JP6547786B2 - Operating method of depressurization type surplus excess water distillation facility and sealing liquid temperature control device - Google Patents

Description

  The present invention relates to a method of operating a pressure reducing type surplus excess water distillation facility and a liquid sealing temperature control device.

Conventionally, as an operation method of a decompression type surplus excess water distillation facility, there are technologies described in Patent Documents 1 and 2, for example. According to the techniques described in Patent Documents 1 and 2, the inside of the reduced-pressure water-separating equipment is removed by removing the naphthalene contained in the excess water by a filter before the excess water is introduced into the reduced-pressure water-soiling equipment. It is disclosed to prevent suction failure due to naphthalene in the following.
However, the techniques described in Patent Documents 1 and 2 require a filter, which may make the equipment expensive, and it is uncertain whether an appropriate effect will actually be obtained.

Japanese Patent Application Laid-Open No. 61-83290 Japanese Patent Application Laid-Open No. 61-83291

  An object of the present invention is to provide a method for operating a pressure reduction type surplus excess water distillation facility and a sealing liquid temperature control device which can prevent the suction failure due to naphthalene more reliably, focusing on the above points.

  In order to solve the above-mentioned subject, one mode of the present invention introduces the ammonia water which is generated at the time of refining of (a) coke oven gas into a vacuum distillation column and carries out vacuum distillation, Ammonia containing distilled from vacuum distillation tower The vapor is introduced into a condenser, cooled and condensed, and the ammonia containing vapor is sucked from the condenser with a liquid ring vacuum pump, and (b) ammonia sucked with a predetermined liquid ring vacuum pump Referring to the correspondence between the concentration of naphthalene contained in the contained vapor and the temperature of the sealing liquid of the liquid-sealed vacuum pump in which naphthalene is deposited in the liquid-sealed vacuum pump, the sealing liquid corresponding to the current concentration of naphthalene It is an operation method of a decompression type surplus excess water distillation facility which sets a temperature higher than the temperature as the target temperature and controls the temperature of the sealing liquid in the liquid ring vacuum pump so as to achieve the target temperature set as (c). Abstract .

  According to another aspect of the present invention, (a) excess ammonia water generated at the time of refining coke oven gas is introduced into a vacuum distillation tower and vacuum distilled, and ammonia-containing vapor distilled from the vacuum distillation tower is introduced into a condenser Sealing temperature control device for controlling the temperature of the sealing liquid in the liquid-sealed vacuum pump of the reduced pressure surplus surplus water distillation equipment that sucks ammonia-containing vapor from the condenser with the liquid-sealed vacuum pump while cooling and condensing (B) Correspondence between the concentration of naphthalene contained in the ammonia-containing vapor sucked by the liquid ring vacuum pump and the temperature of the sealing liquid of the liquid ring vacuum pump in which naphthalene is deposited in the liquid ring vacuum pump Referring to the correspondence relationship between the storage unit storing the relationship, and (c) the concentration of naphthalene stored in the storage unit and the temperature of the sealing solution, from the temperature of the sealing solution corresponding to the current concentration of naphthalene High temperature as the target temperature And, and summarized in that a sealing liquid temperature controller and a sealing liquid temperature controller for controlling the temperature of the sealing liquid in the liquid seal vacuum pump so that the target temperature set.

  According to the present invention, since the deposition of naphthalene in the liquid ring vacuum pump is suppressed, an operation method and sealing liquid temperature control device of the reduced pressure surplus surplus water system capable of more reliably preventing suction failure due to the naphthalene are disclosed. Can be provided.

It is a block diagram showing the structure of the decompression type surplus excess water distillation installation which concerns on embodiment. BRIEF DESCRIPTION OF THE DRAWINGS It is a figure showing the structure of a liquid ring type vacuum pump, (a) is a side view, (b) is sectional drawing which shows the cross section fractured | ruptured by the AA line cross section of (a). It is a graph showing the correspondence between the concentration of naphthalene contained in the ammonia-containing vapor drawn by the liquid ring vacuum pump and the temperature of the sealing liquid of the liquid ring vacuum pump in which the naphthalene is deposited in the liquid ring vacuum pump. . It is a flowchart showing the sealing liquid temperature control processing which CPU performs.

Hereinafter, embodiments of the present invention will be described based on the drawings.
The embodiments described below illustrate apparatuses and methods for embodying the technical idea of the present invention, and the technical idea of the present invention includes the shape, structure, arrangement, and the like of components. Does not specify the following. The technical idea of the present invention can be variously modified within the technical scope defined by the claims described in the claims.

  In the coke plant, the coke oven gas is purified with ammonia water circulating between the coke oven dram main and the tar decanter, so 70 ° C. to 80 ° C. ammonia water containing harmful substances such as ammonia (hereinafter referred to as (Also called "thermal water") occurs. And among the generated heat and water, surplus water is treated by the vacuum distillation equipment to remove ammonia.

  In the operation method of the depressurization type surplus annast water distillation facility of the present embodiment, the surplus ansane water generated at the time of refining the coke oven gas is introduced into the depressurization distillation tower of the depressurization type surplus ansins water distillation facility, and the surplus introduced Remove ammonia from cheap water. Then, the ammonia-containing vapor distilled from the vacuum distillation column is condensed by being introduced into the condenser of the vacuum type surplus excess water distillation facility and cooled. At this time, the condensed ammonia-containing vapor is sucked from the condenser with a liquid ring vacuum pump. At this time, since the sealing solution of the liquid ring vacuum pump and the ammonia-containing vapor are in contact with each other, naphthalene contained in the ammonia-containing vapor is deposited in the liquid ring vacuum pump and the impeller of the liquid ring vacuum pump is fixed And suction failure, that is, vacuum abnormality in the vacuum distillation column may occur.

  However, in the operation method of the reduced pressure type surplus excess water distillation equipment according to the present embodiment, the concentration of naphthalene contained in the ammonia-containing vapor drawn by the sealed liquid vacuum pump and the liquid seal in which the naphthalene is deposited in the liquid ring vacuum pump The correspondence with the temperature of the sealing liquid of the vacuum pump was determined, and the temperature was set as the target temperature higher than the temperature of the sealing corresponding to the current concentration of naphthalene with reference to the correspondence. The temperature of the sealing liquid in the sealing vacuum pump is controlled so as to reach the target temperature. Here, as the target temperature, for example, in consideration of the possibility that the temperature of the sealing liquid fluctuates, it is preferable to set a temperature higher by 2 to 3 ° C. than the temperature of the sealing liquid corresponding to the current concentration of naphthalene. preferable. Therefore, the deposition of naphthalene contained in the ammonia-containing vapor due to the contact between the sealing liquid of the liquid-ring vacuum pump and the ammonia-containing vapor is suppressed in the liquid-ring vacuum pump. Therefore, since the sticking of the impeller of the liquid ring vacuum pump due to the precipitated naphthalene is suppressed and the vacuum abnormality in the vacuum distillation column is suppressed, the suction failure due to the naphthalene is more reliably prevented.

In such an operation method of the depressurization type surplus annast water distillation facility of the present embodiment, for example, naphthalene contained in the surplus ansane water is removed by a filter before the surplus annexed water is introduced into the depressurization type ansus water distillation facility. Equipment is cheaper than the method. Furthermore, since the excess ammonia water is treated by vacuum distillation, it is not necessary to set the excess ammonia water in the vacuum distillation column to a high temperature, and energy costs can be reduced.
Next, the operation method of the decompression type surplus excess water distillation equipment of the present embodiment will be described with reference to a more specific example (see FIGS. 1 to 3).

As shown in FIG. 1, the excess ammonia water generated at the time of refining coke oven gas is reduced pressure distillation tower 1 (hereinafter, “energy saving type (pressure reduction type) surplus moisture treatment distillation tower 1 of vacuum distillation equipment via route 2). (Also referred to as The inside of the depressurization type surplus anhydrate processing distillation column 1 is depressurized by suction of ammonia-containing vapor from a condenser 11 described later by a liquid-sealed vacuum pump 16 described later.
The excess ammonium water introduced into the pressure reduction type excess water treatment distillation column 1 is sent from the bottom to the reboiler 3 via the circulation pump 5 and the path 6 and heated by heat exchange, and then the pressure reduction type excess water treatment distillation It is returned to the bottom of tower 1. As a result, the heated excess ammonia becomes steam under reduced pressure, and the ammonia-containing steam containing ammonia and acid gas at high concentration reaches the top of the decompression excess excess water treatment distillation column 1. As a result, excess waste water is stripped to remove ammonia and acid gas. The excess ammonia water from which the ammonia and the acid gas have been removed is extracted from the bottom of the depressurization type excess anhydrate processing distillation column 1 by a relief water pump 8 and is sent via a path 9.

The heat source of the reboiler 3 is not particularly limited, but may be a hot waste water circulating between the coke oven dram main and the tar decanter. That is, by introducing the circulating heat annex water into the reboiler 3 via the path 4, it may be used as a heat source.
The ammonia-containing vapor removed from the excess ammonia water is drawn from the top of the pressure reduction excess excess water treatment distillation column 1 by the liquid ring vacuum pump 16, and the passage 10 is used to It is introduced into the condenser 11. In the condenser 11, a large number of pipes (not shown) are arranged in the vertical direction, and the ammonia-containing vapor is introduced into the inside of these pipes. Then, the ammonia-containing vapor is condensed by being cooled by the cooling water flowing outside the tubular body.

  Ammonia water obtained by condensing the ammonia-containing vapor is extracted from the bottom of the condenser 11 by the pump 17 and is sent via the path 18. The ammonia water can be used as circulating hot water, or can be distilled to obtain high purity ammonia. Further, the ammonia-containing vapor which has not condensed is discharged from the bottom of the condenser 11 by the liquid-sealed vacuum pump 16 through the passage 15, and is treated in the ammonia removal facility. Further, the ammonia-containing vapor after condensation is sucked from the condenser 11 by the liquid ring vacuum pump 16.

  Here, as shown in FIG. 2, the liquid-sealed vacuum pump 16 is provided eccentrically in the inner space 16 a and a casing 16 d having a cylindrical inner space 16 a, an inlet 16 b and an outlet 16 c. An impeller 16f having 16e, a rotary motor 16g for rotating the impeller 16f, and a sealing liquid supply pipe 16i for supplying the sealing liquid 16h into the casing 16d are provided. Then, the seal liquid 16h is supplied from the seal liquid supply pipe 16i to the internal space 16a of the casing 16d, and the impeller 16f is rotated by the rotary motor 16g to form a liquid ring in the internal space 16a of the casing 16d by centrifugal force. . Further, ammonia-containing vapor taken in from the intake port 16b into the air chamber formed by the adjacent wings 16e and the liquid ring is compressed by the reduction of the volume of the air chamber accompanying the rotation of the impeller 16f, and the rotation of the impeller 16f When the air chamber reaches the exhaust port 16c, the ammonia-containing vapor compressed in the air chamber is exhausted from the exhaust port 16c.

Returning to FIG. 1, the reduced-pressure distillation facility further includes a measuring unit 19, a heater 20 for heating, and a sealing liquid temperature control device 21. The sealing liquid temperature control device 21 includes a storage unit 21a, an information input unit 21b, and a sealing liquid temperature control unit 21c.
The measuring unit 19 is provided in the sealing liquid supply pipe 16i, and measures the temperature of the sealing liquid 16h in the sealing liquid supply pipe 16i, that is, the temperature of the sealing liquid 16h supplied to the liquid ring vacuum pump 16. For example, a thermocouple thermometer is used as the measuring unit 19. And the measurement part 19 outputs a measurement result to the sealing liquid temperature control part 21c.

The heating heater 20 is provided in the sealing liquid supply pipe 16i, and the sealing liquid 16h in the sealing liquid supply pipe 16i, that is, the sealing supplied to the liquid sealing vacuum pump 16 in accordance with a command from the sealing liquid temperature control unit 21c. Heat solution 16h. As the heater 20, for example, an in-line heater or a flange heater is used.
As shown in FIG. 3, the storage unit 21 a includes a concentration of naphthalene contained in the ammonia-containing vapor drawn by the liquid-sealed vacuum pump 16 determined in advance, and a seal in which naphthalene is deposited in the liquid-sealed vacuum pump 16. The correspondence with the temperature of the liquid 16 h is stored. The correspondence relationship between the concentration of these naphthalenes and the temperature of the sealing liquid 16h is examined in advance by using an actual reduced pressure type night water diaphragm for night using experiments and the like. For example, a hard disk is used as the storage unit 21a.

  The information input unit 21 b receives an input from the operator of the concentration of naphthalene contained in the ammonia-containing vapor drawn by the liquid ring vacuum pump 16. Then, the input result is output to the sealing liquid temperature control unit 21c. For example, a keyboard or a touch panel is used as the information input unit 21b. The concentration of naphthalene contained in the ammonia-containing vapor drawn by the liquid ring vacuum pump 16 can be obtained by manually collecting and analyzing the ammonia-containing vapor in the passage 15. It is also possible to measure continuously with a densitometer instead of hand analysis.

  The sealing liquid temperature control unit 21 c is an A / D (Analog to Digital) conversion circuit, a D / A (Digital to Analog) conversion circuit, a CPU (Central Processing Unit), a ROM (Read Only Memory), and a RAM (Random Access Memory). Etc.) and the like. The ROM stores programs for realizing various processes. When the information input unit 21b outputs the input result, the CPU executes a sealing liquid temperature control process for controlling the temperature of the sealing liquid 16h according to the program stored in the ROM.

When the sealing liquid temperature control process is executed, as shown in FIG. 4, first, in step S1, the CPU acquires the input result (current concentration of naphthalene) output from the information input unit 21b.
Subsequently, the process proceeds to step S2, and the CPU refers to the stored contents of the storage unit 21a, and the liquid ring vacuum pump corresponding to the concentration of naphthalene represented by the input result acquired in step S1, that is, the current concentration of naphthalene. A temperature higher than the temperature of the sixteen sealing solutions 16h is set as the target temperature. As a method of setting the target temperature, for example, a method of setting as a target temperature a temperature higher by a predetermined temperature than the temperature of the sealing liquid 16h corresponding to the current concentration of naphthalene can be adopted. For example, in consideration of the possibility that the temperature of the sealing solution 16h fluctuates, it is preferable to set a temperature which is higher by 2 to 3 ° C. than the temperature of the sealing solution 16h corresponding to the current concentration of naphthalene.

Subsequently, the process proceeds to step S3, and the CPU acquires the measurement result of the temperature of the sealing solution 16h output by the measuring unit 19.
Subsequently, the process proceeds to step S4, and the CPU instructs the heating of the sealing liquid 16h in the sealing liquid supply pipe 16i such that the temperature of the sealing liquid 16h acquired in step S3 becomes the target temperature set in step S2. Is output to the heater 20, and then the process returns to step S3. Thereby, it heats with the heater 20 for heating, and controls the temperature of the sealing liquid 16h.

  In the sealing liquid temperature control device 21 of this embodiment, the operator measures the concentration of naphthalene contained in the ammonia-containing vapor and inputs the measurement result, and the sealing liquid 16h corresponding to the current concentration of naphthalene is obtained. Control of the temperature of the sealing liquid 16 h is performed so as to be a temperature (target temperature) higher than the temperature of So, the effort concerning control of the temperature of sealing liquid 16h can be reduced.

Moreover, in the sealing liquid temperature control apparatus 21 of this embodiment, since the apparatus structure for performing temperature control can be simplified, a decompression type surplus surplus water distillation installation can be made into a cheap thing.
In addition, although the example which sets target temperature with the sealing liquid temperature control part 21c was shown in this embodiment, another structure is also employable. For example, a graph representing the correspondence between the concentration of naphthalene contained in the ammonia-containing vapor and the temperature of the sealing liquid 16h at which naphthalene is deposited in the liquid-sealed vacuum pump 16 is prepared, and the operator refers to the graph. The target speed may be manually set based on the concentration of naphthalene contained in the current ammonia-containing vapor.

DESCRIPTION OF SYMBOLS 1 ... Decompression-type surplus annasty water treatment distillation tower, 2 ... path | passage, 3 ... reboiler, 4 ... path | passage, 5 ... circulating pump, 6 .. DESCRIPTION OF SYMBOLS 15 ... Path | pass, 16 ... Liquid-sealed vacuum pump, 16a ... Internal space, 16b ... Intake port, 16c ... Exhaust port, 16d ... Casing, 16e ... Wing, 16f ... Impeller, 16g ... Rotation motor, 16h ... Sealing fluid, DESCRIPTION OF SYMBOLS 16i ... sealing liquid supply pipe | tube, 17 ... pump, 18 ... path | route 19 ... measurement part, 20 ... heater for heating, 21 ... sealing liquid temperature control apparatus, 21a ... memory part, 21b ... information input part, 21c ... sealing liquid temperature Control unit

Claims (3)

Excess ammonia water generated during the purification of coke oven gas is introduced into a vacuum distillation column and distilled under reduced pressure, and the ammonia-containing vapor distilled from the vacuum distillation column is introduced into a condenser for cooling and condensation, and the condenser Aspirating the ammonia-containing vapor with a liquid-sealed vacuum pump from the
The concentration of naphthalene contained in the ammonia-containing vapor drawn by the liquid-sealed vacuum pump and the temperature of the sealing liquid of the liquid-sealed vacuum pump at which the naphthalene is deposited in the liquid-sealed vacuum pump With reference to the correspondence relationship, a temperature higher than the temperature of the sealing solution corresponding to the current concentration of the naphthalene is set as a target temperature, and the sealing solution in the liquid ring vacuum pump is set to achieve the set target temperature. A method of operating a vacuum type surplus excess water distillation facility characterized by controlling a temperature. Excess ammonia water generated during the purification of coke oven gas is introduced into a vacuum distillation column and distilled under reduced pressure, and the ammonia-containing vapor distilled from the vacuum distillation column is introduced into a condenser for cooling and condensation, and the condenser A sealing liquid temperature control device for controlling the temperature of the sealing liquid in the liquid-sealed vacuum pump, of a decompression type surplus excess water distillation facility that sucks ammonia-containing vapor with a liquid-sealed vacuum pump from the
The relationship between the concentration of naphthalene contained in the ammonia-containing vapor drawn by the liquid-sealed vacuum pump and the temperature of the sealing liquid of the liquid-sealed vacuum pump where the naphthalene is deposited in the liquid-sealed vacuum pump is stored And the storage unit
With reference to the correspondence relationship stored in the storage unit, a temperature higher than the temperature of the sealing solution corresponding to the current concentration of the naphthalene is set as a target temperature, and the sealing solution in the liquid ring vacuum pump is And a sealing liquid temperature control unit for controlling the temperature of the sealing liquid in the liquid ring vacuum pump such that the temperature becomes a set target temperature. A measuring unit that measures the temperature of the sealing liquid in the sealing liquid supply pipe of the liquid ring vacuum pump;
And a heater for heating the sealing liquid in the sealing liquid supply pipe,
The sealing liquid temperature control unit causes the heating heater to heat the sealing liquid in the sealing liquid supply pipe so that the temperature of the sealing liquid measured by the measuring unit becomes the target temperature. The sealing liquid temperature control apparatus of claim 2.

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