阅读说明：本技术 一种炼厂胺液分质利用方法 (Method for utilizing amine liquid of refinery plant according to quality ) 是由 赵建炜 庄肃青 李文慧 朱华兴 张帆 王金兰 郭文豪 于 2020-05-29 设计创作，主要内容包括：本发明公开了一种胺液分质利用方法,可以有效降低炼厂能耗,提高炼厂经济效益。其方法是：来自炼厂各产品脱硫系统的A富胺液和炼厂各中间物料脱硫系统的B富胺液分别进行处理,炼厂各产品脱硫系统的A富胺液再生得到硫化氢含量为600～1000mg/L,贫胺液浓度为20～40mol%的低硫化氢含量贫胺液,返回炼厂各产品脱硫系统使用,炼厂各中间物料脱硫系统的B富胺液再生得到硫化氢含量为1000～1800mg/L,贫胺液浓度为20～40mol%的高硫化氢含量贫胺液,返回炼厂各中间物料脱硫系统使用。(The invention discloses a method for utilizing amine liquid according to quality, which can effectively reduce energy consumption of a refinery and improve economic benefits of the refinery. The method comprises the following steps: the method comprises the following steps of respectively treating an A rich amine liquid from each product desulfurization system of a refinery and a B rich amine liquid from each intermediate material desulfurization system of the refinery, regenerating the A rich amine liquid of each product desulfurization system of the refinery to obtain a low hydrogen sulfide content lean amine liquid with the hydrogen sulfide content of 600-1000 mg/L and the lean amine liquid concentration of 20-40 mol%, returning the low hydrogen sulfide content lean amine liquid to each product desulfurization system of the refinery for use, regenerating the B rich amine liquid of each intermediate material desulfurization system of the refinery to obtain a high hydrogen sulfide content lean amine liquid with the hydrogen sulfide content of 1000-1800 mg/L and the lean amine liquid concentration of 20-40 mol%, and returning the high hydrogen sulfide content lean amine liquid to each intermediate material desulfurization system of the refinery for use.)

1. A method for utilizing amine liquid of a refinery by different qualities is characterized by comprising the following steps:

1) respectively treating the A rich amine liquid from each product desulfurization system of the refinery and the B rich amine liquid from each intermediate material desulfurization system of the refinery, and enabling the A rich amine liquid from each product desulfurization system of the refinery to enter the step 2) and the B rich amine liquid from each intermediate material desulfurization system of the refinery to enter the step 3);

2) sending the amine-rich liquid A of each product desulfurization system of the refinery obtained in the step 1) to a liquid-rich A flash tank for flash evaporation, sending the A low-pressure gas obtained by flash evaporation to a refinery low-pressure gas pipe network for use, sending the amine-rich liquid A after flash evaporation to an A regeneration tower system for regeneration after heat exchange to obtain low-hydrogen-sulfide-content amine-poor liquid with the hydrogen sulfide content of 600-1000 mg/L and the amine-poor liquid concentration of 20-40 mol%, returning the low-hydrogen-sulfide-content amine-poor liquid to each product desulfurization system of the refinery after heat exchange and cooling for continuous desulfurization use as a solvent, sending the acid gas A generated by regeneration to a sulfur recovery device for sulfur recovery, wherein the steam consumption required by the A regeneration tower is 115-130 kg/ton of solvent;

3) sending the B rich amine liquid of each intermediate material desulfurization system of the refinery in the step 1) to a rich liquid B flash evaporation tank for flash evaporation, sending the B low-pressure gas obtained by flash evaporation to a refinery low-pressure gas pipe network for use, sending the B rich amine liquid subjected to flash evaporation to a B regeneration tower system for regeneration after heat exchange to obtain a high hydrogen sulfide content lean amine liquid with the hydrogen sulfide content of 1000-1800 mg/L and the lean amine liquid concentration of 20-40 mol%, returning the high hydrogen sulfide content lean amine liquid to each intermediate material desulfurization system of the refinery after heat exchange and cooling for continuous desulfurization use as a solvent, sending the B acid gas generated by regeneration to a sulfur recovery device for sulfur recovery, and enabling the consumption of the regenerated steam required by the B regeneration tower to be 100-115 kg/ton of solvent.

2. The method for the separate utilization of the amine liquid of the refinery according to claim 1, wherein: the rich amine liquid of the desulfurization systems of various products in the refinery is any one of the rich amine liquid of the desulfurization system of dry gas/gas holder gas, the rich amine liquid of the desulfurization system of liquefied gas, the rich amine liquid of the desulfurization system of low-grade gas in the refinery, and the like, and the desulfurization systems of various intermediate materials in the refinery are the rich amine liquid of the desulfurization system of recycle hydrogen materials in the refinery.

3. The method for the separate utilization of the amine liquid of the refinery according to claim 1, wherein: and after heat exchange, the amine-rich liquid flashed by the flash tank for rich liquid A is sent to a regeneration tower system A at the temperature of 90-110 ℃ and the pressure of 0.6-0.8 MPag.

4. The method for the separate utilization of the amine liquid of the refinery according to claim 1, wherein: and the amine-poor liquid with low hydrogen sulfide content after regeneration of the A regeneration tower system is cooled to the temperature of 40-50 ℃ through heat exchange, and returns to the desulfurization systems of various products of the refinery as a solvent for continuous desulfurization after the pressure is 0.6-0.7 MPag.

5. The method for the separate utilization of the amine liquid of the refinery according to claim 1, wherein: the operating temperature of the rich liquid A flash tank is 60-65 ℃, and the operating pressure is 0.08-0.12 MPag.

6. The method for the separate utilization of the amine liquid of the refinery according to claim 1, wherein: the tower top operation temperature of the regeneration tower A system is 110-120 ℃, and the tower top operation pressure is 0.08-0.12 MPag.

7. The method for the separate utilization of the amine liquid of the refinery according to claim 1, wherein: and the amine-rich liquid after flash evaporation of the rich liquid B flash tank is subjected to heat exchange at the temperature of 90-110 ℃ and the pressure of 0.6-0.8 MPag, and then is sent to a B regeneration tower system.

8. The method for the separate utilization of the amine liquid of the refinery according to claim 1, wherein: and after the regeneration of the regeneration tower system B, the amine-poor liquid with high low hydrogen sulfide content is cooled to the temperature of 50-60 ℃ through heat exchange, and the pressure of 0.8-1.0 MPag, and then the amine-poor liquid returns to each intermediate material desulfurization system of the refinery to be used as a solvent for continuous desulfurization.

9. The method for the separate utilization of the amine liquid of the refinery according to claim 1, wherein: the operating temperature of the rich liquid B flash tank is 55-65 ℃, and the operating pressure is 0.08-0.12 MPag.

10. The method for the separate utilization of the amine liquid of the refinery according to claim 1, wherein: the tower top operation temperature of the B regeneration tower system is 110-120 ℃, and the tower top operation pressure is 0.08-0.12 MPag.

Technical Field

The invention relates to a method for utilizing amine liquid according to different qualities in a solvent regenerating device of a refinery, namely, the amine liquid with low hydrogen sulfide content and the amine liquid with high hydrogen sulfide content are respectively regenerated and utilized.

Background

In recent years, with the continuous development of economy in China, the oil refining capacity in China is continuously and rapidly expanded. It is predicted that the oil refining capacity of China will increase to 8.82 hundred million tons by the end of 2020. In the refining production process, raw oil is subjected to primary and secondary processing, partial sulfides in the raw oil are converted into H2S, H2S finally enters products such as dry gas, gasoline, liquefied petroleum gas and the like, the quality of domestic products is upgraded along with the increase of the oil refining capacity, the average sulfur content of the processed raw oil is higher and higher, and if the sulfur-containing products are not desulfurized to reach the standard, the corrosion of equipment and pipelines can be caused when the sulfur-containing products are used as petrochemical raw materials or fuels, the environmental pollution can be caused finally, and the human health is further harmed. In recent years, with the development of national economy, the demand of petroleum is increasing, so that the processing amount of high-sulfur crude oil and poor crude oil in domestic refineries is increasing continuously, a large amount of sulfur-containing products are by-produced in production, and the load of desulfurization is increased. On the other hand, to reduce the environmental pollution caused by emission, the national requirements for the quality of fuel products are becoming stricter. The dosage of the solvent-amine liquid for desulfurization in the refinery is larger and larger, so that the scale of the solvent regeneration device is larger and larger, and the energy consumption of the solvent regeneration device in the refinery is higher and higher.

At present, the regeneration of rich amine liquid desulfurized in a refinery is generally divided into an adjacent hydrogen type and a non-adjacent hydrogen type, the regenerated lean amine liquid respectively returns to a hydrogenation device and a non-hydrogenation device for desulfurization, and the two lean amine liquids are not mixed for use, so as to avoid CO contained in the non-adjacent hydrogen type lean amine liquid₂Affecting the normal safe and stable operation of the hydrogenation device.

Disclosure of Invention

The invention aims to provide a method for utilizing amine liquid of a refinery separately for reducing the energy consumption of a solvent regeneration device, reducing the investment and improving the economic benefit of the refinery.

The invention provides a method for utilizing amine liquid of a refinery plant according to different qualities, which is characterized by comprising the following steps:

1) respectively treating the rich amine liquid A from each product desulfurization system of the refinery and the rich amine liquid B from each intermediate material desulfurization system of the refinery, and enabling the rich amine liquid A from each product desulfurization system of the refinery to enter the step 2) and the rich amine liquid B from each intermediate material desulfurization system of the refinery to enter the step 3);

2) sending the rich amine liquid A of each product material desulfurization system of the refinery obtained in the step 1) to a rich liquid A flash evaporation tank for flash evaporation, lifting the A low-pressure gas obtained by flash evaporation to a refinery low-pressure gas pipe network for use, sending the A rich amine liquid obtained after flash evaporation to an A regeneration tower system for regeneration after heat exchange to obtain low-hydrogen-sulfide-content lean amine liquid with the hydrogen sulfide content of 600-1000 mg/L and the lean amine liquid concentration of 20-40 mol%, returning the low-hydrogen-sulfide-content lean amine liquid to each product desulfurization system of the refinery after heat exchange and cooling for continuous desulfurization use as a solvent, sending the A acid gas generated by regeneration to a sulfur recovery device for sulfur recovery, wherein the steam consumption required by the A regeneration tower is 115-130 kg/ton of solvent;

3) sending the rich amine liquid B of each intermediate material desulfurization system of the refinery in the step 1) to a rich liquid B flash evaporation tank for flash evaporation, sending the low-pressure gas of the B flash evaporation to a low-pressure gas pipe network of the refinery for use, carrying out heat exchange on the B rich amine liquid after flash evaporation, sending the B rich amine liquid to a B regeneration tower system for regeneration, obtaining the lean amine liquid with high hydrogen sulfide content and lean amine liquid concentration of 1000-1800 mg/L and lean amine liquid concentration of 20-40 mol%, carrying out heat exchange and cooling on the lean amine liquid with high hydrogen sulfide content, returning the B acid gas generated by regeneration to each intermediate material desulfurization system of the refinery for continuous desulfurization use as a solvent, sending the B acid gas generated by regeneration to a sulfur recovery device for sulfur recovery, and ensuring the consumption of the regenerated steam required by the B regeneration tower to be 100-115 kg/ton of solvent.

The operation temperature of the top of the regeneration tower B is 110-120 ℃, and the operation pressure of the top of the regeneration tower B is 0.08-0.12 MPag.

The regeneration tower A has tower top operation temperature of 110-120 deg.c and tower top operation pressure of 0.08-0.12 MPag.

The operating temperature of the rich liquid A flash tank is 60-65 ℃, and the operating pressure is 0.08-0.12 MPag.

The operation temperature of the rich liquid B flash tank is 55-65 ℃, and the operation pressure is 0.08-0.12 MPag.

The rich amine liquid of the desulfurization systems of various product materials of the refinery is any one of the rich amine liquid of the desulfurization system of dry gas/gas holder gas, the rich amine liquid of the desulfurization system of liquefied gas, the rich amine liquid of the desulfurization system of low-grade gas of the refinery, and the like, and the desulfurization systems of various intermediate materials of the refinery are the rich amine liquid of the desulfurization systems of materials such as recycle hydrogen of the refinery, and the like.

The invention relates to a method for separately utilizing amine liquid in a refinery, which is mainly used for separately utilizing the amine liquid in a solvent regenerating device in the refinery, namely, the amine liquid with low hydrogen sulfide content and the amine liquid with high hydrogen sulfide content are respectively regenerated. Compared with the prior art, the method has the advantages that: compared with the existing amine liquid utilization methods of refineries which are classified into a critical hydrogen type and a non-critical hydrogen type, the amine liquid utilization method of the invention, namely the amine liquid with low hydrogen sulfide content and the amine liquid with high hydrogen sulfide content, can effectively reduce the energy consumption of solvent regeneration devices of refineries, reduce the fuel consumption of refineries and improve the economic benefits of refineries.

The invention is described in further detail below with reference to the figures and the detailed description, without limiting the scope of the invention.

Drawings

FIG. 1 is a schematic diagram of a simple process for the separate utilization of amine liquid from a refinery plant.

In the figure:

1-desulfurization systems of various products of refineries (such as material desulfurization systems of dry gas/gas holder gas, liquefied gas and the like), 2-A amine-rich liquid, 3-flash tank of rich liquid A, 4-A low-pressure gas, 5-flash-evaporated amine-rich liquid A, 6-A regeneration tower system, 7-amine-lean liquid with low hydrogen sulfide content, 8-A acid gas, 9-desulfurization systems of various intermediate materials of refineries (such as material desulfurization systems of circulating hydrogen and the like), 10-B amine-rich liquid, 11-flash tank of rich liquid B, 12-B low-pressure gas, 13-flash-evaporated amine-rich liquid B, 14-B regeneration tower system, 15-amine-lean liquid with high hydrogen sulfide content and 16-B acid gas.

Detailed Description

As shown in figure 1, the invention relates to a method for utilizing amine liquid of a refinery plant according to different qualities, which comprises the following steps:

1) respectively treating the amine-rich liquid A2 from each product desulfurization system 1 of the refinery and the amine-rich liquid B10 from each intermediate material desulfurization system 9 of the refinery, and enabling the amine-rich liquid A2 from each product desulfurization system 1 of the refinery to enter the step 2) and enabling the amine-rich liquid B10 from each intermediate material desulfurization system 9 of the refinery to enter the step 3);

2) sending the amine-rich liquid A2 of each product desulfurization system 1 of the refinery from the step 1) to a liquid-rich A flash tank 3 for flash evaporation, sending the A low-pressure gas 4 obtained by flash evaporation to a refinery low-pressure gas pipe network for use, sending the amine-rich liquid A5 obtained by flash evaporation to an A regeneration tower system 6 for regeneration after heat exchange to obtain a low-hydrogen-sulfide-content lean amine liquid 7 with the hydrogen sulfide content of 600-1000 mg/L and the lean amine liquid concentration of 20-40 mol%, returning the low-hydrogen-sulfide-content lean amine liquid 7 to each product desulfurization system 1 of the refinery after heat exchange and cooling for continuous desulfurization use as a solvent, sending the acid gas A8 generated by regeneration to a sulfur recovery device for sulfur recovery, wherein the tower top operating temperature of the A regeneration tower is 110-120 ℃, the tower top operating pressure of the tower top is 0.08 MPag-0.12 MPag, and the steam consumption required by the A regeneration tower is 115-130 kg/ton of the solvent;

3) sending the B rich amine liquid 10 of each intermediate material desulfurization system 9 of the refinery in the step 1) to a rich liquid B flash tank 11 for flash evaporation, sending the B low-pressure gas 12 obtained by flash evaporation to a refinery low-pressure gas pipe network for use, sending the B rich amine liquid 13 obtained by flash evaporation to a B regeneration tower system 14 for regeneration after heat exchange to obtain a high hydrogen sulfide content lean amine liquid 15 with the hydrogen sulfide content of 1000-1800 mg/L and the lean amine liquid concentration of 20-40 mol%, returning the high hydrogen sulfide content lean amine liquid 15 to each intermediate material desulfurization system 9 of the refinery after heat exchange and cooling for continuous desulfurization use as a solvent, sending the B acid gas 16 generated by regeneration to a sulfur recovery device for sulfur recovery, wherein the operation temperature at the top of the B regeneration tower is 110-120 ℃, the operation pressure at the top of the B regeneration tower is 0.08-0.12 MPag, and the consumption of the regeneration steam required by the B regeneration tower is 100-115 kg/ton of the solvent.

The rich amine liquid of each intermediate material desulfurization system of the refinery is any one of the rich amine liquid of a dry gas/gas cabinet gas desulfurization system, the rich amine liquid of a liquefied gas desulfurization system, the rich amine liquid of a refinery low-gas separation desulfurization system and the like, and each intermediate material desulfurization system of the refinery is the rich amine liquid of a material desulfurization system such as refinery recycle hydrogen and the like.

The A rich amine liquid 2 from the desulfurization systems 1 of various products of the refinery (such as desulfurization systems of dry gas/gas holder, liquefied gas and the like) is usually at the temperature of 40-50 ℃ and the pressure of 0.5-0.6 MPag.

The low-pressure gas A4 flashed by the rich liquid A flash tank 3 is usually at the temperature of 60-65 ℃ and the pressure of 0.08-0.12 MPag.

The rich amine liquid 5 after being flashed by the rich liquid A flash tank 3 is subjected to heat exchange at the temperature of 90-110 ℃ and the pressure of 0.6-0.8 MPag, and then is sent to the A regeneration tower system 6.

And the amine-poor liquid 7 with low hydrogen sulfide content after being regenerated by the A regeneration tower system 6 is cooled to the temperature of 40-50 ℃ through heat exchange, and returns to the desulfurization systems 1 of various products of the refinery as a solvent to continue desulfurization after the pressure is 0.6-0.7 MPag.

The A acid gas 8 generated by the regeneration of the A regeneration tower system 6 is usually at the temperature of 40-50 ℃ and the pressure of 0.06-0.10 MPag.

The operating temperature of the rich liquid A flash tank 3 is 60-65 ℃, and the operating pressure is 0.08-0.12 MPag.

The operation temperature of the top of the regeneration tower system A6 is 110-120 ℃, and the operation pressure of the top of the regeneration tower system A is 0.08-0.12 MPag.

The B-rich amine liquid 10 from various intermediate material desulfurization systems 9 (such as a recycle hydrogen desulfurization system and the like) of the refinery is usually at the temperature of 55-65 ℃ and the pressure of 0.5-0.6 MPag.

The low-pressure gas 12B flashed out from the rich liquid B flash tank 11 is usually at the temperature of 55-65 ℃ and the pressure of 0.08-0.12 MPag.

And the rich amine liquid 13 flashed by the rich liquid B flash tank 11 is subjected to heat exchange at the temperature of 90-110 ℃ and the pressure of 0.6-0.8 MPag, and then is sent to a B regeneration tower system 14.

And after the regeneration of the B regeneration tower system 14, the lean amine liquid with high low hydrogen sulfide content and 15 is cooled to the temperature of 50-60 ℃ through heat exchange, and the pressure of 0.8-1.0 MPag, the lean amine liquid returns to each intermediate material desulfurization system 9 of the refinery to be used as a solvent for continuous desulfurization.

The temperature of the acid gas B16 generated by the regeneration of the B regeneration tower system 14 is usually 40-50 ℃, and the pressure is 0.06 MPag-0.10 MPag.

The operation temperature of the rich liquid B flash tank 11 is 55-65 ℃, and the operation pressure is 0.08-0.12 MPag.

The tower top operating temperature of the regeneration tower system B14 is 110-120 ℃, and the tower top operating pressure is 0.08-0.12 MPag.

According to the method for utilizing the amine liquid in the refinery separately, the steam consumption for regenerating the amine liquid with low hydrogen sulfide content is 115-130 kg/ton of solvent, the steam consumption for regenerating the amine liquid with high hydrogen sulfide content is 100-115 kg/ton of solvent, and under the same raw material and operation conditions, the production of the amine liquid with high hydrogen sulfide content consumes less steam by 10-20 kg/ton of solvent than the production of the amine liquid with low hydrogen sulfide content, so that the load and the number of equipment of a reboiler and a cooler of a regeneration system can be reduced, and the equipment investment is reduced.