CN111635784A - Coking chemical product recovery method and coking chemical product recovery system - Google Patents

Abstract

The invention discloses a coking chemical product recovery method and a coking chemical product recovery system. The coking chemical product recovery method comprises cooling high-temperature waste gas into primary low-temperature waste gas, and continuing to cool primary low-temperature waste gas into secondary low-temperature waste gas. coal gas, and condensing and separating out the first tar impurities, and purifying the secondary low-temperature waste gas by stages to separate out the second tar impurities, so as to obtain purified coal gas. The condensed water close to room temperature will not generate a large amount of waste water, realize the cooling and purification of waste gas, and obtain tar condensed at different temperatures, which is convenient for the recovery of tar products.

Description

Coking chemical product recovery method and coking chemical product recovery system

technical field

The invention relates to the technical field of waste gas treatment, in particular to a recovery method for coking chemical products and a recovery system for coking chemical products.

Background technique

When coking coal is coking at high temperature in the carbonization chamber, the main product produced is coke, and waste gas is generated at the same time. The temperature of the gas drops to 82-88°C. During this process, the high-temperature sensible heat of the high-temperature waste gas is absorbed by the latent heat of evaporation of ammonia water, and eventually degenerates into low-temperature condensed water. The high-temperature sensible heat of the waste gas is not only not effectively obtained. Utilization, on the contrary, increases the burden on the wastewater treatment system, and because part of the tar is mixed with ammonia water, it is not conducive to the recovery of tar products.

SUMMARY OF THE INVENTION

The main purpose of the present invention is to propose a coking chemical product recovery method and a coking chemical product recovery system, aiming to solve the problem that a large amount of waste water is generated in the existing coking chemical product recovery system and the mixing of some tar and ammonia water is not conducive to the recovery of the tar product. question.

To achieve the above object, the present invention proposes a method for recovering a coking chemical product, comprising:

Cool the high-temperature waste gas to the first-grade low-temperature waste gas;

Continue to cool down the first-level low-temperature waste gas into second-level low-temperature waste gas, and condense and separate out the first tar impurities;

The second tar impurities are separated out by grading and purifying the secondary low-temperature waste gas, so as to obtain purified gas.

Optionally, the temperature of the high-temperature raw gas is T1, and 600°C≤T1≤850°C; and/or,

The temperature of the first-grade low-temperature waste gas is T2, and 150°C≤T2≤250°C; and/or,

The temperature of the secondary low-temperature waste gas is T3, and 20°C≤T3≤30°C; and/or,

The second tar impurities include one or more of tar, naphthalene and crude benzene.

The present invention also proposes a coking chemical product recovery system, the coking chemical product recovery system includes:

Sensible heat recovery system, used to cool the high-temperature waste gas to the first-grade low-temperature waste gas;

a condensation system, the gas inlet of the condensation system is communicated with the gas outlet of the sensible heat recovery system, so that the first-level low-temperature waste gas is continuously cooled to the second-level low-temperature waste gas, and the first tar impurities are condensed and separated; as well as,

A multi-stage purification system, the gas inlet of the multi-stage purification system is communicated with the gas outlet of the condensation system, and is used for grading purification of the secondary low-temperature waste gas to separate out the second tar impurities to obtain purified gas.

Optionally, the sensible heat recovery system includes a vertical heat recovery tower, the heat recovery tower has a heat exchange cavity, and the inner side wall of the heat exchange cavity is provided with an air inlet, an air outlet, and a feeding port. port and discharge port;

The high-temperature waste gas is introduced from the air inlet to the heat exchange chamber, and the heat-absorbing solid medium is introduced into the heat-exchange chamber from the feed port, and the heat-absorbing solid medium is mixed with the high-temperature waste gas. heat exchange, so that the high-temperature waste gas is cooled to the first-stage low-temperature waste gas and discharged from the gas outlet, and the heat-absorbing solid medium is heated to a high-temperature endothermic solid medium and discharged from the discharge port;

Wherein, the gas outlet corresponds to the gas outlet of the sensible heat recovery system.

Optionally, the sensible heat recovery system further includes:

a ventilation device, including an air inlet pipe installed to the air inlet, and used to transport the high-temperature raw gas into the heat exchange chamber; and,

The feeding device includes a feeding pipeline installed to the feeding port, and is used to transport the heat-absorbing solid medium into the heat exchange chamber.

Optionally, the feeding pipeline includes a pressure pipeline and a material pipeline, the pressure pipeline is connected to the heat exchange chamber, the material pipeline is connected to the pressure pipeline, and the heat absorption pipeline is transported in the material pipeline. A solid medium, a pressure gas is passed through the pressure pipeline, and the pressure gas is used to drive the heat-absorbing solid medium to enter the heat exchange chamber to be mixed with the high-temperature waste gas.

Optionally, the heat exchange cavity has an air inlet end and an air outlet end arranged oppositely from bottom to top, the air inlet is arranged on the inner side wall of the air inlet end, and the air outlet is arranged on the side of the air outlet end. On the inner side wall, the feeding port is arranged between the air inlet end and the air outlet end; and/or,

The feeding port is provided with a feeding pipe, the discharging port is provided with a discharging pipe, and both the feeding pipe and the discharging pipe are provided with a screw conveying mechanism, and the screw conveying mechanism is used to The endothermic solid medium is sent into the heat exchange chamber through the feed pipe or the heat endothermic solid medium in the heat exchange chamber is discharged from the heat exchange chamber through the discharge pipe; and/or,

A cyclone dust collector is arranged between the gas outlet and the gas inlet of the condensation system for removing the heat-absorbing solid medium mixed in the first-stage low-temperature waste gas.

Optionally, the air inlet is arranged at the lower part of the heat exchange cavity, the feed port is arranged at the upper part of the heat exchange cavity, and a blanking component is arranged in the heat exchange cavity, and the blanking component is arranged in the heat exchange cavity. Located between the air inlet and the feeding port, the blanking assembly includes:

A plurality of baffle groups are arranged on the inner wall surface of the heat exchange cavity at intervals in the up-down direction, and each baffle group includes a plurality of baffles, and a plurality of the baffles are arranged along the installation cavity. The inner wall surface is arranged at intervals in the circumferential direction, and a material guiding passage for guiding material to the middle position of the heat exchange cavity is formed between two adjacent baffles in the same baffle group;

A guide post, the guide post is extended in the up-down direction, and is arranged in the middle of the heat exchange chamber, and a plurality of annular guide platforms are protruded from the side surface of the guide post. The baffle groups are arranged in a staggered manner, and the annular guide table is used to receive the heat-absorbing solid medium introduced from the material-guiding aisle above, and continue to guide the heat-absorbing solid medium to the guide material below. Inside the aisle.

Optionally, the upper end face of the baffle plate is inclined downward to form a first guide slope; and/or,

The upper end of the annular guide platform is inclined downward to form a second guide slope; and/or,

The upper end face of the baffle plate faces and/or the upper end face of the annular guide table is provided with a plurality of diverting spherical protrusions.

Optionally, the condensation system includes a plurality of condensers, and each of the plurality of condensers includes a condensation gas inlet and a condensation gas outlet, and in two adjacent condensers, the condensation gas inlet of one of the condensers. It is communicated with another said condensation exhaust port, and the condensation gas inlet close to the condenser of the sensible heat recovery system is the gas inlet of the condensation system, and the condensation exhaust gas close to the condenser of the multi-stage purification system The port is the gas outlet of the condensation system.

In the technical scheme of the present invention, the high-temperature waste gas is cooled to the first-stage low-temperature waste gas, the first-stage low-temperature waste gas is continuously cooled to the second-stage low-temperature waste gas, and the first tar impurities are condensed and separated out, and the second-stage low-temperature waste gas is cooled. The second tar impurities are separated out from the waste gas by grading purification, so as to obtain purified gas. In the above implementation manner, a large amount of waste water is not generated, the cooling and purification of the waste gas is realized, and the tar impurities condensed at different temperatures are obtained, which is convenient for the recovery of tar products. .

Description of drawings

In order to explain the embodiments of the present invention or the technical solutions in the prior art more clearly, the following briefly introduces the accompanying drawings that need to be used in the description of the embodiments or the prior art. Obviously, the accompanying drawings in the following description are only These are some embodiments of the present invention, and for those of ordinary skill in the art, other drawings can also be obtained according to the structures shown in these drawings without creative efforts.

Fig. 1 is the flow chart of the coking chemical product recovery method provided by the invention;

2 is a schematic structural diagram of the first embodiment of the sensible heat recovery system in the coking chemical product recovery system provided by the present invention;

3 is a schematic structural diagram of a second embodiment of a sensible heat recovery system in a coking chemical product recovery system provided by the present invention;

4 is a schematic structural diagram of a third embodiment of a sensible heat recovery system in a coking chemical product recovery system provided by the present invention;

FIG. 5 is a schematic top-view structural diagram of a third embodiment provided by the present invention.

Description of reference numbers:

The realization, functional characteristics and advantages of the present invention will be further described with reference to the accompanying drawings in conjunction with the embodiments.

Detailed ways

The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention. Obviously, the described embodiments are only a part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without creative efforts shall fall within the protection scope of the present invention.

It should be noted that, if there is a directional indication involved in the embodiment of the present invention, the directional indication is only used to explain the relative positional relationship, motion, etc. between the components under a certain posture. If the specific posture changes , the directional indication changes accordingly.

In addition, if there are descriptions involving "first", "second", etc. in the embodiments of the present invention, the descriptions of "first", "second", etc. are only used for the purpose of description, and should not be construed as indicating or implying Its relative importance or implicitly indicates the number of technical features indicated. Thus, a feature delimited with "first", "second" may expressly or implicitly include at least one of that feature. In addition, the technical solutions between the various embodiments can be combined with each other, but must be based on the realization by those of ordinary skill in the art. When the combination of technical solutions is contradictory or cannot be realized, it should be considered that the combination of such technical solutions does not exist. , is not within the scope of protection required by the present invention.

When coking coal is coking at high temperature in the carbonization chamber, the main product produced is coke, and waste gas is generated at the same time. The temperature of the gas drops to 82-88°C. During this process, the high-temperature sensible heat of the high-temperature waste gas is absorbed by the latent heat of evaporation of ammonia water, and eventually degenerates into low-temperature condensed water. The high-temperature sensible heat of the waste gas is not only not effectively obtained. Utilization, on the contrary, increases the burden on the wastewater treatment system, and because part of the tar is mixed with ammonia water, it is not conducive to the recovery of tar products.

The present invention provides a coking chemical product recovery method and a coking chemical product recovery system, wherein, FIG. 1 is a flow chart of the coking chemical product recovery method provided by the present invention, and FIGS. 2 to 4 are the coking chemical product recovery system provided by the present invention. Three examples of sensible heat recovery systems.

2 and 3, the present invention provides a coking chemical product recovery system, including a sensible heat recovery system 100, a condensation system 200, and a multi-stage purification system. The sensible heat recovery system 100 is used to cool the high-temperature waste gas to For the first-level low-temperature waste gas, the gas inlet of the condensation system 200 is communicated with the gas outlet of the sensible heat recovery system 100, so that the first-level low-temperature waste gas is continuously cooled to the second-level low-temperature waste gas, and condensed and precipitated. The first tar impurity, the gas inlet of the multi-stage purification system is communicated with the gas outlet of the condensation system 200, and is used for grading and purifying the second-stage low-temperature waste gas to separate out the second tar impurity, so as to obtain purified gas, In the above-mentioned coking chemical product recovery system, the cooling of the high-temperature waste gas is realized and the high-temperature waste gas is purified into purified gas, without additionally generating a large amount of waste water, and obtaining tar impurities condensed at different temperatures, which is convenient for the recovery of tar products .

Specifically, the sensible heat recovery system 100 includes a vertical heat recovery tower 1, the heat recovery tower 1 has a heat exchange cavity 11, and the inner wall of the heat exchange cavity is provided with an air inlet 12, The air outlet 13 , the feeding port 14 and the discharging port 15 , the high-temperature raw gas is introduced from the air inlet 12 to the heat exchange chamber 11 , and the endothermic solid medium is introduced from the feeding port 14 to the heat exchange In the cavity 11, the heat-absorbing solid medium is mixed with the high-temperature waste gas for heat exchange, so that the high-temperature waste gas is cooled to the first-stage low-temperature waste gas and discharged from the gas outlet 13, and the heat-absorbing solid gas is discharged. The medium is heated to a high-temperature endothermic solid medium and is discharged from the discharge port 15 , wherein the gas outlet 13 corresponds to the gas outlet of the sensible heat recovery system 100 . The medium and the high-temperature waste gas are mixed for heat exchange, so that the temperature of the high-temperature waste gas can be cooled, and a large amount of waste water is avoided in the recovery process of coking chemical products.

It should be noted that the high temperature and low temperature in the above-mentioned high-temperature waste gas, primary low-temperature waste gas, secondary low-temperature waste gas and high-temperature endothermic solid medium are relative. In the embodiment of the present application, the high-temperature waste gas is Refers to the waste gas with a temperature of 600 to 850°C, the first-grade low-temperature waste gas refers to the waste gas whose temperature is lower than the high-temperature waste gas after cooling, and the secondary low-temperature waste gas refers to the temperature after cooling is lower than The waste gas of the first-stage low-temperature waste gas, and the high temperature in the heat-absorbing solid medium in which the heat-absorbing solid medium is heated to a high temperature is only higher than that in the heat-absorbing solid medium that is not mixed with the high-temperature waste gas for heat exchange. The temperature, specifically, the high temperature and low temperature in the first-stage low-temperature waste gas, the second-stage low-temperature waste gas, and the high-temperature endothermic solid medium are different in specific embodiments, which are not limited in this application.

FIG. 2 is the first embodiment of the sensible heat recovery system 100 provided by the present application. Referring to FIG. 2 , the sensible heat recovery system 100 further includes a ventilation device and a feeding device. The air inlet pipe 2 of the air port 12 is used to transport the high-temperature raw gas into the heat exchange chamber 11 through the air inlet pipe 2. The feeding device includes a feeding pipe 3 installed to the feeding port 14, and passes through the feeding pipe 3. The feeding pipeline 3 transports the heat-absorbing solid medium into the heat exchange cavity 11 , so that the high-temperature raw gas and the heat-absorbing solid medium are fed into the heat exchange cavity 11 .

Further, the feeding pipeline 3 includes a pressure pipeline 31 and a material pipeline 32. The pressure pipeline 31 is connected to the heat exchange chamber 11, and the material pipeline 32 is connected to the pressure pipeline 31. The material pipeline The endothermic solid medium is transported in 32, the pressure pipeline 31 is filled with pressure gas, and the pressure gas is used to drive the endothermic solid medium into the heat exchange chamber 11 to mix with the high-temperature waste gas, With this arrangement, the endothermic solid medium driven by the pressurized gas to enter the heat exchange chamber 11 can be fully mixed with the high-temperature raw gas, thereby improving the heat exchange efficiency.

FIG. 3 is a second embodiment of the sensible heat recovery system 100 provided by the present application. Referring to FIG. 3 , the heat exchange chamber 11 has an air inlet end and an air outlet end oppositely arranged from bottom to top. 12 is arranged on the inner side wall of the air inlet end, the air outlet 13 is arranged on the inner side wall of the air outlet end, and the feeding port 14 is arranged between the air inlet end and the air outlet end. In the process of rising from bottom to top, the high-temperature waste gas is mixed with the endothermic solid medium for heat exchange, which increases the mixing and contact time of the high-temperature waste gas and the heat-absorbing solid medium, and the heat exchange effect is good.

There are many ways to realize the delivery of the heat-absorbing solid medium into and out of the heat exchange chamber 11 . Specifically, referring to FIG. 3 , the feeding port 14 is provided with a feeding pipe 4 , and the discharging port 15 is provided with a feeding pipe 4 . A discharge pipe 5 is provided, and a screw conveying mechanism 6 is arranged in the feeding pipe 4 and the discharging pipe 5, and the endothermic solid medium is passed through the feeding through the screw conveying mechanism 6. The pipe 4 is sent to the heat exchange chamber 11, and the heat-absorbing solid medium in the heat-exchanging chamber 11 is discharged from the heat-exchanging chamber 11 through the discharge pipe 5. This arrangement improves the heat-absorbing solid medium. The efficiency of entering and exiting the heat exchange chamber 11.

Specifically, the screw conveying mechanism 6 includes a conveying rod 61 that is rotatably installed in the feeding pipe 4 or the discharging pipe 5 , and the outer surface of the conveying rod 61 is provided along the feeding pipe 4 Or the helical blade 62 extending in the axial direction of the discharge pipe 5, the helical blade 62 is used to push the heat-absorbing solid medium into or out of the heat exchange cavity 11, and the heat-absorbing solid medium enters or exits the heat exchange chamber 11. Or when the heat exchange chamber 11 is discharged, the feeding port 14 and the discharging port 15 are sealed to avoid leakage of high-temperature waste gas from the feeding port 14 and the discharging port 15 .

Considering that the first-stage low-temperature waste gas cooled by the sensible heat recovery system 100 is mixed with an endothermic solid medium, a cyclone dust collector is provided between the gas outlet 13 and the gas inlet of the condensation system 200 7. The endothermic solid medium mixed in the first-stage low-temperature waste gas is removed by the cyclone 7, so as to prevent the heat-absorbing solid medium from entering the condensation system 200 with the first-stage low-temperature waste gas, resulting in The condensing system 200 is faulty.

4 to 5 are the third embodiment of the sensible heat recovery system 100 provided by the present application, referring to FIGS. 4 and 5 , the air inlet 12 is provided at the lower part of the heat exchange chamber 11 , and the feeding The port 14 is arranged on the upper part of the heat exchange chamber 11, and the heat exchange chamber 11 is provided with a blanking component 8, and the blanking component 8 is located between the air inlet 12 and the feeding port 14, so The blanking assembly 8 includes a plurality of baffle groups and guide posts 81 , and the plurality of baffle groups are arranged on the inner wall surface of the heat exchange cavity 11 at intervals along the up-down direction, and each baffle group includes a plurality of baffle plates 821 . , a plurality of the baffles 821 are arranged at intervals along the inner wall of the heat exchange cavity 11 , and are formed between two adjacent baffles 821 in the same baffle group to extend to the middle of the heat exchange cavity 11 In the material guide aisle a where the material is guided, the guide post 81 extends from the top to bottom and is located in the middle of the heat exchange chamber 11 . The side surface of the guide post 81 is protruded with a plurality of annular guide platforms 811 . The annular guide platforms 811 are arranged in a staggered manner with the plurality of baffle groups. The annular guide platforms 811 receive the heat-absorbing solid medium introduced from the material-guiding aisle a located above, and transfer the heat-absorbing solid medium. The solid medium continues to be guided into the material-guiding aisle a below, so that the endothermic heat of the high-temperature waste gas sent from the air inlet 12 provided in the lower part of the heat exchange chamber 11 rises and falls. The solid medium is mixed for heat exchange, and the heat exchange effect is good.

In order to facilitate the falling of the heat-absorbing solid medium, referring to FIG. 3 , the upper end of the baffle plate 821 is inclined downward to form a first guiding slope. When the heat-absorbing solid medium falls into the first guiding slope, the The endothermic solid medium falls into the material guide aisle a from the first guide slope under the action of its own gravity. Of course, the upper end surface of the annular guide table 811 can also be inclined downward to form a second guiding inclined surface. In this way, when the heat-absorbing solid medium falls into the second guiding inclined surface, the heat-absorbing solid medium on its own Under the action of gravity, the material falls into the material guide passage a from the second guiding inclined surface, which facilitates the heat exchange between the heat-absorbing solid medium and the high-temperature waste gas.

It should be noted that, the first guide slope and the second guide slope may be provided at the same time or alternatively. Of course, the first guide slope and the second guide slope can be arranged at the same time.

In order to avoid the accumulation of the heat-absorbing solid medium falling on the first guiding slope and/or the second guiding slope, which is not conducive to the heat exchange between the heat-absorbing solid medium and the high-temperature raw gas, the baffle 821 The upper end face of the ring-shaped guide table 811 is provided with a plurality of shunt spherical protrusions, and the plurality of the shunt spherical protrusions make the endothermic solid medium evenly distributed and avoid accumulation. Makes the heat exchange effect good.

It should be noted that in other embodiments of the present application, the gas distributor 9 may also be provided to fully mix the high-temperature raw gas with the heat-absorbing solid medium, thereby improving the heat exchange effect.

The condensation system 200 includes a plurality of condensers, and each of the plurality of condensers includes a condensation gas inlet port and a condensation gas outlet port. In two adjacent condensers, the condensation gas inlet port of one condenser and the condensation gas outlet of the other condenser. The condensation exhaust port is connected, and the condensation gas inlet of the condenser close to the sensible heat recovery system 100 is the gas inlet of the condensation system 200, and the condensation exhaust port of the condenser close to the multi-stage purification system It is the gas outlet of the condensation system 200. In this way, the first-stage low-temperature waste gas is cooled in sequence through a plurality of condensers, so that the cooling effect is better.

Specifically, there are many types of condensers, such as water coolers, air coolers, etc. The condenser can be a shell-and-tube heat exchanger. During heat exchange, the heat exchange liquid water flows in the tubes, The first-stage low-temperature waste gas flows outside the pipe and conducts countercurrent heat exchange, so that the cooling of the first-stage low-temperature waste gas is realized, and the first tar impurities are condensed at the same time.

It should be noted that, in the embodiments of the present application, the first-stage low-temperature waste gas passes through one or more of the shell-and-tube heat exchangers in sequence, so as to realize the cooling of the first-stage low-temperature waste gas to 150-360 °C. ℃, and condensate the tar impurities without water, then enter the air cooler, then pass through the water cooler, and then enter the low-temperature water cooler to obtain the second-level low-temperature waste gas cooled to 20-30 ℃, thus realizing all the The first-stage low-temperature waste gas is rapidly cooled to the second-stage low-temperature waste gas, and the first tar impurities are condensed.

The multi-stage purification system includes a benzene washing tower, a benzene removal tower, and a desulfurization tower, and the temperature is lowered so that the secondary low-temperature waste gas passes through the benzene washing tower, the benzene removal tower and the sulfur absorption tower in sequence to remove the secondary low temperature waste gas. Benzene hydrocarbons and hydrogen sulfide are obtained to obtain purified gas, and benzene hydrocarbon products are separated.

It should be noted that, before the secondary low-temperature waste gas enters the benzene washing tower, a process of removing naphthalene also needs to be carried out. After the process of removing naphthalene, the secondary low-temperature waste gas enters the electric tar trap to capture tar mist droplets. Then enter the benzene washing tower to start the benzene washing process.

Considering the recovery and utilization of the heat of the endothermic solid medium heated to a high temperature after exchanging heat with the high-temperature waste gas, the coking chemical product recovery system further includes an endothermic solid medium collection system, and the endothermic solid medium collection system includes: A receiving port, which is communicated with the discharge port 15, is used to collect the high-temperature endothermic solid medium discharged from the discharge port 15, and send the high-temperature endothermic solid medium into the discharge port 15. The boiler burns to generate electricity or steam, thereby increasing the utilization of sensible heat in the coking chemical product recovery system.

Based on the above-mentioned coking chemical product recovery system, as shown in Figure 1, the present invention also provides a method for recovering a coking chemical product using the above-mentioned coking chemical product recovery system for the recovery of waste gas, comprising:

Step S10, cooling the high-temperature waste gas to the first-level low-temperature waste gas;

In step S20, the first-level low-temperature waste gas is continuously cooled to the second-level low-temperature waste gas, and the first tar impurities are condensed and separated out;

In step S30, the secondary low-temperature waste gas is graded and purified to separate out the second tar impurities, so as to obtain purified gas.

In the above steps, by cooling the high-temperature waste gas to the first-level low-temperature waste gas, the first-level low-temperature waste gas is continuously cooled to the second-level low-temperature waste gas, and the first tar impurities are condensed and separated out, and the second-level low-temperature waste gas is cooled. The second tar impurities are separated out by grading purification, so as to obtain purified gas without generating a large amount of extra waste water, realizing the cooling and purification of waste gas, and obtaining the tar impurities condensed at different temperatures, which is convenient for the recovery of tar products.

Specifically, the high-temperature waste gas, the first-stage low-temperature waste gas, and the second-stage low-temperature waste gas are relative, and refer to the waste gas whose temperature is within a certain range. In this application, the temperature of the high-temperature waste gas is T1 , and 600°C≤T1≤850°C; and/or, the temperature of the primary low-temperature waste gas is T2, and 150°C≤T2≤250°C; and/or, the temperature of the secondary low-temperature waste gas is T3 , and 20℃≤T3≤30℃.

It should be noted that the second tar impurities include one or more of tar, naphthalene and crude benzene.

The above descriptions are only the preferred embodiments of the present invention, and are not intended to limit the scope of the present invention. Under the conception of the present invention, any equivalent structural transformations made by the contents of the description and drawings of the present invention, or direct/indirect application Other related technical fields are included in the scope of patent protection of the present invention.

Claims (10)

1. A coking chemical product recovery process, characterized in that the coking chemical product recovery process comprises:

cooling the high-temperature raw gas into primary low-temperature raw gas;

continuously cooling the primary low-temperature raw gas into secondary low-temperature raw gas, and condensing to separate out first tar impurities;

and purifying the second-stage low-temperature raw gas in a grading manner to separate out second tar impurities so as to obtain purified gas.

2. The coking chemical product recovery method of claim 1, wherein the high temperature raw coke oven gas has a temperature of T1 and T1 of 600 ℃ to 850 ℃; and/or the presence of a gas in the gas,

the temperature of the primary low-temperature raw gas is T2, and T2 is more than or equal to 150 ℃ and less than or equal to 250 ℃; and/or the presence of a gas in the gas,

the temperature of the secondary low-temperature raw gas is T3, and T3 is more than or equal to 20 ℃ and less than or equal to 30 ℃; and/or the presence of a gas in the gas,

the second tar impurities include one or more of tar, naphthalene, and crude benzene.

3. A coking chemical product recovery system, comprising:

the sensible heat recovery system is used for cooling the high-temperature raw gas into primary low-temperature raw gas;

the gas inlet of the condensing system is communicated with the gas outlet of the sensible heat recovery system and is used for continuously cooling the primary low-temperature raw gas into secondary low-temperature raw gas and condensing to separate out first tar impurities; and the number of the first and second groups,

and a gas inlet of the multi-stage purification system is communicated with a gas outlet of the condensation system and is used for purifying the second-stage low-temperature raw coke oven gas in a grading manner to separate out second tar impurities so as to obtain purified gas.

4. The coking chemical product recovery system of claim 3 wherein the sensible heat recovery system comprises a heat recovery tower in a vertical arrangement, the heat recovery tower having a heat exchange chamber therein, the heat exchange chamber having an inner sidewall with an air inlet, an air outlet, a feed port and a discharge port therethrough;

leading the high-temperature raw coke oven gas into the heat exchange cavity from the gas inlet, leading a heat absorption solid medium into the heat exchange cavity from the feeding port, mixing the heat absorption solid medium and the high-temperature raw coke oven gas for heat exchange so as to reduce the temperature of the high-temperature raw coke oven gas into the primary low-temperature raw coke oven gas and discharge the primary low-temperature raw coke oven gas from the gas outlet, and heating the heat absorption solid medium into the high-temperature heat absorption solid medium and discharging the high-temperature heat absorption solid medium from the discharge port;

wherein the gas outlet corresponds to a gas outlet of the sensible heat recovery system.

5. The coking chemical product recovery system of claim 4, wherein the sensible heat recovery system further comprises:

the ventilation device comprises an air inlet pipeline mounted to the air inlet and is used for conveying the high-temperature raw coke oven gas into the heat exchange cavity; and the number of the first and second groups,

and the feeding device comprises a feeding pipeline arranged to the feeding port and is used for conveying heat absorption solid media to the heat exchange cavity.

6. The coking chemical product recovery system according to claim 5, wherein the feed pipeline comprises a pressure pipeline and a material pipeline, the pressure pipeline is communicated with the heat exchange cavity, the material pipeline is communicated with the pressure pipeline, the heat absorption solid medium is transported in the material pipeline, a pressure gas is communicated in the pressure pipeline, and the pressure gas is used for driving the heat absorption solid medium to enter the heat exchange cavity to be mixed with the high-temperature raw coke oven gas.

7. The coking chemical product recovery system of claim 4 wherein the heat exchange chamber has an inlet end and an outlet end opposite from the bottom to the top, the inlet port being disposed on an inside wall of the inlet end, the outlet port being disposed on an inside wall of the outlet end, the feed port being disposed between the inlet end and the outlet end; and/or the presence of a gas in the gas,

the feeding port is provided with a feeding pipeline, the discharging port is provided with a discharging pipeline, spiral conveying mechanisms are arranged in the feeding pipeline and the discharging pipeline respectively, and the spiral conveying mechanisms are used for conveying the heat absorption solid medium into the heat exchange cavity through the feeding pipeline or discharging the heat absorption solid medium in the heat exchange cavity out of the heat exchange cavity through the discharging pipeline; and/or the presence of a gas in the gas,

and a cyclone dust collector is arranged between the gas outlet and the gas inlet of the condensing system and is used for removing the heat absorption solid medium mixed in the primary low-temperature raw gas.

8. The coking chemical product recovery system of claim 4 wherein the air inlet is disposed at a lower portion of the heat exchange chamber and the material feed port is disposed at an upper portion of the heat exchange chamber, and wherein the heat exchange chamber has a material drop assembly disposed therein, the material drop assembly being disposed between the air inlet and the material feed port, the material drop assembly comprising:

the baffle groups are arranged on the inner wall surface of the heat exchange cavity at intervals from top to bottom, each baffle group comprises a plurality of baffles which are arranged at intervals along the circumferential direction of the inner wall surface of the installation cavity, and a material guide passage for guiding materials to the middle position of the heat exchange cavity is formed between every two adjacent baffles in the same baffle group;

the guide pillar extends up and down and is arranged at the middle position of the heat exchange cavity, a plurality of annular guide platforms are convexly arranged on the side surface of the guide pillar, the annular guide platforms and the baffle groups are arranged in a staggered mode, and the annular guide platforms are used for receiving heat absorption solid media guided from the guide passage above and continuously guiding the heat absorption solid media to the guide passage below.

9. The coking chemical product recovery system of claim 8, wherein the baffles are inclined downwardly at their upper ends to form a first guide ramp; and/or the presence of a gas in the gas,

the upper end surface of the annular guide table is arranged in a downward inclined mode to form a second guide inclined surface; and/or the presence of a gas in the gas,

the upper end surface of the baffle faces and/or the upper end surface of the annular guide table is provided with a plurality of shunting spherical protrusions.

10. The coking chemical product recovery system of claim 3 wherein the condensing system includes a plurality of condensers, each of the plurality of condensers including a condensing gas inlet and a condensing gas outlet, the condensing gas inlet of one of the condensers being in communication with the other of the condensing gas outlets of two adjacent condensers, and the condensing gas inlet of the condenser adjacent to the sensible heat recovery system being a gas inlet of the condensing system and the condensing gas outlet of the condenser adjacent to the multi-stage purification system being a gas outlet of the condensing system.

Images