CN219079147U

CN219079147U - Acidic water purifying treatment device

Info

Publication number: CN219079147U
Application number: CN202320140826.2U
Authority: CN
Inventors: 陈宇
Original assignee: Sinoscience Fullcryo Zhongshan Low Temperature Equipment Manufacturing Co Ltd
Current assignee: Sinoscience Fullcryo Zhongshan Low Temperature Equipment Manufacturing Co Ltd
Priority date: 2023-01-31
Filing date: 2023-01-31
Publication date: 2023-05-26
Anticipated expiration: 2033-01-31

Abstract

The application provides an acidic water purifying treatment device, and relates to the technical field of hydrocarbon hydrogen production. The acid water purifying treatment device comprises a high-pressure stripping tower, wherein the bottom of the high-pressure stripping tower is provided with a purified water outlet communicated with a purified water output pipeline and a steam inlet communicated with a steam input pipeline; the top is provided with a temperature sensor and a steam outlet communicated with a steam output pipeline; the side wall is provided with an acid water inlet communicated with an acid water inlet pipeline; and the steam input pipeline is also provided with a steam flow control valve and a steam flow sensor, and the steam flow control valve, the steam flow sensor and the temperature sensor are respectively connected with the controller. The acidic water purifying treatment device is used in a hydrocarbon conversion hydrogen production system, and improves the stripping purification effect of the acidic water purifying treatment device by adopting cascade control of the tower top temperature and the steam flow of a high-pressure stripping tower.

Description

Acidic water purifying treatment device

Technical Field

The application relates to the technical field of hydrogen production by hydrocarbons, in particular to an acidic water purifying treatment device.

Background

Hydrogen energy is a clean and efficient secondary energy source that does not naturally occur on earth like oil or gas, but rather needs to be manufactured. When fossil energy is used for hydrogen production, because natural gas such as hydrocarbon has high hydrogen yield and is cyclic when hydrogen production is carried outEnvironmental friendliness and the like, and has been developed and matured gradually. However, some acidic water is produced during the hydrocarbon steam reforming process due to the dissolution of CO ₂ And some trace low carbon number hydrocarbon impurities, etc., are corrosive to equipment and cannot be directly discharged. In particular, when hydrogen products are produced using hydrocarbon steam reforming hydrogen production facilities, more than 6t/h of sour water is produced per 10000Nm3/h of hydrogen products, which can cause significant losses if the sour water is not reasonably treated.

At present, acid water generated in the existing hydrocarbon steam conversion hydrogen production process is stripped by low-pressure steam in an atmospheric stripping tower to remove carbon dioxide and low-carbon number hydrocarbons in the acid water, and the acid water is recycled after water quality is purified. The atmospheric stripper overhead temperature is at most 100 ℃, but because of the low overhead pressure, hydrocarbons with low carbon numbers are typically stripped. However, although the normal pressure stripping tower can finish the purification of the acid water, the consumption of the stripping steam is usually strictly controlled in order to save energy and reduce consumption in the process, so that when the acid water consumption and the water quality fluctuate greatly, the purified water quality of the stripping tower is likely to be disqualified. When the purified water is used for other purposes, for example, as boiler feed water for producing medium-pressure steam, and the medium-pressure steam is supplied to a turbine or the like, the life of the turbine is likely to be compromised. In addition, first, the pressure at the top of the atmospheric stripping tower is only slightly higher than the atmospheric pressure, so that the atmospheric stripping tower top gas is discharged to the atmosphere, and harmful and toxic substances in the acidic water are stripped to the tower top gas and then enter the atmosphere to pollute the environment; secondly, most of atmospheric stripping tower top gas is water vapor, when the air temperature is low, white gas can be blown around the tower top to influence the beauty of a factory, and partial road surface ice can be caused after the water vapor is condensed, so that the road surface is slippery and harmful and safe; finally, most of the tower top gas is water, and the direct exhaust of the air is a resource waste.

Disclosure of Invention

In view of this, the purpose of this application is to overcome the not enough in the prior art, provides a new sour water purification treatment device, in order to improve the purification effect of sour water in hydrocarbon conversion hydrogen manufacturing system, improve sour water's comprehensive utilization, avoid sour water treatment process to the harmful effect of environment.

The application provides the following technical scheme:

the application provides an acidic water purifying treatment device, which comprises a high-pressure stripping tower;

the bottom of the high-pressure stripping tower is provided with a purified water outlet and a steam inlet, and the purified water outlet is communicated with a purified water output pipeline; the steam inlet is communicated with the steam input pipeline;

the top of the high-pressure stripping tower is provided with a steam outlet and a temperature sensor, and the steam outlet is communicated with a steam output pipeline;

the side wall of the high-pressure stripping tower is provided with an acidic water inlet which is communicated with an acidic water inlet pipeline;

the steam flow control valve is characterized in that a steam flow control valve and a steam flow sensor are further arranged on the steam input pipeline, the steam flow control valve, the steam flow sensor and the temperature sensor are respectively connected with a controller, and the controller is used for collecting data transmitted by the steam flow sensor and the temperature sensor and controlling the opening and closing degree of the steam flow control valve.

Preferably, the bottom of the high-pressure stripping tower is also provided with a liquid level sensor;

the purified water output pipeline is also provided with a liquid level control valve;

the liquid level sensor and the liquid level control valve are respectively connected with the controller.

Preferably, a silk screen packing layer, a tray or packing are respectively arranged in the high-pressure stripping tower from top to bottom;

the acidic water inlet is positioned between the tray and the silk screen packing layer or between the packing and the silk screen packing layer.

Preferably, the acid water inlet pipeline is further provided with an acid water preheater, and the acid water preheater is communicated with the purified water output pipeline.

Preferably, the acidic water purification treatment apparatus is used in a hydrocarbon conversion hydrogen production system.

Preferably, the hydrocarbon conversion hydrogen production system comprises: a desulfurization reactor, a conversion reactor, a medium-change reactor, a gas-liquid separator and a PSA unit;

the desulfurization reactor, the conversion reactor, the medium-change reactor, the gas-liquid separator and the PSA unit are sequentially connected through a gas transmission pipeline.

Further preferably, the acid water inlet is communicated with the gas-liquid separator through the acid water inlet pipeline;

the steam outlet is communicated with a gas raw material inlet of the conversion reaction furnace through the steam output pipeline;

the steam inlet is communicated with a superheated steam outlet of the reforming reaction furnace through the steam input pipeline.

Further preferably, the superheated steam outlet of the reforming reaction furnace is also connected with the steam output pipeline through a superheated steam conveying pipeline;

the superheated steam delivery pipeline is also provided with a pressure control valve, and the steam delivery pipeline is provided with a pressure sensor;

the pressure control valve and the pressure sensor are respectively connected with the controller.

Preferably, the hydrocarbon conversion hydrogen production system further comprises: a steam generator, a heat exchange cooler and a deaerator;

the steam generator is located on a gas transmission pipeline between the reforming reaction furnace and the medium-change reactor, the heat exchange cooler is located on the gas transmission pipeline between the medium-change reactor and the gas-liquid separator, the deaerator is connected with the heat exchange cooler through a first water supply pipeline, the heat exchange cooler is connected with the steam generator through a second water supply pipeline, and the steam generator is connected with the reforming reaction furnace through a saturated steam pipeline.

Further preferably, the purified water output pipeline is divided into two sub-pipelines, wherein a first sub-pipeline is used for circulating purified water when the deaerator generates abnormal working conditions, a second sub-pipeline is used for circulating purified water when the deaerator generates normal production working conditions, valves are respectively arranged on the first sub-pipeline and the second sub-pipeline, and the second sub-pipeline is connected with a liquid inlet of the deaerator.

The technical scheme of the application has the following advantages:

compared with the prior art, the normal pressure stripping tower is often used as the acid water purifying treatment device, and the acid water purifying treatment device can provide higher operation temperature for the acid water stripping process, carry out stripping by excessive steam and carry out totally-enclosed treatment by utilizing the treatment method of a complete closed loop of the high pressure stripping tower, the top gas and the bottom purified water, thereby greatly ensuring the effect of acid water stripping and purifying, improving the comprehensive utilization rate of acid water and avoiding the harmful influence of the acid water treatment process on the environment. In addition, through setting up temperature sensor and steam flow sensor in this application, can collect the flow situation of temperature and steam inlet department in the high pressure stripper overhead of tower in real time, through adopting temperature and flow cascade control, can control the steam quantity of strip in-process more accurately, both can guarantee enough even the excess of strip distillation volume with overhead temperature, can guarantee the strip steam volume enough even excess again through the fixed value of flow setting to ensure the strip effect, improve the quality of water condition after the final sour water purifies. In a conventional stripping tower, the steam flow is difficult to meter accurately, so that the control of the steam flow is more reliable and more accurate than the control of a pure flowmeter after the improvement, and the stripping effect of the sour water and the quality of purified water after the purification treatment are improved. Through using the acid water purification treatment device, the high-efficiency purification treatment and the maximum recycling of the acid water are realized, and the energy waste in the hydrogen production system and the damage of the acid water treatment process to the environment are reduced.

Drawings

In order to more clearly illustrate the technical solutions of the embodiments of the present application, the drawings that are needed in the embodiments will be briefly described below, it being understood that the following drawings only illustrate some embodiments of the present application and therefore should not be considered limiting the scope, and that other related drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.

FIG. 1 is a schematic view showing the structure of an acidic water purifying apparatus in example 1;

FIG. 2 is a schematic view showing the structure of an apparatus for purifying acidic water in example 2;

fig. 3 is a schematic diagram showing the structure of an acidic water purification treatment apparatus for a hydrocarbon conversion hydrogen production system in example 3.

Description of main reference numerals:

100-high pressure stripper; 101-a purified water outlet; 102-steam inlet; 103-steam outlet; 104-a temperature sensor; 105-acid water inlet; 106-a liquid level sensor; 107-trays; 108-a silk screen packing layer; 110-a controller; 120-purified water output pipeline; 121-a first sub-line; 122-a second sub-line; 130-steam input line; 140-steam flow control valve; 150-a flow sensor; 160-steam output line; 170-an acidic water inlet pipeline; 180-acid water preheater; 190-a liquid level control valve;

200-desulfurization reactor; 300-converting reaction furnace; 400-medium shift reactor; 500-a gas-liquid separator; a 600-PSA unit; 700-steam generator; 800-deaerator; 900-a gas transmission line; 301-gas feed inlet; 302-superheated steam outlet; 310-superheated steam delivery line; 320-a pressure control valve; 330-a pressure sensor; 410-a heat exchange cooler; 710-saturated steam line; 810-a first water supply line; 820-a second water supply line.

Detailed Description

Embodiments of the present application are described in detail below, examples of which are illustrated in the accompanying drawings, wherein the same or similar reference numerals refer to the same or similar elements or elements having the same or similar functions throughout. The embodiments described below by referring to the drawings are exemplary only for the purpose of explaining the present application and are not to be construed as limiting the present application.

It will be understood that when an element is referred to as being "fixed to" another element, it can be directly on the other element or intervening elements may also be present. When an element is referred to as being "connected" to another element, it can be directly connected to the other element or intervening elements may also be present. In contrast, when an element is referred to as being "directly on" another element, there are no intervening elements present. The terms "vertical," "horizontal," "left," "right," and the like are used herein for illustrative purposes only.

In this application, unless specifically stated and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communicated with the inside of two elements or the interaction relationship of the two elements. The specific meaning of the terms in this application will be understood by those of ordinary skill in the art as the case may be.

Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. In the description of the present application, the meaning of "a plurality" is two or more, unless explicitly defined otherwise.

Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs. The terminology used herein in the description of the templates is for the purpose of describing particular embodiments only and is not intended to be limiting of the application. The term "and/or" as used herein includes any and all combinations of one or more of the associated listed items.

The present application provides an sour water purification recovery unit comprising a high pressure stripper 100.

It should be noted that, when the high-pressure stripping tower 100 is used for stripping, the steam pressure required in the tower is higher than that of normal pressure, so that the gas temperature of steam is higher, and the temperature in the stripping tower is higher, for example, when stripping steam of 3.8MPa is used, the top temperature of the tower can reach 200 ℃, so that the acid water stripping effect is very good, the removal efficiency of carbon dioxide in the acid water is greater than 99% and other substances are removed by 100% according to specific simulation calculation. Therefore, the process of the high-pressure stripping tower improves the purification efficiency and reduces the influence of acidic water on the environment.

At the bottom of the high pressure stripper 100, a purified water outlet 101 and a steam inlet 102 are provided, wherein the purified water outlet 101 communicates with a purified water outlet line 120 and the steam inlet 102 communicates with a steam inlet line 130.

The top of the high pressure stripper 100 is provided with a steam outlet 103 and a temperature sensor 104, wherein the steam outlet 103 communicates with a steam output line 160.

The side wall of the high-pressure stripping tower 100 is provided with an acid water inlet 105, and the acid water inlet 105 is communicated with an acid water inlet pipeline 170.

A steam flow control valve 140 and a steam flow sensor 150 are also provided on the steam input line 130, and the steam flow control valve 140, the steam flow sensor 150, and the temperature sensor 104 are respectively connected to the controller 110.

The controller 110 can collect data transmitted by the steam flow sensor 150 and the temperature sensor 104, monitor the steam flow at the steam inlet 102 of the high-pressure stripping tower 100 and the temperature at the top of the tower in real time, analyze and judge the data through an internal program, and further control the opening and closing degree of the valve of the steam flow control valve 140 to adjust the entering flow of steam.

Specifically, during the starting stage of the high-pressure stripping tower 100, the controller 110 can firstly disconnect the control of the tower top temperature change on the steam flow control valve 140, then input a fixed steam flow parameter, keep the valve of the steam flow control valve 140 at a fixed position, and transmit steam into the high-pressure stripping tower 100, and after the starting of the high-pressure stripping tower 100 is completed, the controller 110 is used for collecting the temperature information fed back by the tower top temperature sensor 104 in real time, and the valve of the steam flow control valve 140 is regulated and controlled according to the temperature information change. When the temperature of the tower top fluctuates slightly, the controller 110 can only transmit corresponding instructions to the steam flow control valve 140 according to the collected temperature information, and the opening of the valve is finely adjusted at the moment; when the temperature of the top of the tower fluctuates greatly, the controller 110 collects temperature information and steam flow information at the same time, and then automatically judges and transmits related instructions to the steam flow control valve 140 after the comparison of the set values of the program of the controller 110, the valve opening of the steam flow control valve 140 can be roughly adjusted at the moment, and after the temperature fluctuation is small, the program automatically judges and automatically controls the steam flow control valve 140 by using the temperature information, so that the temperature in the stripping tower can be quickly and stably adjusted.

The steam stripping steam quantity of the high-pressure steam stripping tower adopts tower top temperature and steam stripping steam flow cascade control, and in the initial stage of device start-up use, the steam stripping steam quantity is usually inaccurate due to insufficient experience, the temperature measurement is generally easier to measure accurately, and the like, so that an operator can operate to ensure the steam stripping effect. After experience is accumulated, an operator can disconnect the control of the steam flow control valve by the controller, directly determine the opening of the regulating valve according to accumulated operation experience, so that the stripping effect can be well achieved, and the hysteresis of automatic control is reduced.

In a preferred embodiment, the bottom of the high pressure stripper 100 is also provided with a level sensor 106 and the purified water output line 120 is also provided with a level control valve 190. Wherein the level sensor 106 and the level control valve 190 are in communication with the controller 110, respectively.

It will be appreciated that after the controller 110 collects the liquid level information transmitted by the liquid level sensor 106, the opening and closing degree of the liquid level control valve 190 can be controlled, if the liquid level is too high, the valve of the liquid level control valve 190 is opened to enable the purified water to pass through quickly, and when the liquid level is too low, the valve of the liquid level control valve 190 is opened to enable the purified water to flow out slowly, so as to maintain the stability of the internal environment of the high pressure stripping tower 100.

In a preferred embodiment, the inside of the high pressure stripper 100 is provided with a silk screen packing layer 108 and a tray 107 from top to bottom, respectively, wherein the sour water inlet 105 is located between the tray 107 and the silk screen packing layer 108. It should be noted that the tray may be replaced by a filler, and the acidic water inlet is located between the filler and the wire mesh filler layer.

In a preferred embodiment, an acid water preheater 180 is also provided on the acid water feed line 170, and the acid water preheater 180 is also connected to the purified water output line 120.

It will be appreciated that the purified water output pipeline 120 is circulated with the purified water flowing out from the high temperature and high pressure stripper, and the purified water has a certain amount of heat, and when passing through the acid water preheater 180, the heat of the purified water can be transferred to the acid water in the acid water inlet pipeline 170, so that when the acid water reaches the stripper, the temperature difference between steam and the acid water can be reduced, the removal rate of acid gas can be improved, and the stripping efficiency can be accelerated.

In a preferred embodiment, the sour water purification apparatus of the present application is used in a hydrocarbon conversion hydrogen production system.

Specifically, the hydrocarbon conversion hydrogen production system comprises: a desulfurization reactor 200, a conversion reactor 300, a medium shift reactor 400, a gas-liquid separator 500, and a PSA unit 600. Wherein, the desulfurization reactor 200, the conversion reactor 300, the medium shift reactor 400, the gas-liquid separator 500 and the PSA unit 600 are sequentially connected through a gas transmission line 900.

The working principle of the hydrocarbon conversion hydrogen production system is as follows:

(1) Desulfurization of raw materials

And under certain temperature and pressure, the raw natural gas is desulfurized by a desulfurization reactor. Organic sulfur in raw material natural gas and a small amount of hydrogen returned by a hydrogen production system are changed into inorganic sulfur (H) under the action of a cobalt-molybdenum catalyst ₂ S), inorganic sulfur is absorbed by a zinc oxide desulfurizing agent, and sulfur in the raw material is removed to below 0.1ppm so as to meet the requirement of a steam conversion catalyst on sulfur, wherein the main reaction is (RSH represents organic sulfide in the raw material):

RSH+H ₂ →H ₂ S+RH；

H ₂ S+ZnO→ZnS+H ₂ O。

(2) Conversion reaction

The desulfurized raw material hydrocarbon is mixed with water vapor according to a certain proportion (called water-carbon ratio), then enters a conversion reaction furnace, and reacts under the conditions of high temperature and catalyst to generate H ₂ CO and CO ₂ As well as unreacted complete methane and excess steam. The hydrocarbon steam conversion uses steam as an oxidant, so that a steam generator is needed to convert water into steam, and then hydrocarbon substances are converted under the action of a conversion catalyst to obtain the synthesis gas for preparing hydrogen.

The main reactions under the action of the conversion catalyst are as follows:

CH ₄ +H ₂ O→CO+3H ₂ ；

CO+H ₂ O→CO ₂ +H ₂ 。

limited by the equilibrium of the chemical reaction, the export synthesis gas contains about 10% CO under the conditions of the reformer. The CO cannot be removed in the subsequent pressure swing adsorption purification, so that the CO needs to be reacted in the next step to be changed into CO ₂ 。

Generally, when hydrocarbon steam is used for converting hydrogen production, raw material pretreatment is adopted to remove sulfur, chlorine, arsenic and heavy metals in the raw materials, so that the final reaction product mainly comprises hydrogen, carbon monoxide and carbon dioxide, and a small amount of low molecular substances such as methanol, ethanol, formaldehyde and acetic acid can be generated in the side reaction Fischer-Tropsch reaction, but the content is small.

(3) Medium shift reaction

After the synthesis gas exits the conversion reaction furnace, heat exchange is performed with water of the steam generator to generate steam, meanwhile, the temperature of the synthesis gas is reduced to about 340 ℃, then the synthesis gas enters the medium-shift reactor, and under the action of the medium-shift catalyst, CO and steam react as follows:

CO+H ₂ O→CO ₂ +H ₂ 。

the CO conversion reaction is exothermic reaction, and the low temperature pair conversion is flatThe balance is favorable, and higher CO conversion rate can be obtained, so that the hydrogen yield of unit raw materials can be improved. After the CO conversion reaction, the synthesis gas enters a gas-liquid separator after passing through a heat exchange cooler, at the moment, excessive steam in the synthesis gas becomes liquid after cooling and is separated from other gases, the main component of the separated liquid is water, and a small amount of CO is dissolved in the water ₂ But is acidic, so is also called sour water. The acidic water can be recycled after purification treatment, generally steam is used for stripping the acidic water to remove CO in the acidic water ₂ Blowing out to become purified water. The purified water is sent into a deaerator for treatment, then is sent into a steam generator to become saturated medium-pressure steam, the medium-pressure steam is sent into a conversion reaction furnace to exchange heat with high-temperature flue gas to become superheated steam, and the superheated steam is used as raw material steam distribution, and the surplus superheated steam is sent out of the device for other users to use. After the saturated steam is subjected to heat treatment, the saturated steam is not easy to cool and become water in the outward conveying process.

(4) Pressure swing adsorption Purification (PSA)

PSA is a very mature product which is produced by hydrogen purification methods commonly used in hydrogen production at present. A plurality of adsorption towers are arranged in the PSA, and each adsorption tower is filled with the same adsorbent, so that CO in the synthesis gas can be purified ₂ 、CH ₄ And (5) removing by adsorption. After the adsorption saturation of the adsorbent, the adsorbate is desorbed by reducing the pressure of the adsorption tower to become desorption gas, and the desorption gas can be sent to a conversion reaction furnace to be burnt as fuel.

In a hydrocarbon steam reforming hydrogen production system, the reaction pressure is usually designed to be 2-4MPa, the outlet temperature of a reforming reaction furnace is above 800 ℃, and the water-carbon ratio (namely the ratio of water vapor molecules to carbon atoms in the fed hydrocarbon raw materials) is also an important parameter for safe and long-period operation of the system. In practical production, the water-to-carbon ratio of the conversion unit is generally controlled to 3 or more in order to ensure a sufficient conversion rate of hydrocarbons. Complete conversion of carbon atoms to CO ₂ And H ₂ Theoretically, 2 water molecules are required, so that the water vapor in the reaction-generated gas of the hydrocarbon vapor conversion hydrogen production system is largely remained. A large water-carbon ratio and a high reaction temperature determine that a large amount of high temperature remainsThe heat, usually high temperature waste heat, is used to generate medium pressure steam, and the rest steam is sent out from the device to other users except part of medium pressure steam is used for raw material steam distribution.

In some embodiments of the present application, sour water feed inlet 105 communicates with gas-liquid separator 500 via sour water feed line 170; the steam outlet 103 is communicated with a gas raw material inlet 301 of the reforming reaction furnace 300 through a steam output pipeline 160; the steam inlet 102 communicates with a superheated steam outlet 302 of the reformer 300 via a steam input line 130.

It will be appreciated that the steam input line 130 communicates with the superheated steam outlet 302 of the reformer 300, and is a reasonable arrangement of resources to fully utilize the energy generated during the reformer hydrogen production process.

In some preferred embodiments of the present application, the superheated steam outlet 302 of the reformer 300 is also connected to the steam output line 160 by a superheated steam delivery line 310. Wherein, the superheated steam delivery pipeline 310 is also provided with a pressure control valve 320, and the steam output pipeline 160 is provided with a pressure sensor 330; the pressure control valve 320 and the pressure sensor 330 are connected to the controller 110, respectively.

It should be noted that, the atmospheric stripping tower top gas is discharged into the atmosphere, so that harmful substances in the acidic water pollute the environment, most of the tower top gas is water vapor, when the air temperature is low, white gas can be emitted around the tower top, and after the water vapor is condensed, the partial road surface can be frozen, the road surface is slippery, and the potential safety hazard is great. The tower top gas with most of water is directly discharged into the atmosphere, which is also a resource waste.

In this regard, the steam at the top of the high-pressure stripping tower 100 is returned to the gas raw material inlet 301 of the reforming reactor 300 through the steam output pipeline 160, thereby realizing the recycling of the waste gas after the acidified water stripping. Especially in the related process of hydrogen production, most of the acidic water is carbon dioxide, and a small part of the acidic water is methane, carbon monoxide, methanol, ethanol, formaldehyde, acetic acid and other substances, which are originally generated from a conversion reaction furnace, so that substances carried in steam cannot have any toxic effect on a conversion catalyst, wherein carbon dioxide and light hydrocarbons in raw hydrocarbon can also react to form carbon monoxide and hydrogen, and the method is also an advantageous effect.

Because the overhead water vapor can be fully recycled, the steam at the steam inlet of the stripping tower can be used in proper excess, but even if the steam is used in excess, the steam consumption for stripping is more than 0.3-0.5 times of the amount of acid water, in this case, calculated by the water-carbon ratio in the conversion reactor being 3, the overhead water vapor is required to be supplemented with a certain steam amount when being used in the conversion reactor, and the required steam amount to be supplemented is about 3-5 times of that of the overhead steam of the high-pressure stripping tower. Therefore, the superheated steam generated by the high-temperature waste heat of the reforming reactor can be mixed with the steam discharged from the stripping tower in the steam output pipeline 160 through the superheated steam conveying pipeline 310, and the superheated steam and the steam are mixed to form new superheated steam, and then the new superheated steam is conveyed into the raw material reaction gas of the reforming reactor for reaction.

Further, a pressure control valve 320 is arranged on the superheated steam delivery pipeline, a pressure sensor 330 is arranged on the steam delivery pipeline 160, and the pressure stability of the top of the stripping tower is ensured through the real-time detection and control of the controller 110, and sufficient steam is ensured for raw material steam distribution required by the hydrogen production reaction, namely the water-carbon ratio of the hydrogen production reaction is ensured.

The application selects the use of a high pressure stripper for stripping and purifying sour water, where the high pressure referred to herein is primarily described in comparison to an atmospheric stripper, that is, a high pressure if higher than the vapor pressure provided in an atmospheric vapor tower. However, in hydrocarbon steam reforming hydrogen production systems, the reaction pressure of steam is typically designed to be 2-4MPa, so if the high pressure stripper uses the steam pressure in the hydrogen production system, the pressure is essentially in the medium pressure regime. If the original normal pressure stripping tower is to be modified, stainless steel materials such as equipment, pipelines and the like which are in contact with acidic water are arranged in the original normal pressure stripping tower, so that the pressure resistance of the stripping tower is improved only by increasing the wall thickness of the equipment, but the required steam pressure is 2-4MPa of medium pressure, so that the wall thickness is increased slightly, and the investment required for subsequent improvement is also less.

In a preferred embodiment of the present application, the hydrocarbon conversion hydrogen production system further comprises: a steam generator 700, a heat exchange cooler 410, and a deaerator 800.

Wherein the steam generator 700 is located on a gas transfer line between the shift reactor 300 and the intermediate shift reactor 400, and the heat exchange cooler 410 is located on a gas transfer line between the intermediate shift reactor 400 and the gas-liquid separator 500. This is because the temperature of the mixed gas produced in the reformer 300 and the mixed gas reacted in the intermediate shift reactor 400 are relatively high, and thus when the steam generator 700 and the heat exchange cooler 410 are installed in the transfer line, the heat of the transferred mixed gas can be fully utilized, and the water in the steam generator 700 and the heat exchange cooler 410 absorbs heat and becomes hot water vapor.

The deaerator 800 is connected to the heat exchange cooler 410 through a first water supply line 810, the heat exchange cooler 410 is connected to the steam generator 700 through a second water supply line 820, and the steam generator 700 is connected to the shift reactor 300 through a saturated steam line 710.

In a preferred embodiment, the purified water output pipeline 120 is divided into two sub-pipelines, wherein a first sub-pipeline 121 is used for circulating purified water when the deaerator 800 is in an abnormal working condition, a second sub-pipeline 122 is used for circulating purified water when the deaerator 800 is in a normal production working condition, valves are respectively arranged on the first sub-pipeline 121 and the second sub-pipeline 122, and the second sub-pipeline 122 is connected with a liquid inlet of the deaerator 800.

In the open or stop stage of the stripping tower, because the steam and the temperature in the tower are unstable, the purified water mostly does not reach the standard, so that the purified water in the stages cannot be used for recycling water equipment such as a deaerator, and at the moment, the valve on the second sub-pipeline needs to be closed, the valve on the first sub-pipeline needs to be opened, and the purified water which does not reach the standard flows out. After the purified water is sampled and detected, the valve of the second sub-pipeline can be opened and the valve of the first sub-pipeline can be closed after the quality of the purified water is determined to reach the standard, so that the purified water flows into the deaerator through the second sub-pipeline, and after oxygen in the water is removed, the purified water flows into the steam generator to generate water steam. Therefore, the water resources in the acidic water can be fully recovered and recycled, and the utilization rate of the water resources is greatly improved.

Example 1

As shown in fig. 1, the present embodiment provides an acidic water purifying treatment apparatus, specifically including a high-pressure stripper 100.

Wherein, a purified water outlet 101 and a steam inlet 102 are arranged at the bottom of the high-pressure stripping tower 100, the purified water outlet 101 is communicated with a purified water output pipeline 120, and the steam inlet 102 is communicated with a steam input pipeline 130. The purified water output pipeline 120 is divided into two sub-pipelines, wherein one sub-pipeline is used for circulating purified water reaching standards, the other sub-pipeline is used for circulating purified water not reaching standards, and valves are respectively arranged on the first sub-pipeline 121 and the second sub-pipeline 122.

The side wall of the high-pressure stripping tower 100 is provided with an acid water inlet 105, and the acid water inlet 105 is communicated with an acid water inlet pipeline 170. At the top of the high pressure stripper 100 there is provided a steam outlet 103 and a temperature sensor 104, wherein the steam outlet 103 communicates with a steam outlet line 160.

A steam flow control valve 140 and a steam flow sensor 150 are also provided on the steam input line 130, and the steam flow control valve 140, the steam flow sensor 150, and the temperature sensor 104 are respectively connected to the controller 110. The controller 110 can collect data transmitted by the steam flow sensor 150 and the temperature sensor 104, monitor the steam flow at the steam inlet 102 and the temperature at the top of the tower in real time, and analyze and judge the data through an internal program to control the flow at the valve of the steam flow control valve 140.

According to the sour water purification treatment device, the steam stripping steam quantity of the high-pressure stripping tower is controlled in a cascade mode by adopting the temperature of the top of the tower and the steam stripping steam flow, so that an operator can continuously adjust the steam flow control valve according to real-time feedback of the steam flow and the temperature at the beginning of the device operation and the use period, and the steam stripping effect is ensured. After experience is accumulated, an operator can disconnect the control of the controller on the steam flow control valve, and the valve is directly manually adjusted according to accumulated operation experience, so that the stripping effect can be well achieved, and the hysteresis of a computer automatic control system can be reduced.

Example 2

As shown in fig. 2, the present embodiment provides an acidic water purifying treatment apparatus, specifically including a high-pressure stripper 100. As in example 1, except that tray 107 and silk screen packing layer 108 are provided inside high pressure stripper 100 from bottom to top, respectively, acid water feed 105 is located between tray 107 and silk screen packing layer 108. Through the arrangement of the tray and the silk screen packing layer, the sufficient contact between the steam and the acid water is ensured, so that the acid gas in the acid water is separated out into the continuously-rising steam, and clean water is left.

A liquid level sensor 106 is also provided at the bottom of the high pressure stripper 100, and a liquid level control valve 190 is also provided on the purified water output line 120. Wherein the level sensor 106 and the level control valve 190 are in communication with the controller 110, respectively.

Through setting up level sensor 106 and liquid level control valve 190, can real-time supervision, collect the liquid level height of atmospheric pressure tower internal purification water, if the liquid level is too high, open the valve of liquid level control valve for the purification water passes through fast, prevents that the liquid level from reaching tower tray department, influences purifying effect, also can keep the stability of high pressure stripper 100 internal environment simultaneously.

The acidic water purifying treatment device further improves the stripping effect of the acidic water, so that the quality of the purified water is cleaner, and the stable operation of the stripping tower is ensured.

Example 3

As shown in fig. 3, this embodiment provides an acidic water purification treatment apparatus for use in a hydrocarbon conversion hydrogen production system. Wherein, the high-pressure stripping tower 100 in the sour water purifying treatment device is the same as that in the embodiment 2, and the hydrocarbon conversion hydrogen production system comprises: the desulfurization reactor 200, the conversion reactor 300, the medium shift reactor 400, the gas-liquid separator 500, and the PSA unit 600 are sequentially connected through a gas transfer line 900. Wherein the liquid outlet of the gas-liquid separator 500 is in communication with the sour water feed inlet 105 of the high pressure stripper 100 via a sour water feed line 170.

In addition to gas transfer line 900, there is a water supply line for providing the desired water vapor to the hydrocarbon conversion hydrogen production system. On the water supply pipeline, a deaerator 800 is arranged, oxygen and other gases in water can be removed through the deaerator 800, and the quality of the supplied water in the whole system is ensured.

The water added in the deaerator 800, a part of which is demineralized water from the outside, and a part of which is purified water purified by the high-pressure stripping tower 100, flows into the deaerator 800 through the second sub-pipeline 122 of the purified water output pipeline 120, so that the water resource in the acidic water can be fully recovered and recycled, and the utilization rate of the water resource is greatly improved.

Then, the deaerator 800 is connected to the heat exchange cooler 410 through the first water supply line 810, and the heat exchange cooler 410 is disposed on the gas transmission line between the medium-shift reactor 400 and the gas-liquid separator 500, so that the temperature of water in the water supply line can be primarily increased, and the temperature on the gas transmission line can be reduced; the heat exchange cooler 410 is connected to the steam generator 700 through a second water supply line 820, and the steam generator 700 is disposed on a gas transfer line between the shift reactor 300 and the medium shift reactor 400, in which the gas temperature is higher, so that the conversion of water into water vapor can be promoted. The steam generator 700 is further connected to the shift reactor 300 through a saturated steam line 710, and prevents condensation from occurring due to temperature decrease during the subsequent transfer process by heating the steam to superheated saturated steam using the high temperature in the shift reactor.

The superheated steam outlet 302 of the reformer 300 is then in communication with the steam inlet 102 of the high pressure stripper 100 via the steam inlet line 130. The steam outlet 103 of the high pressure stripper 100 is in communication with the gaseous feed inlet 301 of the reformer 300 via the steam outlet line 160.

The superheated steam outlet 302 of the reformer 300 is also connected to the steam outlet line 160 by a superheated steam delivery line 310. A pressure control valve 320 is also arranged on the superheated steam delivery pipeline 310, and a pressure sensor 330 is arranged on the steam output pipeline 160; the pressure control valve 320 and the pressure sensor 330 are connected to the controller 110, respectively.

The steam discharged from the top of the high pressure stripper 100 is generally difficult to be transferred to the reformer 300 through a long-distance transfer line, and thus, by mixing the steam transferred in the superheated steam transfer line 310 with the steam discharged from the top of the column and then transferring the mixture to the reformer 300, the energy of the superheated steam can be fully utilized and the recovery of the steam in the stripper can be realized. In particular, the controller 110 may collect the gas pressure measured by the pressure sensor 330 on the steam output line 160, and if the gas pressure is too high, the valve of the pressure control valve 320 on the superheated steam delivery line 310 is decreased, and conversely, the valve is increased. In addition, by the pressure control valve 320, it is also ensured that these vapors after mixing can be mixed with a water to carbon ratio of 3:1, and is transferred to a conversion reaction furnace for reaction.

The acidic water purifying treatment device for the hydrocarbon conversion hydrogen production system realizes 100% closed cycle of the acidic water in the hydrocarbon conversion hydrogen production system, and has little influence on environment. The superheated steam generated by the conversion reaction furnace is reasonably utilized to be used for the stripping treatment of the acid water, and the steam stripping of the acid water with higher temperature and excessive steam is adopted, so that the stripping effect of the acid water is ensured. Then, the waste gas at the top of the tower generated after the stripping purification treatment is fully recovered as the steam of the raw material hydrocarbon distribution in the conversion reaction furnace, so that the water and the energy in the water vapor at the top of the tower are 100 percent recovered and utilized; and the purified water is used in the deaerator 800, so that the recycling of the purified water can be realized.

In addition, the steam stripping steam quantity of the high-pressure steam stripping tower 100 adopts cascade control of the tower top temperature and the steam stripping steam flow, so that poor steam stripping effect caused by inaccurate flow meters is avoided, and the cascade control is more reliable and more accurate than the simple flow meter control; the pressure of the stripping overhead vapor output line 160 is automatically controlled by the superheated vapor self-produced by the reformer 300 through the pressure control valve 320, ensuring the stability of the stripping overhead pressure and ensuring that there is sufficient vapor for raw material steam distribution, i.e., water-to-carbon ratio.

Any particular values in all examples shown and described herein are to be construed as merely illustrative and not a limitation, and thus other examples of exemplary embodiments may have different values.

It should be noted that: like reference numerals and letters denote like items in the following figures, and thus once an item is defined in one figure, no further definition or explanation thereof is necessary in the following figures.

The above examples only represent a few embodiments of the present application, which are described in more detail and are not to be construed as limiting the scope of the present application. It should be noted that it would be apparent to those skilled in the art that various modifications and improvements could be made without departing from the spirit of the present application, which would be within the scope of the present application.

Claims

1. The acidic water purifying treatment device is characterized by comprising a high-pressure stripping tower;

2. The sour water purification treatment device of claim 1, wherein the bottom of the high pressure stripper is further provided with a liquid level sensor;

3. The acidic water purifying treatment device according to claim 1, wherein the inside of the high-pressure stripping tower is provided with a silk screen packing layer, a tray or a packing respectively from top to bottom;

4. The sour water purification treatment device of claim 1, wherein the sour water inlet pipeline is further provided with a sour water preheater, and the sour water preheater is communicated with the purified water output pipeline.

5. An acidic water purification treatment apparatus according to any one of claims 1 to 4 wherein the acidic water purification treatment apparatus is for use in a hydrocarbon conversion hydrogen production system.

6. The sour water purification apparatus of claim 5, wherein the hydrocarbon conversion hydrogen production system comprises: a desulfurization reactor, a conversion reactor, a medium-change reactor, a gas-liquid separator and a PSA unit;

7. The sour water purification treatment apparatus of claim 6, wherein the sour water inlet communicates with the gas-liquid separator through the sour water inlet line;

8. The sour water purification apparatus of claim 6, wherein the superheated steam outlet of the reformer is further connected to the steam outlet line by a superheated steam delivery line;

9. The sour water purification apparatus of claim 6, wherein the hydrocarbon conversion hydrogen production system further comprises: a steam generator, a heat exchange cooler and a deaerator;

10. The apparatus according to claim 9, wherein the purified water output line is divided into two sub-lines, wherein a first sub-line is used for circulating the purified water when the deaerator is under an abnormal condition, a second sub-line is used for circulating the purified water when the deaerator is under a normal production condition, valves are respectively provided on the first sub-line and the second sub-line, and the second sub-line is connected to the liquid inlet of the deaerator.