Carbonization tower alternating system of sodium carbonate production device

Abstract

The invention relates to the field of sodium carbonate production, in particular to a carbonization tower alternating system of a sodium carbonate production device, which is characterized by comprising carbonization tower groups, each carbonization tower group comprises a plurality of carbonization towers, and the plurality of carbonization towers are switched between an alkali production state and a cleaning state in turn; the crystallized ammonia two-liquid pipeline is respectively connected with each carbonization tower and is used for cleaning the carbonization towers; the cleaning gas pipeline is respectively connected with each carbonization tower and is used for cleaning the carbonization towers; the lower section gas pipeline is respectively connected with each carbonization tower and is used for preparing alkali by the carbonization towers; the alkali outlet pipeline is used for discharging alkali from the carbonization tower; the second cleaning ammonia liquid outlet pipeline is connected with a second cleaning ammonia barrel, is used for storing second cleaning ammonia liquid and is connected with the second cleaning ammonia liquid inlet pipeline; and the cleaning ammonia two-liquid inlet pipeline is used for conveying cleaning ammonia two-liquid to the carbonizer of the group for alkali production and cleaning the alkali outlet pipe cleaning pipeline of the carbonizer. The automation degree of the carbonization tower alternation process in the sodium carbonate production process can be improved, and the labor intensity of workers is reduced.

Description

TECHNICAL FIELD

[0001] The present application relates to the field of soda production, and particularly relates to a carbonation tower rotation system for a soda production device. BACKGROUND

[0002] The operation state of the carbonation tower includes an alkali production state, a cleaning state and a shutdown state. After one round of alkali production operation, the carbonation tower is generally changed to the cleaning state due to the scab formed in the tower, which affects the alkali production operation of the carbonation tower. After the tower is changed to the cleaning state, the scab condition in the tower is improved, and after 18-48 hours of cleaning, the tower is put into the alkali production state again, and the above process is repeated. If the carbonation tower needs to be inspected and repaired, the carbonation tower needs to be stopped and disconnected from the system for the inspection and repair operation.

[0003] The carbonation tower rotation method mainly includes two methods, i.e. a tower pressure method and a tower pressure holding method. The tower pressure method is to simultaneously increase the tower pressure of the original alkali production tower and decrease the tower pressure of the original cleaning tower before rotation, and finally the saturated solution and the suspension in the original alkali production tower are pressed into the original cleaning tower by the pressure difference, so that the tower pressure of the two towers is balanced, the original alkali production tower enters the cleaning state, and the original cleaning tower enters the alkali production state. The tower pressure holding method is to directly put the original cleaning tower into the alkali production state, so that the carbonation tower enters the alkali production state, and the original alkali production tower decreases the solid-liquid ratio and then changes to the cleaning state.

[0004] The tower pressure holding method has better flexibility and simpler process. As long as the production conditions are met, the alkali production operation can be implemented, and the disadvantage is that there are many fine crystals in the initial alkali production stage, and the influence on production is large. The tower pressure method is more complex in process and operation than the tower pressure holding method, and the fine crystals generated in the rotation process are relatively less, but the operation is complex, more valves need to be manually switched, the manual labor intensity is large, and the efficiency is low. The existing method has the problem that the crystallization is poor in the initial alkali production stage during the rotation of the carbonation tower, which affects the product quality, the product energy consumption and the like. At the same time, the low degree of automation leads to large labor intensity of the site personnel and low production efficiency. SUMMARY

[0005] The present application relates to the field of soda production, and particularly relates to a carbonation tower rotation system for a soda production device.

[0006] In order to achieve the above object, the present application adopts the following technical scheme:

[0007] The present application relates to the field of soda production, and particularly relates to a carbonation tower rotation system for a soda production device.

[0008] The carbonation tower group includes a plurality of carbonation towers, and the plurality of carbonation towers are switched between the alkali production state and the cleaning state in turn.

[0009] The crystallized ammonia liquid pipeline is connected with each carbonation tower respectively, and provides crystallized ammonia liquid for cleaning of the carbonation tower.

[0010] The cleaning gas pipeline is connected to each carbonization tower respectively for cleaning the carbonization tower;

[0011] The lower section gas pipeline is connected to each carbonization tower respectively for producing alkali in the carbonization tower;

[0012] The alkali outlet pipeline is connected to the alkali outlet tank respectively for discharging alkali from the carbonization tower;

[0013] The cleaning ammonia liquid outlet pipeline is connected to the cleaning ammonia bucket for storing cleaning ammonia liquid and connected to the cleaning ammonia liquid inlet pipeline of the group;

[0014] The cleaning ammonia liquid inlet pipeline of the group is used for conveying cleaning ammonia liquid to the carbonization tower of the group for alkali production and cleaning the alkali outlet pipeline of the tower.

[0015] As a further preferred solution, at least four carbonization towers are included in each carbonization tower group, and the four carbonization towers are switched between the alkali production state and the cleaning state in turn to form a cleaning tower, an alkali production tower I, an alkali production tower II, and an alkali production tower III, and the cleaning tower, the alkali production tower I, the alkali production tower II, and the alkali production tower III have a gas inlet pipeline and a discharge pipeline;

[0016] The crystallized ammonia liquid pipeline includes an ammonia liquid main pipeline, an ammonia bucket, and a heater, the ammonia bucket is connected to the pipeline of the crystallized ammonia liquid, the ammonia bucket is connected to the cleaning tower, the alkali production tower I, the alkali production tower II, and the alkali production tower III through the ammonia liquid main pipeline, and the ammonia liquid main pipeline has an ammonia pump and a heater;

[0017] The cleaning gas pipeline is a low-pressure nitrogen gas pipeline from the air separation, connected to the cleaning gas source, and connected to the gas inlet pipelines of the cleaning tower, the alkali production tower I, the alkali production tower II, and the alkali production tower III through branch pipelines;

[0018] The lower section gas pipeline is a compressed lower section gas pipeline, connected to the lower section gas source, and connected to the gas inlet pipelines of the cleaning tower, the alkali production tower I, the alkali production tower II, and the alkali production tower III through branch pipelines;

[0019] The alkali outlet pipeline includes an alkali outlet tank, an alkali outlet pipeline of the cleaning tower, an alkali outlet pipeline of the alkali production tower III, an alkali outlet pipeline of the alkali production tower II, and an alkali outlet pipeline of the alkali production tower I, the discharge pipeline of the cleaning tower is connected to the alkali outlet tank through the alkali outlet pipeline of the cleaning tower, the discharge pipeline of the alkali production tower III is connected to the alkali outlet tank through the alkali outlet pipeline of the alkali production tower III, the discharge pipeline of the alkali production tower II is connected to the alkali outlet tank through the alkali outlet pipeline of the alkali production tower II, the discharge pipeline of the alkali production tower I is connected to the alkali outlet tank through the alkali outlet pipeline of the alkali production tower I, and the alkali outlet tank is discharged through the alkali outlet main pipeline;

[0020] The ammonia cleaning solution outlet pipeline includes five sets of ammonia cleaning connection pipes, ammonia cleaning tank, a main pipe for inlet to ammonia cleaning tank, a main pipe for ammonia cleaning pumps, and five sets of ammonia cleaning pumps (P01). One end of the five sets of ammonia cleaning connection pipes is connected to the outlet pipelines of the cleaning tower, alkali production tower I, alkali production tower II, and alkali production tower III respectively through branch pipes. The other end is divided into two paths: one path is connected to the ammonia cleaning tank through the main pipe for inlet to ammonia cleaning tank, and the other path is connected to the five sets of ammonia cleaning pumps (P01). The ammonia cleaning tank is also connected to the five sets of ammonia cleaning pumps (P01) through a branch pipe of the main pipe for ammonia cleaning pumps (P01).

[0021] This group of ammonia 2 cleaning liquid inlet pipelines includes five sets of ammonia 2 cleaning liquid inlet main pipes. One end is connected to the five sets of ammonia 2 cleaning pumps P01, and the other end is connected to the cleaning tower, alkali production tower I, alkali production tower II, and alkali production tower III respectively through branch pipelines.

[0022] As a further preferred option, the ammonia liquid inlet pipeline of this group also includes an alkali outlet backwash main pipe connected to the main inlet pipe of the five groups of ammonia liquid. The alkali outlet backwash main pipe is connected to the alkali outlet pipe of the cleaning tower through the backwash pipe of the cleaning tower and the alkali outlet pipe connecting pipe. It is connected to the alkali outlet pipe of the alkali production tower III through the backwash pipe of the alkali production tower III and the alkali outlet pipe connecting pipe. It is connected to the alkali outlet pipe of the alkali production tower II through the backwash pipe of the alkali production tower II and the alkali outlet pipe connecting pipe. It is connected to the alkali outlet pipe of the alkali production tower I through the backwash pipe of the alkali production tower I and the alkali outlet pipe connecting pipe.

[0023] As a further preferred option, the system includes five relatively independent carbonization tower groups, and the ammonia 2 liquid outlet pipeline also includes four sets of ammonia 2 cleaning pumps (PO2), three sets of ammonia 2 cleaning pumps (PO3), two sets of ammonia 2 cleaning pumps (PO4), one set of ammonia 2 cleaning pumps (PO5), as well as four sets of ammonia 2 connecting pipes, three sets of ammonia 2 connecting pipes, two sets of ammonia 2 connecting pipes, one set of ammonia 2 connecting pipes, and the main outlet pipe of the ammonia 2 pump group.

[0024] One end of the four sets of ammonia cleaning pipes is connected to each carbonization tower in the four systems through branch pipes. The other end is divided into two paths: one path is connected to the ammonia cleaning tank through the main pipe into the ammonia cleaning tank, and the other path is connected to the four sets of ammonia cleaning pumps in P02. The ammonia cleaning tank is also connected to the four sets of ammonia cleaning pumps in P02 through the branch pipes of the main pipe connecting the ammonia cleaning pumps.

[0025] One end of the three sets of ammonia cleaning pipes is connected to each carbonization tower in the three systems through branch pipes. The other end is divided into two paths: one path is connected to the ammonia cleaning tank through the main pipe into the ammonia cleaning tank, and the other path is connected to the three sets of ammonia cleaning pumps in P03. The ammonia cleaning tank is also connected to the three sets of ammonia cleaning pumps in P03 through the branch pipe of the main pipe connecting the ammonia cleaning pumps.

[0026] One end of the two sets of ammonia cleaning pipes is connected to each carbonization tower in the two sets of systems through branch pipes. The other end is divided into two paths: one path is connected to the ammonia cleaning tank through the main pipe into the ammonia cleaning tank, and the other path is connected to the second ammonia cleaning pump of the second set of P04. The ammonia cleaning tank is also connected to the second ammonia cleaning pump of the second set of P04 through the branch pipe of the main pipe connecting the ammonia cleaning pump.

[0027] One end of a set of ammonia cleaning pipes is connected to each carbonization tower in a set of systems via branch pipes. The other end is divided into two paths: one path is connected to the ammonia cleaning tank via the main pipe into the ammonia cleaning tank, and the other path is connected to the P05 set of ammonia cleaning pumps. The ammonia cleaning tank is also connected to the P05 set of ammonia cleaning pumps via a branch pipe of the main pipe connecting to the ammonia cleaning pumps.

[0028] The P01 fifth set of ammonia cleaning pumps is also connected to the outlet main pipe of the ammonia cleaning pump set.

[0029] The P02 fourth set of cleaning ammonia pumps is also connected to the outlet main pipe of the cleaning ammonia pump set, and is connected to each carbonization tower in the four sets through the four sets of cleaning ammonia inlet main pipes.

[0030] The P03 three-group cleaning ammonia pump is also connected to the outlet main pipe of the cleaning ammonia pump group, and is connected to each carbonization tower in the three groups through the three-group cleaning ammonia inlet main pipe.

[0031] The second set of cleaning ammonia pumps P04 is also connected to the outlet main pipe of the second set of cleaning ammonia pumps, and to each carbonization tower in the second set through the inlet main pipe of the second set of cleaning ammonia.

[0032] The P06 set of ammonia cleaning pumps is also connected to the outlet main pipe of the ammonia cleaning pump set, and to each carbonization tower in the set through the ammonia cleaning inlet main pipe.

[0033] As a further preferred option, the outlet pipeline for cleaning ammonia solution 2 also includes a spare cleaning ammonia solution 2 pump (P06) and a de-crystallizing cleaning ammonia solution 2 pipeline. The spare cleaning ammonia solution 2 pump (P06) is connected to the main pipeline connecting the cleaning ammonia solution 2 pump and the main outlet pipeline of the cleaning ammonia solution 2 pump group, respectively. The main outlet pipeline of the cleaning ammonia solution 2 pump group is connected to the ammonia solution 2 tank through the de-crystallizing cleaning ammonia solution 2 pipeline.

[0034] As a further preferred option, the main ammonia liquid pipeline is also equipped with ammonia liquid pipelines to other groups, which connect to multiple carbonization towers in each group of carbonization towers.

[0035] Beneficial effects:

[0036] 1. Improve the automation level of the carbonation tower rotation process in soda ash production to reduce the intensity of manual labor;

[0037] 2. During the carbonation tower rotation process, the fine sodium bicarbonate crystals in the alkaline solution from the new tower decrease, the settling time of the alkaline solution (based on the appearance of obvious stratification and stable solid-liquid ratio) is shortened to less than 60 seconds, and the solid-liquid ratio is increased to 25%-30%.

[0038] 3. During the cleaning process, under the same load, the liquid inlet flow rate of the cleaning tower is increased by 20% to ensure thorough cleaning. Attached Figure Description

[0039] Figure 1 This is a process flow diagram of the carbonization tower of the present invention;

[0040] Figure 2 The present invention provides a process flow for cleaning the ammonia pump unit. Detailed Implementation

[0041] The technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings of the embodiments of the present invention. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments.

[0042] During the carbonization tower rotation process, numerous valves need to be manually opened and closed, resulting in significant labor intensity. This invention employs reliable remote control valves in its process design, enabling remote control via a DCS system. This eliminates the need for on-site personnel, greatly reducing manual labor intensity and providing the hardware foundation for future intelligent control operations. Furthermore, the process flow has been optimized for greater flexibility, allowing for use in alkali production, cleaning, and maintenance phases, thus promoting safer and more stable production.

[0043] The initial stage of alkali production in the new carbonation tower during the carbonation tower rotation process causes fluctuations in subsequent operations, such as increased moisture content in the heavy alkali, increased steam consumption in the calciner, unstable gas pressure in the calciner, and fluctuations in the gas concentration in the calciner. This invention also addresses the adverse effects of carbonation tower rotation on production by refining the process parameters during the carbonation tower rotation process, thereby reducing the amount of fine crystals formed in the initial stage of alkali production in the carbonation tower. This plays a positive role in improving product quality and reducing energy consumption.

[0044] The present invention provides a carbonation tower rotation system for a soda ash production unit, such as... Figure 1 and Figure 2 As shown, it includes:

[0045] The carbonization tower group consists of multiple carbonization towers, which alternate between alkali production and cleaning states.

[0046] Each carbonization tower group includes at least four carbonization towers, which alternately switch between alkali production and cleaning states, forming cleaning tower 5, alkali production tower I10, alkali production tower II11, and alkali production tower III12. Cleaning tower 5, alkali production tower I10, alkali production tower II11, and alkali production tower III12 have air inlet pipes and material outlet pipes.

[0047] The crystallized ammonia liquid pipelines are connected to each carbonization tower for cleaning the carbonization towers;

[0048] The crystallizing ammonia liquid pipeline includes an ammonia liquid main pipe 4, an ammonia liquid tank 2, and a heater. The ammonia liquid tank 2 is connected to a pipe from the crystallizing ammonia liquid 1. The ammonia liquid tank 2 is connected to the cleaning tower 5, the alkali production tower I10, the alkali production tower II11, and the alkali production tower III12 through the ammonia liquid main pipe 4. The ammonia liquid main pipe 4 is equipped with an ammonia pump 3 and a heater.

[0049] Cleaning gas pipelines are connected to each carbonization tower for cleaning the carbonization towers;

[0050] The cleaning gas pipeline is a low-pressure nitrogen 20 pipeline from the air separation unit, connected to an external cleaning gas source, and connected to the inlet pipelines of cleaning tower 5, alkali production tower I10, alkali production tower II11, and alkali production tower III12 respectively through branch pipelines.

[0051] The lower gas pipeline connects to each carbonization tower and is used for alkali production in the carbonization tower;

[0052] The lower section gas pipeline is the lower section gas 19 pipeline from the compressed gas, which is connected to the lower section gas source and is connected to the gas inlet pipelines of cleaning tower 5, alkali tower I10, alkali tower II11, and alkali tower III12 through branch pipelines respectively.

[0053] The alkali outlet pipeline is connected to the alkali outlet tank for alkali outlet from the carbonization tower;

[0054] The alkali discharge pipeline includes an alkali discharge tank 16, an alkali discharge pipe 6 from the washing tower, an alkali discharge pipe 13 from alkali production tower III, an alkali discharge pipe 14 from alkali production tower II, and an alkali discharge pipe 15 from alkali production tower I. The discharge pipeline of the washing tower 5 is connected to the alkali discharge tank 16 through the alkali discharge pipe 6 of the washing tower. The discharge pipeline of the alkali production tower III 12 is connected to the alkali discharge tank 16 through the alkali discharge pipe 13 of the alkali production tower III. The discharge pipeline of the alkali production tower II 11 is connected to the alkali discharge tank 16 through the alkali discharge pipe 14 of the alkali production tower II. The discharge pipeline of the alkali production tower I 10 is connected to the alkali discharge tank 16 through the alkali discharge pipe 15 of the alkali production tower I. The alkali discharge tank 16 discharges through the alkali discharge main pipe 17.

[0055] Clean the ammonia solution outlet pipeline, connect the ammonia solution tank for storing the ammonia solution, and connect the ammonia solution inlet pipeline of this group.

[0056] The ammonia 2 liquid outlet pipeline includes five sets of ammonia 2 connecting pipes 7, ammonia 2 tank 37, a main pipe 36 for inlet to ammonia 2 tank, a main pipe 25 for ammonia 2 pumps, and five sets of ammonia 2 pumps (P01). One end of the five sets of ammonia 2 connecting pipes 7 is connected to the outlet pipelines of cleaning tower 5, alkali tower I10, alkali tower II11, and alkali tower III12 respectively through branch pipes. The other end is divided into two paths: one path is connected to ammonia 2 tank 37 through the main pipe 36 for inlet to ammonia 2 tank, and the other path is connected to the five sets of ammonia 2 pumps (P01). Ammonia 2 tank 37 is also connected to the five sets of ammonia 2 pumps (P01) through a branch pipe of the main pipe 25 for ammonia 2 pumps.

[0057] The ammonia 2 liquid inlet pipeline of this group is used to transport the ammonia 2 liquid to the carbonization tower of this group for alkali production and to clean the alkali outlet pipeline of the cleaning tower.

[0058] This group of ammonia 2 cleaning liquid inlet pipelines includes five sets of ammonia 2 cleaning liquid inlet main pipes 9, one end of which is connected to the five sets of ammonia 2 cleaning pumps P01, and the other end is connected to cleaning tower 5, alkali production tower I10, alkali production tower II11, and alkali production tower III12 respectively through branch pipelines.

[0059] The ammonia 2 liquid inlet pipeline of this group also includes the alkali outlet pipe backwash main pipe 35 connected to the five groups of ammonia 2 liquid inlet main pipes 9. The alkali outlet pipe backwash main pipe 35 is connected to the alkali outlet pipe 6 of the cleaning tower through the backwash pipe of the cleaning tower and the alkali outlet pipe connecting pipe 31, connected to the alkali outlet pipe 13 of the alkali production tower III through the backwash pipe of the alkali production tower III and the alkali outlet pipe connecting pipe 32, connected to the alkali outlet pipe 14 of the alkali production tower II through the backwash pipe of the alkali production tower II and the alkali outlet pipe connecting pipe 33, and connected to the alkali outlet pipe 15 of the alkali production tower I through the backwash pipe of the alkali production tower I and the alkali outlet pipe connecting pipe 34.

[0060] The system includes five relatively independent carbonization tower groups. The ammonia 2 liquid outlet pipeline also includes four sets of ammonia 2 cleaning pumps (P02), three sets of ammonia 2 cleaning pumps (P03), two sets of ammonia 2 cleaning pumps (P04), one set of ammonia 2 cleaning pumps (P05), four sets of ammonia 2 cleaning connecting pipes 21, three sets of ammonia 2 cleaning connecting pipes 22, two sets of ammonia 2 cleaning connecting pipes 23, one set of ammonia 2 cleaning connecting pipes 24, and the main outlet pipe 26 of the ammonia 2 pump group.

[0061] One end of the four sets of ammonia cleaning two connecting pipes 21 is connected to each carbonization tower in the four sets of systems through branch pipes, and the other end is divided into two paths. One path is connected to the ammonia cleaning tank 37 through the main pipe 36 of the ammonia cleaning tank 37, and the other path is connected to the four sets of ammonia cleaning pumps P02. The ammonia cleaning tank 37 is also connected to the four sets of ammonia cleaning pumps P02 through the branch pipe of the main pipe 25 of the ammonia cleaning pump connecting pipe.

[0062] One end of the three sets of ammonia cleaning two connecting pipes 22 is connected to each carbonization tower in the three systems through branch pipes, and the other end is divided into two paths. One path is connected to the ammonia cleaning two tank 37 through the main pipe 36 leading to the ammonia cleaning two tank, and the other path is connected to the three sets of ammonia cleaning two pumps in P03. The ammonia cleaning two tank 37 is also connected to the three sets of ammonia cleaning two pumps in P03 through the branch pipe of the main pipe 25 connecting to the ammonia cleaning two pumps.

[0063] One end of the second set of ammonia cleaning pipe 23 is connected to each carbonization tower in the second set of systems through a branch pipe. The other end is divided into two paths. One path is connected to the second ammonia cleaning tank 37 through the main pipe 36 leading to the second ammonia cleaning tank. The other path is connected to the second ammonia cleaning pump of the second set of P04. The second ammonia cleaning tank 37 is also connected to the second ammonia cleaning pump of the second set of P04 through a branch pipe of the main pipe 25 connecting to the second ammonia cleaning pump.

[0064] One end of a set of ammonia cleaning two connecting pipes 24 is connected to each carbonization tower in a set of systems through a branch pipe, and the other end is divided into two paths. One path is connected to the ammonia cleaning tank 37 through the main pipe 36 leading to the ammonia cleaning tank 37, and the other path is connected to the ammonia cleaning pump of set P05. The ammonia cleaning tank 37 is also connected to the ammonia cleaning pump of set P05 through a branch pipe of the main pipe 25 connecting to the ammonia cleaning pump.

[0065] P01 five-group cleaning ammonia pump 2 is also connected to the outlet main pipe 26 of the cleaning ammonia pump 2 group;

[0066] The four sets of cleaning ammonia pumps are also connected to the outlet main pipe 26 of the cleaning ammonia pump set, and to each carbonization tower in the four sets through the inlet main pipe 27 of the four sets of cleaning ammonia.

[0067] The three sets of cleaning ammonia pumps are also connected to the outlet main pipe 26 of the cleaning ammonia pump set, and to each carbonization tower in the three sets through the inlet main pipe 28 of the three sets of cleaning ammonia.

[0068] The second set of cleaning ammonia pumps P04 is also connected to the outlet main pipe 26 of the second set of cleaning ammonia pumps, and to each carbonization tower in the second set through the inlet main pipe 29 of the second set of cleaning ammonia.

[0069] The P05 set of cleaning ammonia pump 2 is also connected to the outlet manifold 26 of the cleaning ammonia pump 2 set, and to each carbonization tower in the set through the cleaning ammonia pump 2 inlet manifold 30.

[0070] The ammonia 2 liquid outlet pipeline also includes a spare ammonia 2 cleaning pump (P06) and a de-crystallizing ammonia 2 liquid cleaning pipe (8). The spare ammonia 2 cleaning pump (P06) is connected to the main ammonia 2 cleaning pump connection pipe (25) and the main outlet pipe (26) of the ammonia 2 cleaning pump group, respectively. The main outlet pipe (26) of the ammonia 2 cleaning pump group is connected to the ammonia 2 tank (2) through the de-crystallizing ammonia 2 liquid cleaning pipe (8).

[0071] The main ammonia liquid 4 is also equipped with ammonia liquid 18 to other groups, which connects to multiple carbonization towers in each group of carbonization towers.

[0072] The main ammonia liquid pipe 4 is equipped with ammonia liquid inlet control valves on the pipes connecting to the cleaning tower 5, alkali tower I 10, alkali tower II 11, and alkali tower III 12 of the carbonization tower group. Ammonia liquid inlet control valves are also equipped on the pipes connecting to other groups' ammonia liquid pipes 18 and each carbonization tower of each group.

[0073] The five sets of ammonia 2 inlet main pipes 9, 27, 28, 29, and 30 are each equipped with ammonia 2 inlet control valves on the pipelines connected to the respective carbonization towers of their respective groups.

[0074] The lower section gas 19 pipeline from the compressor and the low-pressure nitrogen 20 pipeline from the air separation are also connected to the carbonization towers in each group. The lower section gas 19 pipeline from the compressor is connected to the inlet pipeline of the carbonization tower in each group with a carbonization tower lower section gas switch valve. The low-pressure nitrogen 20 pipeline from the air separation is connected to the inlet pipeline of the carbonization tower in each group with a carbonization tower cleaning gas switch valve. The inlet pipeline of the carbonization tower in each group has a carbonization tower inlet control valve.

[0075] Each carbonization tower is equipped with a carbonization tower connection control valve on its connecting pipeline to the cleaning ammonia connection pipe in the same group (e.g., the fifth cleaning ammonia connection pipe 7 in the fifth group).

[0076] Alkali outlet tank 16 in this group is connected to each carbonization tower in this group by a carbonization tower alkali outlet control valve. For example, carbonization tower alkali outlet control valves are arranged on the alkali outlet pipe 6 of the cleaning tower, the alkali outlet pipe 13 of the alkali production tower III, the alkali outlet pipe 14 of the alkali production tower II, and the alkali outlet pipe 15 of the alkali production tower I in the fifth group.

[0077] The backwash pipe and alkali outlet pipe connecting pipe 31 of the cleaning tower, the backwash pipe and alkali outlet pipe connecting pipe 32 of the alkali production tower III, the backwash pipe and alkali outlet pipe connecting pipe 33 of the alkali production tower II, and the backwash pipe and alkali outlet pipe connecting pipe 34 of the alkali production tower I are respectively equipped with a backwash switch valve for the alkali outlet pipe of the carbonation tower.

[0078] The main pipe 36 for the second ammonia tank is connected to five sets of ammonia tank cleaning connecting pipes 7, 21, 22, 23, and 24, respectively, and each set is equipped with a switching valve connecting to the second ammonia tank. The connecting pipes of the five sets of ammonia tank cleaning connecting pipes 7, 21, 22, 23, and 24 are equipped with switching valves connecting to the inlet of the corresponding P01 fifth-set ammonia tank cleaning pump, P02 fourth-set ammonia tank cleaning pump, P03 third-set ammonia tank cleaning pump, P04 second-set ammonia tank cleaning pump, and P05 first-set ammonia tank cleaning pump are equipped with switching valves connecting to the inlet of the corresponding pump.

[0079] The main pipe 25 connecting to the second ammonia cleaning pump is equipped with a switch valve connecting the second ammonia cleaning tank and the inlet main pipe of the second ammonia cleaning pump. The main pipe 25 connecting to the second ammonia cleaning pump is equipped with a switch valve connecting each second ammonia cleaning pump to the inlet main pipe on the connecting pipes of the second ammonia cleaning pumps P01 (five groups), P02 (four groups), P03 (three groups), P04 (two groups), and P05 (one group). A switch valve is also equipped on the connecting pipe between the main pipe 25 connecting to the second ammonia cleaning pump and the standby second ammonia cleaning pump P06.

[0080] Valves are installed between the five sets of ammonia cleaning pumps (P01, P02, P03, P04, P05) and their corresponding ammonia cleaning pumps (P01, P02, P03, P04, P05) and their respective ammonia cleaning pump inlet manifolds (P01, P02, P03, P04, P05) and (P05, P05, P06, P04, P05, P05) and their respective outlet manifolds (P05, P02, P03, P04, P05, P05).

[0081] Carbonization tower grouping scheme:

[0082] Two grouping modes are adopted: 1+3 and 1+4 ("1" represents one cleaning tower, and "3" and "4" represent the number of alkali production towers in the group of 3 and 4, respectively). In the 1+3 mode, the cleaning tower cleaning time is 24 hours, and the feed rate is 200-240 m³ / h. 3 / h; the alkali production time of the alkali production tower is 72 hours, and the alkali output of the alkali production tower is 75-85m³. 3 / h. For the 1+4 mode tower group, the cleaning tower cleaning time is 18 hours, and the feed rate is 280-300m³. 3 / h; the alkali production time of the alkali production tower is 72 hours, and the alkali output of the alkali production tower is 70-75m³. 3 / h. Each group has a cleaning ammonia second connecting pipe connected to each tower within the group. Each group's cleaning ammonia second connecting pipe is connected to the inlet main pipe of the cleaning ammonia second tank, and also to the inlet of the cleaning ammonia second pump in its group. Each cleaning ammonia second pump inlet is equipped with a cleaning ammonia second pump connecting main pipe, which connects to each cleaning ammonia second pump. A T-junction is provided between the two, and then it connects to the cleaning ammonia second connecting pipe of its group. The cleaning ammonia second pump connecting main pipe is also connected to the outlet of the cleaning ammonia second tank. The above scheme solves the problem of effective grouping of carbonization towers and realizes process optimization of the carbonization tower rotation process.

[0083] Process flow plan for cleaning the outlet of the ammonia pump unit:

[0084] A tee is installed after the manual valve at the pump outlet. The other two ends are connected to the outlet main pipe of the second ammonia cleaning pump group and the inlet main pipe of the same group via remote on / off valves. A branch pipe is led out from the outlet main pipe of the second ammonia cleaning pump group for supplying liquid to the second crystallizing ammonia tank during maintenance and repair, and for warming the carbonization tower during start-up in conjunction with the heater.

[0085] Carbonization tower inlet process flow scheme:

[0086] The lower-stage gas main pipe and the lower-stage gas branch pipe of the single tower are connected via a manual valve and a remote on / off valve; the cleaning gas main pipe and the cleaning gas branch pipe of the single tower are also connected via a manual valve and a remote on / off valve. The cleaning gas branch pipe of the single tower and the lower-stage gas branch pipe are connected to the single tower inlet valve assembly via a tee. This enables remote switching and control of the cleaning gas and the lower-stage gas.

[0087] Carbonization tower alkali discharge and backwashing process flow scheme:

[0088] A tee is installed between the bottom outlet of the carbonization tower and the connecting valve of the main ammonia cleaning pipe of the group. One end of the tee is connected to the alkali outlet pipe of the carbonization tower for alkali discharge during the alkali production process. The alkali outlet pipe has a manual alkali outlet valve, a remote control valve, and a remote on / off valve from bottom to top, used for alkali discharge adjustment, carbonization tower rotation, and alkali outlet pipe backwashing. The remote on / off valve and the remote control valve on the alkali outlet pipe of the carbonization tower are connected to the alkali outlet pipe backwash pipe via a tee and a remote on / off valve is installed therefore for backwashing control.

[0089] The carbonization tower rotation process is as follows:

[0090] 1. Carbonization tower rotation scheme using the tower-holding method

[0091] Before converting the cleaning tower to alkali production, the tower pressure should be adjusted to 240-270 kPa; after changing the inlet gas from cleaning gas to lower stage gas, the initial inlet gas flow rate of the lower stage gas should be 3500-4500 Nm³. 3 / h, maintain 20-30m per hour 3The feed and discharge rates are [ / h]. The discharged liquid enters the second cleaning ammonia tank for temporary storage through the second cleaning ammonia connection pipe of this group (this process keeps the bottom of the carbonization tower flowing to reduce the deposition of fine crystals). When the temperature of the 17th cycle rises to 45-55℃, the alkali discharged from the carbonization tower stops flowing into the second cleaning ammonia tank and is redirected to the alkali outlet tank. The circulating cooling water is then slightly turned on to cool the discharged alkali. After the temperature of the old alkali production tower drops below 50℃ in the 17th cycle, the valve connecting this tower to the second cleaning ammonia connection pipe of this group is opened to enter the cleaning state.

[0092] 2. Carbonization tower rotation scheme using the pressure tower method

[0093] Before pressurizing the tower, open the valve connecting this group to the second ammonia cleaning tank to reduce the pressure in the cleaning tower to no higher than 120 kPa; simultaneously, increase the inlet flow rate to raise the pressure in the old alkali production tower to 280-300 kPa, preparing for subsequent pressurization. Once both towers reach the specified pressure range, close the valve connecting this group to the second ammonia cleaning pump and the second ammonia cleaning tank, and begin the pressurization operation. During pressurization, no liquid is introduced into the original cleaning tower, and the inlet flow rate to the old alkali production tower is controlled at 200-280 m³ / h. 3 The pressure is increased by 100°C / h to accelerate the pressure tower operation. Pressure tower operation is stopped when the pressures of the two towers are close or the original cleaning tower pressure reaches 270-280 kPa. During pressure tower operation, the outlet valve of the second cleaning ammonia tank and the connecting valve of the main pipe between the second cleaning ammonia pump and the second cleaning ammonia pump are opened to evacuate the liquid from the second cleaning ammonia tank. After pressure tower operation, the old alkali production tower enters the cleaning state, and the original cleaning tower is switched to alkali production state. Approximately 10-15 minutes after pressure tower operation, alkali begins to be discharged, with an initial discharge rate of 40-50 m³ / h. 3 The system operates at a rate of / h, and the circulating cooling water is turned on. As the temperature index recovers, the system gradually returns to normal alkali production status.

[0094] 3. Implementation of alternating carbonization towers using the tower-holding method (taking cleaning tower 5 and alkali production tower I as examples)

[0095] The initial status table of remote control valves before carbonization tower rotation is as follows:

[0096]

[0097]

[0098] The carbonization tower transitions from cleaning mode to alkali production mode (5 examples of cleaning towers).

[0099] Step 1: Adjust the opening of the ammonia liquid 1 inlet control valve AC1 of the cleaning tower 5 to reduce the flow rate of ammonia liquid 1 from crystallization entering the cleaning tower 5, and adjust the tower pressure of the cleaning tower 5 to the range of 240-270 kPa.

[0100] Step 2: Open the switch valves GF1 and GF2 that connect the cleaning ammonia pump 2 to the main inlet pipe of the pump to connect the inlet of the cleaning ammonia pump 2, so as to ensure the normal inlet of cleaning ammonia liquid to the alkali production tower.

[0101] Step 3: Close the ammonia liquid inlet control valve AC1 of cleaning tower 5 to stop the liquid inlet of cleaning tower 5.

[0102] Step 4: Close the connection control valve LC1 of the cleaning tower 5, the connection switch valve PF1 between this group and the inlet of the second cleaning ammonia pump, and the backwash switch valve F1 of the alkali outlet pipe of the carbonization tower to cut off the connection between this group and the second cleaning ammonia pump.

[0103] Step 5: Close the cleaning gas switch valve QF1 of cleaning tower 5, and open the lower section gas switch valve XF1 of cleaning tower 5 to change the carbonization tower inlet gas from cleaning gas to lower section gas. Control the opening of the inlet control valve QC1 of cleaning tower 5 to maintain the lower section gas inlet flow rate at 3500-4500 Nm³. 3 / h.

[0104] Step Six: Open the TF5 switch valve connecting this group to the second ammonia cleaning tank, connecting the main ammonia cleaning pipe of this group to the second ammonia cleaning tank 37. Open the LC1 connection control valve of cleaning tower 5. Open the ZC1 control valve for the second ammonia cleaning liquid inlet of cleaning tower 5, controlling the flow rate to 20-30m. 3 The feed rate is maintained at 260-275 kPa, with a feed rate of / h. (If on-site cleaning or maintenance of the ammonia pipeline is required, control the flow rate by 20-30m.) 3 The feed rate can also be controlled by opening the ammonia liquid inlet control valve AC1 of the cleaning tower 5.

[0105] Step 7: After the lower section gas has been introduced for 20-30 minutes, open the alkali outlet valve JF1 of the cleaning tower 5, and control the alkali outlet flow rate to 30-50 m³ / h by adjusting the opening of the alkali outlet control valve JC1 of the cleaning tower 5. 3 / h, synchronously adjust the ammonia inlet control valve ZC1 or AC1 of the cleaning tower 5 to control the inlet flow rate and maintain the tower pressure at 270-280 kPa. Close the carbonization tower connection control valve LC1 to achieve normal alkali discharge process. Slightly open the circulating cooling water to cool the alkali discharge solution and control the alkali discharge temperature to 45-50℃.

[0106] Step 8: When the temperature in the middle of the new alkali production tower reaches 55-65℃, appropriately increase the alkali output to produce 60-70m³. 3 The influent flow rate is controlled at 42-45℃; subsequently, as the temperature of the carbonization tower increases, when the temperature at the top of the carbonization tower rises to 45-55℃, the alkali outlet temperature of the new alkali production tower is controlled at 36-40℃; the influent flow rate and alkali outlet flow rate are adjusted according to the actual production load requirements.

[0107] The carbonization tower switches from alkali production to cleaning mode (taking alkali production tower I10 as an example).

[0108] Step 1: Operate synchronously with the alkali production tower (modified from cleaning tower 5). Adjust the opening of the air inlet control valve QC4 of alkali production tower I10 to control the air inlet flow rate to 1000-1500 Nm³. 3 / h, close the lower gas switch valve XF4 of the alkali production tower I10, and open the cleaning gas switch valve QF4 of the alkali production tower I10 to change the lower gas to cleaning gas.

[0109] Step 2: Maintain the inlet and outlet alkali flow rates at 40-60 m³ / h. 3 The alkali outlet temperature is set at 42-45℃ per hour. When the temperature in the middle of the alkali production tower I10 drops below 50℃, the circulating water is shut off to stop cooling. The main purpose of this process is to remove all crystals from the alkali production tower.

[0110] Step 3: Close the ammonia inlet control valve ZC4 of the alkali production tower I10 and open the ammonia inlet control valve AC4 of the alkali production tower I10. When step 7 in 1.1 and step 2 in 1.2 are completed, open the alkali production tower I10 connection control valve LC4 to connect the alkali outlet main pipe of the alkali production tower I10 with the ammonia inlet main pipe of this group (7). Simultaneously close the alkali outlet switch valve JF4 of the carbonization tower and open the backwash switch valve F4 of the alkali outlet pipe of the carbonization tower.

[0111] Step 4: Open valve TF6, which connects the cleaning ammonia tank 2 to the inlet main of the cleaning ammonia pump 2, to connect the cleaning ammonia tank 2 to the pump. Then close valve GF2, which connects the cleaning ammonia pump 2 to the pump inlet main, to stop borrowing cleaning ammonia solution from other groups.

[0112] Step 5: Open the switch valve PF1 connecting this group to the inlet of the second ammonia cleaning pump, and close the switch valve TF5 connecting this group to the second ammonia cleaning tank and the switch valve GF1 connecting the second ammonia cleaning pump to the main pump inlet pipe, so as to normalize the cleaning of the alkali tower I10.

[0113] Step Six: Open the switch valve GF6 connecting the second ammonia cleaning pump to the pump inlet main pipe, then turn on the standby second ammonia cleaning pump P06, and open the switch valves ZF1-ZF6 connecting the second ammonia cleaning pump to the pump outlet main pipe one by one to achieve the purpose of sending away the liquid stored in the second ammonia cleaning tank.

[0114] Step 7: When the current or outlet pressure of the standby ammonia cleaning pump P06 fluctuates significantly, stop the standby ammonia cleaning pump P06. Then, close the connecting valves ZF1-ZF6 between the ammonia cleaning pump and the pump outlet main pipe, close the connecting valve TF6 between the ammonia cleaning tank and the ammonia cleaning pump inlet main pipe, and close the connecting valve GF6 between the ammonia cleaning pump and the pump inlet main pipe.

[0115] The remote control valve on / off status table after the carbonization tower rotation is completed is as follows:

[0116]

[0117]

[0118] The carbonization tower rotation method is implemented using the pressure tower method (taking cleaning tower 5 and alkali production tower I10 as examples).

[0119] The initial status table of remote control valves before carbonization tower rotation is as follows:

[0120]

[0121] Step 1: Contact the crystallizer to reduce the amount of ammonia solution 1 from the crystallizer by 200-300 ml. 3 / h. Then close the ammonia liquid inlet control valve AC1 of the cleaning tower 5 to stop the liquid inlet.

[0122] Step 2: Open valve TF6 connecting the inlet main of the second ammonia cleaning tank and the second ammonia cleaning pump, open valve TF5 connecting this group to the second ammonia cleaning tank, and open valve GF1 connecting the second ammonia cleaning pump to the pump inlet main. This connects the pump inlet to the second ammonia cleaning tank and the cleaning tower 5 to the second ammonia cleaning tank.

[0123] Step 3: When the pressure in cleaning tower 5 drops below 120 kPa, close the backwash valve F1 on the alkali outlet pipe of cleaning tower 5, and close the valve TF5 connecting this group to the second cleaning ammonia tank and the valve PF1 connecting this group to the inlet of the second cleaning ammonia pump. Then open the valve GF2 connecting the second cleaning ammonia pump to the main pump inlet pipe, and close the valve TF6 connecting the second cleaning ammonia tank to the main inlet pipe of the second cleaning ammonia pump. This isolates the second cleaning ammonia tank connection pipe from the system and ensures normal liquid intake to the alkali tower.

[0124] Step 4: Open the connection control valve LC4 of the alkali production tower I10 to connect the two towers and start the pressure tower operation.

[0125] Step 5: Close the ammonia 2 liquid inlet control valve ZC4 of the alkali production tower I10, open the ammonia 2 liquid inlet control valve AC4 of the alkali production tower I10, and contact the crystallizer to increase the ammonia 2 liquid flow rate by 200-300 mg / L. 3 / h, control the flow rate of ammonia solution I10 in the alkali preparation tower to be no less than 300m³ / h. 3 / h, to ensure smooth operation of the pressure tower.

[0126] Step Six: Close the lower gas switch valve XF4 of the alkali production tower I10, open the cleaning gas switch valve QF4 of the alkali production tower I10, and adjust the carbonization tower inlet control valve QC4 to control the cleaning flow rate at 1000-1200 Nm. 3 / h; Simultaneously, reverse the operation of cleaning tower 5, i.e., close the cleaning gas switch valve QF1 of cleaning tower 5, open the lower section gas switch valve XF1 of cleaning tower 5, and adjust the carbonization tower inlet control valve QC1 to control the lower section gas flow rate at 3500-4000 Nm. 3 / h; After the gas conversion is completed, turn off the cooling water of the alkali production tower I10 to stop cooling and temperature reduction.

[0127] Step 7: When the pressure of the cleaning tower 5 and the alkali production tower I10 is close to equilibrium and the pressure is 270-280 kPa, close the connection control valve LC1 of the cleaning tower 5 to disconnect the connection with the cleaning ammonia connection pipe. Also, close the alkali outlet valve JF4 of the alkali production tower I10 and open the backwash valve F4 of the alkali outlet pipe of the alkali production tower I10.

[0128] Step 8: Open valve PF1, which connects to the inlet of the second ammonia cleaning pump, and close valves GF1 and GF2, which connect the second ammonia cleaning pump to the main pump inlet pipe. This completes the normal cleaning process for alkali production tower I10.

[0129] Step Nine: 10-15 minutes after the pressure tower is pressed, open the alkali outlet switch valve JF1 of the carbonization tower of cleaning tower 5 and the cleaning ammonia liquid inlet control valve ZC1 of cleaning tower 5, and start with a flow rate of 30-50m. 3 The alkali output flow rate is set at / h, maintaining the tower pressure within the range of 265-285 kPa. The influent flow rate is adjusted, and cooling water is turned on appropriately after alkali output to lower the temperature, controlling the output temperature to 42-45℃. When the carbonization tower parameters approach normal levels, the output temperature is normally controlled at 36-40℃, and the output flow rate is controlled at 75-85 m³ / h. 3 / h.

[0130] Step 10: Open the switch valve GF6 connecting the second ammonia cleaning pump to the pump inlet main pipe and the switch valve TF6 connecting the second ammonia cleaning tank to the inlet main pipe of the second ammonia cleaning pump. Then turn on the standby second ammonia cleaning pump P06. Open the switch valves ZF1-ZF6 connecting the second ammonia cleaning pump to the pump outlet main pipe one by one to achieve the purpose of sending away the liquid stored in the second ammonia cleaning tank.

[0131] Step 11: When the current or outlet pressure of the standby ammonia cleaning pump P06 fluctuates significantly, stop the standby ammonia cleaning pump P06, and close the connecting valves ZF1-ZF6 between the ammonia cleaning pump and the pump outlet main pipe one by one, close the connecting valve TF6 between the ammonia cleaning tank and the ammonia cleaning pump inlet main pipe, and close the connecting valve GF6 between the ammonia cleaning pump and the pump inlet main pipe.

[0132] The remote control valve on / off status table after the carbonization tower rotation is completed is as follows:

[0133]

[0134]

[0135] Carbonization tower shutdown and maintenance implementation:

[0136] During the production process, the carbonization tower may experience equipment malfunctions that require shutdown and maintenance. This mainly involves cleaning.

[0137] There are three scenarios: shutdown during operation, shutdown during alkali production, and shutdown of the carbonization tower system.

[0138] 1. Shutdown during cleaning (taking cleaning tower 5 as an example)

[0139] Step 1: Reduce the amount of ammonia by 200-300 mg / L through crystallization. 3 / h.

[0140] Step 2: Stop the liquid and gas inlet of the tower, that is, close the carbonization tower gas inlet control valve QC1 and manual valve of the cleaning tower 5 in the attached diagram, the carbonization tower cleaning gas switch valve QF1 and manual valve, close the carbonization tower ammonia liquid inlet control valve AC1 and manual valve, and the cleaning ammonia liquid inlet control valve ZC1 and related manual valves.

[0141] Step 3: Use five sets of ammonia cleaning pumps P01 to collect the liquid in cleaning tower 5 into the system.

[0142] Step 4: When the pressure of cleaning tower 5 is below 20 kPa, open the switch valves ZF1-ZF6 connecting the cleaning ammonia pump 2 to the pump outlet main pipe, and stop the five sets of cleaning ammonia pump 2 P01.

[0143] Step 5: Close the control valve LC1 and manual valve connecting the cleaning tower 5 and the carbonization tower, close the control valve JC1 and manual valve for the alkali solution outlet of the carbonization tower, and close the backwash switch valve F1 for the alkali outlet pipe of the carbonization tower. Finally, close the tail gas valve of the cleaning tower 5, completely cutting off the process of this tower from the system.

[0144] 2. Shutdown of the carbonation tower during alkali production (taking alkali production tower I10 as an example):

[0145] Step 1: Set the carbonization tower inlet control valve QC4 to control the inlet air volume to 1000-1500 Nm. 3 / h, close the lower section gas switch valve XF4 of the carbonization tower and open the cleaning gas switch valve QF4 of the carbonization tower to change the lower section gas to cleaning gas.

[0146] Step 2: Maintain the inlet and outlet alkali flow rates at 60-80 m³ / h 3 The alkali outlet temperature is set at 42-45℃ per hour. When the temperature of the 17th cycle of the alkali production tower I10 drops below 50℃, the circulating water is shut off to stop cooling. The main purpose of this process is to remove all crystals from the alkali production tower.

[0147] Step 3: Open the carbonization tower connection control valve LC4 to connect the alkali outlet main pipe of alkali tower I10 with the ammonia cleaning main pipe of this group. Simultaneously close the carbonization tower alkali outlet switch valve JF4 and open the carbonization tower alkali outlet pipe backwash switch valve F4.

[0148] Step 4: Open valve TF5, which connects the ammonia cleaning tank 2 to the main inlet pipe of the ammonia cleaning tank 2, and valve TF6, which connects the ammonia cleaning tank 2 to the main inlet pipe of the ammonia cleaning pump, to connect the ammonia cleaning tank 2 to the pump. Open valve GF1, which connects the ammonia cleaning pump 2 to the main inlet pipe of the pump, to connect the carbonization tower, the ammonia cleaning tank 2, and the pump group.

[0149] Step 5: Close the control valve LC1 connecting the carbonization tower of cleaning tower 5 and the ammonia liquid inlet control valve AC1 of cleaning tower 5, cutting off the connection with the cleaning ammonia tank and the cleaning ammonia pump. Close the gas inlet control valve QC4 of alkali production tower I10, the cleaning gas switch valve QF4 and the manual valve of alkali production tower I10, close the manual valve corresponding to the ammonia liquid inlet control valve AC4 of alkali production tower I10, and the cleaning ammonia liquid inlet control valve ZC4 and the manual valve of alkali production tower I10.

[0150] Step 6: When the pressure of the alkali production tower I10 drops to 20 kPa, close the carbonization tower connection control valve LC4 and the manual valve, and then open the carbonization tower connection control valve LC1 of the cleaning tower 5 and the ammonia liquid inlet control valve AC1 of the cleaning tower 5.

[0151] Step 7: Close the switch valve TF5 connecting this group to the second ammonia cleaning tank and the switch valve GF1 connecting the second ammonia cleaning pump to the pump inlet main pipe, and open the switch valve GF6 connecting the second ammonia cleaning pump to the pump inlet main pipe. Then start the standby second ammonia cleaning pump P06, and open the switch valves ZF1-ZF6 connecting the second ammonia cleaning pump to the pump outlet main pipe one by one to achieve the purpose of sending away the liquid stored in the second ammonia cleaning tank.

[0152] Step 8: When the current or outlet pressure of the standby ammonia cleaning pump P06 fluctuates significantly, stop the standby ammonia cleaning pump P06, and close the connecting valves ZF1-ZF6 between the ammonia cleaning pump and the pump outlet main pipe one by one, close the connecting valve TF6 between the ammonia cleaning tank and the ammonia cleaning pump inlet main pipe, and close the connecting valve GF6 between the ammonia cleaning pump and the pump inlet main pipe.

[0153] Step 9: Confirm that the manual valve of the alkali solution control valve JC4 of the carbonization tower is closed, and close the tail gas valve. The shutdown of the alkali tower I10 is now complete.

[0154] 3. For the shutdown of the carbonization tower system

[0155] Step 1: Convert all alkali production towers into cleaning towers according to the steps in 1.2 for converting alkali production towers into cleaning towers;

[0156] Step 2: Contact the crystallizer to stop the second ammonia pump 3.

[0157] Step 3: Open the valve of the de-crystallization cleaning ammonia liquid pipe (8), and use the cleaning ammonia liquid pump set to send the excess cleaning ammonia liquid from the carbonization tower system to ammonia tank 2.

[0158] Step 4: When the liquid level in each carbonization tower drops to the level required for shutdown and maintenance (below 100 kPa), stop the second ammonia cleaning pump.

[0159] Step 5: Close all carbonization inlet, inlet, outlet, and outlet control valves, as well as the manual valves.

[0160] The above description is only a preferred embodiment of the present invention, but the scope of protection of the present invention is not limited thereto. Any equivalent substitutions or modifications made by those skilled in the art within the scope of the technology disclosed in the present invention, based on the technical solution and inventive concept of the present invention, should be covered within the scope of protection of the present invention.

Claims

1. A carbonation tower rotation system for a soda ash production unit, characterized in that, include: The carbonization tower group consists of multiple carbonization towers, which alternate between alkali production and cleaning states. The crystallized ammonia solution pipelines are connected to each carbonization tower to provide crystallized ammonia solution for cleaning the carbonization towers; Cleaning gas pipelines are connected to each carbonization tower for cleaning the carbonization towers; The lower gas pipeline connects to each carbonization tower and is used for alkali production in the carbonization tower; The alkali outlet pipeline is connected to the alkali outlet tank for alkali outlet from the carbonization tower; Clean the ammonia solution outlet pipeline, connect the ammonia solution tank for storing the ammonia solution, and connect the ammonia solution inlet pipeline of this group. This group's ammonia inlet pipeline is used to transport the ammonia solution to the carbonization tower for alkali production and to clean the alkali outlet pipeline of the cleaning tower.

2. The carbonation tower rotation system for a soda ash production unit according to claim 1, characterized in that: Each carbonization tower group includes at least four carbonization towers, which take turns switching to the cleaning state to form a cleaning tower (5), an alkali production tower I (10), an alkali production tower II (11), and an alkali production tower III (12). The cleaning tower (5), the alkali production tower I (10), the alkali production tower II (11), and the alkali production tower III (12) have an air inlet pipe and a material outlet pipe. The crystallized ammonia liquid pipeline includes an ammonia liquid main pipe (4), an ammonia tank (2), and a heater. The ammonia tank (2) is connected to a pipe from the crystallized ammonia liquid (1). The ammonia tank (2) is connected to a cleaning tower (5), an alkali production tower I (10), an alkali production tower II (11), and an alkali production tower III (12) through the ammonia liquid main pipe (4). The ammonia liquid main pipe (4) is equipped with an ammonia pump (3) and a heater. The cleaning gas pipeline is a low-pressure nitrogen (20) pipeline from the air separation unit, connected to an external cleaning gas source, and connected to the inlet pipelines of the cleaning tower (5), alkali tower I (10), alkali tower II (11), and alkali tower III (12) respectively through branch pipelines. The lower section gas pipeline is a lower section gas (19) pipeline from the compressed lower section gas, which is connected to the lower section gas source and is connected to the inlet pipelines of the cleaning tower (5), alkali tower I (10), alkali tower II (11) and alkali tower III (12) respectively through branch pipelines. The alkali outlet pipeline includes an alkali outlet tank (16), an alkali outlet pipe (6) of the washing tower, an alkali outlet pipe (13) of the alkali production tower III, an alkali outlet pipe (14) of the alkali production tower II, and an alkali outlet pipe (15) of the alkali production tower I. The discharge pipeline of the washing tower (5) is connected to the alkali outlet tank (16) through the alkali outlet pipe (6) of the washing tower. The discharge pipeline of the alkali production tower III (12) is connected to the alkali outlet tank (16) through the alkali outlet pipe (13) of the alkali production tower III. The discharge pipeline of the alkali production tower II (11) is connected to the alkali outlet tank (16) through the alkali outlet pipe (14) of the alkali production tower II. The discharge pipeline of the alkali production tower I (10) is connected to the alkali outlet tank (16) through the alkali outlet pipe (15) of the alkali production tower I. The alkali outlet tank (16) is discharged through the alkali outlet main pipe (17). The ammonia 2 liquid outlet pipeline includes five sets of ammonia 2 connecting pipes (7), ammonia 2 tank (37), a main pipe for inlet to ammonia 2 tank (36), a main pipe for ammonia 2 pump (25), and five sets of ammonia 2 pumps in P01; one end of the five sets of ammonia 2 connecting pipes (7) is connected to the outlet pipelines of the cleaning tower (5), alkali tower I (10), alkali tower II (11), and alkali tower III (12) respectively through branch pipes, and the other end is divided into two paths, one path is connected to ammonia 2 tank (37) through the main pipe for inlet to ammonia 2 tank (36), and the other path is connected to five sets of ammonia 2 pumps in P01. Ammonia 2 tank (37) is also connected to five sets of ammonia 2 pumps in P01 through the branch pipe of the main pipe for ammonia 2 pump (25); The ammonia 2 cleaning liquid inlet pipeline of this group includes five sets of ammonia 2 cleaning liquid inlet main pipes (9), one end of which is connected to the five sets of ammonia 2 cleaning pumps P01, and the other end is connected to the cleaning tower (5), alkali tower I (10), alkali tower II (11), and alkali tower III (12) respectively through branch pipelines.

3. The carbonation tower rotation system for a soda ash production unit according to claim 2, characterized in that: The ammonia liquid inlet pipeline of this group also includes the alkali outlet backwash main pipe (35) connected to the five groups of ammonia liquid inlet main pipes (9). The alkali outlet backwash main pipe (35) is connected to the alkali outlet pipe (6) of the cleaning tower through the backwash pipe and the alkali outlet pipe connecting pipe (31), connected to the alkali outlet pipe (13) of the alkali production tower III through the backwash pipe and the alkali outlet pipe connecting pipe (32), connected to the alkali outlet pipe (14) of the alkali production tower II through the backwash pipe and the alkali outlet pipe connecting pipe (33), and connected to the alkali outlet pipe (15) of the alkali production tower I through the backwash pipe and the alkali outlet pipe connecting pipe (34).

4. The carbonation tower rotation system for a soda ash production unit according to claim 3, characterized in that: The system includes five carbonization tower groups, and the ammonia liquid outlet pipeline also includes four ammonia cleaning pumps (P02), three ammonia cleaning pumps (P03), two ammonia cleaning pumps (P04), one ammonia cleaning pump (P05), four ammonia cleaning connecting pipes (21), three ammonia cleaning connecting pipes (22), two ammonia cleaning connecting pipes (23), one ammonia cleaning connecting pipe (24), and the main outlet pipe of the ammonia cleaning pump group (26). One end of the four sets of ammonia cleaning two connecting pipes (21) is connected to each carbonization tower in the four sets of systems through branch pipes, and the other end is divided into two paths. One path is connected to the ammonia cleaning tank (37) through the main pipe (36) of the ammonia cleaning tank, and the other path is connected to the four sets of ammonia cleaning pumps of P02. The ammonia cleaning tank (37) is also connected to the four sets of ammonia cleaning pumps of P02 through the branch pipe of the main pipe (25) of the ammonia cleaning pump. One end of the three sets of ammonia cleaning two connecting pipes (22) is connected to each carbonization tower in the three sets of systems through branch pipes, and the other end is divided into two paths. One path is connected to the ammonia cleaning tank (37) through the main pipe (36) of the ammonia cleaning tank, and the other path is connected to the three sets of ammonia cleaning pumps in P03. The ammonia cleaning tank (37) is also connected to the three sets of ammonia cleaning pumps in P03 through the branch pipe of the main pipe (25) of the ammonia cleaning pump connecting pipe. One end of the two sets of ammonia cleaning pipes (23) is connected to each carbonization tower in the two sets of systems through branch pipes. The other end is divided into two paths. One path is connected to the ammonia cleaning tank (37) through the main pipe (36) leading to the ammonia cleaning tank, and the other path is connected to the second pump of the second set of P04 ammonia cleaning system. The ammonia cleaning tank (37) is also connected to the second pump of the second set of P04 ammonia cleaning system through the branch pipe of the main pipe (25) connecting to the second pump of the second set of P04 ammonia cleaning system. One end of a set of ammonia cleaning two connecting pipes (24) is connected to each carbonization tower in a set of systems through a branch pipe, and the other end is divided into two paths. One path is connected to the ammonia cleaning tank (37) through the main pipe (36) of the ammonia cleaning tank, and the other path is connected to the P05 set of ammonia cleaning pump. The ammonia cleaning tank (37) is also connected to the P05 set of ammonia cleaning pump through a branch pipe of the main pipe (25) of the ammonia cleaning pump. The P01 fifth set of ammonia cleaning pumps is also connected to the outlet main pipe (26) of the ammonia cleaning pump set; The P02 four-group cleaning ammonia pump is also connected to the outlet main pipe (26) of the cleaning ammonia pump group, and is connected to each carbonization tower in the four groups through the four-group cleaning ammonia inlet main pipe (27). The three sets of cleaning ammonia pumps are also connected to the outlet main pipe (26) of the cleaning ammonia pump set, and to each carbonization tower in the three sets through the three sets of cleaning ammonia inlet main pipe (28). The second set of cleaning ammonia pumps is also connected to the outlet main pipe (26) of the second set of cleaning ammonia pumps, and to each carbonization tower in the second set through the inlet main pipe (29) of the second set of cleaning ammonia. The P05 set of cleaning ammonia pumps is also connected to the outlet manifold (26) of the cleaning ammonia pump set, and to each carbonization tower in the set via the cleaning ammonia inlet manifold (30).

5. A carbonation tower rotation system for a soda ash production unit according to claim 4, characterized in that: The outlet pipeline for cleaning ammonia solution 2 also includes a spare cleaning ammonia solution 2 pump (P06) and a de-crystallizing cleaning ammonia solution 2 pipe (8). The spare cleaning ammonia solution 2 pump (P06) is connected to the main pipe (25) connecting the cleaning ammonia solution 2 pump and the main outlet pipe (26) of the cleaning ammonia solution 2 pump group, respectively. The main outlet pipe (26) of the cleaning ammonia solution 2 pump group is connected to the ammonia solution 2 tank (2) through the de-crystallizing cleaning ammonia solution 2 pipe (8).

6. A carbonation tower rotation system for a soda ash production unit according to claim 2 or 5, characterized in that: The main ammonia liquid pipe (4) is also equipped with ammonia liquid pipe (18) to other groups, which connects to multiple carbonization towers in each group of carbonization towers.

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