CN216005762U

CN216005762U - Tar dewatering system

Info

Publication number: CN216005762U
Application number: CN202122238174.XU
Authority: CN
Inventors: 刘永家
Original assignee: Shandong Wanhe Environmental Protection And Energy Saving Technology Co ltd
Current assignee: Shandong Wanhe Environmental Protection And Energy Saving Technology Co ltd
Priority date: 2021-09-15
Filing date: 2021-09-15
Publication date: 2022-03-11
Anticipated expiration: 2031-09-15

Abstract

The utility model discloses a tar dehydration system, wherein the tar dehydration system comprises a heating tank, a transition chamber, a heat exchanger, a separation chamber and a condensed water tank, the feed inlet of the heating tank is used for feeding water-containing tar, the feeding port of the heating tank is used for adding an entrainer, the discharge hole of the heating tank is used for discharging finished tar, the mixed steam discharge port of the heating tank is communicated with the first air inlet of the transition chamber, the first air outlet of the transition chamber is communicated with the second air inlet of the heat exchanger, the second liquid return port of the heat exchanger is communicated with the first liquid return port of the transition chamber, the first liquid outlet of the transition chamber is communicated with the liquid inlet of the separation chamber, the agent outlet of the separation chamber is communicated with the agent returning port of the heating tank, and the water outlet of the separation chamber is communicated with the water inlet of the condensed water tank. The technical proposal of the utility model can improve the dehydration efficiency of the water-containing tar.

Description

Tar dewatering system

Technical Field

The utility model relates to a water treatment technical field, in particular to tar dewatering system.

Background

Black or black brown viscous liquid with pungent odor, which is generated during coal dry distillation, is called tar for short. The tar is generally used as a raw material for processing and refining to prepare various chemical products, can also be directly utilized, such as a material component of a binder for industrial briquette, formed coke and coal-based activated carbon, can also be used as a fuel oil, a blast furnace injection fuel, a raw material of wood preservative oil and carbon black burning, and has a wide application range.

The semi-finished product tar of the coking plant contains a large amount of water, the moisture content is usually between 4% and 30%, and the water can be sold after being reduced to below 4%. In the prior art, a demulsifier is added into a semi-finished product tar storage tank, the semi-finished product tar storage tank is heated and kept stand for about 10 days, and tar and water are separated due to different densities.

However, this method is not effective, and tar is often not dehydrated at a planned time, resulting in low tar dehydration efficiency.

SUMMERY OF THE UTILITY MODEL

The utility model mainly aims to provide a tar dewatering system, which aims to improve the dewatering efficiency of water-containing tar.

In order to achieve the purpose, the tar dehydration system provided by the utility model comprises a heating tank, a transition chamber, a heat exchanger, a separation chamber and a condensed water tank, the feed inlet of the heating tank is used for feeding water-containing tar, the feeding port of the heating tank is used for adding an entrainer, the discharge hole of the heating tank is used for discharging finished tar, the mixed steam discharge port of the heating tank is communicated with the first air inlet of the transition chamber, the first air outlet of the transition chamber is communicated with the second air inlet of the heat exchanger, the second liquid return port of the heat exchanger is communicated with the first liquid return port of the transition chamber, the first liquid outlet of the transition chamber is communicated with the liquid inlet of the separation chamber, the agent outlet of the separation chamber is communicated with the agent returning port of the heating tank, and the water outlet of the separation chamber is communicated with the water inlet of the condensed water tank.

Optionally, the heat exchanger comprises a first heat exchanger and a second heat exchanger, the first heat exchanger being arranged in series with the second heat exchanger.

Optionally, the first heat exchanger is provided with the second air inlet, the second air inlet is communicated with the first air outlet, the first heat exchanger is provided with a first water inlet hole and a first water outlet hole, and circulating cooling water in the cooling tower enters the first heat exchanger through the first water inlet hole and flows back to the cooling tower through the first water outlet hole.

Optionally, a third air inlet of the second heat exchanger is communicated with a second air outlet of the first heat exchanger, the second heat exchanger is provided with a second water inlet hole and a second water outlet hole, condensed water in the refrigerator enters the second heat exchanger through the second water inlet hole and flows back to the refrigerator through the second water outlet hole, the second heat exchanger is provided with the second liquid return port, and the second liquid return port is communicated with the first liquid return port.

Optionally, the cooling tower is in communication with the chiller, and circulating cooling water in the cooling tower provides heat for the chiller.

Optionally, the tar dewatering system further comprises an adsorption device, the adsorption device is communicated with the heat exchanger and used for adsorbing tail gas escaping from the heat exchanger, and the adsorption device is communicated with the waste gas collecting system.

Optionally, the heating tank is heated using a steam coil.

Optionally, a temperature sensor, a pressure sensor and a liquid level sensor are arranged in the heating tank.

Optionally, a heating tank circulating pump is arranged outside the heating tank to pump the mixed liquid at the bottom of the heating tank to a spraying device in the heating tank.

The utility model discloses a technical scheme adopts including the heating tank, excessive room, heat exchanger, the tar dewatering system of disengagement chamber and condensation water pitcher dewaters the processing to aqueous tar, drop into the heating tank with aqueous tar and entrainer and heat so that the water azeotropic distillation in entrainer and the aqueous tar, form mixed steam and elementary tar, mixed steam discharges from the top of heating tank and gets into excessive room in proper order, heat exchanger and disengagement chamber, accomplish mixed steam's condensation separation, make mixed steam become liquid, wherein liquid entrainer flows back to the heating tank and continues to participate in azeotropic distillation reaction, wherein liquid condensate water gets into in the condensation tank. In this manner, a single azeotropic distillation of the aqueous tar was completed to obtain a primary tar from which a part of water was removed. The primary tar and the entrainer are subjected to azeotropic distillation, and the circulation is carried out so that the water content in the water-containing tar is gradually reduced, and the finished tar is obtained. Compared with a dehydration method of adding a demulsifier into the water-containing tar and heating and standing, the scheme has the advantages that on one hand, the dehydration treatment speed of the water-containing tar is accelerated, the dehydration treatment efficiency of the water-containing tar is improved, and a storage tank required by heating and standing of the water-containing tar is not required to be emptied after the water-containing tar is dehydrated, so that the production efficiency of the water-containing tar is improved; on the other hand, through one-time azeotropic distillation circulation, the water-containing tar can be dehydrated within the planned time, the dehydration time can not be prolonged due to poor static effect, and further the possible reduction of tar quality due to the lengthening of dehydration time is avoided; on the other hand, the scheme does not need to add a large amount of demulsifier, and reduces the dehydration treatment cost of the water-containing tar.

Drawings

In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings needed to be used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the structures shown in the drawings without creative efforts.

FIG. 1 is a schematic structural view of an embodiment of the tar dewatering system of the present invention;

FIG. 2 is a schematic diagram of a circulation path of an embodiment of the tar dewatering system of FIG. 1.

The reference numbers illustrate:

the objects, features and advantages of the present invention will be further described with reference to the accompanying drawings.

Detailed Description

The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative efforts belong to the protection scope of the present invention.

It should be noted that all the directional indicators (such as upper, lower, left, right, front and rear … …) in the embodiment of the present invention are only used to explain the relative position relationship between the components, the motion situation, etc. in a specific posture (as shown in the drawings), and if the specific posture is changed, the directional indicator is changed accordingly.

In addition, the descriptions related to "first", "second", etc. in the present invention are for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicit ly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature. In addition, "and/or" in the whole text includes three schemes, taking a and/or B as an example, including a technical scheme, and a technical scheme that a and B meet simultaneously; in addition, the technical solutions in the embodiments may be combined with each other, but it must be based on the realization of those skilled in the art, and when the technical solutions are contradictory or cannot be realized, the combination of the technical solutions should not be considered to exist, and is not within the protection scope of the present invention.

On the one hand, the method has unstable effect, and the condition that semi-finished product tar cannot be dehydrated according to the planned time often occurs, so that the quality of the tar is reduced; on the other hand, the method needs longer dehydration time, if the semi-finished product tar can not be dehydrated according to the planned time, a storage tank can not be provided for the subsequent newly produced semi-finished product tar, and further the production efficiency of the semi-finished product tar is influenced; on the other hand, the method needs to add a large amount of demulsifier, and has higher dehydration cost. In view of this, the utility model provides a tar dewatering system.

Referring to fig. 1 and 2, in an embodiment of the present invention, the tar dehydration system includes a heating tank 100, a transition chamber 200, a heat exchanger 300, a separation chamber 400, and a condensed water tank 500. The heating tank 100 is provided with a feed inlet 110, a feed inlet 120, a discharge outlet 130, a mixed vapor discharge port 140, and a return agent port 150, the transition chamber 200 is provided with a first air inlet 210, a first air outlet 220, a first return liquid port 230, and a first liquid outlet 240, the heat exchanger 300 is provided with a second air inlet (not shown) and a second return liquid port (not shown), the separation chamber 400 is provided with a liquid inlet 410, a return agent port 420, and a water outlet 430, and the condensate tank 500 is provided with a water inlet 510.

The feeding port 110 of the heating tank 100 is used for feeding water-containing tar, the feeding port 120 of the heating tank 100 is used for adding an entrainer, the discharging port 130 of the heating tank 100 is used for discharging finished tar, the mixed steam discharging port 140 of the heating tank 100 is communicated with the first air inlet 210 of the transition chamber 200, the first air outlet 220 of the transition chamber 200 is communicated with the second air inlet of the heat exchanger 300, the second liquid return port of the heat exchanger 300 is communicated with the first liquid return port 230 of the transition chamber 200, the first liquid outlet 240 of the transition chamber 200 is communicated with the liquid inlet 410 of the separation chamber 400, the liquid outlet 420 of the separation chamber 400 is communicated with the agent return port 150 of the heating tank 100, and the water outlet 430 of the separation chamber 400 is communicated with the water inlet 510 of the condensate water tank 500.

When the tar dehydration system is used for dehydrating the water-containing tar, the water-containing tar is firstly conveyed into the heating tank 100 through the feed inlet 110 of the heating tank 100, the entrainer is put into the heating tank 100 through the input port 120 of the heating tank 100, then the heating tank 100 is heated, the entrainer and water in the water-containing tar are evaporated together to form mixed steam, the mixed steam is discharged from the mixed steam discharge port 140 of the heating tank 100, enters the transition chamber 200 through the first air inlet 210 of the transition chamber 200, enters the heat exchanger 300 through the first air outlet 220 of the transition chamber 200 and the second air inlet of the heat exchanger 300, the mixed steam is changed into liquid after condensation heat exchange in the heat exchanger 300, and the liquid enters the transition chamber 200 through the second liquid return port of the heat exchanger 300 and the first liquid return port 230 of the transition chamber 200 and passes through the first liquid outlet 240 of the transition chamber 200, The liquid inlet 410 of the separation chamber 400 enters the separation chamber 400, the liquid in the separation chamber 400 is separated, the separated liquid entrainer flows back into the heating tank 100 through the agent outlet 420 of the separation chamber 400 and the agent return port 150 of the heating tank 100, and the separated liquid condensate enters the condensing tank through the water outlet 430 of the separation chamber 400 and the water inlet 510 of the condensing tank. In this way, a single azeotropic distillation of the hydrous tar is completed, and a part of water in the hydrous tar is primarily removed to obtain the primary tar left at the bottom of the heating tank 100. The liquid entrainer refluxed into the heating tank 100 is subjected to azeotropic distillation again in the heating tank 100 together with the primary tar, and the circulation is performed to reduce the water content in the primary tar, so as to obtain the finished tar.

Of course, depending on the circulation of the azeotropic distillation of the aqueous tar, when the amount of the azeotropic agent is insufficient, the azeotropic agent may be supplied to the heating tank 100 through the inlet 120 of the heating tank 100 to ensure the azeotropic distillation effect of the water in the tar and the azeotropic agent, and the water content in the aqueous tar may be gradually reduced by the azeotropic distillation in one step until the water content reaches the standard water content. It should be noted that the standard moisture content may be defined according to different target products, such as 4% standard moisture content, 1% standard moisture content, etc., and the moisture content of the finished tar is not limited herein.

Specifically, the entrainer can be azeotropically distilled with water in the aqueous tar to form a gas mixture and primary tar, and the entrainer can be crude benzene, toluene or cyclohexane, and the like, and the kind of the entrainer is not limited.

In one embodiment, a liquid level sensor is provided in the condensate tank 500 to measure the water level in the condensate tank 500 in real time to discharge the condensate in the condensate tank 500 in time. A water pump is provided in the condensed water discharge line of the condensed water tank 500 to more conveniently discharge the condensed water in the condensed water tank 500. The condensed water in the condensed water tank 500 may be directly discharged or discharged after being treated to meet a discharge standard, or may be introduced into the condensation separation process of the mixed vapor to provide cooling water for the condensation separation process.

The utility model discloses a technical scheme adopts including heating tank 100, excessive room 200, heat exchanger 300, the tar dewatering system of separation chamber 400 and condensation water pitcher 500 carries out dehydration to moisture tar, drop into heating tank 100 with moisture tar and entrainer and heat so that the water azeotropic distillation in entrainer and the moisture tar, form mixed vapor and elementary tar, mixed vapor discharges from the top of heating tank 100 and gets into excessive room 200 in proper order, heat exchanger 300 and separation chamber 400, accomplish the condensation separation of mixed vapor, make mixed vapor become liquid, wherein liquid entrainer flows back heating tank 100 and continues to participate in azeotropic distillation reaction, wherein liquid condensate water gets into in the condensation jar. In this manner, a single azeotropic distillation of the aqueous tar was completed to obtain a primary tar from which a part of water was removed. The primary tar and the entrainer are subjected to azeotropic distillation again, and the circulation is carried out in such a way that the water content in the primary tar is gradually reduced, so that the finished product tar is obtained. Compared with a dehydration method of adding a demulsifier into the water-containing tar and heating and standing, the scheme has the advantages that on one hand, the dehydration treatment speed of the water-containing tar is accelerated, the dehydration treatment efficiency of the water-containing tar is improved, and a storage tank required by heating and standing of the water-containing tar is not required to be emptied after the water-containing tar is dehydrated, so that the production efficiency of the water-containing tar is improved; on the other hand, through one-time azeotropic distillation circulation, the water-containing tar can be dehydrated within the planned time, the condition that the dehydration time needs to be prolonged due to poor static effect can not occur, and further the possible reduction of tar quality due to the lengthening of the dehydration time can be avoided; on the other hand, the scheme does not need to add a large amount of demulsifier, and reduces the dehydration treatment cost of the water-containing tar.

Further, in order to improve the condensation separation effect of the mixed vapor in the tar dehydration process, the heat exchanger 300 includes a first heat exchanger 310 and a second heat exchanger 320, and the first heat exchanger 310 is arranged in series with the second heat exchanger 320. The heat exchanger 300 may be a dividing wall type, a hybrid type, a regenerative type, etc., and in one embodiment, the first heat exchanger 310 and the second heat exchanger 320 are both tube type heat exchangers 300, and the type of the heat exchangers 300 is not limited herein. Therefore, the condensation separation effect of the mixed steam is improved through two-stage low-temperature condensation heat exchange.

Specifically, the first heat exchanger 310 is provided with a second air inlet, the second air inlet is communicated with the first air outlet 220, the first heat exchanger 310 is provided with a first water inlet 311 and a first water outlet 312, and circulating cooling water in the cooling tower 600 enters the first heat exchanger 310 through the first water inlet 311 and flows back to the cooling tower 600 through the first water outlet 312. In the first heat exchanger 310, the circulating cooling water in the cooling tower 600 enters from the first water inlet hole 311 and is discharged from the first water outlet hole 312 to exchange heat with the mixed vapor in the first heat exchanger 310, and the condensation and separation of the mixed vapor are completed. The mixed vapor enters the first heat exchanger 310 from the first air outlet 220 of the transition chamber 200 and the second air inlet of the first heat exchanger 310, and enters the second heat exchanger 320 through the second air outlet (not shown) of the first heat exchanger 310 after heat exchange with the circulating cooling water in the first heat exchanger 310 is completed. The first condensation separation of the mixed vapor is completed, and in order to ensure good condensation separation effect, the temperature of the circulating cooling water in the first heat exchanger 310 is not higher than 35 ℃.

A third air inlet (not shown) of the second heat exchanger 320 is communicated with the second air outlet of the first heat exchanger 310, the second heat exchanger 320 is provided with a second water inlet 321 and a second water outlet 322, condensed water in the refrigerator 700 enters the second heat exchanger 320 through the second water inlet 321 and returns to the refrigerator 700 through the second water outlet 322, and the second heat exchanger 320 is provided with a second liquid return port (not shown) communicated with the first liquid return port 230. In the second heat exchanger 320, the condensed water in the refrigerator 700 enters from the second water inlet hole 321 and is discharged from the second water outlet hole 322 to exchange heat with the mixed vapor in the second heat exchanger 320, thereby completing condensation and separation of the mixed vapor. The mixed vapor enters the second heat exchanger 320 from the second outlet of the first heat exchanger 310 and the third inlet of the second heat exchanger 320, and after heat exchange with the condensed water in the second heat exchanger 320 is completed, the mixed vapor becomes liquid, and enters the transition chamber 200 through the second liquid return port of the second heat exchanger 320 and the first liquid return port 230 of the transition chamber 200. The second condensation separation of the mixed vapor is thus completed, and in order to ensure a good condensation separation effect, the temperature of the condensed water in the second heat exchanger 320 is not higher than 25 ℃.

Thus, the mixed steam discharged from the upper part of the heating tank 100 is condensed by the two-stage heat exchanger 300, the temperature of the circulating cooling water in the first heat exchanger 310 is not higher than 35C degrees, the temperature of the condensed water in the second heat exchanger 320 is not higher than 25C degrees, the mixed steam is fully condensed, the condensation effect of the mixed steam is ensured, and the dehydration effect of tar is further ensured. Meanwhile, the escape of the mixed steam caused by insufficient condensation is avoided, and further the pollution of the mixed steam to the atmosphere is avoided.

Further, the refrigerator 700 circulates the condensed water in the second heat exchanger 320 to perform condensation separation in the second heat exchanger 320, and to solve the problem of heat dissipation in operation of the refrigerator 700, the cooling tower 600 communicates with the refrigerator 700, and the circulating cooling water in the cooling tower 600 dissipates heat in the refrigerator 700. A circulation path for circulating cooling water is formed between the cooling tower 600 and the refrigerator 700, and the circulating cooling water flows through the refrigerator 700 to radiate heat from the refrigerator 700, thereby ensuring a normal operating temperature of the refrigerator 700. A circulation pump is provided in a circulation cooling water flow path of the cooling tower 600, and the circulation pump may deliver circulation cooling water to the first heat exchanger 310 and the refrigerator 700.

Further, in order to prevent the mixed vapor from escaping in the condensation process to pollute the atmosphere, the tar dehydration system further comprises an adsorption device 800, the adsorption device 800 is communicated with the heat exchanger 300 and used for adsorbing the tail gas escaping from the heat exchanger 300, and the adsorption device 800 is communicated with the waste gas collection system 900. Specifically, the mixed vapor contains entrainer vapor, and commonly used entrainers such as crude benzene, toluene, cyclohexane and the like are toxic or harmful gases, and if the entrainer escapes without treatment, the entrainer vapor affects human bodies and atmospheric environment. In this embodiment, the adsorption device 800 is in communication with the second heat exchanger 320 and is configured to adsorb the tail gas escaping from the second heat exchanger 320, and activated carbon may be disposed in the adsorption device 800 to perform an adsorption treatment on the escaping tail gas. Meanwhile, the adsorption apparatus 800 is communicated with a waste gas collection system 900 of the plant. The escaped tail gas is firstly adsorbed and treated by the adsorption device 800, then the adsorbed and treated tail gas is conveyed to the waste gas collecting system 900 of the factory by the adsorption device 800, and is uniformly treated by the waste gas treatment system of the factory, and is discharged to the atmosphere after reaching the discharge standard, thereby avoiding the influence of toxic and harmful gases on human bodies and the atmosphere.

Further, to improve the efficiency and effectiveness of the azeotropic distillation, the heating tank 100 is heated using a steam coil 10. In this manner, the heating tank 100 can be heated by steam from the plant to provide a heating source for azeotropic distillation of the aqueous tar and the entrainer. Generally, the temperature of the produced water-containing tar is 50-60 ℃, the entrainer is crude benzene as an example, the boiling point of the crude benzene is 60-70 ℃, so that the azeotropic temperature difference of the water-containing tar and the azeotropic distillation is not large, and the azeotropic temperature can be reached by heating the water-containing tar and the entrainer by using a small amount of steam in a plant area. On one hand, the amount of steam required by heating is less, and the heating cost is lower, so that the tar dehydration treatment cost is reduced; on the other hand, the azeotropic temperature is low, the high-temperature treatment of the water-containing tar and the entrainer is not needed, and the quality of the tar is not influenced by the high temperature.

Meanwhile, a temperature sensor 20, a pressure sensor 30 and a liquid level sensor 40 are provided in the heating tank 100 to facilitate timely adjustment of the temperature, the pressure and the liquid level in the heating tank 100.

In order to improve the effect of azeotropic distillation, a heating tank circulating pump 50 is disposed outside the heating tank 100 to pump the mixture at the bottom of the heating tank 100 to the spraying device 60 in the heating tank 100. Since the density of the entrainer is different from that of the aqueous tar, crude benzene, for example, has a lower density than the aqueous tar, and a large amount of crude benzene is present in the upper layer of the aqueous tar. A spray device 60 is provided above the heating tank 100, the hydrous tar at the bottom of the heating tank 100 is sucked into the spray device 60 by the heating tank circulation pump 50, and the hydrous tar is sprayed to the upper layer of the heating tank 100 by the spray device 60 to be sufficiently mixed with the crude benzene at the upper layer. So, spray set 60 makes the mixture between aqueous tar and the entrainer more even on the one hand, is favorable to azeotropic distillation, and on the other hand spray set 60's spraying process also can increase the evaporation capacity of aqueous tar and entrainer, provides azeotropic distillation's efficiency. Additionally, when the finished tar with the water content meeting the standard is obtained at the bottom of the heating tank 100 through multiple times of azeotropic distillation, the finished tar can be conveyed to the tar tank by the heating tank circulating pump 50.

The above is only the optional embodiment of the present invention, and not the scope of the present invention is limited thereby, all the equivalent structure changes made by the contents of the specification and the drawings are utilized under the inventive concept of the present invention, or the direct/indirect application in other related technical fields is included in the patent protection scope of the present invention.

Claims

1. The utility model provides a tar dewatering system, its characterized in that, includes heating jar, excessive room, heat exchanger, separation chamber and condensation water pitcher, the feed inlet of heating jar is used for the feeding of hydrous tar, the entry of throwing of heating jar is used for adding entrainer, the discharge gate of heating jar is used for the discharge of finished product tar, the mixed vapour discharge port of heating jar with the first air inlet of excessive room is linked together, the first gas outlet of excessive room with heat exchanger's second air inlet is linked together, heat exchanger's second return liquid mouth with the first return liquid mouth of excessive room is linked together, the first liquid outlet of excessive room with the inlet of separation chamber is linked together, the agent mouth of separation chamber with the return agent mouth of heating jar is linked together, the delivery port of separation chamber with the water inlet of condensation water pitcher is linked together.

2. The tar dewatering system of claim 1, wherein the heat exchanger comprises a first heat exchanger and a second heat exchanger, the first heat exchanger being disposed in series with the second heat exchanger.

3. The tar dewatering system of claim 2, wherein the first heat exchanger is provided with the second inlet, the second inlet is communicated with the first outlet, the first heat exchanger is provided with a first inlet hole and a first outlet hole, and the circulating cooling water in the cooling tower enters the first heat exchanger through the first inlet hole and flows back to the cooling tower through the first outlet hole.

4. The tar dewatering system according to claim 3, wherein the third air inlet of the second heat exchanger is communicated with the second air outlet of the first heat exchanger, the second heat exchanger is provided with a second water inlet hole and a second water outlet hole, condensed water in the refrigerator enters the second heat exchanger through the second water inlet hole and flows back to the refrigerator through the second water outlet hole, the second heat exchanger is provided with the second liquid return port, and the second liquid return port is communicated with the first liquid return port.

5. The tar dewatering system of claim 4, wherein the cooling tower is in communication with the chiller, and wherein the circulating cooling water in the cooling tower provides heat for the chiller.

6. The tar dewatering system of claim 1, further comprising an adsorption device in communication with the heat exchanger for adsorbing tail gas escaping from the heat exchanger, the adsorption device in communication with a waste gas collection system.

7. The tar dewatering system of claim 1, wherein the heating tank is heated using a steam coil.

8. The tar dewatering system of claim 1, wherein a temperature sensor, a pressure sensor, and a level sensor are disposed within the heating tank.

9. The tar dewatering system of claim 1, wherein a heating tank circulation pump is disposed outside the heating tank to pump the mixture at the bottom of the heating tank to a spray device in the heating tank.