CN214260711U - Negative pressure evaporation system for secondary steam utilization of stripping tower - Google Patents
Negative pressure evaporation system for secondary steam utilization of stripping tower Download PDFInfo
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- CN214260711U CN214260711U CN202022623400.1U CN202022623400U CN214260711U CN 214260711 U CN214260711 U CN 214260711U CN 202022623400 U CN202022623400 U CN 202022623400U CN 214260711 U CN214260711 U CN 214260711U
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Abstract
A negative pressure evaporation system for secondary steam utilization of a stripping tower belongs to the technical field of grease processing. The utility model discloses the steam stripping tower's steam enters the second heat exchanger through the pipeline and carries out the heat transfer, and the steam after the heat transfer enters the steam stripping condenser and carries out the cooling heat transfer with the circulating water, and the gas that cools off and condenses is sent the knockout drum by the pump sending, and the gas that does not cool off and condense is discharged into tail gas condenser by the water ring vacuum pump, gets into tail gas absorption system at last; and the mixed oil of the first evaporation flash tank enters a second heat exchanger through a second evaporation oil supply pump through a pipeline for heat exchange, and the mixed oil after heat exchange flows into the first heat exchanger to exchange heat with the crude oil at 110 ℃ coming out of the stripping tower again and then enters a second evaporator. The purpose is in order to solve the problem of retrieving the steam stripping tower secondary steam stripping heat energy, reduce steam consumption, reduce circulation hydrothermal load, not only can save a large amount of steam and cooling water, but also can improve the quality of crude oil, to reducing the cost of enterprises, improve economic benefits and have an important effect.
Description
Technical Field
The utility model relates to a negative pressure vaporization system that strip tower secondary steam utilized belongs to grease processing technology field.
Background
The extraction method for preparing soybean oil has been used in China for decades, a mixed oil negative pressure evaporation system in an extraction workshop is also greatly popularized, about 25% of mixed oil is pumped out of an extractor by a pump and is sent into a hydrocyclone separator, a self-cleaning filter is used for removing impurities and then enters primary steam, and a primary steam heating medium is secondary steam generated by a steam-stripping machine. The mixed oil after the first steaming is pumped into the second steaming by a pump. Pumping the mixed oil after secondary evaporation into a stripping tower, and leading the residual solution of the crude oil to reach below 100mg/kg under the vacuum of about-75 kPa and the action of introduced direct steam. The secondary steam generated by the primary steam, the secondary steam and the stripping tower respectively enters a distillation condenser and a stripping condenser, is condensed by circulating water from a water cooling tower, and the condensed solvent is recycled.
Practice finds that the secondary steam that the stripper produced directly gets into the stripper condenser, carries out the condensation and retrieves the solvent, and heat energy has not obtained abundant utilization, has not only caused certain steam extravagant, has increased circulating water load simultaneously, especially summer, and circulating water temperature is high when the gas temperature is high, and the circulating water quantity is big, and condensation effect is poor moreover, and problem such as vacuum unstability also can appear in evaporating system.
Therefore, it is desirable to provide a negative pressure evaporation system for secondary steam utilization in a stripping tower to solve the above technical problems.
SUMMERY OF THE UTILITY MODEL
The present invention is developed to solve the problems of recovering the heat energy of the secondary stripping of the stripping tower, reducing the steam consumption, reducing the heat load of the circulating water, and the following brief summary of the present invention is given in order to provide a basic understanding of some aspects of the present invention. It should be understood that this summary is not an exhaustive overview of the invention. It is not intended to identify key or critical elements of the invention or to delineate the scope of the invention.
The technical scheme of the utility model:
a negative pressure evaporation system for secondary steam utilization of a stripping tower comprises the stripping tower, a first evaporator, a first evaporation and flash tank, a second evaporator, a second evaporation and flash tank, a first heat exchanger, an evaporation condenser, a stripping condenser, a second evaporation and oil supply pump, a first steam supply oil pump, a second stripping and extraction pump and a second heat exchanger;
the first evaporator is communicated with the first evaporation and flash tank through a pipeline, the first evaporation and flash tank is communicated with the second evaporation and flash tank and the second evaporation and oil supply pump through pipelines respectively, and the second evaporation and oil supply pump and the first evaporation and flash tank are communicated with the evaporation condenser through a pipeline after confluence;
the second evaporation and flash tank and the second evaporator are installed in a communicated mode through a pipeline, the second evaporator and the first heat exchanger are installed in a communicated mode through a pipeline, the first heat exchanger and the second evaporation and oil supply pump are installed in a communicated mode through a pipeline, and the second evaporation and flash tank and the first steam and oil supply pump are installed in a communicated mode through a pipeline;
the first steam supply oil pump is communicated with the stripping tower through a pipeline, the stripping tower is communicated with the second stripping extraction pump through a pipeline, and the second stripping extraction pump is communicated with the first heat exchanger through a pipeline;
the stripping tower and the second heat exchanger are communicated and installed through a pipeline, and the second heat exchanger is respectively communicated and installed with the stripping condenser and the second oil supply pump through pipelines.
The utility model discloses a solve the control problem of pipeline valve flow, propose the technical scheme of the utility model be:
a negative pressure evaporation system for secondary steam utilization of a stripping tower comprises the stripping tower, a first evaporator, a first evaporation and flash tank, a second evaporator, a second evaporation and flash tank, a first heat exchanger, an evaporation condenser, a stripping condenser, a second evaporation and oil supply pump, a first steam supply oil pump, a second stripping and extraction pump and a second heat exchanger;
the first evaporator is communicated with the first evaporation and flash tank through a pipeline, the first evaporation and flash tank is communicated with the second evaporation and flash tank and the second evaporation and oil supply pump through pipelines respectively, and the second evaporation and oil supply pump and the first evaporation and flash tank are communicated with the evaporation condenser through a pipeline after confluence;
the second evaporation and flash tank and the second evaporator are installed in a communicated mode through a pipeline, the second evaporator and the first heat exchanger are installed in a communicated mode through a pipeline, the first heat exchanger and the second evaporation and oil supply pump are installed in a communicated mode through a pipeline, and the second evaporation and flash tank and the first steam and oil supply pump are installed in a communicated mode through a pipeline;
the first steam supply oil pump is communicated with the stripping tower through a pipeline, the stripping tower is communicated with the second stripping extraction pump through a pipeline, and the second stripping extraction pump is communicated with the first heat exchanger through a pipeline;
the stripping tower and the second heat exchanger are communicated and installed through a pipeline, and the second heat exchanger is respectively communicated and installed with the stripping condenser and the second oil supply pump through pipelines.
Preferably: a plurality of control valves are arranged and installed on the pipeline.
The utility model discloses a solve the problem that the strip tower secondary steam is not utilized, its technical scheme is:
a negative pressure evaporation system for secondary steam utilization of a stripping tower comprises the stripping tower, a first evaporator, a first evaporation and flash tank, a second evaporator, a second evaporation and flash tank, a first heat exchanger, an evaporation condenser, a stripping condenser, a second evaporation and oil supply pump, a first steam supply oil pump, a second stripping and extraction pump and a second heat exchanger;
the first evaporator is communicated with the first evaporation and flash tank through a pipeline, the first evaporation and flash tank is communicated with the second evaporation and flash tank and the second evaporation and oil supply pump through pipelines respectively, and the second evaporation and oil supply pump and the first evaporation and flash tank are communicated with the evaporation condenser through a pipeline after confluence;
the second evaporation and flash tank and the second evaporator are installed in a communicated mode through a pipeline, the second evaporator and the first heat exchanger are installed in a communicated mode through a pipeline, the first heat exchanger and the second evaporation and oil supply pump are installed in a communicated mode through a pipeline, and the second evaporation and flash tank and the first steam and oil supply pump are installed in a communicated mode through a pipeline;
the first steam supply oil pump is communicated with the stripping tower through a pipeline, the stripping tower is communicated with the second stripping extraction pump through a pipeline, and the second stripping extraction pump is communicated with the first heat exchanger through a pipeline;
the stripping tower and the second heat exchanger are communicated and installed through a pipeline, and the second heat exchanger is respectively communicated and installed with the stripping condenser and the second oil supply pump through pipelines.
Preferably: a plurality of control valves are arranged and installed on the pipeline.
The secondary steam of the stripping tower enters a second heat exchanger through a pipeline for heat exchange, the secondary steam after heat exchange enters a stripping condenser for cooling and heat exchange with circulating water, the gas which is cooled and condensed into condensate flows into a water diversion process for solvent recovery, and the gas which is not cooled and condensed enters a tail gas absorption process;
and the mixed oil of the first evaporation flash tank enters a second heat exchanger through a second evaporation oil supply pump through a pipeline for heat exchange, and the mixed oil after heat exchange flows into the first heat exchanger to exchange heat with the crude oil at 110 ℃ coming out of the stripping tower again and then enters a second evaporator.
Preferably: the temperature of the mixed oil subjected to heat exchange in the second heat exchanger is increased from 55 ℃ to 62 ℃.
The utility model discloses following beneficial effect has:
1. the utility model discloses a negative pressure evaporation system that stripper secondary steam utilized not only can save a large amount of steam and cooling water, but also can improve the quality of crude oil, has important effect to reducing the cost of enterprises, improve economic benefits;
2. the utility model discloses a negative pressure evaporation system that stripper secondary steam utilized retrieves stripper secondary steam stripping heat energy, reduces steam consumption, reduces the circulation hydrothermal load and has very important practice circulation energy-saving production significance to oil mill;
3. the utility model discloses a negative pressure evaporation system that stripper steam utilized, use stripper steam to heat the mixed oil that evaporates out, make heat energy obtain reasonable abundant utilization, more green energy-conservation;
4. the utility model discloses a negative pressure vaporization system that strip tower secondary steam utilized, simple structure, design benefit, low cost are suitable for using widely.
Drawings
FIG. 1 is a block diagram of a negative pressure vaporization system for stripping column secondary steam utilization;
FIG. 2 is a block diagram of a prior art stripper vaporization system;
in the figure, T01-a stripping tower, E01-a first evaporator, E02-a flash evaporation box, E03-a second evaporator, E04-a second flash evaporation box, E05-a first heat exchanger, E06-an evaporative condenser, E07-a stripping condenser, E08-a second heat exchanger, P01-a second evaporation oil pump, P02-a first vapor supply oil pump and P03-a second stripping extraction pump.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be described below with reference to specific embodiments shown in the accompanying drawings. It should be understood that the description is intended to be illustrative only and is not intended to limit the scope of the present invention. Moreover, in the following description, descriptions of well-known structures and techniques are omitted so as to not unnecessarily obscure the concepts of the present invention.
The utility model discloses the connection that mentions divide into fixed connection and can dismantle the connection, fixed connection is for the conventional fixed connection mode such as undetachable connection including but not limited to hem connection, rivet connection, adhesive connection and welded connection, can dismantle the connection including but not limited to conventional dismantlement modes such as threaded connection, buckle connection, pin joint and hinged joint, when not clearly prescribing a limit to concrete connection mode, acquiesces to always can find at least one kind of connected mode in current connected mode and can realize this function, and the technical staff in the art can select by oneself as required. For example: the fixed connection selects welding connection, and the detachable connection selects hinge connection.
The first embodiment is as follows: the present embodiment is described with reference to fig. 1 to fig. 2, and the negative pressure evaporation system for secondary steam utilization in a stripping column of the present embodiment includes a stripping column T01, a first evaporator E01, a first evaporation flash tank E02, a second evaporator E03, a second evaporation flash tank E04, a first heat exchanger E05, an evaporation condenser E06, a stripping condenser E07, a second evaporation oil pump P01, a first steam supply oil pump P02, and a second stripping extraction pump P03, and is characterized in that: the heat exchanger further comprises a second heat exchanger E08, wherein the second heat exchanger E08 is a 200m2 heat exchanger;
the first evaporator E01 is communicated with a first evaporation and flash tank E02 through a pipeline, the first evaporation and flash tank E02 is communicated with a second evaporation and flash tank E04 and a second evaporation and flash pump P01 through pipelines respectively, and the second evaporation and flash pump P01 and the first evaporation and flash tank E02 are communicated with the evaporation and flash tank E06 through a pipeline after confluence;
the second evaporation flash tank E04 and the second evaporator E03 are installed in a communicated mode through pipelines, the second evaporator E03 and the first heat exchanger E05 are installed in a communicated mode through pipelines, the first heat exchanger E05 and the second evaporation oil pump P01 are installed in a communicated mode through pipelines, and the second evaporation flash tank E04 and the first vapor supply oil pump P02 are installed in a communicated mode through pipelines;
the first steam supply oil pump P02 and the stripping tower T01 are installed in a communicated mode through a pipeline with the pipe diameter of DN300 mm, the stripping tower T01 and the second stripping extraction pump P03 are installed in a communicated mode through a pipeline, and the second stripping extraction pump P03 and the first heat exchanger E05 are installed in a communicated mode through a pipeline;
the stripping tower T01 is communicated with a second heat exchanger E08 through a pipeline, and a second heat exchanger E08 is respectively communicated with a stripping condenser E07 and a second steam feed pump P01 through pipelines.
The secondary steam produced by the stripping tower T01 and the mixed oil before entering the secondary steam flash tank E04 exchange heat by using a two-process tube type heat exchanger, part of the secondary steam of the stripping tower T01 in the existing stripping tower evaporation system directly enters a stripping tower condenser to be condensed to recover a solvent, heat energy is not fully utilized, certain steam waste is caused, and meanwhile, the circulating water load is increased, the oil inlet temperature of the secondary steam mixed oil is increased after the implementation of the embodiment, the using amount of the secondary steam is reduced, for example, the effective enthalpy value of 10kg/cm2 steam for secondary steam is 2388.81kJ/kg, the steam using amount of 205.94kg/h of a 2500T/d soybean processing plant can be saved as 491952.71/2388.81, the steam saving of 1.98kg/T of a ton of bean is implemented by the scheme as 205.94/104166.67/1000, and the circulating hydrothermal load of 491952.71kJ/h is reduced. The cost can be saved by 30.89 ten thousand yuan (1.98 x 75 x 208/1000) per year according to the calculation of 75 ten thousand of soybeans processed per 2500t/d factory year and the calculation of steam per 208 yuan/ton; the cost for purchasing and installing the heat exchanger is 32 ten thousand yuan, and after 12.5 months of recovery cost, 30.89 ten thousand yuan of benefit is brought each year.
The second embodiment is as follows: the embodiment is described with reference to fig. 1 to fig. 2, and based on the first embodiment, the negative pressure evaporation system for utilizing secondary steam of the stripping tower of the embodiment is provided with a plurality of control valves on the pipeline, so that the flow rate of the switch and the maintenance are conveniently controlled.
The third concrete implementation mode: the embodiment is described with reference to fig. 1-2, and based on a first specific embodiment, the negative pressure evaporation system for secondary steam utilization of the stripping tower of the embodiment is that secondary steam generated by the stripping tower T01 enters a second heat exchanger E08 through a pipeline to exchange heat with a distilled mixed oil at about 55 ℃, the secondary steam after heat exchange enters a stripping condenser E07 to exchange cooling heat with circulating water, and a cooled and condensed gas (a mixture of water and a solvent) is pumped to a water separation tank to be separated from water and then is sent to a wastewater boiling system; gas which is not cooled and condensed (mainly air containing a small amount of solvent) is discharged into a tail gas condenser by a water ring vacuum pump and finally enters a tail gas absorption system;
the mixed oil at about 55 ℃ from the first evaporation flash tank E02 enters a second heat exchanger E08 through a pipeline through a second evaporation oil supply pump P01 for heat exchange, and the mixed oil after heat exchange flows into the first heat exchanger E05 for heat exchange again with the crude oil at 110 ℃ from the stripping tower T01 and then enters a second evaporator E03.
The fourth concrete implementation mode: in the negative pressure evaporation system for secondary steam utilization of the stripping tower of the embodiment, the temperature of the mixed oil subjected to heat exchange in the second heat exchanger E08 is increased from 55 ℃ to 62 ℃ by combining with the description of the embodiment with the figures 1-2.
The fifth concrete implementation mode: the embodiment is described with reference to fig. 1 to 2, and the working principle of the negative pressure evaporation system for secondary steam utilization of the stripping tower of the embodiment is as follows:
when the solvent of crude oil is removed from the stripping tower T01 at about negative 75KPa by using direct steam with the pressure of 4kg/cm2, a large amount of secondary steam containing the solvent at about 100 ℃ is generated, the part of gas enters the shell side of a second heat exchanger E08 through a pipeline and exchanges heat with the mixture of the mixed oil soybean oil with about 55 ℃ and the solvent from a first evaporator E01 and a first evaporation flash tank E02, and the mixture is conveyed into a heat exchange pipe of the second heat exchanger E08 by a second evaporation oil supply pump P01; after heat exchange, the temperature of the mixed oil is raised to about 62 ℃, the mixed oil enters a shell pass of a first heat exchanger E05 through a pipeline, the mixed oil and crude oil with about 100ppm of solvent in 110 ℃ crude oil from a stripping tower T01 are conveyed to a tube pass of the first heat exchanger E05 through a second stripping extraction pump P03 for heat exchange, the temperature of the crude oil is raised to about 72 ℃ and then enters a tube pass of a second evaporator E03, the crude oil is heated to 110 ℃ by fresh steam with the pressure of 104kg/cm2 of the shell pass, then the boiling point of the solvent is distilled out, the mixed oil with the temperature of 110 ℃ enters a second evaporation flash box E04, and the mixed oil is gasified in a large amount of solvent in the second evaporation flash box E04 with the negative pressure of about 60KP and enters an evaporation condenser E06 to be condensed into liquid below 30 ℃ by circulating water and recovered by a water separating system; the mixed oil with the concentration of 97 percent from the secondary evaporation flash tank E04 enters a first steam providing oil pump P02, is conveyed to a stripping tower T01 to be stripped by direct steam with the pressure of 4kg/cm2 under the pressure of about negative 75KPa, and secondary steam after being stripped enters a second heat exchanger for heat exchange and then enters a stripping condenser E07 shell pass through a pipeline to be condensed and recovered by circulating water below 30 tube passes. The technology exchanges heat between secondary steam generated by the stripping tower and the mixed oil after primary steaming through a newly installed heat exchanger, recovers 181799.9kcal/h heat, and raises the temperature of the mixed oil after primary steaming to about 7 ℃, so that the steam consumption of two tons of beans is reduced by 3.1 kg; the purposes of further saving steam and reducing the load of circulating water heat are achieved after the soybean is modified by calculating the daily processing of 2500t soybeans.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of example embodiments according to the present application. As used herein, the singular forms "a", "an" and "the" are intended to include the plural forms as well, and it should be understood that when the terms "comprises" and/or "comprising" are used in this specification, they specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof, unless the context clearly indicates otherwise.
The relative arrangement of the components and steps, the numerical expressions and numerical values set forth in these embodiments do not limit the scope of the present invention unless specifically stated otherwise. Meanwhile, it should be understood that the sizes of the respective portions shown in the drawings are not drawn in an actual proportional relationship for the convenience of description. Techniques, methods, and apparatus known to those of ordinary skill in the relevant art may not be discussed in detail but are intended to be part of the specification where appropriate. In all examples shown and discussed herein, any particular value should be construed as merely illustrative, and not limiting. Thus, other examples of the exemplary embodiments may have different values. It should be noted that: like reference numbers and letters refer to like items in the following figures, and thus, once an item is defined in one figure, further discussion thereof is not required in subsequent figures.
In the description of the present invention, it is to be understood that the orientation or positional relationship indicated by the orientation words such as "front, rear, upper, lower, left, right", "lateral, vertical, horizontal" and "top, bottom", etc. are usually based on the orientation or positional relationship shown in the drawings, and are only for convenience of description and simplicity of description, and in the case of not making a reverse description, these orientation words do not indicate and imply that the device or element being referred to must have a specific orientation or be constructed and operated in a specific orientation, and therefore, should not be considered as limiting the scope of the present invention; the terms "inner and outer" refer to the inner and outer relative to the profile of the respective component itself.
Spatially relative terms, such as "above … …," "above … …," "above … …," "above," and the like, may be used herein for ease of description to describe one device or feature's spatial relationship to another device or feature as illustrated in the figures. It will be understood that the spatially relative terms are intended to encompass different orientations of the device in use or operation in addition to the orientation depicted in the figures. For example, if a device in the figures is turned over, devices described as "above" or "on" other devices or configurations would then be oriented "below" or "under" the other devices or configurations. Thus, the exemplary term "above … …" can include both an orientation of "above … …" and "below … …". The device may be otherwise variously oriented (rotated 90 degrees or at other orientations) and the spatially relative descriptors used herein interpreted accordingly.
It should be noted that the terms "first," "second," and the like in the description and claims of this application and in the drawings described above are used for distinguishing between similar elements and not necessarily for describing a particular sequential or chronological order. It is to be understood that the data so used is interchangeable under appropriate circumstances such that the embodiments of the application described herein are capable of operation in sequences other than those illustrated or described herein.
It should be noted that, in the above embodiments, as long as the technical solutions can be aligned and combined without contradiction, those skilled in the art can exhaust all possibilities according to the mathematical knowledge of the alignment and combination, and therefore, the present invention does not describe the technical solutions after alignment and combination one by one, but it should be understood that the technical solutions after alignment and combination have been disclosed by the present invention.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (1)
1. The utility model provides a negative pressure vaporization system that stripper secondary steam utilized, includes stripper (T01), first evaporimeter (E01), a evaporation flash tank (E02), second evaporimeter (E03), two evaporation flash tank (E04), first heat exchanger (E05), evaporative condenser (E06), stripping condenser (E07), two evaporate fuel feed pump (P01), first vapour provides oil pump (P02) and second vapour and draws pump (P03), its characterized in that: further comprising a second heat exchanger (E08);
the first evaporator (E01) is communicated with the first evaporation and flash box (E02) through a pipeline, the first evaporation and flash box (E02) is communicated with the second evaporation and flash box (E04) and the second evaporation and oil supply pump (P01) through pipelines respectively, and the second evaporation and flash box (E04) and the first evaporation and flash box (E02) are communicated with the evaporation condenser (E06) through pipelines after confluence;
the second evaporation flash tank (E04) and the second evaporator (E03) are installed in a communicated mode through pipelines, the second evaporator (E03) and the first heat exchanger (E05) are installed in a communicated mode through pipelines, the first heat exchanger (E05) and the second evaporation oil supply pump (P01) are installed in a communicated mode through pipelines, and the second evaporation flash tank (E04) and the first evaporation oil supply pump (P02) are installed in a communicated mode through pipelines;
the first steam supply oil pump (P02) is communicated with a stripping tower (T01) through a pipeline, the stripping tower (T01) is communicated with a second stripping extraction pump (P03) through a pipeline, and the second stripping extraction pump (P03) is communicated with a first heat exchanger (E05) through a pipeline;
the stripping tower (T01) is communicated with a second heat exchanger (E08) through a pipeline, and the second heat exchanger (E08) is respectively communicated with a stripping condenser (E07) and a second steam feed pump (P01) through a pipeline.
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| CN202022623400.1U CN214260711U (en) | 2020-11-13 | 2020-11-13 | Negative pressure evaporation system for secondary steam utilization of stripping tower |
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| CN202022623400.1U CN214260711U (en) | 2020-11-13 | 2020-11-13 | Negative pressure evaporation system for secondary steam utilization of stripping tower |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114470841A (en) * | 2022-03-15 | 2022-05-13 | 郑州良弓工程有限公司 | Heat energy recovery equipment for pre-dipping workshop section |
| CN115253348A (en) * | 2022-07-11 | 2022-11-01 | 山东凯斯达机械制造有限公司 | Evaporation device and process for mixed oil of leaching system |
-
2020
- 2020-11-13 CN CN202022623400.1U patent/CN214260711U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114470841A (en) * | 2022-03-15 | 2022-05-13 | 郑州良弓工程有限公司 | Heat energy recovery equipment for pre-dipping workshop section |
| CN115253348A (en) * | 2022-07-11 | 2022-11-01 | 山东凯斯达机械制造有限公司 | Evaporation device and process for mixed oil of leaching system |
| CN115253348B (en) * | 2022-07-11 | 2023-10-20 | 山东凯斯达机械制造有限公司 | Evaporation device and technology for mixed oil of leaching system |
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