CN209974661U

CN209974661U - Waste heat recovery device and coking crude benzene hydrogenation system

Info

Publication number: CN209974661U
Application number: CN201920744099.4U
Authority: CN
Inventors: 刘萍; 王建华; 李卫刚; 张志敏; 翁继; 张国卿; 王国会; 秦桂涛; 王博; 吕红强
Original assignee: XINGTAI RISUN COAL CHEMICAL INDUSTRY Co Ltd
Current assignee: XINGTAI RISUN COAL CHEMICAL INDUSTRY Co Ltd
Priority date: 2019-05-22
Filing date: 2019-05-22
Publication date: 2020-01-21
Anticipated expiration: 2029-05-22

Abstract

The utility model provides a waste heat recovery device and coking crude benzol hydrogenation system, waste heat recovery device are used for coking crude benzol hydrogenation system, and coking crude benzol hydrogenation system includes pre-evaporator, high-pressure separating tank and stabilizer, and pre-evaporator passes through the circulating gas pipeline with the high-pressure separating tank and is connected, and waste heat recovery device includes: the heat exchanger is arranged on the circulating gas pipeline so that a medium in the circulating gas pipeline flows through the heat exchanger; the two ends of the oil inlet pipeline are respectively connected with a liquid phase outlet of the high-pressure separation tank and an inlet of the heat exchanger; one end of the oil return pipeline is connected with an outlet of the heat exchanger, and the other end of the oil return pipeline is connected with a feeding port of the stabilizing tower; and the medium in the oil inlet pipeline flows through the heat exchanger, exchanges heat with the medium in the circulating gas pipeline and then flows into the oil return pipeline. The waste heat recovery device and the coking crude benzene hydrogenation system can reduce the temperature of circulating gas generated after the coking crude benzene hydrogenation system reacts, improve the feeding temperature of hydrogenated oil entering the stabilizing tower, and further reduce the energy consumption of the whole system.

Description

Waste heat recovery device and coking crude benzene hydrogenation system

Technical Field

The utility model relates to a waste heat recovery device especially relates to a waste heat recovery device and with coking crude benzol hydrogenation system who has this waste heat recovery device.

Background

The main reaction system of the coking crude benzene hydrofining process is a hydrogenation unit, crude benzene and external hydrogen with the content of 99.99 percent are subjected to hydrogenation reaction in the hydrogenation unit, and the obtained hydrogenated oil enters a stabilizing tower. The main process of the hydrogenation unit comprises the steps that coking crude benzene passes through a raw material filter and a raw material buffer tank and then is pressurized by a high-speed pump to enter a pre-evaporator, the coking crude benzene is heated and vaporized in the pre-evaporator and then enters a multi-section evaporator for further gasification, a gaseous mixture at the top of the multi-section evaporator enters a pre-reactor, catalytic hydrogenation reaction is carried out in the pre-reactor and then enters a main reaction heating furnace for further heating, and the gaseous mixture is subjected to desulfurization, denitrification, deoxidation and olefin hydrogenation saturation reaction in the main reaction heating furnace under the action of a catalyst. The product after reaction, namely circulating gas, is subjected to heat exchange through a series of heat exchangers, and enters a high-pressure separation tank after being cooled, the hydrogenated material of the liquid phase, namely hydrocarbon hydrogenated oil, is separated out, the hydrogenated oil of the liquid phase is sent into a stabilizing tower, and the material at the bottom of the stabilizing tower enters a pre-distillation tower.

The heat quantity of the circulating gas after the coking crude benzene hydrogenation system is reacted is high, the circulating gas can not be effectively utilized, and the temperature of the liquid-phase hydrogenated oil separated by the high-pressure separation tank entering the stabilizing tower is low, so that the temperature rise is required by extra heat, and the energy consumption of the system is high.

SUMMERY OF THE UTILITY MODEL

In view of the above problem that prior art exists, the utility model provides an aim at provides a can effectively utilize the heat of coking crude benzol hydrogenation system reaction back material, improve the waste heat recovery device of the temperature that the hydrogenated oil got into the stabilizer.

The embodiment of the utility model provides a technical scheme who adopts is, a waste heat recovery device for coking crude benzol hydrogenation system, coking crude benzol hydrogenation system includes pre-evaporator, high-pressure separating tank and stabilizer, pre-evaporator with the high-pressure separating tank passes through the circulating gas pipeline and connects, its characterized in that, waste heat recovery device includes:

the heat exchanger is arranged on the circulating gas pipeline so that the medium in the circulating gas pipeline flows through the heat exchanger;

one end of the oil inlet pipeline is connected with a liquid phase outlet of the high-pressure separation tank, and the other end of the oil inlet pipeline is connected with an inlet of the heat exchanger;

one end of the oil return pipeline is connected with an outlet of the heat exchanger, and the other end of the oil return pipeline is connected with a feeding port of the stabilizing tower; and the medium in the oil inlet pipeline flows through the heat exchanger and flows into the oil return pipeline after exchanging heat with the medium in the circulating gas pipeline.

In some embodiments, the waste heat recovery device further comprises a first bypass pipeline and a first valve arranged on the first bypass pipeline, one end of the first bypass pipeline is connected to the circulating gas pipeline between the pre-evaporator and the heat exchanger, and the other end of the first bypass pipeline is connected to the circulating gas pipeline between the heat exchanger and the high-pressure separation tank;

and a second valve is arranged on the circulating gas pipeline between the pre-evaporator and the heat exchanger.

In some embodiments, the waste heat recovery device further includes a second bypass line and a third valve disposed on the second bypass line, and two ends of the second bypass line are respectively connected to the oil inlet line and the oil return line;

and a fourth valve is arranged on the oil inlet pipeline, and a fifth valve is arranged on the oil return pipeline.

In some embodiments, the heat exchanger is a shell-and-tube heat exchanger, the circulating gas pipeline is communicated with a shell pass of the heat exchanger, and the oil inlet pipeline and the oil return pipeline are respectively connected with an inlet and an outlet of the tube pass of the heat exchanger.

In some embodiments, a cooler is provided on the circulating gas line, and the heat exchanger is provided on the circulating gas line between the pre-evaporator and the cooler.

The utility model discloses provide a coking crude benzol hydrogenation system simultaneously, its including the pre-evaporator, multistage evaporimeter, pre-reactor heater, pre-reactor, main reactor that connect gradually and with the high-pressure separate tank that the pre-evaporator is connected and with the stabilizer that the high-pressure separate tank is connected, coking crude benzol hydrogenation system still includes foretell waste heat recovery device.

Compared with the prior art, the embodiment of the utility model provides a waste heat recovery device and coking crude benzol hydrogenation system can reduce the temperature of the circulating gas that the coking crude benzol hydrogenation system generated after the reaction, improves the feeding temperature that the hydrogenated oil got into the stabilizer, and then reduces entire system's energy resource consumption.

It is to be understood that both the foregoing general description and the following detailed description are exemplary and explanatory only and are not restrictive of the invention.

The summary of various implementations or examples of the technology described in this disclosure is not a comprehensive disclosure of the full scope or all features of the disclosed technology.

Drawings

In the drawings, which are not necessarily drawn to scale, like reference numerals may describe similar components in different views. Like reference numerals having letter suffixes or different letter suffixes may represent different instances of similar components. The drawings illustrate various embodiments, by way of example and not by way of limitation, and together with the description and claims, serve to explain the embodiments of the invention. The same reference numbers will be used throughout the drawings to refer to the same or like parts, where appropriate. Such embodiments are illustrative, and are not intended to be exhaustive or exclusive embodiments of the present apparatus or method.

Fig. 1 is a schematic structural diagram of a waste heat recovery device according to an embodiment of the present invention.

Fig. 2 is a schematic structural diagram of a coking crude benzene hydrogenation system of the embodiment of the utility model.

Reference numerals:

1-a heat exchanger; 2-oil inlet pipeline; 3-oil return pipeline; 4-a first bypass line; 5-a second bypass line; 6-a first valve; 7-a second valve; 8-a third valve; 9-a fourth valve; 10-a fifth valve; 11-a pre-evaporator; 12-a high pressure separation tank; 13-circulating gas line; 14-a stabilizer column; 15-a cooler; 16-stabilizer column feed preheater; 17-a raw material tank; 18-a raw material filter; 19-raw material buffer tank; 20-a feedstock pump; 21-a recycle gas compressor; 22-a first mixing nozzle; 23-a multi-stage evaporator reboiler; 24-a second mixing nozzle; 25-a multi-stage evaporator; 26-a third mixing nozzle; 27-a sump; 28-pre-reactor heater; 29-pre-reactor; 30-a main reactor; 31-main reactor heater; 32-a heating furnace; 33-make-up hydrogen compressor; 34-a recycle gas capture tank; 35-stabilizer reboiler.

Detailed Description

In order to make the purpose, technical solution and advantages of the embodiments of the present invention clearer, the drawings of the embodiments of the present invention are combined below to clearly and completely describe the technical solution of the embodiments of the present invention. It is to be understood that the embodiments described are only some of the embodiments of the present invention, and not all of them. All other embodiments, which can be obtained by a person skilled in the art without any inventive work based on the described embodiments of the present invention, belong to the protection scope of the present invention.

Unless defined otherwise, technical or scientific terms used herein shall have the ordinary meaning as understood by those of ordinary skill in the art to which the invention belongs. The use of "first," "second," and similar terms in the description herein do not denote any order, quantity, or importance, but rather the terms are used to distinguish one element from another. The word "comprising" or "comprises", and the like, means that the element or item listed before the word covers the element or item listed after the word and its equivalents, but does not exclude other elements or items. The terms "connected" or "coupled" and the like are not restricted to physical or mechanical connections, but may include electrical connections, whether direct or indirect. "upper", "lower", "left", "right", and the like are used merely to indicate relative positional relationships, and when the absolute position of the object being described is changed, the relative positional relationships may also be changed accordingly.

To maintain the following description of the embodiments of the present invention clear and concise, detailed descriptions of well-known functions and components may be omitted.

As shown in fig. 1 and fig. 2, the embodiment of the utility model provides a waste heat recovery device for coking crude benzol hydrogenation system, coking crude benzol hydrogenation system includes pre-evaporator 11, high-pressure separating tank 12 and stabilizer 12, and pre-evaporator 11 passes through circulating gas pipeline 13 with high-pressure separating tank 12 and is connected, waste heat recovery device includes:

a heat exchanger 1 which is arranged on the circulating gas pipeline 13 so that the medium in the circulating gas pipeline 13 flows through the heat exchanger 1;

one end of the oil inlet pipeline 2 is connected with a liquid phase outlet of the high-pressure separation tank 12, and the other end of the oil inlet pipeline is connected with an inlet of the heat exchanger 1;

one end of the oil return pipeline 3 is connected with an outlet of the heat exchanger 1, and the other end of the oil return pipeline is connected with a feeding port of the stabilizing tower 12; the medium in the oil inlet pipeline 2 flows through the heat exchanger 1, exchanges heat with the medium in the circulating gas pipeline 13 and then flows into the oil return pipeline 3.

The utility model discloses waste heat recovery device can make the liquid phase hydrogenated oil that separates by high pressure separator 12 rise temperature with the circulation gas heat transfer that comes out by pre-evaporator 11 in heat exchanger 1 before getting into stabilizer 12, improves the temperature that the hydrogenated oil got into stabilizer 12, reduces the temperature of the circulation gas that gets into high pressure separator 12 simultaneously, effectively utilizes the heat after the coking crude benzol hydrogenation system reaction, energy saving and consumption reduction.

In some embodiments, as shown in fig. 1, the waste heat recovery device further includes a first bypass line 4 and a first valve 6 disposed on the first bypass line 4, one end of the first bypass line 4 is connected to the circulating gas line 13 between the pre-evaporator 11 and the heat exchanger 1, and the other end of the first bypass line 4 is connected to the circulating gas line 13 between the heat exchanger 1 and the high-pressure separation tank 12; a second valve 7 is arranged in the circulating gas line 13 between the pre-evaporator 11 and the heat exchanger 1. By means of the first bypass line 4, the heat exchanger 1 can be selectively used, i.e. the recycle gas from the pre-evaporator 11 can flow through or not flow through the heat exchanger 1, thereby conveniently adjusting and controlling the temperature of the hydrogenated oil entering the stabilizer 12. For example, when heat exchange is not needed for the hydrogenated oil, the first valve 6 on the first bypass pipeline 4 is opened, the second valve 7 is closed, the recycle gas directly enters the high-pressure separation tank 12 through the first bypass pipeline 4, and does not exchange heat with the hydrogenated oil through the heat exchanger 1, so that the heat exchanger 1 is isolated out of the coking crude benzene hydrogenation system; when heat exchange is needed for the hydrogenated oil, the first valve 6 on the first bypass pipeline 4 is closed, the second valve 7 is opened, and the circulating gas enters the high-pressure separation tank 12 after flowing through the heat exchanger 1, so that the circulating gas and the hydrogenated oil exchange heat, and the temperature of the hydrogenated oil is increased.

In some embodiments, as shown in fig. 1, the waste heat recovery device further includes a second bypass line 5 and a third valve 8 disposed on the second bypass line 5, wherein two ends of the second bypass line 5 are respectively connected to the oil inlet line 2 and the oil return line 3; the oil inlet pipeline 2 is provided with a fourth valve 9, and the oil return pipeline 3 is provided with a fifth valve 10. The second bypass line 5 is arranged so that the hydrogenated oil from the high-pressure separation tank 12 can selectively flow through the heat exchanger 1 according to the actual production requirements, for example, when heat exchange for the hydrogenated oil is not required, the hydrogenated oil can directly enter the stabilizer 12 through the second bypass line 5 without flowing through the heat exchanger 1, that is, the hydrogenated oil does not exchange heat with the circulating gas, and at this time, the fourth valve 9 and the fifth valve 10 need to be closed, and the third valve 8 needs to be opened.

In addition, when heat exchange is required for the hydrogenated oil, but the required temperature is not too high, the flow rate of the hydrogenated oil can be adjusted by adjusting the opening degrees of the fourth valve 9 and the fifth valve 10, so that the temperature of the hydrogenated oil entering the stabilizer 12 meets the requirement, the temperature of the hydrogenated oil is not too high, and the purpose of strictly controlling the feeding temperature of the stabilizer 12 is achieved.

Heat exchanger 1 can be selected according to the actual production needs, the embodiment of the utility model provides a do not specifically prescribe a limit to this, as shown in fig. 1, the heat exchanger 1 that this embodiment shows is shell-and-tube heat exchanger 1, and its type is E-114, and circulating gas pipeline 13 communicates with the shell side of heat exchanger 1, advances oil pipe way 2 and returns oil pipe way 3 respectively with the import and the exit linkage of the tube side of heat exchanger 1.

With continuing reference to fig. 1 and 2, a cooler 15 is provided on the circulating gas line 13, the heat exchanger 1 is provided on the circulating gas line 13 between the pre-evaporator 11 and the cooler 15, and the circulating gas flows out of the heat exchanger 1, is cooled by the cooler 15, and then enters the high-pressure separation tank 12.

As shown in fig. 1 and 2, a stabilizer feed preheater 16 is further disposed between the stabilizer 12 and the high-pressure separation tank 12, and the stabilizer feed preheater 16 is disposed on the oil return line 3, that is, the hydrogenated oil from the oil return line 3 first enters the stabilizer feed preheater 16 to be preheated and then enters the stabilizer 12.

The embodiment of the utility model provides a coking crude benzol hydrogenation system simultaneously, its including the high pressure splitter 12 that connects gradually of pre-evaporator 11, multistage evaporimeter 25, pre-reactor heater 28, pre-reactor 29, main reactor 30 and be connected with pre-evaporator 11 and the stabilizer 12 of being connected with high pressure splitter 12, coking crude benzol hydrogenation system still includes foretell waste heat recovery device.

Specifically, as shown in FIG. 1, crude benzene feed from feed tank 17 enters feed filter 18 where solid particles and aggregates, if any, are removed. Then enters a raw material buffer tank 19, 90 percent of the raw material pressurized by a raw material pump 20 (model P-101A/B) enters a pre-evaporator 11 (model E-101A-E), is subjected to reverse heat exchange and partial evaporation, and then is mixed with the circulating gas from a circulating gas compressor 21 (model C-102A/B) at a first mixing nozzle 22 of the pre-evaporator 11. The partially evaporated material in the pre-evaporator 11 is sent to the bottom of the multi-stage evaporator 25 through the second mixing nozzle 24 of the multi-stage evaporator reboiler 23.

The crude benzene is evaporated at the bottom of a multi-stage evaporator 25, and the heat required for the evaporation is provided by a multi-stage evaporator reboiler 23 which supplies heat to the reaction materials. The liquid under the bottom tray is mixed with the vapor-like material from the baffles in the third mixing nozzle 26 of the multi-stage evaporator 25 and fed into the middle of the multi-stage evaporator 25.

A small amount of crude benzene from the feed pump 20 is refluxed to the top of the multistage evaporator 25. The high boiling compounds in the bottom of the multistage evaporator 25 are discharged as a residual oil to a residual oil tank 27, and the light fraction in the residual oil tank 27 is flashed off in the residual oil tank 27 and returned to the raw material buffer tank 19 as a vapor.

All the steam-like process materials from the top of the multi-section evaporator 25 pass through the pre-reactor heater 28 to exchange heat with the main reaction materials coming reversely to the temperature required by the reaction, then enter from the bottom of the pre-reactor 29 and flow upwards through the catalyst bed layer in the pre-reactor 29, the diolefin and the styrene are saturated by hydrogenation under the action of the catalyst Ni-Mo, and the gas mixture is discharged from the top of the pre-reactor 29. Exothermic reactions take place in the prereactor 29 and the temperature at the outlet of the prereactor 29 rises, which depends on the catalyst life and inlet temperature as well as on the composition of the starting materials. The high boiling point liquid compounds are discharged from the bottom of the pre-reactor 29 to the raffinate tank 27, and the vapor separated in the raffinate tank 27 is returned to the raw material buffer tank 19.

The material from the pre-reactor 29 is heated by heat exchange with the main reaction product by a main reactor heater 31, and then further heated in a main reaction furnace 32 before being fed into the top of the main reactor 30. In the main reactor 30, the process material passes through the CoMo catalyst bed from top to bottom, undergoing desulfurization, denitrification and olefin saturation, where an exothermic reaction occurs and the outlet temperature of the main reactor 30 will rise.

The main reaction product from the bottom of the main reactor 30 passes through the main reactor heater 31, the pre-reactor heater 28 and the multi-section evaporator reboiler 23 for heat exchange and cooling, and is partially condensed in the pre-evaporator 11, the reacted material is cooled by the cooler 15 of the hydrogenation reaction product and then sent into the high-pressure separation tank 12, the material is separated into gas and liquid phases in the high-pressure separation tank 12, and the separated liquid-phase hydrogenated oil passes through the heat exchanger 1 for heat exchange with the circulating gas sent into the cooler 15 from the pre-evaporator 11 and then enters the stabilizer 12.

The new hydrogen needed by the hydrogenation reaction is compressed by a supplementary hydrogen compressor 33 (model C-101A/B) and then enters the circulating system through a circulating gas collecting tank 34, and is sent to the inlet of a circulating gas compressor 21 (model C-102A/B) as circulating gas. After compression to the prescribed pressure, the recycle gas is reintroduced into the reaction section. The pressure of the reaction was controlled by supplying fresh hydrogen to the reaction part.

The liquid phase component, hydrogenated oil, separated in the high-pressure separation tank 12 exchanges heat with the circulating gas, and then is sent to the middle part of the stabilizer 12 after exchanging heat with the material at the bottom outlet of the stabilizer again through the stabilizer feed preheater 16, and the dissolved gas is discharged by heating through the stabilizer reboiler 35.

The hydrogenated oil fraction withdrawn from the bottom of the stabilizer column 12 heats the feed to the stabilizer column 12 by the stabilizer column feed heater and is sent to the preliminary distillation column.

The utility model discloses coking crude benzol hydrogenation system has effectively utilized the heat of the circulating gas that comes out by pre-evaporator 11, has reduced the temperature of circulating gas, has reduced the energy consumption that is used for cooling circulating gas's cooler 15, has improved the feed temperature that the hydrogenated oil got into stabilizer 12 moreover, has reduced coking crude benzol hydrogenation system's energy consumption.

The above description is intended to be illustrative and not restrictive. For example, the above-described examples (or one or more versions thereof) may be used in combination with each other, and it is contemplated that the embodiments may be combined with each other in various combinations or permutations. The scope of the invention should be determined with reference to the appended claims, along with the full scope of equivalents to which such claims are entitled.

Claims

1. Waste heat recovery device for coking crude benzol hydrogenation system, coking crude benzol hydrogenation system includes pre-evaporator, high-pressure separation tank and stabilizer, pre-evaporator with the high-pressure separation tank passes through the circulating gas pipe connection, its characterized in that, waste heat recovery device includes:

2. The waste heat recovery device according to claim 1, further comprising a first bypass pipeline and a first valve arranged on the first bypass pipeline, wherein one end of the first bypass pipeline is connected to the circulating gas pipeline between the pre-evaporator and the heat exchanger, and the other end of the first bypass pipeline is connected to the circulating gas pipeline between the heat exchanger and the high-pressure separation tank;

3. The waste heat recovery device according to claim 1, further comprising a second bypass line and a third valve disposed on the second bypass line, wherein two ends of the second bypass line are respectively connected to the oil inlet line and the oil return line;

4. The waste heat recovery device according to claim 1, wherein the heat exchanger is a shell-and-tube heat exchanger, the circulating gas pipeline is communicated with a shell pass of the heat exchanger, and the oil inlet pipeline and the oil return pipeline are respectively connected with an inlet and an outlet of the tube pass of the heat exchanger.

5. The waste heat recovery device according to claim 1, wherein a cooler is provided on the circulating gas line, and the heat exchanger is provided on the circulating gas line between the pre-evaporator and the cooler.

6. The coking crude benzene hydrogenation system comprises a pre-evaporator, a multi-section evaporator, a pre-reactor heater, a pre-reactor, a main reactor, a high-pressure separation tank connected with the pre-evaporator and a stabilizing tower connected with the high-pressure separation tank which are connected in sequence, and is characterized by further comprising the waste heat recovery device of any one of claims 1 to 5.