CN211284252U - Continuous production device for directly preparing aromatic hydrocarbon from coal - Google Patents
Continuous production device for directly preparing aromatic hydrocarbon from coal Download PDFInfo
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- CN211284252U CN211284252U CN201921505506.2U CN201921505506U CN211284252U CN 211284252 U CN211284252 U CN 211284252U CN 201921505506 U CN201921505506 U CN 201921505506U CN 211284252 U CN211284252 U CN 211284252U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
The utility model discloses a coal directly makes aromatic hydrocarbon continuous production device, including raw coal warehouse, raw coal auger delivery ware, 1# preparation jar, 1# preparation pump, 2# preparation jar, 2# preparation pump, screw reactor, from the hot section condenser, from hot section condensate tank, low temperature section condenser, low temperature section condensate tank, high temperature section condenser, high temperature section condensate tank, clean coal auger delivery ware and clean coal warehouse, raw coal auger delivery ware carry extremely in the screw reactor, 1# preparation jar with preparation is used respectively in the 2# preparation jar 1# preparation pump with 2# preparation pump carry extremely in the screw reactor. The utility model discloses make the coal adopt the direct system arene of one-step method to avoid "high input, high energy consumption, high water consumption, high pollution" shortcoming, the direct system arene of coal device is compact little, continuous high efficiency, energy-concerving and environment-protective simultaneously.
Description
Technical Field
The invention relates to the technical field of preparation of aromatic hydrocarbon from petroleum, in particular to a continuous production device for directly preparing aromatic hydrocarbon from coal.
Background
At present, aromatic hydrocarbon products are mainly prepared at home and abroad by adopting the following process routes: the technical route of preparing the aromatic hydrocarbon by using the petroleum, the technical route of preparing the aromatic hydrocarbon by using the coal-based methanol, the technical route of preparing the aromatic hydrocarbon by using the coal coking oil and the like are adopted. The technical routes all have the four high disadvantages of high investment, high energy consumption, high water consumption and high pollution, and are terribly and difficultly continued to exist. At present, the industrial production of aromatics directly from coal by a one-step method is still blank worldwide.
Disclosure of Invention
Based on the technical problems in the background art, the invention provides a continuous production device for directly preparing aromatic hydrocarbon from coal.
The invention provides a continuous production device for directly preparing aromatic hydrocarbon from coal, which comprises a raw coal storage bin, a raw coal screw conveyor, a 1# preparation tank, a 1# preparation pump, a 2# preparation tank, a 2# preparation pump, a screw reactor, a self-heating section condenser, a self-heating section condensate tank, a low-temperature section condenser, a low-temperature section condensate tank, a high-temperature section condenser, a high-temperature section condensate tank, a clean coal screw conveyor and a clean coal storage bin, wherein the raw coal screw conveyor is conveyed into the screw reactor, the preparations in the 1# preparation tank and the 2# preparation tank are respectively conveyed into the screw reactor by the 1# preparation pump and the 2# preparation pump, gas generated by the reaction of the screw reactor is respectively condensed by the self-heating section condenser, the low-temperature section condenser and the high-temperature section condenser, and the condensate is respectively conveyed into the self-heating section condensate tank, Clean coal is conveyed to the clean coal storage bin by the clean coal spiral conveyor in the low-temperature section condensate tank and the high-temperature section condensate tank.
Preferably, the spiral reactor comprises a motor, a speed reducer, a self-heating section steam collecting tank, a low-temperature section steam collecting tank, a high-temperature section steam collecting tank, a cooling section, a low-temperature section heating system, a high-temperature section heating system and a cooling section cooling system, wherein the motor and the speed reducer are connected with the spiral of the spiral reactor, the self-heating section steam collecting tank, the low-temperature section steam collecting tank and the high-temperature section steam collecting tank are respectively communicated with the self-heating section condenser, the low-temperature section condenser and the high-temperature section condenser, the low-temperature section heating system and the high-temperature section heating system respectively heat the low-temperature section and the high-temperature section of the spiral reactor, the cooling section cooling system cools the cooling section of the spiral reactor, and the cooling section is communicated with the clean coal spiral conveyor.
Preferably, the self-heating section condenser comprises a first shell, a first tube plate, a first tube bundle and a first seal head, wherein the first tube plate and the first tube bundle are arranged in the first shell, the first tube plate is arranged at the upper end of the first tube bundle, the first seal head is arranged at the bottom of the first shell, the spiral reactor is connected to the upper end of the self-heating section condenser through a self-heating section steam collecting groove, and the lower end of the self-heating section condenser is connected to the interior of the self-heating section condensate tank through a pipeline.
Preferably, the low temperature section condenser includes second casing, second tube sheet, second tube bank and second head, second tube sheet and second tube bank all set up in the second casing, just the second tube sheet sets up the upper end of second tube bank, the second head sets up the bottom of second casing, spiral reactor passes through the low temperature section vapour collecting groove and connects in the low temperature section condenser upper end the low temperature section condenser lower extreme passes through pipe connection to in the low temperature section condensate tank.
Preferably, the high temperature section condenser includes third casing, third tube sheet, third tube bank and third head, third tube sheet and third tube bank all set up in the third casing, just the third tube sheet sets up the upper end of third tube bank, the third head sets up the bottom of third casing, the spiral reactor passes through the high temperature section vapour collecting tank and connects high temperature section condenser upper end, high temperature section condenser lower extreme passes through the pipe connection to in the high temperature section condensate tank.
Preferably, the temperatures of the low-temperature section heating system, the high-temperature section heating system and the cooling section cooling system are respectively from room temperature to 100 ℃, from 100 ℃ to 400 ℃ and from 400 ℃ to not higher than 50 ℃, and the pressures of the low-temperature section heating system, the high-temperature section heating system and the cooling section cooling system are not higher than 0.1 MPa.
The invention has the following advantages and beneficial effects:
1. the continuous production device for directly preparing the aromatic hydrocarbon from the coal enables the coal to directly prepare the aromatic hydrocarbon by adopting a one-step method, thereby avoiding the defects of high investment, high energy consumption, high water consumption and high pollution in the background technology, which is the most scientific and ideal technical route for preparing the aromatic hydrocarbon from the coal;
2. the continuous production device for directly preparing the aromatic hydrocarbon from the coal has the advantages of compactness, small size, continuity, high efficiency, energy conservation and environmental protection.
Drawings
FIG. 1 is a schematic structural diagram of a continuous production apparatus for directly preparing aromatic hydrocarbons from coal according to the present invention;
FIG. 2 is a schematic structural diagram of a spiral reactor of a continuous production device for directly preparing aromatic hydrocarbons from coal according to the present invention;
FIG. 3 is a schematic view of a self-heating-section condenser of a continuous production apparatus for producing aromatics directly from coal according to the present invention;
FIG. 4 is a schematic structural diagram of a low-temperature section condenser of a continuous production device for directly preparing aromatic hydrocarbons from coal according to the present invention;
FIG. 5 is a schematic structural view of a high-temperature condenser of a continuous production device for directly preparing aromatic hydrocarbons from coal.
In the figure: 101 raw coal storage bin, 102 raw coal screw conveyor, 1031# preparation tank, 1041 # preparation pump, 1052# preparation tank, 1062# preparation pump, 201 screw reactor, 201-1 motor, 201-2 reducer, 201-3 self-heating section steam collecting tank, 201-4 low-temperature section steam collecting tank, 201-5 high-temperature section steam collecting tank, 201-6 cooling section, 201-7 low-temperature section heating system, 201-8 high-temperature section heating system, 201-9 cooling section cooling system, 301 self-heating section condenser, 301-1 first shell, 301-2 first tube plate, 301-3 first tube plate, 301-4 first head, 302 self-heating section condensation liquid tank, 401 low-temperature section condenser, 401-1 second shell, 401-2 second tube plate, 401-3 second tube plate, 401-4 second head, 402 low-temperature condensation liquid tank, The system comprises a high-temperature section condenser 501, a third shell 501-1, a third tube plate 501-2, a third tube bundle 501-3, a third end socket 501-4, a high-temperature section condensate tank 502, a clean coal screw conveyor 601 and a clean coal storage bin 701.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. The components of embodiments of the present invention generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations. Thus, the following detailed description of the embodiments of the present invention, presented in the figures, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should also be noted that, unless otherwise explicitly specified or limited, the terms "disposed," "mounted," "connected," and "connected" are to be construed broadly and may, for example, be fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
The invention will be further described with reference to the drawings and specific examples.
As shown in fig. 1 to 5: the invention provides a continuous production device for directly preparing aromatic hydrocarbon from coal. The system comprises a raw coal storage bin 101, a raw coal screw conveyor 102, a No. 1 preparation tank 103, a No. 1 preparation pump 104, a No. 2 preparation tank 105, a No. 2 preparation pump 106, a screw reactor 201, a self-heating section condenser 301, a self-heating section condensate tank 302, a low-temperature section condenser 401, a low-temperature section condensate tank 402, a high-temperature section condenser 501, a high-temperature section condensate tank 502, a clean coal screw conveyor 601 and a clean coal storage bin 701.
Wherein the raw coal in the raw coal silo 101 is transported into the screw reactor 201 by the raw coal screw conveyor 102; the preparation in the # 1 preparation tank 103 and the # 2 preparation tank 105 is transferred into the screw reactor 201 by the # 1 preparation pump 104 and the # 2 preparation pump 106, respectively; the gas generated by the reaction of the spiral reactor 201 is condensed by the self-heating section condenser 301, the low-temperature section condenser 401 and the high-temperature section condenser 501, and the condensate is sent to the self-heating section condensate tank 302, the low-temperature section condensate tank 402 and the high-temperature section condensate tank 502; clean coal is fed into the clean coal bunker 701 by the clean coal auger 601.
The spiral reactor 201 comprises a motor 201-1, a speed reducer 201-2, a self-heating section steam collecting groove 201-3, a low-temperature section steam collecting groove 201-4, a high-temperature section steam collecting groove 201-5, a cooling section 201-6, a low-temperature section heating system 201-7, a high-temperature section heating system 201-8 and a cooling section cooling system 201-9. The motor 201-1 and the speed reducer 201-2 are connected with the screw of the screw reactor 201. The self-heating section steam collecting groove 201-3, the low-temperature section steam collecting groove 201-4 and the high-temperature section steam collecting groove 201-5 are respectively communicated with the self-heating section condenser 301, the low-temperature section condenser 401 and the high-temperature section condenser 501. The low-temperature section heating system 201-7 and the high-temperature section heating system 201-8 respectively heat the low-temperature section and the high-temperature section of the spiral reactor 201. The cooling section cooling system 201-9 cools the cooling section 201-6 of the screw reactor 201. The cooling section 201-6 is communicated with the clean coal screw conveyor 601.
The condenser 301 comprises a first shell 301-1, a first tube sheet 301-2, a first tube bundle 301-3, and a first head 301-4. The first tube plate 301-2 and the first tube bundle 301-3 are both disposed in the first shell 301-1, the first tube plate 301-2 is disposed at the upper end of the first tube bundle 301-3, and the first head 301-4 is disposed at the bottom of the first shell 301-1. Steam in the spiral reactor 201 enters the self-heating section condenser 301 from the upper end of the self-heating section condenser 301 through the self-heating section steam collecting groove 201-3 for condensation treatment, the steam is changed into liquid after the condensation treatment, and the liquid enters the self-heating section condensate tank 302 from the lower end of the self-heating section condenser 301 through a pipeline for storage for later use.
The low-temperature section condenser 401 comprises a second shell 401-1, a second tube plate 401-2, a second tube bundle 401-3 and a second head 401-4. The second tube plate 401-2 and the second tube bundle 401-3 are both arranged in the second shell 401-1, the second tube plate 401-2 is arranged at the upper end of the second tube bundle 401-3, and the second head 401-4 is arranged at the bottom of the second shell 401-1. Steam in the spiral reactor 201 enters the low-temperature section condenser 401 from the upper end of the low-temperature section condenser 401 through the low-temperature section steam collecting groove 201-4 for condensation treatment, the steam is changed into liquid after condensation treatment, and the liquid enters the low-temperature section condensate tank 402 from the lower end of the low-temperature section condenser 401 through a pipeline for storage for later use.
The high-temperature section condenser 501 comprises a third shell 501-1, a third tube plate 501-2, a third tube bundle 501-3 and a third head 501-4. The third tube plate 501-2 and the third tube bundle 501-3 are both arranged in the third shell 501-1, the third tube plate 501-2 is arranged at the upper end of the third tube bundle 501-3, and the third seal head 501-4 is arranged at the bottom of the third shell 501-1. Steam in the spiral reactor 201 enters the high-temperature section condenser 501 from the upper end of the high-temperature section condenser 501 through the high-temperature section steam collecting groove 201-5 for condensation treatment, the steam is changed into liquid after condensation treatment, and the liquid enters the high-temperature section condensate tank 502 from the lower end of the high-temperature section condenser 501 through a pipeline for storage for later use.
The temperatures of the low-temperature section heating system 201-7, the high-temperature section heating system 201-8 and the cooling section cooling system 201-9 are respectively from room temperature to 100 ℃, from 100 ℃ to 400 ℃ and from 400 ℃ to not higher than 50 ℃, and the pressures of the low-temperature section heating system 201-7, the high-temperature section heating system 201-8 and the cooling section cooling system 201-9 are not higher than 0.1 MPa.
In the invention, raw coal in a raw coal storage bin 101 is conveyed to a spiral reactor 201 by a raw coal spiral conveyor 102, preparations in a preparation tank 1# 103 and a preparation tank 2# 105 are respectively conveyed to the spiral reactor 201 by a preparation pump 1# 104 and a preparation pump 2# 106, gas generated by the reaction of the spiral reactor 201 is respectively condensed by a self-heating section condenser 301, a low-temperature section condenser 401 and a high-temperature section condenser 501, condensate is respectively conveyed to a self-heating section condensate tank 302, a low-temperature section condensate tank 402 and a high-temperature section condensate tank 502, and clean coal is conveyed to a clean coal storage bin 701 by a clean coal spiral conveyor 601.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and the technical solutions and the inventive concepts thereof according to the present invention should be equivalent or changed within the scope of the present invention.
Claims (6)
1. A continuous production device for preparing aromatic hydrocarbon directly from coal comprises a raw coal storage bin (101), a raw coal screw conveyor (102), a 1# preparation tank (103), a 1# preparation pump (104), a 2# preparation tank (105), a 2# preparation pump (106), a screw reactor (201), a self-heating section condenser (301), a self-heating section condensate tank (302), a low-temperature section condenser (401), a low-temperature section condensate tank (402), a high-temperature section condenser (501), a high-temperature section condensate tank (502), a clean coal screw conveyor (601) and a clean coal storage bin (701), and is characterized in that the raw coal screw conveyor (102) is conveyed into the screw reactor (201), preparations in the 1# preparation tank (103) and the 2# preparation tank (105) are conveyed into the screw reactor (201) by the 1# preparation pump (104) and the 2# preparation pump (106) respectively, and the gas generated by the reaction of the spiral reactor (201) is condensed by the self-heating section condenser (301), the low-temperature section condenser (401) and the high-temperature section condenser (501), condensate is respectively sent to the self-heating section condensate tank (302), the low-temperature section condensate tank (402) and the high-temperature section condensate tank (502), and clean coal is sent to the clean coal storage bin (701) by the clean coal spiral conveyor (601).
2. The continuous production device for preparing the aromatic hydrocarbon directly from the coal according to claim 1, wherein the spiral reactor (201) comprises a motor (201-1), a reducer (201-2), a self-heating section steam collection tank (201-3), a low-temperature section steam collection tank (201-4), a high-temperature section steam collection tank (201-5), a cooling section (201-6), a low-temperature section heating system (201-7), a high-temperature section heating system (201-8) and a cooling section cooling system (201-9), the motor (201-1) and the reducer 201-2 are connected with a spiral of the spiral reactor (201), and the self-heating section steam collection tank (201-3), the low-temperature section steam collection tank (201-4) and the high-temperature section steam collection tank (201-5) are respectively connected with the self-heating section condenser (301), The low-temperature section condenser (401) and the high-temperature section condenser (501) are communicated, the low-temperature section heating system (201-7) and the high-temperature section heating system (201-8) respectively heat the low-temperature section and the high-temperature section of the spiral reactor (201), the cooling section cooling system (201-9) cools the cooling section (201-6) of the spiral reactor (201), and the cooling section (201-6) is communicated with the clean coal spiral conveyor (601).
3. The continuous production device for preparing arene from coal directly according to claim 1, the self-heating section condenser (301) comprises a first shell (301-1), a first tube plate (301-2), a first tube bundle (301-3) and a first seal head (301-4), the first tube sheet (301-2) and first tube bundle (301-3) are disposed within the first shell (301-1), and the first tube sheet (301-2) is disposed at an upper end of the first tube bundle (301-3), the first seal head (301-4) is arranged at the bottom of the first shell (301-1), the spiral reactor (201) is connected with the upper end of the self-heating section condenser (301) through a self-heating section steam collecting groove (201-3), the lower end of the self-heating section condenser (301) is connected into the self-heating section condensate tank (302) through a pipeline.
4. The continuous production device for preparing arene from coal directly according to claim 1, the low-temperature section condenser (401) comprises a second shell (401-1), a second tube plate (401-2), a second tube bundle (401-3) and a second seal head (401-4), the second tube sheet (401-2) and second tube bundle (401-3) are both disposed within the second shell (401-1), and the second tube sheet (401-2) is arranged at the upper end of the second tube bundle (401-3), the second seal head (401-4) is arranged at the bottom of the second shell (401-1), the spiral reactor (201) is connected to the upper end of a low-temperature section condenser (401) through a low-temperature section steam collecting groove (201-4), and the lower end of the low-temperature section condenser (401) is connected to a low-temperature section condensate tank (402) through a pipeline.
5. The continuous production device for preparing arene from coal directly according to claim 1, the high-temperature section condenser (501) comprises a third shell (501-1), a third tube plate (501-2), a third tube bank (501-3) and a third seal head (501-4), the third tube sheet (501-2) and the third tube bank (501-3) are both disposed within the third shell (501-1), and the third tube sheet (501-2) is arranged at the upper end of the third tube bundle (501-3), the third seal head (501-4) is arranged at the bottom of the third shell (501-1), the spiral reactor (201) is connected with the upper end of the high-temperature section condenser (501) through a high-temperature section steam collecting groove (201-5), the lower end of the high-temperature section condenser (501) is connected into a high-temperature section condensate tank (502) through a pipeline.
6. The continuous production device for preparing the aromatic hydrocarbon directly from the coal according to claim 2, wherein the temperatures of the low-temperature section heating system (201-7), the high-temperature section heating system (201-8) and the cooling section cooling system (201-9) are respectively from room temperature to 100 ℃, from 100 ℃ to 400 ℃ and from 400 ℃ to not more than 50 ℃, and the pressures of the low-temperature section heating system (201-7), the high-temperature section heating system (201-8) and the cooling section cooling system (201-9) are not more than 0.1 MPa.
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| CN201921505506.2U CN211284252U (en) | 2019-09-11 | 2019-09-11 | Continuous production device for directly preparing aromatic hydrocarbon from coal |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112852465A (en) * | 2019-11-12 | 2021-05-28 | 任永飞 | Continuous production device for directly preparing aromatic hydrocarbon from coal |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112852465A (en) * | 2019-11-12 | 2021-05-28 | 任永飞 | Continuous production device for directly preparing aromatic hydrocarbon from coal |
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