CN209612254U - Thermo-compression evaporation crystal system - Google Patents
Thermo-compression evaporation crystal system Download PDFInfo
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- CN209612254U CN209612254U CN201821888956.XU CN201821888956U CN209612254U CN 209612254 U CN209612254 U CN 209612254U CN 201821888956 U CN201821888956 U CN 201821888956U CN 209612254 U CN209612254 U CN 209612254U
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Abstract
The utility model relates to a kind of thermo-compression evaporation crystal systems, comprising: generate the heat pump of the first heat transferring medium；First heat-exchange device, the temperature for flowing through the solution of the first heat-exchange device are increased to the temperature of non-evaporation；Evaporator, the evaporator are connect with the first heat-exchange device output end；The second heat-exchange device with the second heat transferring medium, second heat-exchange device is connect with heat pump, second heat-exchange device is connect with evaporator, second heat-exchange device is also connect with the first heat-exchange device, and the first switch and the second switch form the channel for circulating the second heat transferring medium；First cooling device, one end of first cooling device is connect with the first heat-exchange device, the other end of first cooling device is connect with heat pump, and the first cooling device receives the first heat transferring medium exported from the second heat-exchange device, and will be conveyed to heat pump after the cooling of the first heat transferring medium.The utility model has the advantages that improve efficiency.
Description
Technical field
The utility model relates to a kind of evaporative crystallization technique field more particularly to a kind of thermo-compression evaporation crystal systems.
Background technique
Acid cleaning process is widely used in many industrial departments in China, and steel and iron industry, metal product industry are in production process
In need to remove metal material surface oxide layer and hydrochloric acid used to carry out pickling, it is useless that a large amount of pickling can be generated in acid cleaning process
The ingredient of liquid, hydrochloric acid pickling waste liquor is mainly: free acid, metal salt and water.Its content is with acid cleaning process, operation temperature, metal
Material, specification are different and different.According to national environmental protection regulations of rules, spent acid does not allow direct emission, and the such pickle liquor in China
Quantum of output it is surprising, steathily arrange phenomenon remain incessant after repeated prohibition.Such as the zinc-plated industry of steel: one ton of galvanized steel of production to can produce pickling useless
Liquid is aboutAccording to the statistics made by the departments concerned, only the pickle liquor amount of the annual output of Key Iron And Steel just has more than 100,000,000 tons.
CN103394206A discloses a kind of high-efficiency and energy-saving type hydrochloric acid pickling waste liquor triple effect negative-pressure graphite evaporated crystallization device,
The evaporated crystallization device due to carrying out triple effect evaporation, imitate in evaporator earlier above by the boiling point of pressure and solution in aftereffect evaporator
The low boiling point of pressure and solution, heat medium of the secondary steam of effect evaporator as aftereffect evaporator before introducing, only an effect is steamed
It sends out device and consumes raw steam, therefore improve the utilization rate of raw steam, improve economy.
However, for the processing mode of triple effect evaporation, firstly, the steam that evaporation needs is by burning coal or being produced with electric energy
It is raw, a large amount of energy is not only needed, but also steam is that unidirectional work done causes low efficiency.After steam and waste liquid carry out heat exchange, steam
Vapour need to be discharged into outside device, need to increase refrigeration equipment in this way, improve the cost of processing.And in each of triple effect evaporation
The tubule for being MVR evaporator (monomer evaporator), imitating that internal portion is arrangement being generally used is imitated, is product inside pipe, it is external
For steam, make product in membranaceous flowing since pipe inner area increases in the flow process of product from top to bottom, with increase by
Heat area forms negative pressure in effect by vacuum pump in vivo, reduces the boiling point of water in product, to reach concentration, at work with
The evaporation of moisture be easy to make salt fouling on the inner wall of tubule, in addition the internal diameter of the pipeline in MVR evaporator is small, therefore,
Blocking is easily caused after a period of use.
Utility model content
The utility model provides a kind of thermo-compression evaporation crystal system for improving efficiency.
The utility model is achieved through the following technical solutions:
Thermo-compression evaporation crystal system, comprising:
Generate the heat pump of the first heat transferring medium；
First heat-exchange device, the temperature for flowing through the solution of the first heat-exchange device are increased to the temperature of non-evaporation；
Evaporator, the evaporator are connect with the first heat-exchange device output end；
The second heat-exchange device with the second heat transferring medium, the second heat-exchange device are connect with heat pump, the second heat exchange
Device is connect with evaporator, and the second heat-exchange device is also connect with the first heat-exchange device, the first switch and the second exchange
Device forms the channel for circulating the second heat transferring medium, the second heat transferring medium and first heat transferring medium when system is run
Heat carry out heat exchange, the first heat-exchange device acquisition so that solution temperature is increased to the energy of non-evaporating temperature, enter steaming
Solution in hair tank evaporates after carrying out heat exchange with the second heat transferring medium, and the crystallization concentrate of solution remaining after evaporation is in evaporator
It is interior；
First cooling device, one end of the first cooling device are connect with the first heat-exchange device, the first cooling device it is another
One end is connect with heat pump, and the first cooling device receives the first heat transferring medium exported from the second heat-exchange device, and first is changed
Heat pump is conveyed to after thermal medium cooling.
Using above scheme, so that the temperature of solution is increased to non-evaporating temperature by the first heat-exchange device, have in this way
Conducive to being evaporated solution after entering in evaporator, also, the embodiment of the utility model is compared with prior art, and solution is not
Be evaporated in the first heat-exchange device, i.e., do not allow solution to be evaporated in the first heat-exchange device, thus can avoid because
The salt fouling left after evaporation is in the first heat-exchange device, it is therefore prevented that the first heat-exchange device of blocking.Pass through the first exchange
Device and the second switch form the channel for circulating the second heat transferring medium, also, pass through the first switch, second
Switch and the first cooling device yet form the channel for circulating the first heat transferring medium, the first heat transferring medium circulation
Acting is so that the efficiency of system is promoted, and this structure has taken into account the temperature with the second heat transferring medium before solution evaporation
It is promoted, no longer needs to add heat source to be that solution evaporates the promotion of advance trip temperature, therefore has cloth tool rationally and the first heat exchange is made to be situated between
Matter obtains the advantages of reasonable utilization.
Detailed description of the invention
Fig. 1 is the schematic diagram of the thermo-compression evaporation crystal system of the utility model.
Label in attached drawing:
B1 is the first water pump, and B2 is the second water pump, and B3 is vacuum pump；
1 is evaporator, and 2 be aerial cooler, and 3 be condenser, and 4 be cool exchanger, and 5 be heat pump, and 6 be solution pool, and 7 are
Third exchanger, 8 be the 4th exchanger, and 9 be the second exchanger, and 10 be the first exchanger, and 11 be the 5th exchanger, and 12 are
Cold tank, 13 be filter, and 14 be temperature compensator, and 15 be screw auger, and 16 be drier；
In addition, the explanation about arrows several in attached drawing:
Filled arrows indicate the flow path of the first heat transferring medium；
Hollow arrow indicates the flow path of the second heat transferring medium；
The flow path of semisolid arrow expression solution；
→ non-close arrow indicates the flow path of liquid after cooling；
Specific embodiment
The utility model is described further with reference to the accompanying drawing:
As shown in Figure 1, the thermo-compression evaporation crystal system of the utility model, comprising: heat pump 5, the first heat-exchange device, evaporation
Tank 1, the second heat-exchange device, the first cooling device, the relationship to each section and between them is described in detail below:
Heat pump 5 generates the first heat transferring medium, and the first heat transferring medium that heat pump 5 generates provides required heat when evaporating for solution
Amount, and increase the temperature of solution in solution evaporation and institute's calorific requirement is provided, the heat pump 5 preferentially uses carbon dioxide heat-pump
(i.e. refrigerant be R744 heat pump), carbon dioxide heat-pump generate the first heat transferring medium be carbon dioxide gas, by titanium dioxide
It is 130 DEG C that the temperature for the carbon dioxide gas that carbon heat pump generates, which most reaches temperature, therefore, in the present embodiment, the first heat transferring medium
Temperature is able to satisfy temperature required for solution evaporates either in flat-bottomed land still in plateau band.
The temperature for flowing through the solution of the first heat-exchange device is increased to the temperature of non-evaporation, the first heat-exchange device and offer
The solution equipment of required evaporation connects, and in the present embodiment, solution equipment includes the first water pump B1 and solution pool 6, in solution pool 6
It is inside stored with and solution to be processed is carried out by the system of the utility model, the first water pump B1 is connect with solution pool 6, the first water pump B1
Solution in solution pool 6 is transported in the first heat-exchange device, solution is handed over when flowing through the first heat-exchange device with the first heat
Changing device carries out heat exchange, and after solution and the first heat-exchange device carry out heat exchange and export, the temperature prioritised of solution rises to 55
℃。
The frame mode that first heat-exchange device preferentially uses are as follows: including the first exchanger 10 and the second exchanger 9, first
Exchanger 10 is connect with the second heat-exchange device and the first cooling device respectively, the second exchanger 9 respectively with the first exchanger 10,
Second heat-exchange device and evaporator 1 connect.First exchanger 10 and the second exchanger 9 preferentially use plate heat exchanger, the
One exchanger 10 and the second exchanger 9 can also use pipe heat exchanger.
First exchanger 10 is connect with the first water pump B1, and the solution in solution pool 6 is transported to first by the first water pump B1
In exchanger 10, solution and the first exchanger 10 carry out first time heat exchange, and the temperature of the solution by first time heat exchange is excellent
45 DEG C are first risen to, the solution exported from the first exchanger 10 enters in the second exchanger 9 and carries out second of heat exchange, by the
The temperature prioritised of the solution of heat exchange rises to 55 DEG C, and the solution exported from the second exchanger 9, which enters in evaporator 1, to carry out
Evaporative crystallization.
Evaporator 1 is connect with the first heat-exchange device output end；Evaporator 1 is exchanged with second in the first heat-exchange device
The output end of device 9 connects, the frame mode that evaporator 1 preferentially uses are as follows: including tank body and be set to the intracorporal heat exchanger of tank
(not shown), heat exchanger preferentially use plate heat exchanger.
Second exchanger, 9 output end connecting pipe, pipeline are passed into tank body, and pipeline is located at the intracorporal end of tank and is equipped with spray
Head, therefore, solution are sprayed onto the surface of the intracorporal heat exchanger of tank in the form sprayed, and (reach since the temperature on heat exchanger is higher
90 to 100 DEG C), it is sprayed onto the moisture evaporation of the solution on heat exchanger surface, remaining concentrate then stays in tank body.Pass through
Scrape mechanism (such as the scraper driven by driver) and the concentrate on heat exchanger surface scraped into tank base, and by with steaming
Concentrate is sent into drier 16 by the screw auger 15 that hair tank 1 connects to be dried, and concentrate is packed after drying.
Drier 16 preferentially uses blade dryer.
There is the second heat transferring medium, the second heat transferring medium preferentially uses liquid, and the liquid is preferential in second heat-exchange device
Using water.Second heat-exchange device is connect with heat pump 5, and the second heat-exchange device is connect with evaporator 1, and the second heat-exchange device is also
It is connect with the first heat-exchange device, the first switch and the second switch form circulate the second heat transferring medium logical
Road, the heat of the second heat transferring medium and first heat transferring medium carries out heat exchange when system is run, and the first heat-exchange device obtains
Solution temperature must be made to be increased to the energy of non-evaporating temperature, the solution and the second heat transferring medium entered in evaporator 1 carries out heat
It is evaporated after exchange, the concentrate of solution remaining after evaporation remains in evaporator 1.
The frame mode of second heat-exchange device preferentially used are as follows: including third exchanger 7 and the 4th exchanger 8,
Three exchangers 7 and the 4th exchanger 8 preferentially use plate heat exchanger, and third exchanger 7 and the 4th exchanger 8 can also be using pipes
Formula heat exchanger.Third exchanger 7 is connect with heat pump 5, the 4th exchanger 8 and evaporator 1 respectively, and the 4th exchanger 8 is also with
The connection of one heat-exchange device, i.e. the 4th exchanger 8 distinguish the first exchanger 10 and the connection of the second exchanger 9, third exchanger 7
Second heat transferring medium is input in the heat exchanger in evaporator 1, the second heat exchange medium temperature after heat exchange passes through after reducing
Conveyance conduit is delivered in the second exchanger 9, at this point, the second heat transferring medium and entering in the second exchanger 9 solution and carrying out the
Secondary heat exchange, the temperature prioritised of solution rise to 55 DEG C.Since four exchangers 8 are connect with the first exchanger 10, heat pump 5
After first heat transferring medium of output passes sequentially through third exchanger 7, the 4th exchanger 8, the first heat transferring medium enters first
In exchanger 10, heat exchange is carried out with the solution entered in the first exchanger 10, so that the temperature of the solution of first time heat exchange
Degree is preferentially promoted to 45 DEG C.
In the present embodiment, the heat of the second heat transferring medium and first heat transferring medium carries out the process of heat exchange are as follows: from
Heat pump 5 preferentially exports such as 120 DEG C of the first heat transferring medium, after 120 DEG C of the first heat transferring medium enters third exchanger 7
After carrying out heat exchange with the second heat transferring medium, the temperature prioritised of the first heat transferring medium exported from third exchanger 7 is reduced to 110
DEG C, 110 DEG C of the first heat transferring medium enters after the 4th exchanger 8 with after the progress heat exchange of the second heat transferring medium, hands over from the 4th
The temperature prioritised of the first heat transferring medium that parallel operation 8 exports is reduced to 80 DEG C.The second heat transferring medium exported out of second exchanger 9
It successively exchanges heat with the 4th exchanger 8 and third exchanger 7, since the first heat transferring medium that heat pump 5 exports flows successively through the
Three exchangers 7, the 4th exchanger 8, the second heat transferring medium exported out of second exchanger 9 pass through temperature after the 4th exchanger 8
Preferentially rise to 80 DEG C, the second heat transferring medium exported out of the 4th exchanger 8 pass through third exchanger 7 after it is temperature prioritised on
Rise to 90 DEG C.
One end of first cooling device is connect with the first heat-exchange device, and the other end and heat pump 5 of the first cooling device connect
It connects, the first cooling device receives the first heat transferring medium exported from the first heat-exchange device, and will be after the cooling of the first heat transferring medium
It is conveyed to heat pump 5.Preferably, one end of the first cooling device is connect with the first exchanger 10.
First cooling device include the 5th exchanger 11, in cold tank 12, the 5th exchanger 11 and the first heat-exchange device company
Connect, in cold tank 12 connect with the 5th exchanger 11.5th exchanger 11 preferentially uses plate heat exchanger, and the 5th exchanger 11 may be used also
To use pipe heat exchanger.After the first heat transferring medium that heat pump 5 exports passes sequentially through third exchanger 7, the 4th exchanger 8,
The first exchanger 10 is entered into heat exchange, the 5th exchanger 11 preferentially with the first exchanger 10 in the first heat-exchange device
Connection, therefore, the first heat transferring medium is output in the 5th exchanger 11 from the first exchanger 10, then is exported by the 5th exchanger 11
In in cold tank 12, the first heat transferring medium carries out heat exchange in cold tank 12 in, to make the temperature of the first heat transferring medium into one
Step reduces.
The structure that the utility model is not limited to the above embodiments, further includes:
(a) further include temperature compensator 14, the temperature compensator 14 be set to the second heat-exchange device and evaporator 1 it
Between, temperature compensator 14 preferentially uses vapor (steam) temperature compensator, for the solution having, it may be necessary to higher evaporation temperature
Degree, and the evaporating temperature that the second heat transferring medium can not be made to reach this solution by the first heat transferring medium that heat pump 5 generates, because
This, improves the temperature of the second heat transferring medium exported from third exchanger 7 further by temperature compensator 14.
(b) further, further include the second cooling device connecting with evaporator 1 and connect with the second cooling device
Negative pressure device, the vapor that the second cooling device generates when evaporating solution are converted into liquid (condensed water), negative pressure device storage
The liquid formed after second cooling device is cooling, negative pressure device preferentially use vacuum negative pressure device, by the second cooling device and bear
Pressure device makes solution low-temperature evaporation (being applicable in the utility model also can in highlands), when reducing energy consumption and solution evaporation
The temperature needed, improves evaporation rate and evaporation capacity.
Second cooling device includes aerial cooler 2, condenser 3, and aerial cooler 2 preferentially uses blower, air
One end of cooler 2 is connect with evaporator 1, and aerial cooler 2 makes the carry out Gravity Separation of the water vapour exported from evaporator 1,
The other end of aerial cooler 2 is connect with negative pressure device, and a part is passed through negative by the water vapour that aerial cooler 2 reduces temperature
The effect of pressure device enters in negative pressure device.
Condenser 3 is connect with aerial cooler 2, the first cooling device, negative pressure device respectively.Condenser 3 and the first cooling
The output end connection of cold tank 12 in device, condenser 3 is to the temperature for the first heat transferring medium that therefrom cold tank 12 exports again into one
Step ground reduces.Another part is entered in condenser 3 by the water vapour that aerial cooler 2 reduces temperature, passes through condenser 3
Effect enters back into low-temperature condenser 3 by the processed gas-liquid Gravity Separation of aerial cooler 2 and carries out depth cooling, after cooling
Temperature prioritised to be reduced to 25 DEG C of degree, so that water vapour is converted into liquid, these liquid enter under the action of negative pressure device
In negative pressure device.
Negative pressure device includes filter 13 and vacuum pump B3, and vacuum pump B3 is connect with filter 13, and filter 13 is distinguished
It is connect with aerial cooler 2 and condenser 3, to receive water vapour and liquid, vacuum pump B3 generates negative pressure, makes aerial cooler
2 a part of water vapours after cooling are transported in filter 13, are transported to the liquid in filter 13 with condenser 3 and are carried out hot friendship
It changes, water vapour is made to be converted into liquid.
It (c) further, further include cold switch, cold switch is equipped with first input end and the second input terminal, cold
Switch is additionally provided with the first output end and second output terminal, and the first input end is connect with negative pressure device, and described second is defeated
Enter end to connect with the first cooling device, first output end is connect with heat pump 5.Cold switch include cool exchanger 4 and
The second water pump B2 connecting with the cooler 4, the first input end and the second input terminal are set on cool exchanger, and first is defeated
Outlet and second output terminal are set on cool exchanger.First input end on cool exchanger 4 is connect with the vacuum pump B3, cold
The second input terminal on exchanger 4 output end of cold tank 12 in is connect, and the first output end on cool exchanger 4 and heat pump 5 connect
It connects, second output terminal is connect with the second water pump B2 on cool exchanger 4.
In a part of the first heat transferring medium for exporting of cold tank 12 enter in cool exchanger 4, vacuum pump B3 is by filter
Liquid in 13 is transported in cool exchanger 4, and the first heat transferring medium and liquid carry out heat exchange, and the first heat exchange after heat exchange is situated between
Matter is transported to heat pump 5 by first output end, the first heat transferring medium (carbon dioxide gas) benefit after vacuum pump B3 will be condensed
Vacuum early period is established with condensate water circulatory injecting type, when 4 water temperature of cool exchanger is higher than setting value, heat pump 5 is given cold source cool-down and mentioned
High-vacuum pump B3 efficiency, when 4 liquid level of cool exchanger reaches setting water level, the second water pump B2 is defeated by the second water pump B2 by condensed water
Out in the 5th exchanger 11, exported after carrying out heat exchange with the first heat transferring medium for flowing through the 5th exchanger 11 again, with into
Row secondary use.
In the above-described embodiments, so that the temperature of solution is increased to non-evaporating temperature by the first heat-exchange device, have in this way
Conducive to being evaporated solution after entering in evaporator 1, also, the embodiment of the utility model is compared with prior art, solution
It is not evaporated in the first heat-exchange device, i.e., solution is not allowed to be evaporated in the first exchanger 10 and the second exchanger 9,
To can avoid preventing the first heat-exchange device of blocking because the salt fouling left after evaporation is in the first heat-exchange device.It is logical
It crosses the first switch and the second switch forms the channel for circulating the second heat transferring medium, also, handed over by first
Changing device and the second switch yet form the portion of channel for circulating the first heat transferring medium, and this structure design is simultaneous
Before having cared for solution evaporation and the second heat transferring medium temperature is promoted, and no longer needs to add heat source to be that solution evaporation advance trip temperature mentions
It rises, therefore, the system of the utility model has the advantages that cloth tool rationally and the first heat transferring medium is made to obtain reasonable utilization.Separately
Outside, by the effect of the second cooling device, negative pressure device and cold switch, the water vapour after making evaporation is converted to cooling
Water, by the effect of various heat exchanges, so that the system of the utility model has the function of refrigeration, therefore, the utility model
Heat pump is formd with the first heat-exchange device, the second heat-exchange device, the first cooling device, the first cooling device, negative pressure device
Cooling and warming two-direction heat-exchanging single cycle not only provided and has evaporated the heat that water needs in treatment liquid, but also provided steam condensation institute
The cold source needed, and reduce the energy consumption of heat pump and the temperature that needs when solution evaporates, improve evaporation rate and evaporation capacity.
Using the model of Germany's production are as follows: the heat pump of 380-420V Y/YY-3-50Hz PW carries out simulation test, has simulated
Afterwards, following data are shown on computers:
130 degree of 5 delivery temperature highest of heat pump, the maximum heating capacity 313KW of heat pump 5,25 degree of evaporating temperature, heat pump 5 is maximum to be steamed
Refrigerating capacity 260KW is sent out, power 53.1KW is consumed, consumes electric current (400V) 90.5A, refrigerant R744, exchanger pressure is greater than
70bar。
It is above-mentioned statistics indicate that, the every consumption power 53.1KW of separate unit heat pump 5, the heating capacity converted is 313KW, the system of conversion
Cooling capacity 260KW, heating capacity are 5.89 times for consuming power, and refrigerating capacity is 4.89 times for consuming power.In the prior art using more
The processing mode of evaporation is imitated, for heats power compared with consuming power, heats power is twice of power or so of consumption, also, existing
Heat transferring medium used in multiple-effect evaporation in technology (steam) not can be carried out refrigeration.
Claims (10)
1. thermo-compression evaporation crystal system characterized by comprising
Generate the heat pump of the first heat transferring medium；
First heat-exchange device, the temperature for flowing through the solution of the first heat-exchange device are increased to the temperature of non-evaporation；
Evaporator, the evaporator are connect with the first heat-exchange device output end；
The second heat-exchange device with the second heat transferring medium, the second heat-exchange device are connect with heat pump, the second heat-exchange device
It is connect with evaporator, the second heat-exchange device is also connect with the first heat-exchange device, the first switch and the second switch
The channel for circulating the second heat transferring medium is formed, the heat of the second heat transferring medium and first heat transferring medium when system is run
Amount carries out heat exchange, and the acquisition of the first heat-exchange device makes solution temperature be increased to the energy of non-evaporating temperature, enters evaporator
Interior solution evaporates after carrying out heat exchange with the second heat transferring medium, and the concentrate of solution remaining after evaporation remains in evaporator；
First cooling device, one end of the first cooling device are connect with the first heat-exchange device, the other end of the first cooling device
It is connect with heat pump, the first cooling device receives the first heat transferring medium exported from the first heat-exchange device, and the first heat exchange is situated between
Heat pump is conveyed to after matter cooling.
2. thermo-compression evaporation crystal system according to claim 1, which is characterized in that further include:
With tank connected second cooling device of evaporation, the vapor that the second cooling device generates when evaporating solution is converted into liquid
Body；
The negative pressure device connecting with the second cooling device, negative pressure device store the liquid formed after the cooling of the second cooling device.
3. thermo-compression evaporation crystal system according to claim 2, which is characterized in that second cooling device includes:
Aerial cooler, the aerial cooler are connect with evaporator, and aerial cooler is also connect with negative pressure device；
Condenser, condenser are connect with aerial cooler, the first cooling device, negative pressure device respectively.
4. thermo-compression evaporation crystal system according to claim 2, which is characterized in that further include:
Cold switch, cold switch are equipped with first input end and the second input terminal, and cold switch is additionally provided with the first output
End and second output terminal, the first input end are connect with negative pressure device, and second input terminal is connect with the first cooling device,
First output end is connect with heat pump.
5. thermo-compression evaporation crystal system according to claim 4, which is characterized in that cold switch includes:
Cool exchanger and the second water pump connecting with the cooler, the first input end and the second input terminal are set to cold friendship
On parallel operation, the first output end and second output terminal are set on cool exchanger.
6. thermo-compression evaporation crystal system according to claim 1, which is characterized in that it further include temperature compensator, the temperature
Compensator is set between the second heat-exchange device and evaporator.
7. thermo-compression evaporation crystal system according to one of claims 1 to 6, which is characterized in that the heat pump is titanium dioxide
Carbon heat pump.
8. thermo-compression evaporation crystal system according to one of claims 1 to 6, which is characterized in that the first heat exchange dress
It sets including the first exchanger and the second exchanger, the first exchanger connects with the second heat-exchange device and the first cooling device respectively
It connects；Second exchanger is connect with the first exchanger, the second heat-exchange device and evaporator respectively.
9. thermo-compression evaporation crystal system according to one of claims 1 to 6, which is characterized in that the second heat-exchange device packet
Third exchanger and the 4th exchanger are included, third exchanger is connect with heat pump, the 4th exchanger and evaporator respectively, and the 4th hands over
Parallel operation is also connect with the first heat-exchange device.
10. thermo-compression evaporation crystal system according to one of claims 1 to 6, which is characterized in that the first cooling device packet
It includes:
5th exchanger, the 5th exchanger are connect with the first heat-exchange device；
In cold tank, cold tank is connect with the 5th exchanger in this.
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| CN201821888956.XU CN209612254U (en) | 2018-11-16 | 2018-11-16 | Thermo-compression evaporation crystal system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109289238A (en) * | 2018-11-16 | 2019-02-01 | 江苏博莱客冷冻科技发展有限公司 | Thermo-compression evaporation crystal system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109289238A (en) * | 2018-11-16 | 2019-02-01 | 江苏博莱客冷冻科技发展有限公司 | Thermo-compression evaporation crystal system |
| CN109289238B (en) * | 2018-11-16 | 2024-07-09 | 江苏博莱客冷冻科技发展有限公司 | Heat pump evaporation crystallization system |
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