CN214075129U - Distillation system - Google Patents
Distillation system Download PDFInfo
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- CN214075129U CN214075129U CN202023023846.7U CN202023023846U CN214075129U CN 214075129 U CN214075129 U CN 214075129U CN 202023023846 U CN202023023846 U CN 202023023846U CN 214075129 U CN214075129 U CN 214075129U
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Abstract
The utility model relates to a distillation system. The distillation system comprises: the rectifying tower is provided with an air inlet and a liquid outlet; the heat exchanger is provided with a tube pass feed inlet, a tube pass discharge outlet, a shell pass inlet and a shell pass outlet, the tube pass feed inlet is communicated with the liquid outlet, the tube pass discharge outlet is communicated with the gas inlet liquid outlet, so that liquid-phase materials entering the tube pass of the heat exchanger from the rectifying tower can exchange heat with heat exchange media in the shell pass of the heat exchanger to generate gas-liquid-phase materials, and the gas-liquid-phase materials flow back to the rectifying tower to be further separated into gas-liquid two phases, and the heat exchanger is also provided with a connecting interface communicated with the shell pass of the heat exchanger; and a shell pass outlet of the heat exchanger is communicated with a liquid inlet of the condensate tank, and a first outlet of the condensate tank is communicated with the connecting interface through a gas phase balance pipe. The utility model discloses can improve steam heat utilization ratio, practice thrift steam, distillation system easily operates and job stabilization, and product quality after the distillation is more excellent, the composition is more stable, can effectively improve the distillation effect.
Description
Technical Field
The utility model relates to a distillation evaporation technology field, concretely relates to distillation system.
Background
In the existing continuous distillation process of chemical production, no matter equilibrium distillation or normal, reduced and pressurized rectification, a distillation tower is generally arranged, and tower bottoms in the tower are heated by steam through a reboiler.
In a general continuous distillation process, taking distillation as an example, a distillation column is a main device in the distillation process, the distillation column is roughly divided into two sections, the bottom section is a column bottom section, and a packing section (or a tower plate section) is arranged above the column bottom section. Introducing the gas phase at the tower top into a condenser and a tail gas cooler, introducing the condensed liquid phase into a reflux tank, pumping part of the liquid in the reflux tank to the tower top for reflux after the liquid in the reflux tank is qualified, and extracting part of the liquid to obtain a finished product or a semi-finished product for continuous rectification. The evaporation and maintenance of the tower bottom liquid of the rectifying tower are completed by heating in a reboiler, the tube side of the reboiler is filled with materials, and the shell side is filled with steam. Because of the superiority of superheated steam in terms of transport quality and heat carrying capacity, superheated steam is generally used as steam. The condensate of the shell side of the reboiler flows into a condensate tank by means of potential difference, so that the condensate tank keeps a certain liquid level, and the gas phase part at the upper part in the tank is connected with a gas phase balance pipe for removing a reboiler steam inlet pipe, so as to ensure the balance of the gas phase pressure in the reboiler steam inlet and the condensate tank, and ensure that the condensate of the shell layer of the reboiler smoothly enters the condensate tank.
In the existing distillation process, a gas phase balance pipe of a condensate tank is generally directly connected to a steam pipe in front of a steam inlet of a reboiler, so that fresh superheated steam can partially flow into the condensate tank, and because a certain temperature difference exists between the fresh superheated steam and a water vapor system in the condensate tank, a heat exchange phenomenon can occur, so that a part of fresh steam is lost, and steam waste is caused; in addition, the total amount of condensate is increased because part of the fresh steam is directly condensed in the condensate tank without passing through the reboiler. In addition, in the prior art, the heating steam entering amount of the reboiler is controlled by the shell steam pressure of the tower kettle temperature cascade reboiler, and the condition that the tower kettle temperature and the reboiler steam pressure change in step are inconsistent often occurs due to the slowness of the temperature adjusting process, so that the tower kettle temperature fluctuation is large, and the adjusting process is slow.
SUMMERY OF THE UTILITY MODEL
In view of the above problems in the prior art, the present invention is directed to a distillation system, which can effectively reduce the waste of steam during distillation and save the cost; meanwhile, the temperature deviation of the tower kettle can be timely and conveniently adjusted.
In order to achieve the above object, the present invention provides a distillation system comprising:
the rectifying tower is provided with an air inlet and a liquid outlet;
the heat exchanger is provided with a tube pass feeding hole, a tube pass discharging hole, a shell pass inlet and a shell pass outlet, the tube pass feeding hole is communicated with the liquid outlet, the tube pass discharging hole is communicated with the gas inlet liquid port, so that liquid-phase materials entering the tube pass of the heat exchanger from the rectifying tower can exchange heat with heat exchange media in the shell pass of the heat exchanger to generate gas-liquid-phase materials, the gas-liquid-phase materials flow back to the rectifying tower to be further separated into gas and liquid phases, and the heat exchanger is also provided with a connecting interface communicated with the shell pass of the heat exchanger;
and a shell pass outlet of the heat exchanger is communicated with a liquid inlet of the condensate tank, and a first outlet of the condensate tank is communicated with the connecting interface through a gas phase balance pipe.
In some embodiments, the shell-side outlet and the connection interface are both disposed on a side wall of the heat exchanger near a bottom thereof, and the connection interface is located at an upper portion of the shell-side outlet.
In some embodiments, the distance between the connection interface and the shell-side outlet is 350-1000 mm.
In some embodiments, the shell side inlet is connected with a medium inlet pipe, and the medium inlet pipe is provided with a first regulating valve for controlling the inlet amount of the heat exchange medium.
In some embodiments, a pressure sensor is further disposed on the medium inlet pipe to monitor the pressure in the shell side of the heat exchanger, so as to control the opening and closing of the first regulating valve.
In some embodiments, the rectifying tower is further provided with a discharge port, the discharge port is connected with a discharge pipe, and the discharge pipe is provided with a second regulating valve.
In some embodiments, the rectifying tower is further provided with a first liquid level detector for detecting a tower kettle liquid level in the rectifying tower, and the first liquid level detector is electrically connected with the second regulating valve so as to control the opening and closing of the second regulating valve according to the detected tower kettle liquid level, so as to control the discharge amount of the discharge port.
In some embodiments, a second outlet is arranged at the bottom of the condensate tank, a condensate pipe is connected to the second outlet, and a condensate adjusting valve is arranged on the condensate pipe.
In some embodiments, the condensate tank is further provided with a second liquid level detector for detecting a condensate liquid level in the condensate tank, and the second liquid level detector is electrically connected with the condensate regulating valve, so that the opening and closing of the condensate regulating valve are controlled according to the detected condensate liquid level, and the liquid outlet amount of the second outlet is controlled.
In some embodiments, the heat exchanger is a reboiler; or the heat exchanger is replaced by a heater, and the heater is provided with the tube side feed inlet, the tube side discharge outlet, the shell side inlet and the shell side outlet.
Compared with the prior art, the utility model provides a distillation system is through the connection interface that sets up the shell side intercommunication with the heat exchanger on the heat exchanger to through the first exit linkage of gas phase balance pipe with connection interface and condensate tank, make the gas phase saturated steam of condensate tank and the shell of reboiler be close nearly saturated (or slightly overheated) steam phase equilibrium, avoided in the condensate tank because the heat transfer that leads to of scurrying into of live steam, thereby improved the utilization ratio of steam heat energy, practiced thrift steam. Additionally, the utility model discloses easily operate and can the steady operation, the product quality after the distillation is more excellent, the composition is more stable, can effectively improve the distillation effect.
Drawings
In the drawings, which are not necessarily drawn to scale, like reference numerals may describe similar components in different views. Like reference numerals having letter suffixes or different letter suffixes may represent different instances of similar components. The drawings illustrate various embodiments, by way of example and not by way of limitation, and together with the description and claims, serve to explain the embodiments of the invention. The same reference numbers will be used throughout the drawings to refer to the same or like parts, where appropriate. Such embodiments are illustrative, and are not intended to be exhaustive or exclusive embodiments of the present apparatus or method.
Fig. 1 is a schematic structural diagram of a distillation system according to an embodiment of the present invention.
Reference numerals:
1-a rectifying tower, 11-a gas-liquid inlet, 12-a liquid outlet and 13-a discharge port; 2-heat exchanger, 21-tube pass feed inlet, 22-tube pass discharge outlet, 23-shell pass inlet, 24-shell pass outlet and 25-connecting interface; 3-a condensate tank, 31-a liquid inlet, 32-a first outlet and 33-a second outlet; 41-first regulating valve, 42-second regulating valve, 43-condensate regulating valve; 5-a pressure sensor; 61-a first liquid level detector, 62-a second liquid level detector;
10-gas phase balance pipe, 20-medium outlet pipe, 30-medium inlet pipe, 40-discharge pipe and 50-condensation inlet pipe.
Detailed Description
In order to make the purpose, technical solution and advantages of the embodiments of the present invention clearer, the drawings of the embodiments of the present invention are combined below to clearly and completely describe the technical solution of the embodiments of the present invention.
Unless defined otherwise, technical or scientific terms used herein shall have the ordinary meaning as understood by those of ordinary skill in the art to which the invention belongs. The use of "first," "second," and similar terms in the description herein do not denote any order, quantity, or importance, but rather the terms are used to distinguish one element from another. The word "comprising" or "comprises", and the like, means that the element or item listed before the word covers the element or item listed after the word and its equivalents, but does not exclude other elements or items. The terms "connected" or "coupled" and the like are not restricted to physical or mechanical connections, but may include electrical connections, whether direct or indirect. "upper", "lower", "left", "right", and the like are used merely to indicate relative positional relationships, and when the absolute position of the object being described is changed, the relative positional relationships may also be changed accordingly.
To maintain the following description of the embodiments of the present invention clear and concise, detailed descriptions of well-known functions and components may be omitted.
Fig. 1 is a schematic structural diagram of a distillation system according to an embodiment of the present invention (the direction of arrows in the figure is a gas or liquid flow direction). As shown in fig. 1, embodiments of the present invention provide a distillation system, comprising:
the rectifying tower 1 is provided with a gas-liquid inlet 11 and a liquid outlet 12;
the heat exchanger 2 is provided with a tube pass feeding hole 21, a tube pass discharging hole 22, a shell pass inlet 23 and a shell pass outlet 24, the tube pass feeding hole 21 is communicated with a liquid outlet 12 of the rectifying tower 1, the tube pass discharging hole 22 is communicated with a liquid inlet 11 of the rectifying tower 1, so that a liquid-phase material entering a tube pass of the heat exchanger 2 from the rectifying tower 1 can exchange heat with a heat exchange medium in a shell pass of the heat exchanger 2 to generate a gas-liquid-phase material, the gas-liquid-phase material flows back to the rectifying tower 1 to be further separated into a gas phase and a liquid phase, and the heat exchanger 2 is further provided with a connecting interface 25 communicated with the shell pass of the heat exchanger 2;
the shell side outlet 24 of the condensate tank 3 and the heat exchanger 2 is communicated with the liquid inlet 31 of the condensate tank 3, and the first outlet 32 of the condensate tank 3 is communicated with the connecting interface 25 through the gas phase balance pipe 10.
Specifically, the gas inlet liquid port 11 is arranged at the middle upper part of the tower kettle of the rectifying tower 1, and the liquid outlet liquid port 12 is arranged at the lower part of the tower kettle of the rectifying tower 1, so that the material exchange with the heat exchanger 2 is facilitated. The heat exchanger 2 is a reboiler, a heat exchange medium in the shell pass is superheated steam, the superheated steam in the shell pass exchanges heat with tower bottoms in the tube pass, the tower bottoms are vaporized and evaporated to generate gas-liquid phase materials, and the gas-liquid phase materials flow back to the rectifying tower 1; the shell pass outlet 24 of the heat exchanger 2 is communicated with the liquid inlet 31 of the condensate tank 3 through the medium outlet pipe 20, and the heat exchange medium after heat exchange enters the condensate tank 3. When the heat exchange medium is superheated steam, the condensate of the condensate tank 3 may be condensate water.
The embodiment of the utility model provides a distillation system is through setting up the interface 25 of being connected with heat exchanger 2's shell side intercommunication on heat exchanger 2 to connect interface 25 and condensate tank 31's first export 32 through vapor balance pipe 10, make the vapor phase saturated steam of condensate tank 3 and the shell of reboiler be close nearly saturated (or slightly overheated) steam phase balance, avoided the heat transfer that leads to because scurrying into of live steam in condensate tank 3, thereby improved the utilization ratio of steam heat energy, practiced thrift steam. Additionally, the utility model discloses easily operate and can the steady operation, the product quality after the distillation is more excellent, the composition is more stable, can effectively improve the distillation effect.
In specific implementation, the heat exchange medium may also be other gas medium, or may also be a liquid medium, for example, a liquid medium with a higher temperature, and the tower bottoms in the rectifying tower 1 may be heated to vaporize and evaporate the tower bottoms; the liquid medium after heat exchange flows into the condensate tank 3, and a liquid phase balance pipe is arranged between the first outlet 32 of the condensate tank 3 and the shell pass of the heat exchanger 2 to maintain the liquid phase balance between the heat exchanger 2 and the condensate tank 3.
In some embodiments, as shown in fig. 1, both the shell-side outlet 24 and the connection interface 25 are disposed on the side wall of the heat exchanger 2 near the bottom thereof, and the connection interface 25 is located at the upper portion of the shell-side outlet 24. The connecting interface 25 is arranged close to the shell pass outlet 24 at the bottom of the heat exchanger 2, so that the gas phase saturated steam of the condensate tank 3 and the shell layer of the reboiler are almost in equilibrium with saturated (or slightly superheated) steam, and the heat exchange caused by the fresh steam entering is further reduced.
Preferably, the distance between the connection interface 25 and the shell-side outlet 24 is 350-1000mm, so as to ensure the circulation balance of the steam. The connection interface 25 can be a flange interface, which is convenient to disassemble and assemble and reliable in connection.
As shown in fig. 1, the liquid inlet 31 of the condensate tank 3 is disposed at the top of the condensate tank 3, so that the heat exchange medium in the shell pass of the heat exchanger 2 can automatically flow into the condensate tank 3 through the medium outlet pipe 20. In this embodiment, since the heat exchange medium is superheated steam, the first outlet 32 is also disposed at the top of the condensate tank 3, so as to facilitate the balance of the gas flowing in the gas phase equilibrium tube 10. The specific position of the first outlet 32 may be set according to actual needs, and the present invention is not limited specifically.
In some embodiments, the shell-side inlet 23 is connected to a medium inlet pipe 30, and a first regulating valve 41 for controlling the inlet amount of the heat exchange medium is disposed on the medium inlet pipe 30.
Further, the medium inlet pipe 30 is further provided with a pressure sensor 5 to monitor the pressure in the shell side of the heat exchanger 2, so as to control the opening and closing of the first regulating valve 41.
In this embodiment, the steam pressure in the shell side of the heat exchanger 2 is used to control the steam amount of the shell side inlet 23, and the steam amount is not adjusted in cascade with the temperature of the tower kettle, so that the adjustment and tracking can be faster, the defect of large temperature fluctuation of the tower kettle is avoided, and the temperature of the tower kettle is convenient to stabilize.
In some embodiments, as shown in fig. 1, the rectifying tower 1 is further provided with a discharge port 13, the discharge port 13 is connected with a discharge pipe 40, the discharge pipe 40 is provided with a second regulating valve 42, and the second regulating valve 42 is a rectifying tower bottom discharge regulating valve. In this embodiment, the discharge port 13 is disposed at the bottom of the tower bottom of the rectifying tower 1, so as to facilitate discharging, and the discharge port 13 may also be disposed at a position on the side wall of the tower bottom near the bottom thereof.
In some embodiments, the rectifying tower 1 is further provided with a first liquid level detector 61 for detecting a tower still liquid level in the rectifying tower 1, and the first liquid level detector 61 is electrically connected to the second regulating valve 42 to control the opening and closing of the second regulating valve 42 according to the detected tower still liquid level, so as to control the discharge amount of the discharge port 13.
In some embodiments, the bottom of the condensate tank 3 is provided with a second outlet 33, the second outlet 33 is a condensate outlet, the second outlet 33 is connected with a condensate pipe 50, and the condensate pipe 50 is provided with a condensate adjusting valve 43.
In some embodiments, the condensate tank 3 is further provided with a second liquid level detector 62 for detecting a liquid level of the condensate in the condensate tank 3, and the second liquid level detector 62 is electrically connected to the condensate adjusting valve 43, so as to control opening and closing of the condensate adjusting valve 43 according to the detected liquid level of the condensate, and thus control the liquid output amount of the second outlet 33.
In this embodiment, the discharge pipe 40 of the rectifying tower 1 and the condensate pipe 50 of the condensate tank 3 are respectively provided with an adjusting valve and are respectively controlled by the respective liquid levels, so that the loss of steam energy can be effectively reduced, and the purpose of stable control can be achieved.
In some embodiments, the heat exchanger may be replaced with a heater having the tube-side feed port 21, tube-side discharge port 22, shell-side inlet 23, and shell-side outlet 24 described above. The heater can utilize the heating medium in the shell pass to heat the tower bottom liquid, so that the tower bottom liquid is evaporated to generate gas-liquid phase materials.
The embodiment of the utility model provides a distillation system's concrete working process and effect as follows:
example 1
In a certain benzene rectifying tower, the high-pressure tower bottom liquid is heated by superheated steam of 0.4MPa (G) and 290 ℃, the temperature of the bottom liquid is about 115 ℃, the temperature of the top of the tower is about 107 ℃, the heating steam amount is controlled by the steam pressure in the shell layer of a reboiler, a gas phase balance pipe 10 of a condensate tank 3 is connected with a connecting interface 25 at the middle lower part of the shell layer of the reboiler, the steam in the condensate tank 3 flows into the shell layer of the reboiler from the middle lower part of the reboiler through the gas phase balance pipe 10 to balance the steam pressure, the opening and closing of a condensate regulating valve 43 are controlled by the liquid level of the condensate tank, and the opening and closing of a discharging regulating valve of the rectifying tower bottom is controlled by the liquid level of the tower bottom. The whole control operation is stable, and particularly, the temperature of the tower kettle basically does not fluctuate. The liquid level of the tower bottom and the liquid level of the condensate are normal, and the liquid outlet temperature of the condensate is reduced by 5 ℃ compared with that before the distillation system provided by the embodiment is not adopted.
Example 2
In the first-effect tower of a certain three-effect rectifying tower, tower bottom liquid is heated by superheated steam of 1.1MPa (G) and 320 ℃, the temperature of the tower bottom liquid is about 156 ℃, the temperature of the tower top is about 153 ℃, the heating steam amount is controlled by the steam pressure in a shell layer of a reboiler, a gas phase balance pipe 10 of a condensate tank 3 is connected with a connecting interface 25 at the middle lower part of the shell layer of the reboiler, the steam in the condensate tank 3 flows into the shell layer of the reboiler from the middle lower part of the reboiler through the gas phase balance pipe 10 to balance the steam pressure, the opening and closing of a condensate regulating valve 43 are controlled by the liquid level of the condensate tank, and the opening and closing of a discharge regulating valve of a rectifying tower kettle are controlled by the liquid level of the tower bottom. The whole control operation is stable, and particularly, the temperature of the tower kettle basically does not fluctuate. The liquid level of the tower bottom and the liquid level of the condensate are normal, and the liquid outlet temperature of the condensate is reduced by 6 ℃ compared with that before the method is adopted.
Example 3
In a certain stripping tower, tower bottom liquid is heated by superheated steam of 1.3MPa (G) and 320 ℃, the temperature of the tower bottom liquid is about 145 ℃, the temperature of the top of the tower is about 140 ℃, the heating steam amount is controlled by the steam pressure in the shell layer of a reboiler, a gas phase balance pipe 10 of a condensate tank 3 is connected with a connecting interface 25 at the middle lower part of the shell layer of the reboiler, the steam in the condensate tank 3 flows into the shell layer of the reboiler from the middle lower part of the reboiler through the gas phase balance pipe 10 to balance the steam pressure, the opening and closing of a condensate regulating valve 43 are controlled by the liquid level of the condensate tank, and the opening and closing of a discharging regulating valve of a rectifying tower kettle are controlled by the liquid level of the tower kettle. The whole control operation is stable, and particularly, the temperature of the tower kettle basically does not fluctuate. The liquid level of the tower bottom and the liquid level of the condensate are normal, and the liquid outlet temperature of the condensate is reduced by 7 ℃ compared with that before the method is adopted.
According to the specific distillation of the three distillation towers, the distillation system of the embodiment ensures that the temperature of the tower kettle is stable and the liquid levels in the rectifying tower 1 and the condensate tank 3 are stable in the distillation process, so that the whole distillation process is more stable in operation; and the temperature of the condensate liquid can be effectively reduced.
The above embodiments are only exemplary embodiments of the present invention, and are not intended to limit the present invention, and the protection scope of the present invention is defined by the claims. Various modifications and equivalents of the invention can be made by those skilled in the art within the spirit and scope of the invention, and such modifications and equivalents should also be considered as falling within the scope of the invention.
Claims (10)
1. A distillation system, comprising:
the rectifying tower is provided with an air inlet and a liquid outlet;
the heat exchanger is provided with a tube pass feeding hole, a tube pass discharging hole, a shell pass inlet and a shell pass outlet, the tube pass feeding hole is communicated with the liquid outlet, the tube pass discharging hole is communicated with the gas inlet liquid port, so that liquid-phase materials entering the tube pass of the heat exchanger from the rectifying tower can exchange heat with heat exchange media in the shell pass of the heat exchanger to generate gas-liquid-phase materials, the gas-liquid-phase materials flow back to the rectifying tower to be further separated into gas and liquid phases, and the heat exchanger is also provided with a connecting interface communicated with the shell pass of the heat exchanger;
and a shell pass outlet of the heat exchanger is communicated with a liquid inlet of the condensate tank, and a first outlet of the condensate tank is communicated with the connecting interface through a gas phase balance pipe.
2. A distillation system according to claim 1, wherein the shell-side outlet and the connection interface are both provided in a side wall of the heat exchanger near a bottom thereof, and the connection interface is located at an upper portion of the shell-side outlet.
3. A distillation system according to claim 2, wherein the distance between the connection interface and the shell-side outlet is 350-1000 mm.
4. The distillation system according to claim 1, wherein the shell side inlet is connected with a medium inlet pipe, and a first regulating valve for controlling the inlet amount of the heat exchange medium is arranged on the medium inlet pipe.
5. The distillation system according to claim 4, wherein a pressure sensor is further disposed on the medium inlet pipe to monitor the pressure in the shell side of the heat exchanger, so as to control the opening and closing of the first regulating valve.
6. The distillation system according to claim 1, wherein the distillation tower is further provided with a discharge port, the discharge port is connected with a discharge pipe, and the discharge pipe is provided with a second regulating valve.
7. The distillation system as claimed in claim 6, wherein the distillation column is further provided with a first liquid level detector for detecting the liquid level of the column bottom in the distillation column, and the first liquid level detector is electrically connected with the second regulating valve so as to control the opening and closing of the second regulating valve according to the detected liquid level of the column bottom, thereby controlling the discharge amount of the discharge hole.
8. The distillation system as claimed in claim 1, wherein a second outlet is provided at the bottom of the condensate tank, a condensate pipe is connected to the second outlet, and a condensate regulating valve is provided on the condensate pipe.
9. The distillation system as claimed in claim 8, wherein a second level detector is further disposed on the condensate tank for detecting a level of condensate in the condensate tank, and the second level detector is electrically connected to the condensate regulating valve, so as to control the opening and closing of the condensate regulating valve according to the detected level of condensate, thereby controlling the amount of liquid discharged from the second outlet.
10. A distillation system according to any one of claims 1 to 9, wherein the heat exchanger is a reboiler; or the heat exchanger is replaced by a heater, and the heater is provided with the tube side feed inlet, the tube side discharge outlet, the shell side inlet and the shell side outlet.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202023023846.7U CN214075129U (en) | 2020-12-15 | 2020-12-15 | Distillation system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202023023846.7U CN214075129U (en) | 2020-12-15 | 2020-12-15 | Distillation system |
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| CN214075129U true CN214075129U (en) | 2021-08-31 |
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| CN202023023846.7U Active CN214075129U (en) | 2020-12-15 | 2020-12-15 | Distillation system |
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Effective date of registration: 20230914 Address after: 274500 Yuwo Street Office, Dongming County, Heze City, Shandong Province, Northeast corner of the intersection of Provincial Road 252 and Wei'er Road Patentee after: Dongming Xuyang Chemical Co.,Ltd. Address before: 274500 Fangming Chemical Co., Ltd., South Chemical Industry Park, Dongming County, Heze City, Shandong Province Patentee before: SHANDONG FANGMING CHEMICAL Co.,Ltd. |
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