Device for reducing storage temperature and pressure of ultra-pure ammonia
By designing devices of heavy-weight de-light de-tube, light-weight de-tube, flash tank and reboiler in the ultrapure ammonia production process, using compressed high-temperature ammonia to provide heat source, reducing the storage temperature and pressure of ultrapure ammonia, solving high-pressure storage The problems of safety risks and high energy consumption have achieved reduced power consumption and improved safety.
Patent Information
- Application Number
- CN202323618202.6
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2023-12-29
- Publication Date
- 2024-12-27
- Estimated Expiration
- 2033-12-29
AI Technical Summary
In the existing ultrapure ammonia production process, high-voltage storage has safety risks and high energy consumption, especially the refrigerated water cooling scheme consumes high power and is expensive in equipment.
Design a device, including a de-heavy tower, a de-light tower, a flash tank, a reboiler and a compressor, provides a heat source by providing a high-temperature ammonia after compression, reduces the storage temperature and pressure of ultrapure ammonia, and reduces the amount of frozen water and electricity consumption. .
It achieves a reduction in power consumption, reduces the hot water consumption of the de-heating tower reboiler, reduces the power consumption, reduces the temperature and pressure of ultra-pure ammonia storage, and improves safety.
Smart Images
Figure CN222238825U_ABST
Abstract
Description
Technical Field
[0001] The utility model relates to ultra-pure ammonia production equipment, in particular to a device for reducing the storage temperature and pressure of ultra-pure ammonia. Background Art
[0002] Ultra-pure ammonia is made from industrial ammonia. It is purified through processes such as adsorption and distillation to remove impurities such as moisture from industrial ammonia to obtain high-purity ammonia.
[0003] The core process of industrial ammonia purification is distillation, which is the process of separating and removing components in a distillation tower according to the different boiling points of different components. Distillation generally involves two distillation towers, one of which is called a de-heavy tower to remove heavy components such as water, heavy metals, and oil with higher boiling points than ammonia, and the other is called a de-light tower to remove light components such as nitrogen, hydrogen, and oxygen with lower boiling points than ammonia. The distillation temperature can be selected at a lower temperature such as -30℃-5℃ distillation. At this time, a lower temperature environment needs to be provided, and ammonia or Freon and other media compression cycle refrigeration are required. The refrigeration process requires more moving equipment and consumes electricity; the distillation temperature can also be selected to be 5℃-15℃. At this time, chilled water is required as the cold source at the top of the distillation tower, and hot water is used as the heat source at the bottom of the tower. Such a process requires more chilled water and the preparation cost of chilled water is also high. A higher distillation temperature can also be selected, such as the distillation temperature of about 50°C or above selected in this technology. In this case, industrial circulating cooling water can be used as a cold source at the top of the tower. After the circulating cooling water is heated, it only needs to be cooled by air before it can be recycled, which is more cost-effective.
[0004] In the process that selects a higher distillation temperature of about 50°C or above, the temperature of the liquid ultra-pure ammonia product is about 48°C and the pressure is about 19 bar, and then it needs to be stored in the ultra-pure ammonia product storage tank. Due to the high pressure, if it is directly stored in the storage tank, the design pressure of the storage tank is high and the cost is high. At the same time, ammonia is flammable and toxic. If the storage pressure is too high, there will be certain safety risks in the event of leakage. The conventional solution is to use chilled water at a temperature of 5°C to cool the ultra-pure ammonia product, cool the ultra-pure ammonia product to about 10°C and reduce the pressure to about 6 bar before storing it in the ultra-pure ammonia product storage tank. However, the chilled water cooling solution requires the configuration of a chiller, which consumes electricity to produce chilled water, and has high energy consumption. Utility Model Content
[0005] The utility model aims to provide a device for reducing the storage temperature and pressure of ultrapure ammonia, which helps to reduce power consumption and reduce the amount of hot water used in the reboiler of the deweighting tower.
[0006] The technical solution of the utility model is: a device for reducing the storage temperature and pressure of ultra-pure ammonia, comprising a deweighting tower, the top of the deweighting tower is connected to a deweighting tower water condenser, the gas phase output end of the deweighting tower water condenser is connected to a lightness removing tower, the bottom of the lightness removing tower is connected to a flash tank via a pipeline, the bottom of the lightness removing tower is also connected to a first lightness removing tower reboiler and a second lightness removing tower reboiler in parallel, the cooling output end of the second lightness removing tower reboiler is connected to the flash tank, the gaseous output end of the flash tank is connected to a heat source input end of the second lightness removing tower reboiler via a compressor, and the bottom of the flash tank is provided with a liquid phase output pipeline for connecting to an ultra-pure ammonia storage tank.
[0007] Furthermore, a raw material input pipe is arranged in the middle of the deweighting tower, and a waste ammonia output pipe for connecting with the waste ammonia pipe is arranged at the bottom of the deweighting tower.
[0008] Furthermore, the liquid phase output end of the deweighting tower water condenser is connected to the top of the deweighting tower.
[0009] Furthermore, a deweighting tower reboiler is also provided at the bottom of the deweighting tower, and a gas phase pipeline of the deweighting tower reboiler is connected to the deweighting tower.
[0010] Furthermore, the gas phase output end of the lightness removal tower top is connected to a lightness removal tower condenser, the gas phase output end of the lightness removal tower condenser is connected to a deammonification absorption system, and the liquid phase output end of the lightness removal tower condenser is connected to the top of the lightness removal tower.
[0011] Furthermore, a first liquid phase output pipeline and a second liquid phase output pipeline are provided at the bottom of the light-removal tower, the first liquid phase output pipeline is connected to the flash tank, the second liquid phase output pipeline is respectively connected to the first light-removal tower reboiler and the second light-removal tower reboiler, and the gas phase output ends of the first light-removal tower reboiler and the second light-removal tower reboiler are respectively connected to the bottom of the light-removal tower.
[0012] Furthermore, the heat source input into the heat source input end of the first light removal tower reboiler is hot water.
[0013] Compared with the prior art, the utility model has the following advantages:
[0014] The device does not use chilled water, which reduces power consumption. At the same time, the compressed high-temperature ammonia is used as a partial heat source for the reboiler at the bottom of the de-weighting tower, reducing the amount of hot water used in the reboiler. For example, in a process with an annual output of 10,000 tons of ultra-pure ammonia, the amount of 80°C hot water can be reduced by about 2t / h; if a chiller with a power of about 30kw is used and the additional compressor power is about 20kw, the power consumption is reduced by 10kw·h / h. BRIEF DESCRIPTION OF THE DRAWINGS
[0015] Figure 1 It is a schematic diagram of the structure of the utility model;
[0016] Figure 2 For the utility model Figure 1 A partial enlarged view of
[0017] In the figure: T1-de-weight removal tower T11-raw material input pipe T12-waste ammonia output pipe T2-de-lightness removal tower T21-first liquid phase output pipeline T22-second liquid phase output pipeline E2-de-weight removal tower water condenser E3-de-weight removal tower reboiler E4-de-lightness removal tower condenser E41-gas phase output end E5-first lightness removal tower reboiler E6-second lightness removal tower reboiler V1-flash tank V11-liquid phase output pipeline C1-compressor. DETAILED DESCRIPTION
[0018] In order to make the above features and advantages of the present invention more understandable, embodiments are given below with reference to the accompanying drawings for detailed description, but the present invention is not limited thereto.
[0019] refer to Figure 1 to Figure 2
[0020] A device for reducing the storage temperature and pressure of ultra-pure ammonia comprises a de-weighting tower T1, the top of the de-weighting tower is connected to a de-weighting tower water condenser E2, the gas phase output end of the de-weighting tower water condenser is connected to a lightness-removing tower T2, the liquid phase output end of the de-weighting tower water condenser is connected to the top of the de-weighting tower, the bottom of the lightness-removing tower is connected to a flash tank V1 via a pipeline, the bottom of the lightness-removing tower is also connected to a first lightness-removing tower reboiler E5 and a second lightness-removing tower reboiler E6 connected in parallel, the cooling output end of the second lightness-removing tower reboiler is connected to the flash tank V1, the gaseous output end of the flash tank is connected to a heat source input end of the second lightness-removing tower reboiler via a compressor C1, and the bottom of the flash tank is provided with a liquid phase output pipeline V11 for connecting to an ultra-pure ammonia storage tank.
[0021] In this embodiment, a raw material input pipe T11 is provided in the middle of the deweighting tower, and a waste ammonia output pipe T12 for connecting with the waste ammonia pipe is provided at the bottom of the deweighting tower.
[0022] In this embodiment, a deweighting tower reboiler E3 is further provided at the bottom of the deweighting tower, and a gas phase pipeline of the deweighting tower reboiler is connected to the bottom of the deweighting tower.
[0023] In this embodiment, the gas phase output end of the top of the light-removal tower is connected to the light-removal tower condenser E4, the gas phase output end E41 of the light-removal tower condenser is connected to the deammonia absorption system, and the liquid phase output end of the light-removal tower condenser is connected to the top of the light-removal tower.
[0024] In this embodiment, the bottom of the light-removal tower is provided with a first liquid phase output pipeline T21 and a second liquid phase output pipeline T22, the first liquid phase output pipeline is connected to the flash tank, the second liquid phase output pipeline is respectively connected to the first light-removal tower reboiler and the second light-removal tower reboiler, and the gas phase output ends of the first light-removal tower reboiler and the second light-removal tower reboiler are respectively connected to the bottom of the light-removal tower.
[0025] In this embodiment, the heat source input to the heat source input end of the first light removal tower reboiler is hot water.
[0026] The specific implementation method is:
[0027] The raw ammonia gas is fed into the middle part of the de-weighting tower T1, and gas-liquid mass transfer is carried out in the tower to remove the heavy components. The top of the de-weighting tower is the ammonia gas for removing the heavy components. After it is partially liquefied by the de-weighting tower condenser E2, the liquid phase refluxes to the top of the de-weighting tower by gravity, and the gas phase enters the middle part of the de-lighting tower T2 to remove the light components.
[0028] The material undergoes gas-liquid mass transfer in the light-removal tower T2. The top of the light-removal tower is ammonia containing light component impurities. After being cooled by the light-removal tower condenser E4, the gas phase is sent out of the boundary area and connected to the ammonia removal absorption system (absorbed by water), and the liquid phase is returned to the top of the light-removal tower as reflux. The tower bottom is the output of ultra-pure ammonia product.
[0029] The ultra-pure ammonia product with a temperature of about 50°C and a pressure of 19 bar first enters the flash tank V1, where the ultra-pure ammonia product is partially vaporized and flashed, the pressure is reduced to 6ar, and the temperature is reduced to 10°C. The 10°C liquid in the flash tank is drawn out from the bottom and sent to the ultra-pure ammonia storage tank for storage.
[0030] The flash tank produces about 260Nm³ / h of gaseous ammonia which is drawn out from the top and enters compressor C1 for compression to 29bar. After compression, the temperature rises to about 120℃.
[0031] A portion of the liquid ammonia at the bottom of the light-removing tower enters the first light-removing tower reboiler E5, and a portion of the liquid ammonia at the bottom of the light-removing tower enters the second light-removing tower reboiler E6 to be heated and vaporized and returned to the light-removing tower. The first light-removing tower reboiler E5 uses hot water as a heat source, and the second light-removing tower reboiler E6 uses high-temperature ammonia from the compressor C1 as a heat source. The ammonia as a heat source is cooled to about 65°C in the second light-removing tower reboiler E6 and then returned to the flash tank V1 for flash evaporation to reduce temperature and pressure.
[0032] If the words "first", "second" and the like are used in the above-mentioned utility model to limit components, those skilled in the art should know that the use of "first" and "second" is only for the convenience of description to distinguish the components. Unless otherwise stated, the above-mentioned words have no special meaning.
[0033] If the present invention discloses or involves components or structures that are fixedly connected to each other, then, unless otherwise stated, the fixed connection can be understood as: a detachable fixed connection (for example, connection using bolts or screws), and can also be understood as: a non-detachable fixed connection (for example, riveting, welding). Of course, the fixed connection to each other can also be replaced by an integrated structure (for example, manufactured by one-piece molding using a casting process) (except where it is obviously impossible to use an one-piece molding process).
[0034] In addition, unless otherwise stated, the terms used to indicate positional relationships or shapes in any of the technical solutions disclosed in the above utility model include states or shapes that are approximate, similar or close thereto.
[0035] Any component provided by the utility model can be assembled from multiple separate components, or can be a separate component manufactured by an integrated molding process.
[0036] The above description is only a preferred embodiment of the present invention. All equivalent changes and modifications made according to the scope of the patent application of the present invention should fall within the scope of the present invention.
Claims
1. A device for reducing the storage temperature and pressure of ultrapure ammonia, comprising a deweighting tower, characterized in that: The top of the de-weighting tower is connected to a de-weighting tower water condenser, the gas phase output end of the de-weighting tower water condenser is connected to a lightness-removing tower, the bottom of the lightness-removing tower is connected to a flash tank via a pipeline, the bottom of the lightness-removing tower is also connected to a first lightness-removing tower reboiler and a second lightness-removing tower reboiler in parallel, the cooling output end of the second lightness-removing tower reboiler is connected to the flash tank, the gaseous output end of the flash tank is connected to a heat source input end of the second lightness-removing tower reboiler via a compressor, and a liquid phase output pipeline for connecting to an ultra-pure ammonia storage tank is provided at the bottom of the flash tank.
2. The device for reducing the storage temperature and pressure of ultra-pure ammonia according to claim 1, characterized in that: A raw material input pipe is arranged in the middle of the de-weighting tower, and a waste ammonia output pipe for connecting with the waste ammonia pipe is arranged at the bottom of the de-weighting tower.
3. The device for reducing the storage temperature and pressure of ultrapure ammonia according to claim 1 or 2, characterized in that: The liquid phase output end of the deweighting tower water condenser is connected to the top of the deweighting tower.
4. The device for reducing the storage temperature and pressure of ultra-pure ammonia according to claim 1, characterized in that: A de-weighting tower reboiler is also provided at the bottom of the de-weighting tower, and a gas phase pipeline of the de-weighting tower reboiler is connected to the de-weighting tower.
5. The device for reducing the storage temperature and pressure of ultrapure ammonia according to claim 1, 2 or 4, characterized in that: The gas phase output end of the lightness removal tower top is connected to a lightness removal tower condenser, the gas phase output end of the lightness removal tower condenser is connected to a deammoniation absorption system, and the liquid phase output end of the lightness removal tower condenser is connected to the top of the lightness removal tower.
6. The device for reducing the storage temperature and pressure of ultrapure ammonia according to claim 1, characterized in that: The bottom of the light-removal tower is provided with a first liquid phase output pipeline and a second liquid phase output pipeline, the first liquid phase output pipeline is connected to a flash tank, the second liquid phase output pipeline is respectively connected to the first light-removal tower reboiler and the second light-removal tower reboiler, and the gas phase output ends of the first light-removal tower reboiler and the second light-removal tower reboiler are respectively connected to the bottom of the light-removal tower.
7. The device for reducing the storage temperature and pressure of ultrapure ammonia according to claim 1 or 6, characterized in that: The heat source input into the heat source input end of the first light removal tower reboiler is hot water.