阅读说明：本技术 一种高效节能的环保型吸氨工艺 (Efficient energy-saving environment-friendly ammonia absorption process ) 是由 赵祥海 相入宣 张井柱 裔传国 霍介方 李磊 刘明 宋志兰 方细康 陈海波 于 2019-08-15 设计创作，主要内容包括：本发明属于环保型吸氨工艺技术领域,尤其为一种高效节能的环保型吸氨工艺,包括如下设备：1#蒸氨塔、1#预热器A、1#预热器B、1#残液换热器、2#蒸氨塔、2#预热器A、2#预热器B、2#残液换热器、母液分离罐、母I桶、氨水回洗水桶、吸收塔、原料泵、回收软水桶、冷却塔,所述1#蒸氨塔内部设置有一个分凝器,所述2#蒸氨塔内部设置有上下分布的两个分凝器,通过MII吸氨改为使用MI吸氨,吸收后的液进入气液分离器分离,液相回MI桶,气相进入尾气净化塔使用淡液净化后排空,逸散出的气氨显著减少,现场环境明显改善,更多的气氨回收到系统,降低了氨耗,增加了效益。(The invention belongs to the technical field of environment-friendly ammonia absorption processes, and particularly relates to an efficient energy-saving environment-friendly ammonia absorption process, which comprises the following equipment: the ammonia recovery system comprises a 1# ammonia still, a 1# preheater A, a 1# preheater B, a 1# raffinate heat exchanger, a 2# ammonia still, a 2# preheater A, a 2# preheater B, a 2# raffinate heat exchanger, a mother liquor separation tank, a mother I bucket, an ammonia water backwashing bucket, an absorption tower, a raw material pump, a soft water recovery bucket and a cooling tower, wherein a dephlegmator is arranged inside the 1# ammonia still, two dephlegmators which are distributed up and down are arranged inside the 2# ammonia still, MI ammonia is used instead of being absorbed through MII ammonia absorption, the absorbed liquid enters a gas-liquid separator for separation, the liquid phase returns to the bucket, the gas phase enters a tail gas purification tower and is emptied after being purified by using fresh liquid, the escaped gas ammonia is remarkably reduced, the field environment is remarkably improved, more gas ammonia is recovered to the system, the ammonia consumption is reduced, and the benefit is increased.)

1. An efficient energy-saving environment-friendly ammonia absorption process comprises the following equipment: 1# ammonia still, 1# preheater A, 1# preheater B, 1# raffinate heat exchanger, 2# ammonia still, 2# preheater A, 2# preheater B, 2# raffinate heat exchanger, mother liquor knockout drum, female I bucket, aqueous ammonia backwash cask, absorption tower, raw material pump, retrieve soft water bucket, cooling tower, 1# ammonia still inside is provided with a dephlegmator, inside two dephlegmators that distribute from top to bottom that are provided with of 2# ammonia still, its characterized in that: the process comprises the following processing steps:

the method comprises the following steps: circulating water enters a dephlegmator in the No. 1 ammonia still from the cooling tower and flows back to the cooling tower through a pipeline to be cooled again; meanwhile, circulating water enters a partial condenser in the No. 2 ammonia still from the cooling tower and flows back to the cooling tower to be cooled again;

step two: low-pressure steam respectively enters a 1# ammonia still and a 2# ammonia still through pipelines, respectively enters the 1# preheater A and the 2# preheater A through pipelines, and respectively leads the steam into a 1# raffinate heat exchanger and a 2# raffinate heat exchanger through pipelines, meanwhile, a raw material pump respectively leads ammonia water into the 1# raffinate heat exchanger and the 2# raffinate heat exchanger through pipelines to heat, and respectively leads the ammonia water into the 1# ammonia still and the 2# ammonia still, meanwhile, the 1# raffinate heat exchanger and the 2# raffinate heat exchanger are respectively provided with pipelines to be connected with soft buckets, and simultaneously, the 1# ammonia still and the 2# ammonia still respectively separate ammonia gas through a dephlegmator and respectively enter the 1# preheater B and the 2# preheater B, and MI respectively enter the 1# preheater B and the 2# preheater B through pipelines, and simultaneously, the low-pressure steam also enters the 1# B, the 2# preheater B through pipelines, A # 2 preheater B, wherein PGL is obtained and enters a mother liquor separation tank through a pipeline;

step three: an emptying pipe is arranged at the upper part of the mother liquor separation tank, the middle part of the emptying pipe is also communicated with a low-pressure steam pipe, the other end of the emptying pipe is connected with an absorption tower, the upper part of the absorption tower is connected with an ammonia recovery soft water bucket through a pipeline, and the bottom of the absorption tower is connected with an ammonia water backwashing water bucket through a pipeline; an emptying pipe B is arranged at the top of the absorption tower for emptying operation;

step four: the bottom of the mother liquor separation tank is also connected with an MI (micro emulsion) barrel through a pipeline, and meanwhile, the bottom of the mother liquor separation tank is also provided with a normal pressure carbonization cleaning pipe reserved head;

step five: the MI barrel is also provided with an MI ammonia purification pump which is communicated with the MI pipeline through a pipeline to form circulation.

2. The high-efficiency energy-saving environment-friendly ammonia absorption process according to claim 1, characterized in that: UVS processes are arranged among connecting pipelines of the low-pressure steam and ammonia distillation tower No. 1, the ammonia distillation tower No. 2, the preheater No. 1, the preheater No. 2, the mother liquid separation tank and the absorption tower.

3. The high-efficiency energy-saving environment-friendly ammonia absorption process according to claim 1, characterized in that: and a circulating water inlet and a circulating water outlet of a partial condenser in the 1# ammonia still are both provided with TIJ, a circulating water inlet and a circulating water outlet of an upper partial condenser in the 2# ammonia still are both provided with TIJ, and pipelines among the 1# raffinate heat exchanger, the 2# raffinate heat exchanger and the soft water barrel are all provided with TIJ.

4. The high-efficiency energy-saving environment-friendly ammonia absorption process according to claim 1, characterized in that: FIC are arranged between the 1# ammonia still, the 1# preheater B, the 2# ammonia still, the 2# preheater B and the low-pressure steam pipeline.

5. The high-efficiency energy-saving environment-friendly ammonia absorption process according to claim 1, characterized in that: the raw material pumps are three.

6. The high-efficiency energy-saving environment-friendly ammonia absorption process according to claim 1, characterized in that: the pipeline between 1# raffinate heat exchanger, 2# raffinate heat exchanger and the soft water bucket all is provided with alarm device, is provided with alarm device between the pipeline that 1# preheater B, 2# preheater B and mother liquor knockout drum are connected, and the pipeline between mother liquor knockout drum and the absorption tower also is provided with alarm device, all is provided with alarm device between the aqueous ammonia backwash cask is connected to the blow-down pipe B of absorption tower on, the absorption tower bottom.

Technical Field

The invention belongs to the technical field of environment-friendly ammonia absorption processes, and particularly relates to an efficient and energy-saving environment-friendly ammonia absorption process.

Background

The ammonia still is an operation device which is subordinate to the desorption tower and volatilizes and releases ammonia dissolved in circulating water through heat transfer of a heat carrier. The method adopts general heat-carrying agent steam as a heating agent, so that the equilibrium steam pressure of ammonia on the liquid level of circulating water is greater than the partial pressure of ammonia in a heat-carrying agent, and vapor-liquid two phases are in countercurrent contact to carry out mass transfer and heat transfer, so that the ammonia is gradually released from the circulating water, a mixture of the ammonia steam and the steam is obtained at the tower top, purer circulating water is obtained at the tower bottom, a tower kettle can adopt direct steam or indirect steam (reboiler) as a heat supply mode, a liquid phase obtained by condensation of a top ammonia dephlegmator directly enters the tower to carry out reflux, and ammonia-rich water after ammonia is evaporated is converted into ammonia evaporation wastewater to flow out from the tower. The ammonia still is divided into a plate tower and a packed tower according to the internal structure. The plate tower is composed of a tower body and a tower internal part (tray), and the commonly used plate tray is provided with a sieve tray and a bubble cap tray; the packed tower consists of tower body, packing layer, liquid distributor, etc. The packed tower is mass transfer equipment with packing in the tower as a gas-liquid two-phase contact member. The packed tower belongs to continuous contact type gas-liquid mass transfer equipment, the composition of two phases continuously changes along the height of the tower, and under the normal operation state, a gas phase is a continuous phase, and a liquid phase is a dispersed phase. The high-concentration ammonia gas distilled from the ammonia still is absorbed by MII, and the absorbed AII enters an AII clarifying tank.

The problems of the prior art are as follows:

the existing ammonia gas has higher temperature, the ammonia absorption reaction releases heat to ensure that the AII temperature is higher, the equilibrium partial pressure of ammonia in liquid surface vapor is high, and the escaped ammonia gas causes environmental pollution and resource waste.

Disclosure of Invention

To solve the problems set forth in the background art described above. The invention provides an efficient energy-saving environment-friendly ammonia absorption process which has the characteristics of reducing gas ammonia, reducing ammonia consumption and increasing benefits.

In order to achieve the purpose, the invention provides the following technical scheme: an efficient energy-saving environment-friendly ammonia absorption process comprises the following equipment: 1# ammonia still, 1# preheater A, 1# preheater B, 1# raffinate heat exchanger, 2# ammonia still, 2# preheater A, 2# preheater B, 2# raffinate heat exchanger, mother liquor knockout drum, female I bucket, aqueous ammonia backwash cask, absorption tower, raw material pump, retrieve soft water bucket, cooling tower, 1# ammonia still inside is provided with a dephlegmator, inside two dephlegmators that distribute from top to bottom that are provided with of 2# ammonia still, its characterized in that: the process comprises the following processing steps:

the method comprises the following steps: circulating water enters a dephlegmator in the No. 1 ammonia still from the cooling tower and flows back to the cooling tower through a pipeline to be cooled again; meanwhile, circulating water enters a partial condenser in the No. 2 ammonia still from the cooling tower and flows back to the cooling tower to be cooled again;

step two: low-pressure steam respectively enters a 1# ammonia still and a 2# ammonia still through pipelines, respectively enters the 1# preheater A and the 2# preheater A through pipelines, and respectively leads the steam into a 1# raffinate heat exchanger and a 2# raffinate heat exchanger through pipelines, meanwhile, a raw material pump respectively leads ammonia water into the 1# raffinate heat exchanger and the 2# raffinate heat exchanger through pipelines to heat, and respectively leads the ammonia water into the 1# ammonia still and the 2# ammonia still, meanwhile, the 1# raffinate heat exchanger and the 2# raffinate heat exchanger are respectively provided with pipelines to be connected with soft buckets, and simultaneously, the 1# ammonia still and the 2# ammonia still respectively separate ammonia gas through a dephlegmator and respectively enter the 1# preheater B and the 2# preheater B, and MI respectively enter the 1# preheater B and the 2# preheater B through pipelines, and simultaneously, the low-pressure steam also enters the 1# B, the 2# preheater B through pipelines, A # 2 preheater B, wherein PGL is obtained and enters a mother liquor separation tank through a pipeline;

step three: an emptying pipe is arranged at the upper part of the mother liquor separation tank, the middle part of the emptying pipe is also communicated with a low-pressure steam pipe, the other end of the emptying pipe is connected with an absorption tower, the upper part of the absorption tower is connected with an ammonia recovery soft water bucket through a pipeline, and the bottom of the absorption tower is connected with an ammonia water backwashing water bucket through a pipeline; an emptying pipe B is arranged at the top of the absorption tower for emptying operation;

step four: the bottom of the mother liquor separation tank is also connected with an MI (micro emulsion) barrel through a pipeline, and meanwhile, the bottom of the mother liquor separation tank is also provided with a normal pressure carbonization cleaning pipe reserved head;

step five: the MI barrel is also provided with an MI ammonia purification pump which is communicated with the MI pipeline through a pipeline to form circulation.

Preferably, the UVS process is provided between the low-pressure steam and the connecting pipelines of the ammonia distillation tower # 1, the ammonia distillation tower # 2, the preheater # 1B, the preheater # 2B, the mother liquor separation tank and the absorption tower.

Preferably, a circulating water inlet and a circulating water outlet of a partial condenser in the 1# ammonia still are both provided with TIJ, a circulating water inlet and a circulating water outlet of an upper partial condenser in the 2# ammonia still are both provided with TIJ, and pipelines among the 1# raffinate heat exchanger, the 2# raffinate heat exchanger and the soft water bucket are all provided with TIJ.

Preferably, FICs are arranged between the 1# ammonia still, the 1# preheater B, the 2# ammonia still, the 2# preheater B and the low-pressure steam pipeline.

Preferably, there are three feedstock pumps.

Preferably, the pipelines between the 1# raffinate heat exchanger, the 2# raffinate heat exchanger and the soft water bucket are all provided with alarm devices, the pipelines between the 1# preheater B, the 2# preheater B and the mother liquor knockout drum are connected are provided with alarm devices, the pipelines between the mother liquor knockout drum and the absorption tower are also provided with alarm devices, and the alarm devices are arranged between the vent pipe B of the absorption tower and the ammonia water backwashing water bucket connected to the bottom of the absorption tower.

Compared with the prior art, the invention has the beneficial effects that: the MII ammonia absorption is changed into MI ammonia absorption, the absorbed liquid enters a gas-liquid separator for separation, the liquid phase returns to an MI barrel, the gas phase enters a tail gas purification tower and is purified by using a weak liquid and then is emptied, the escaped gas ammonia is obviously reduced, the field environment is obviously improved, more gas ammonia is recycled to the system, the ammonia consumption is reduced, and the benefit is increased.

Drawings

The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention and not to limit the invention. In the drawings:

FIG. 1 is a flow chart of the improved process structure with control points of the ammonia distillation system.

Detailed Description

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 only a part of the embodiments of the present invention, and not all of the embodiments. 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.