Production waste heat recovery system of organic silicon rectification device

Abstract

The utility model discloses an organic silicon rectification device production waste heat recovery system which comprises a flash tank, the liquid inlet end of the flash tank is connected with a plurality of waste heat recovery modules in parallel, and the air inlet end of each waste heat recovery module is connected with a high-temperature steam source of the corresponding air pressure; each waste heat recovery module comprises a steam header pipe, a steam condensate header pipe and a plurality of rectifying tower reboilers, the rectifying tower reboilers are connected between the corresponding steam header pipe and steam condensate header pipe in parallel, and steam in the steam header pipe and each rectifying tower reboiler form heat supply cooperation; and the corresponding high-temperature steam high-product heat is utilized through the multi-module rectifying tower reboiler, the waste heat utilization effect is good, and the applicability is high.

Description

Technical Field

[0001] The utility model relates to the technical field of organosilicon production, in particular to an organosilicon rectification device production waste heat recovery system. Background Art

[0002] During the production of an organosilicon distillation system using water vapor as a heat source, the system will also produce a large amount of high-temperature water vapor. The high-temperature water vapor is usually converted into high-temperature hot water through a cooling system. Currently, the production hot water is usually flash-evaporated at atmospheric pressure to convert the high-temperature hot water into atmospheric pressure hot water. The disadvantage of this method is that the high-temperature water vapor and the residual heat in the high-temperature hot water are eventually dissipated into the environment through the cooling system without being effectively recovered or utilized, and waste heat is generated for the environment. Therefore, it is necessary to conduct relevant technical research and innovation on the hot water system of the organosilicon monomer distillation system. Utility Model Content

[0003] The utility model provides a waste heat recovery system for an organosilicon distillation device, aiming to solve the problem that waste heat is generated by high-temperature steam and high-temperature hot water in the organosilicon distillation process and the waste heat is not utilized and recovered.

[0004] In order to solve the above technical problems, the technical solution adopted by the utility model is:

[0005] A waste heat recovery system for the production of an organosilicon rectification device comprises a flash tank, a liquid inlet end of the flash tank is connected in parallel with a plurality of waste heat recovery modules, and an air inlet end of each waste heat recovery module is connected to a high-temperature steam source of a corresponding air pressure;

[0006] Each of the waste heat recovery modules includes a steam main pipe, a steam condensate main pipe and a plurality of distillation tower reboilers. The plurality of distillation tower reboilers are connected in parallel between the corresponding steam main pipe and the steam condensate main pipe, and the steam in the steam main pipe forms a heat supply coordination with each distillation tower reboiler.

[0007] Preferably, the air inlet end of the steam main is connected to a high-temperature steam source of a corresponding air pressure, and a flow meter, a pressure gauge and a thermometer are provided on the steam main, and a plurality of distillation tower reboilers are connected in parallel to the air outlet end of the steam main.

[0008] As a more preferred embodiment, the air inlet end of each distillation tower reboiler is connected to the air outlet end of the corresponding steam main pipe through a valve and a flow meter, and the liquid outlet end of each distillation tower reboiler is connected in parallel to the same corresponding steam condensate main pipe.

[0009] Furthermore, a pressure gauge and a thermometer are provided on the steam condensate main pipe, and the liquid outlet of the steam condensate main pipe is connected to the liquid inlet of the flash tank through a flow meter.

[0010] Furthermore, the flash tank is provided with a pressure gauge and a liquid level gauge.

[0011] Specifically, the upper gas phase pipe of the flash tank is connected to the steam recovery pipe through a flow meter, and the lower liquid phase pipe of the flash tank is connected to the steam condensate recovery pipe through a flow meter.

[0012] Preferably, the number of the waste heat recovery module is at least one.

[0013] More preferably, the number of the distillation tower reboiler in each of the waste heat recovery modules is at least one.

[0014] Beneficial effects of the utility model:

[0015] 1. Multiple waste heat recovery modules correspond to high-temperature steam of different pressures, and several distillation tower reboilers in the module absorb high-quality heat, use the heat for the operation of the distillation tower, use the high-quality heat of the high-temperature steam, and reduce the temperature of the subsequent steam condensate;

[0016] 2. The steam condensate produced by multiple waste heat recovery modules is passed into the flash tank, and the saturated gas and saturated liquid are separated by flash evaporation and recovered for utilization respectively, and the low-quality heat of the steam condensate is recovered to solve the problem of waste heat of high-temperature hot water. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] Figure 1 This is a schematic diagram of the process connection of Example 2 of the utility model;

[0018] In the figure: 1. Waste heat recovery module; 2. Steam main pipe; 3. Distillation tower reboiler; 4. Steam condensate main pipe; 5. Flash tank; 6. Steam recovery pipe; 7. Steam condensate recovery pipe; 8. Flow meter; 9. Pressure gauge; 10. Thermometer; 11. Valve; 12. Liquid level meter. DETAILED DESCRIPTION

[0019] As follows, embodiments are further described with reference to the accompanying drawings.

[0020] like Figure 1 As shown, as a preferred embodiment 1, a waste heat recovery system for the production of an organosilicon distillation device includes a flash tank 5, a liquid inlet end of the flash tank 5 is connected in parallel with a plurality of waste heat recovery modules 1, and the gas inlet end of each waste heat recovery module 1 is connected to a high-temperature steam source of a corresponding gas pressure;

[0021] Each of the waste heat recovery modules 1 includes a steam main pipe 2, a steam condensate main pipe 4 and a plurality of distillation tower reboilers 3. The plurality of distillation tower reboilers 3 are connected in parallel between the corresponding steam main pipe 2 and the steam condensate main pipe 4, and the steam in the steam main pipe 2 forms a heat supply coordination with each distillation tower reboiler 3. The device utilizes the waste heat in the steam by utilizing high-temperature steam to heat the distillation tower reboiler 3. After the waste heat is utilized, the waste heat enters the flash tank 5 for flash evaporation separation of gas and liquid, and is recovered separately.

[0022] The air inlet end of the steam main pipe 2 is connected to a high-temperature steam source of a corresponding air pressure, and a flow meter 8, a pressure gauge 9 and a thermometer 10 are provided on the steam main pipe 2. The air outlet end of the steam main pipe 2 is connected in parallel with a plurality of distillation tower reboilers 3.

[0023] The air inlet end of each distillation tower reboiler 3 is connected to the air outlet end of the corresponding steam main pipe 2 through a valve 11 and a flow meter 8, and the liquid outlet end of each distillation tower reboiler 3 is connected in parallel to the same corresponding steam condensate main pipe 4.

[0024] The steam condensate main pipe 4 is provided with a pressure gauge 9 and a thermometer 10 , and the liquid outlet of the steam condensate main pipe 4 is connected to the liquid inlet of the flash tank 5 through a flow meter 8 .

[0025] The flash tank 5 is provided with a pressure gauge 9 and a liquid level gauge 12 .

[0026] The upper gas phase pipe of the flash tank 5 is connected to the steam recovery pipe 6 through a flow meter 8 , and the lower liquid phase pipe of the flash tank 5 is connected to the steam condensate recovery pipe 7 through a flow meter 8 .

[0027] The number of the waste heat recovery module 1 is at least one, and the specific number is set according to the number of high-temperature steam sources.

[0028] There is at least one distillation tower reboiler 3 in each waste heat recovery module 1. The specific number is set according to the distillation tower reboiler 3 corresponding to the high-temperature steam source as required.

[0029] like Figure 1 As shown, as a preferred embodiment 2, a flow meter 8 (F1), a pressure gauge 9 (P1), and a thermometer 10 (T1) are provided on the 10 MPAG steam main pipe 1 (S1) of a waste heat recovery module 1. When the system operates normally, the flow range of the flow meter 8 (F1) is 20210 kg / h-48510 kg / h, the pressure range of the pressure gauge 9 (P1) is 0.95 MPAG -1.05 MPAG, and the temperature range of the thermometer 10 (T1) is 182.05°C-186.08°C.

[0030] The 5 MPAG steam main pipe 1 (S2) is provided with a flow meter 8 (F2), a pressure gauge 9 (P2) and a thermometer 10 (T2). When the system operates normally, the flow range of the flow meter 8 (F2) is 5935kg / h-14260kg / h, the pressure range of the pressure gauge 9 (P2) is 0.48 MPAG -0.52 MPAG, and the temperature range of the thermometer 10 (T2) is 157.5℃-160.1℃.

[0031] Flow meters 8 (F3) and (F4) are provided on the steam inlet pipelines of the distillation tower reboilers 3 (E1A) and (E1B). When the system operates normally, the flow range of the flow meter 8 (F3) is 9645 kg / h-23150 kg / h, and the flow range of the flow meter 8 (F4) is 9645 kg / h-23150 kg / h.

[0032] A flow meter 8 (F5) is provided on the steam inlet pipeline of the distillation tower reboiler 3 (E2). When the system operates normally, the flow range of the flow meter 8 (F5) is 920 kg / h - 2210 kg / h.

[0033] A flow meter 8 (F6) is provided on the steam inlet pipeline of the distillation tower reboiler 3 (E3). When the system operates normally, the flow range of the flow meter 8 (F6) is 2100 kg / h - 5050 kg / h.

[0034] A flow meter 8 (F7) is provided on the steam inlet pipeline of the distillation tower reboiler 3 (E4). When the system operates normally, the flow range of the flow meter 8 (F7) is 1025 kg / h - 2460 kg / h.

[0035] A flow meter 8 (F8) is provided on the steam inlet pipeline of the distillation tower reboiler 3 (E5). When the system operates normally, the flow range of the flow meter 8 (F8) is 1090 kg / h - 2620 kg / h.

[0036] A flow meter 8 (F9) is provided on the steam inlet pipeline of the distillation tower reboiler 3 (E6). When the system operates normally, the flow range of the flow meter 8 (F9) is 920 kg / h - 2210 kg / h.

[0037] A flow meter 8 (F10) is provided on the steam inlet pipeline of the distillation tower reboiler 3 (E7). When the system operates normally, the flow range of the flow meter 8 (F10) is 800 kg / h - 1920 kg / h.

[0038] The 10 MPAG steam condensate main pipe 4 (C1) is provided with a flow meter 8 (F11), a pressure gauge 9 (P3) and a thermometer 10 (T3). When the system is operating normally, the flow range of the flow meter 8 (F11) is 20210 kg / h-48510 kg / h, the pressure range of the pressure gauge 9 (P3) is 0.68 MPAG-0.72 MPAG, and the temperature range of the thermometer 10 (T3) is 169.4°C-171.5°C.

[0039] The 5 MPAG steam condensate main pipe 4 (C2) is provided with a flow meter 8 (F12), a pressure gauge 9 (P4) and a thermometer 10 (T4). When the system is operating normally, the flow range of the flow meter 8 (F12) is 5935kg / h-14260kg / h, the pressure range of the pressure gauge 9 (P4) is 0.29 MPAG -0.31 MPAG, and the temperature range of the thermometer 10 (T4) is 142.7℃-144.5℃.

[0040] The 2 MPAG flash tank 55 (V1) is provided with a pressure gauge 9 (P5) and a liquid level gauge 12 (L1). When the system operates normally, the pressure of the pressure gauge 9 (P5) is 0.2 MPAG, and the liquid level range of the liquid level gauge 12 (L1) is 1%-20% of the tank liquid level range.

[0041] The 2 MPAG steam recovery pipe 6 is provided with a flow meter 8 (F13). When the system operates normally, the flow range of the flow meter 8 (F13) is 6622.9 kg / h -16102.5 kg / h.

[0042] The 2 MPAG steam condensate recovery pipe 7 (C3) is provided with a flow meter 8 (F14). When the system operates normally, the flow range of the flow meter 8 (F14) is 19522.03 kg / h -46667.53 kg / h.

[0043] As a preferred embodiment 3, based on embodiment 2, the steam recovery data of the distillation system of this system under the conditions of designed minimum load (50%) and maximum load (120%) are compared with the conventional process as follows:

[0044]

[0045] The working principle of this utility model:

[0046] The utility model uses multiple waste heat recovery modules 1 to correspond to high-temperature steam of different pressures respectively, and absorbs heat through a plurality of distillation tower reboilers 3 in the module, so that the high-quality heat of the high-temperature steam is used for the operation of the distillation tower, and the waste heat of the high-temperature steam is used to reduce the temperature of the steam condensate generated subsequently; the steam condensate generated by the multiple waste heat recovery modules 1 is all passed into the flash tank 5, and the saturated gas and saturated liquid are separated by flash evaporation and recovered for utilization respectively, and the low-quality heat in the steam condensate is recovered, thereby solving the problem of waste heat of high-temperature hot water.

Claims

1. A waste heat recovery system for production of an organosilicon distillation device, comprising a flash tank (5), characterized in that: The liquid inlet end of the flash tank (5) is connected in parallel with a plurality of waste heat recovery modules (1), and the air inlet end of each waste heat recovery module (1) is connected to a high-temperature steam source of a corresponding air pressure; Each of the waste heat recovery modules (1) comprises a steam main pipe (2), a steam condensate main pipe (4) and a plurality of distillation tower reboilers (3); the plurality of distillation tower reboilers (3) are connected in parallel between the corresponding steam main pipe (2) and the steam condensate main pipe (4), and the steam in the steam main pipe (2) forms a heat supply coordination with each distillation tower reboiler (3).

2. The waste heat recovery system for production of an organosilicon distillation device according to claim 1, characterized in that: The air inlet end of the steam main pipe (2) is connected to a high-temperature steam source of corresponding air pressure, and a flow meter (8), a pressure gauge (9) and a thermometer (10) are provided on the steam main pipe (2). The air outlet end of the steam main pipe (2) is connected in parallel to a plurality of distillation tower reboilers (3).

3. The waste heat recovery system for production of an organosilicon distillation device according to claim 2, characterized in that: The gas inlet end of each distillation tower reboiler (3) is connected to the gas outlet end of the corresponding steam main pipe (2) through a valve (11) and a flow meter (8), and the liquid outlet end of each distillation tower reboiler (3) is connected in parallel to the same corresponding steam condensate main pipe (4).

4. The waste heat recovery system for production of an organosilicon distillation device according to claim 3, characterized in that: The steam condensate main pipe (4) is provided with a pressure gauge (9) and a thermometer (10), and the liquid outlet end of the steam condensate main pipe (4) is connected to the liquid inlet end of the flash tank (5) via a flow meter (8).

5. The waste heat recovery system for production of organosilicon distillation device according to claim 4, characterized in that: The flash tank (5) is provided with a pressure gauge (9) and a liquid level gauge (12).

6. The waste heat recovery system for production of an organosilicon distillation device according to claim 5, characterized in that: The upper gas phase pipe of the flash tank (5) is connected to the steam recovery pipe (6) through a flow meter (8), and the lower liquid phase pipe of the flash tank (5) is connected to the steam condensate recovery pipe (7) through a flow meter (8).

7. The waste heat recovery system for production of an organosilicon distillation device according to any one of claims 1 to 6, characterized in that: The number of the waste heat recovery module (1) is at least one.

8. The waste heat recovery system for production of organosilicon rectification device according to claim 7, characterized in that: The number of the distillation tower reboiler (3) in each of the waste heat recovery modules (1) is at least one.

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