Hydrocarbon waste liquid vaporization process and device

Abstract

The invention provides a hydrocarbon waste liquid vaporization process and device, hydrocarbon gases such as butane and butene separated from methyl chloride synthesized by organic silicon monomers are pressurized and cooled into liquid, sent to a storage tank for storage, vaporized by a waste liquid vaporization device, and sent to an incineration device for stable combustion by controlling the liquid level of the vaporization device and the pressure of a gas phase outlet. The hydrocarbon waste liquid vaporization device can vaporize hydrocarbon waste liquid in an active mode, steam serves as a heating medium, the vaporization process is stable and safe, it is ensured that the hydrocarbon waste liquid is completely vaporized, meanwhile, condensed impurities in liquid hydrocarbons are removed in a precipitation mode, and the hydrocarbon gas quality is improved while efficient vaporization is conducted; hydrocarbon waste liquid flow input, the liquid level of the vaporizer and hydrocarbon waste liquid gas phase pressure are controlled through the self-control valve, stable operation of the vaporizing system is ensured, the combustion flame shape of the incineration device is stable, and combustion is more sufficient; the vaporizer adopts a coaxial sleeve type structure, is pressure-resistant and shock-resistant, is not easy to deform and block, performs forced convection heat exchange, and saves the heat exchange area.

Description

Technical Field

[0001] The present invention relates to the fields of silicone production, environmental protection treatment and chemical equipment, and particularly relates to a vaporizer and a vaporization system. Background Art

[0002] With the rapid development of the economy and the improvement of silicone monomer synthesis technology, a small amount of hydrocarbon heavy fraction impurities such as butane and butene are by-produced during the synthesis process. During the chlorosilane synthesis process, in order to avoid the participation of heavy fraction impurities in the reaction, resulting in an increase in side reactions in the monomer synthesis reaction, and to avoid scaling on the tubes of the chloromethane vaporizer and superheater, affecting the vaporization effect and reducing the maintenance frequency of cleaning the tubes, it is necessary to separate the heavy fraction impurities.

[0003] The separated hydrocarbon waste liquid contains butane, butene, chloromethane, silane, silicon powder and rust, etc. It has a complex composition and is flammable and explosive. It is a highly dangerous substance and needs to be treated in time. It can be incinerated to by-produce steam. To ensure the safety and full combustion of the waste liquid incineration, it is necessary to vaporize the waste liquid. Summary of the Invention

[0004] In order to ensure that the hydrocarbon waste liquid can be safely and stably incinerated after being completely vaporized, it is necessary to provide a hydrocarbon waste liquid vaporization process and device.

[0005] An object of the present invention is to provide a hydrocarbon waste liquid vaporization device. The vaporizer shell body includes at least two outer heat exchange tubes, at least two inner heat exchange tubes, a tube sheet, a spacer tube, an upper head flat cover, a lower head transition plate, a lower head tube sheet, etc.; The outer heat exchange tube is sleeved outside the inner heat exchange tube to form a set of coaxial sleeve structures; among them, the outer heat exchange tube can be a steel pipe with a diameter of φ32*2.5~φ45*3.5mm, and the inner heat exchange tube can be a steel pipe with a diameter of φ18*2.0~φ32*2.5mm. The verticality deviation of the steel pipe is not more than 2mm; the distance between the inner wall of the outer heat exchange tube and the outer wall of the inner tube is between 5 and 10mm; the top of the outer heat exchange tube is sealed by welding a tube cap or a flat plate, and the top of the inner heat exchange tube is open; a distance of 50~100mm is reserved between the top of the outer heat exchange tube and the top of the inner heat exchange tube.

[0006] The inner heat exchange tube is welded to the lower head transition plate and is fixedly welded to the vaporizer shell body; the outer heat exchange tubes are welded to each other by a tube sheet, and are fixed in position by screwing and fastening with a spacer tube. The outer heat exchange tube is welded to the lower head tube sheet.

[0007] Both the upper head flat cover and the lower head tube sheet are fastened by flange bolts, which is convenient for disassembly, inspection and maintenance. A wire mesh demister is arranged below the upper head flat cover, and the wire mesh demister is laid on a support plate. The support plate is bolted to the vaporizer shell body; A liquid-phase thermometer, a vaporizer gas-phase pressure gauge, and a vaporizer liquid-level gauge are installed on the vaporizer housing.

[0008] A hydrocarbon waste liquid delivery pipeline is provided on the side of the vaporizer housing. A waste liquid input flowmeter, a waste liquid input thermometer, a waste liquid input pressure gauge, and a waste liquid input regulating valve are provided on the delivery pipeline.

[0009] A gas-phase waste liquid discharge pipe is provided on the top of the vaporizer housing. A safety valve is installed on the gas-phase discharge pipe. A gas-phase output thermometer, a gas-phase output pressure gauge, and a gas-phase output regulating valve are provided on the gas-phase waste liquid discharge pipe.

[0010] A heat medium steam delivery pipeline is provided at the bottom of the vaporizer housing. A steam pressure gauge, a steam thermometer, and a steam input regulating valve are provided on the pipeline.

[0011] A steam condensate discharge pipe is provided between the lower head tube sheet and the lower head transition plate. A steam trap is provided on the steam condensate discharge pipe.

[0012] A nitrogen pipeline is provided on the vaporizer housing. A vaporizer nitrogen protection switch valve is provided on the pipeline. The vaporizer nitrogen protection switch valve is in loop control with the vaporizer gas-phase pressure gauge. Nitrogen purging is provided on the hydrocarbon waste liquid pipeline and is transported through the pipeline. A nitrogen purging switch valve and a check valve are provided on the pipeline.

[0013] Another technical solution of the present invention is to provide a hydrocarbon waste liquid vaporization process, and its steps are as follows: The hydrocarbon waste liquid with a pressure of 0.3 Mpa to 0.5 Mpa and a temperature ≤ 40 °C transported from the front-end device storage tank through the pipeline enters the side of the vaporizer housing by adjusting the waste liquid input flow rate (100 - 800 kg / h) through the waste liquid input regulating valve. The heat medium steam enters from the lower part of the vaporizer housing, passes through the inner tube of the coaxial sleeve type heat exchange tube, and then to the outer tube of the heat exchange tube to heat the hydrocarbon waste liquid in the shell side. After being heated, the hydrocarbon waste liquid is vaporized into a gas phase, and then the gas-phase pressure (30 - 80 kpa) is controlled through the gas-phase output regulating valve. The gas-phase waste liquid is sent to the burner for incineration treatment under positive pressure through the pipeline.

[0014] The components of the hydrocarbon waste liquid contain 90 - 92% butane, 6 - 8% butene, 0.4 - 0.6% chloromethane, 0.6 - 1.0% silane, and may inevitably also contain a small amount of silicon powder, rust, etc. The waste liquid in the vaporizer is controlled at 45 - 60 °C and 0.25 - 0.3 Mpa (G). At this time, n-butane, butene, and chloromethane are vaporized into a gaseous state, and other silane, silicon powder, rust, etc. remain in the liquid phase part, ensuring thorough separation of hydrocarbons and impurities, effectively removing other impurities entrained in the waste liquid, ensuring the quality of hydrocarbons in the gas phase, and ensuring stable incineration.

[0015] The heat medium is 0.18 - 0.2 Mpa (G) saturated steam. It exchanges heat with the hydrocarbon waste liquid in a convective manner through the inner and outer tubes of the heat exchange tubes, heating the hydrocarbon waste liquid to 45 - 60 °C. The pressure in the vaporizer shell is maintained at 0.25 - 0.3 Mpa (G), with stable vaporization. Moreover, convective heat exchange can significantly reduce the heat exchange area and shrink the volume of the vaporizer. The vaporizer adopts a coaxial sleeve structure. The saturated steam in the inner tube heats the steam-water mixture flowing reversely in the outer tube during the upward process, and the steam-water mixture in the outer tube transfers heat evenly to the liquid and gas waste liquids (outside the tube bundle) in the vaporizer shell in a convective manner. The liquid waste liquid vaporizes after absorbing heat to ensure stable vaporization, and the gas phase is reheated to maintain complete vaporization and a uniform temperature (when the liquid feed rate and steam rate of the waste liquid are constant, the maximum deviation of the gas phase temperature of the waste liquid is ±0.5 °C). A PID loop is set for the vaporizer liquid temperature and the steam input regulating valve to control the vaporization rate. And using steam as the heat medium is safer than electric heating.

[0016] After vaporization, part of the entrained liquid droplets of the hydrocarbon waste liquid is separated by a wire mesh demister. The opening of the gas phase output regulating valve is adjusted to control the gas phase pressure at 30 - 80 kpa, and it is transported to the incinerator for incineration treatment through a pipeline. The wire mesh demister is made of stainless steel, with a diameter 20 - 50 mm smaller than the diameter of the vaporizer shell and a thickness of 5 - 10 mm.

[0017] The waste liquid input flowmeter and the waste liquid input regulating valve form an automatic control loop to input the hydrocarbon waste liquid (100 - 800 kg / h) for vaporization; the gas phase output pressure and the gas phase output regulating valve form an automatic control loop to control the stability of the hydrocarbon gas phase output pressure (30 - 80 kpa); the vaporizer liquid level (0 - 500 mm) and the steam input regulating valve (100 - 300 kg / h) form an automatic control loop. An interlock for high-high liquid level (≥440 mm) is set for the vaporizer liquid level and the waste liquid input regulating valve to control the liquid level in the vaporizer; an interlock for low-low pressure (≤30 kpa) is set for the vaporizer gas phase pressure and the nitrogen protection switch valve of the vaporizer. A safety valve is installed at the top of the vaporizer. When the gas phase pressure is too high (≥0.5 Mpa), the safety valve opens for safety pressure relief to ensure the safety of the vaporizer.

[0018] Technical advantages of the present invention: The components of the hydrocarbon waste liquid are complex. Saturated vapor pressures of butane, butene, chloromethane, etc. are relatively low, and they are active. During liquid atomization incineration, the gas expands at the burner outlet, the incineration flame is not concentrated, and it is prone to flameout. Also, when the furnace is shut down, there is residual combustible liquid in the pipeline, which is prone to backfire phenomenon, presenting potential safety hazards. Using a vaporizer to heat and vaporize the hydrocarbon waste liquid, the vaporization process is stable and controlled. After vaporization, the gaseous waste is fed into incineration treatment with stable pressure, which is safer, the incineration process is more stable, the combustion is more complete, avoiding backfire and flameout of the burner, and a large amount of recoverable steam with calorific value can be obtained from the hydrocarbon incineration; the remaining silane after vaporization is returned to the upstream device for refining and recovery.

[0019] Since hydrocarbon waste liquid is a flammable and explosive substance, using a steam heating vaporizer is safer than methods such as electric heating or oil bath heating. The vaporizer adopts a coaxial sleeve structure, with a stable temperature rise process, avoiding sudden rises and falls in the liquid phase temperature of the hydrocarbon waste liquid, and stable vaporization control. The heating medium steam flows through the tube side, and the hydrocarbon waste liquid flows through the shell side, which is better for monitoring the liquid level of the hydrocarbon waste liquid.

[0020] A wire mesh demister is installed in the vaporizer to further separate the small liquid droplets entrained in the gas phase, ensuring the safety of subsequent incineration.

[0021] This hydrocarbon waste liquid vaporization device can vaporize hydrocarbon waste liquid in the active mode, using steam as the heating medium. The vaporization process is stable and safe, ensuring complete vaporization of the hydrocarbon waste liquid. At the same time, impurities condensed in the liquid hydrocarbon are removed by precipitation, improving the quality of the hydrocarbon gas while achieving efficient vaporization. The flow rate of the hydrocarbon waste liquid input, the liquid level of the vaporizer, and the gas phase pressure of the hydrocarbon waste liquid are controlled by self-control valves to ensure the stable operation of the vaporization system, the stable shape of the combustion flame of the incineration device, and more complete combustion. The vaporizer adopts a coaxial sleeve structure, with high pressure resistance and earthquake resistance, not easily deformed or blocked, high safety, and forced convection heat transfer, saving the heat transfer area. Description of the Drawings Figure 1 It is the process flow diagram of the hydrocarbon waste liquid vaporization process.

[0022] Figure 2 is Figure 1 The top view of the heat exchange tube and the spacer tube.

[0023] Figure 3 is Figure 1 The connection part diagram of the heat exchange tubes.

[0024] Figure 4 is Figure 1 The connection part diagram of the spacer tubes.

[0025] In the figure: 1. Vaporizer shell; 2. Outer tube of the heat exchange tube; 3. Inner tube of the heat exchange tube; 4. Manhole cover; 5. Spacer tube; 6. Wire mesh demister; 7. Upper head flat cover; 8. Lower head tube sheet; 9. Waste liquid input regulating valve; 10. Liquid phase thermometer; 11. Vaporizer gas phase pressure gauge; 12. Vaporizer liquid level gauge; 13. Waste liquid input flowmeter; 14. Waste liquid input thermometer; 15. Waste liquid input pressure gauge; 16. Gas phase output thermometer; 17. Gas phase output pressure gauge; 18. Gas phase output regulating valve; 19. Vaporizer nitrogen protection switch valve; 20. Nitrogen purge switch valve; 21. Safety valve; 22. Steam pressure gauge; 23. Steam thermometer; 24. Steam input regulating valve; 25. Steam trap; 26. Lower head transition plate; 27. Vaporizer base; 28. Support plate. Detailed Embodiments

[0026] Example 1 As Figure 1 shown, the hydrocarbon waste liquid vaporization device mainly includes a vaporizer, a feeding system, a discharging system, a heating system and a nitrogen protection system. The vaporizer is composed of a vaporizer shell 1, an outer heat exchange tube 2, an inner heat exchange tube 3, a perforated plate 4, a spacer tube 5, a wire mesh demister 6, an upper head flat cover 7, a lower head tube sheet 8, a safety valve 21, a lower head transition plate 26 and a vaporizer base 27.

[0027] The outer heat exchange tube is sleeved outside the inner heat exchange tube to form a set of coaxial sleeve structures; among them, the outer heat exchange tube can be a steel pipe with a diameter of φ45*3.5mm, and the inner heat exchange tube can be a steel pipe with a diameter of φ18*2.0. The verticality deviation of the steel pipe is not more than 2mm; the distance between the inner wall of the outer heat exchange tube and the outer wall of the inner tube is within 10mm; the top of the outer heat exchange tube is sealed by welding a pipe cap or a flat plate, and the top of the inner heat exchange tube is open; a 100mm gap is reserved between the top of the outer heat exchange tube and the top of the inner heat exchange tube.

[0028] The hydrocarbon waste liquid (the hydrocarbon waste liquid components contain 92% butane, 7% butene, 0.4% chloromethane, and 0.6% silane) with a pressure of 0.45 Mpa and a temperature of 32 °C transported from the storage tank of the front-end device through a pipeline enters the side of the vaporizer shell 1 by adjusting the opening of the waste liquid input regulating valve 9 to the waste liquid input flowmeter 13 (500 kg / h). The pressure of the vaporizer shell is maintained at 0.25 Mpa; adjusting the opening of the steam input regulating valve to send 200 kg / h of 0.2 Mpa(G) steam into the lower part of the vaporizer shell 1, passing through the inner heat exchange tube 3 of the coaxial sleeve structure, and then to the outer heat exchange tube 2 to heat the hydrocarbon waste liquid in the shell side. After being heated, the hydrocarbon waste liquid is vaporized into a gas phase, and then the gas phase pressure is controlled by the gas phase output regulating valve 18 to be sent to the burner for incineration treatment at a slightly positive pressure of 50 kpa in the pipeline, and the gas phase temperature is at 50 ± 1 °C.

[0029] Example 2 The device structure is basically the same as that of Example 1, only a 50mm gap is reserved between the top of the outer heat exchange tube and the top of the inner heat exchange tube. The hydrocarbon waste liquid vaporization treatment is carried out in the same way as in Example 1. The hydrocarbon waste liquid with a pressure of 0.45 Mpa and a temperature of 32 °C transported through a pipeline from the storage tank of the front-end device (the components of the hydrocarbon waste liquid include 92% butane, 7% butene, 0.4% chloromethane, and 0.6% silane) enters the side of the vaporizer shell 1 through the waste liquid input flowmeter 13 (500 kg / h) by adjusting the opening of the waste liquid input regulating valve 9. The pressure of the vaporizer shell is maintained at 0.25 Mpa; the opening of the steam input regulating valve is adjusted to send 200 kg / h of 0.2 Mpa(G) steam into the lower part of the vaporizer shell 1, passing through the inner tube 3 of the coaxial sleeve type heat exchange tube and then to the outer tube 2 of the heat exchange tube to heat the hydrocarbon waste liquid in the shell side. After being heated, the hydrocarbon waste liquid vaporizes into a gas phase, and then the gas phase pressure is controlled by the gas phase output regulating valve 18 to be sent to the burner for incineration treatment under a slightly positive pressure of 50 kpa in the pipeline. The gas phase temperature is 48 ± 0.5 °C.

[0030] Example 3 The device structure is basically the same as that of Example 1, except that a 200-mm gap is reserved between the top of the outer tube of the heat exchange tube and the top of the inner tube of the heat exchange tube. The hydrocarbon waste liquid vaporization treatment is carried out in the same way as in Example 1. The hydrocarbon waste liquid with a pressure of 0.45 Mpa and a temperature of 32 °C transported through a pipeline from the storage tank of the front-end device (the components of the hydrocarbon waste liquid include 92% butane, 7% butene, 0.4% chloromethane, and 0.6% silane) enters the side of the vaporizer shell 1 through the waste liquid input flowmeter 13 (500 kg / h) by adjusting the opening of the waste liquid input regulating valve 9. The pressure of the vaporizer shell is maintained at 0.25 Mpa; the opening of the steam input regulating valve is adjusted to send 200 kg / h of 0.2 Mpa(G) steam into the lower part of the vaporizer shell 1, passing through the inner tube 3 of the coaxial sleeve type heat exchange tube and then to the outer tube 2 of the heat exchange tube to heat the hydrocarbon waste liquid in the shell side. After being heated, the hydrocarbon waste liquid vaporizes into a gas phase, and the gas phase pressure is controlled by the gas phase output regulating valve 18 to be sent to the burner for incineration treatment under a slightly positive pressure of 50 kpa in the pipeline. The gas phase temperature is 54 ± 3 °C.

[0031] Example 4 The structure of the heat exchange tube is different from that of Example 1, and a single-row tube heat exchanger structure is adopted; among them, the heat exchange tube is a steel pipe with a diameter of φ18*2.0 mm, and the heat exchange area is the same.

[0032] The hydrocarbon waste liquid with a pressure of 0.45 Mpa and a temperature of 32°C transported from the storage tank of the front-end device through a pipeline (the components of the hydrocarbon waste liquid include 92% butane, 7% butene, 0.4% chloromethane, and 0.6% silane) enters the side of the vaporizer shell 1 through the waste liquid input flowmeter 13 (500 kg / h) by adjusting the opening of the waste liquid input regulating valve 9. The pressure of the vaporizer shell is maintained at 0.25 Mpa; the opening of the steam input regulating valve is adjusted to send 200 kg / h of 0.2 Mpa(G) steam into the lower part of the vaporizer shell 1. After being heated by a single-row tubular heat exchanger, the hydrocarbon waste liquid is vaporized into a gas phase, and then the gas phase pressure is controlled by the gas phase output regulating valve 18 and sent to the burner for incineration treatment under a slightly positive pressure of 50 kpa in the pipeline. The gas phase temperature is 58 ± 2°C.

[0033] Through the comparison of Examples 1, 2, and 3, it is found that when the reserved space between the top of the coaxial sleeve type heat exchange tube and the top of the inner tube of the heat exchange tube decreases, the temperature difference of the hydrocarbon waste liquid is smaller, the heating is gentler, the vaporization is more stable, and the temperature difference after the hydrocarbon waste liquid becomes a gas phase is smaller.

[0034] Through the comparison of Example 1 and Example 4, it is found that compared with the straight tube type heat exchanger structure, the coaxial sleeve type heat exchanger has a lower gas phase temperature of the waste liquid, and the vaporization of the waste liquid is stable and easy to control and adjust, which can better avoid the safety risks brought by rapid vaporization.

[0035] The above is only the preferred specific implementation manner of the present invention, but the protection scope of the present invention is not limited thereto. Any person skilled in the art within the technical scope disclosed by the present invention, according to the technical solution of the present invention and its inventive concept, makes equivalent substitutions or changes, and all should be covered within the protection scope of the present invention.

Claims

1. A hydrocarbon waste liquid vaporization device, characterized in that, The vaporizer housing (1) includes at least two outer heat exchange tubes, at least two inner heat exchange tubes, a tube sheet (4), spacer tubes (5), an upper head flat cover (7), a lower head transition plate (26), and a lower head tube sheet (8); The outer heat exchange tube (2) is sleeved outside the inner heat exchange tube (3) to form a coaxial sleeve structure; the distance between the inner wall of the outer heat exchange tube and the outer wall of the inner tube is between 5 and 10 mm; The inner heat exchange tube (3) is welded to the lower head transition plate (26) and is fixedly welded to the vaporizer housing (1); the outer heat exchange tubes (2) are connected by the tube sheet (4) and are thread-fixed through the spacer tubes (5), and the outer heat exchange tube (3) is welded to the lower head transition plate (26).

2. The hydrocarbon waste liquid vaporization device according to claim 1, wherein The upper head flat cover (7) and the lower head tube sheet (8) are fastened by flange bolts; A wire mesh demister (6) is provided below the upper head flat cover (7), and the wire mesh demister (6) is laid on the support plate (28), and the support plate (28) is bolted to the vaporizer housing (1); A gas-phase discharge pipe is provided at the top of the vaporizer housing (1), and a safety valve (21) is installed on the gas-phase discharge pipe; a liquid-phase thermometer (10), a vaporizer gas-phase pressure gauge (11), and a vaporizer liquid level gauge (12) are installed on the vaporizer housing (1).

3. The hydrocarbon waste liquid vaporization device according to claim 1, wherein The top end of the outer heat exchange tube is welded and sealed with a tube cap or a flat plate, and the top end of the inner heat exchange tube is open; a 50-100 mm gap is reserved between the top end of the outer heat exchange tube and the top end of the inner heat exchange tube.

4. The hydrocarbon waste liquid vaporization device according to claim 1, characterized in that, A hydrocarbon waste liquid conveying pipeline is provided on the side of the vaporizer housing (1), and a waste liquid input flowmeter (13), a waste liquid input thermometer (14), a waste liquid input pressure gauge (15), and a waste liquid input regulating valve (9) are provided on the conveying pipeline. A gas-phase waste liquid discharge pipe is provided at the top of the vaporizer housing (1), and a gas-phase output thermometer (16), a gas-phase output pressure gauge (17), and a gas-phase output regulating valve (18) are provided on the gas-phase waste liquid discharge pipe.

5. The hydrocarbon waste liquid vaporization device according to claim 1, wherein A heat medium steam conveying pipeline is provided at the bottom of the vaporizer housing (1), and a steam pressure gauge (22), a steam thermometer (23), and a steam input regulating valve (24) are provided on the pipeline.

6. The hydrocarbon waste liquid vaporization device according to claim 1, characterized in that, A steam condensate discharge pipe is provided between the lower head tube sheet (8) and the lower head transition plate (26), and a steam trap (25) is provided on the steam condensate discharge pipe.

7. The hydrocarbon waste liquid vaporization device according to claim 1, characterized in that, A nitrogen pipeline is provided on the vaporizer housing (1), and a vaporizer nitrogen protection switch valve (19) is provided on the pipeline. The vaporizer nitrogen protection switch valve (19) is in loop control with the vaporizer gas-phase pressure gauge (11). Nitrogen purging is provided on the hydrocarbon waste liquid pipeline and is transported through the pipeline. A nitrogen purging switch valve (20) and a check valve are provided on the pipeline.

8. A hydrocarbon waste liquid vaporization process, which uses the device described in any one of claims 1-7, characterized in that, It includes the following steps: The hydrocarbon waste liquid with a pressure of 0.3 Mpa to 0.5 Mpa and a temperature of ≤ 40°C, transported through a pipeline from the storage tank of the front-end device, enters the vaporizer shell by adjusting the waste liquid input flow rate of 100 to 800 kg / h through the opening of the waste liquid input regulating valve. The heat transfer medium of 100 to 300 kg / h enters from the lower part of the vaporizer shell, passes through the inner pipe of the coaxial sleeve type heat exchange pipe, and then to the outer pipe of the heat exchange pipe to heat the hydrocarbon waste liquid in the shell side. After the hydrocarbon waste liquid is heated to 45 to 60°C, it is vaporized into a gas phase, and then the gas phase pressure of 30 to 80 kpa is controlled by the gas phase output regulating valve. The gas phase waste liquid is sent to the burner for incineration treatment under positive pressure through a pipeline.

9. The hydrocarbon waste liquid vaporization process according to claim 8, wherein, The heat transfer medium uses 0.18 to 0.2 Mpa (G) saturated steam, and convectively exchanges heat with the hydrocarbon waste liquid through the inner pipe and the outer pipe of the heat exchange pipe, heating the hydrocarbon waste liquid to 45 to 60°C. The pressure of the vaporizer shell is maintained at 0.25 to 0.3 Mpa (G).

10. The hydrocarbon waste liquid vaporization process according to claim 8, wherein, The vaporized hydrocarbon waste liquid is separated from part of the entrained droplets by a wire mesh demister. The opening of the gas phase output regulating valve is adjusted to control the gas phase pressure to be 30 to 80 kpa, and it is transported to the incinerator for incineration treatment through a pipeline; the wire mesh demister is made of stainless steel, with a diameter 20 to 50 mm smaller than the diameter of the vaporizer shell and a thickness of 5 to 10 mm.

Images