600 ppm/mol, which is discharged through pipe 109;

- 1.75 t/h of water with low solvent content (7 weight. %) used for washing the condensed hydrocarbon phase coming from the vessel B1;

- 4,70 t/h condensed hydrocarbon phase, which optionally may be recycled (with feed pipe 107B) or set aside in the stabilization column (pipe 107A).

The remaining part of the produced gas (45%) served in contae solvent, received from the container B1, to the head portion of the contactor through the pipeline 103, and the fraction of an aqueous solution formed by leaching of the condensate in the pipe 119, served on the side. At the end stage of contacting an aqueous solution depleted in solvent content, is withdrawn from the contactor through the pipeline 105. In this solution, the content of solvent is 140 ppm weight. The flow rate of the aqueous phase which is withdrawn from the contact zone of about 2 t/h, approximately corresponds to the amount of water contained originally in 380 t/h of treated gas.

The gas discharged through the pipeline 104 of the head portion of the nozzle, when in contact with aqueous solutions contaminated solvent. It is mixed with gas from the tank B51 and receive a Supplement of the solvent in a quantity of 50 kg/h before you enter exchangers E22 and E1. This additive is selected so that you can avoid any risk of hydrate formation.

At the exit of the heat exchanger E1, the temperature is -35oC. Capacity B1 allows a division into the following three phases:

- 320 t/h of treated gas with a residual moisture content 5,13 ppm/mol. This gas may, if desired, be BR>
- 1 t/h of the aqueous phase with solvent, supplied partially in the contact area G100 and partly in the upper part of the heat exchanger E101;

- 55,4 t/h condensed hydrocarbon phase, which is mixed with the condensate formed in the vessel B51, prior to its stabilization. At the stage of stabilization of a large part of the methane and ethane, contained in the condensate is removed. 50,60 t/h stabilized condensates are mixed in the mixer M100 with water containing a small amount of solvent and received from the tank B51.

After settling in the tank B100 formed two phases:

- washed condensates with a residual solvent content of 700 ppm weight. and

- water phase content of recycled solvent, as described above.

This example shows that dehydration, extraction of gasoline with chilled solvent and washing of the condensates can be accessed by using the method according to the invention in contact only 45% of the produced gas.

Like in example 1, the size, weight and cost of the contactor, which is crucial for a method of this type is significantly reduced. In addition, we reduced the consumption rastvoritelyami fact, it contains the following stages: a) the processed gas is divided into two parts (1) and (2); b) volume of gas (1) is cooled, resulting in the condensation of the aqueous liquid phase and the liquid phase of higher hydrocarbons; C) share phase, formed during cooling (b); d) the specified volume (2) processed gas formed under division (a) bring into contact with water containing solvent phase within the contact zone, while contained in the aqueous phase of the solvent extracted gas, which at the end of this stage (g) contaminated with a solvent, and purified, at least in part on the solvent, the aqueous phase is given in base contact zone; d) the system is injected additive solvent; (e) cooling the gas formed at stages (C) and (d), in the presence of a solvent, separately or at least in a partial mixture, with the possibility of partial condensation of the water-containing solvent phase and a liquid hydrocarbon phase; and (g) share of processed gas from which at least partially removed water and higher hydrocarbons, an aqueous phase and a liquid hydrocarbon phase formed during cooling (e); C) at least partially aqueous phase is, that formed in stage (g) liquid hydrocarbon phase is brought into contact with an aqueous phase formed at least in part on stage (in) for at least partial removal of the contained solvent.

3. The method according to p. 2, characterized in that the aqueous phase containing the solvent and formed at the stage of contact, is used at the beginning of the cooling phase (b) and/or stage of contact (d).

4. The method according to one of paragraphs. 1-3, characterized in that the rinsing liquid phase hydrocarbons formed in stage (e) is carried out after the stage of stabilization that allows you to remove the contained volatile components.

5. The method according to one of paragraphs. 1-4, characterized in that the solvent is selected from the range of: methanol, ethanol, propanol, methylpropyloxy ether, ethylpropyl ether, DIPROPYLENE ether, the ether methyltricyclo butyl, dimethoxymethane, dimethoxyethane and methoxyethanol.

6. The method according to one of paragraphs. 1-5, characterized in that the solvent is methanol.

7. The method according to one of paragraphs. 1-6, characterized in that the recycled submitted at stage (g) the aqueous phase contains from 40 to 90 weight. % solvent.

8. The method according to one of the LASS="ptx2">

9. The method according to one of paragraphs. 1-8, characterized in that the gas volume flow through the area on stage (d) is from 10 to 50% of the total amount of gas.

10. The method according to one of paragraphs. 1-9, characterized in that it contains, in addition, the stage of washing liquid hydrocarbon phase to extract the solvent.

11. The method according to p. 10, characterized in that the specified stage leaching is carried out through the use of mixer-settlers.

12. The method according to p. 10, characterized in that the specified stage leaching is carried out by contacting inside the column.

13. The method according to one of paragraphs. 1-12, characterized in that the amount of the (2) supplied in the contact zone together with the water formed in stage (C) phase, pre-heated.

 

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