CN105236645A - Hydrogenation acid water hydrogen sulfide recycling process and system thereof - Google Patents
Hydrogenation acid water hydrogen sulfide recycling process and system thereof Download PDFInfo
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- CN105236645A CN105236645A CN201510578474.9A CN201510578474A CN105236645A CN 105236645 A CN105236645 A CN 105236645A CN 201510578474 A CN201510578474 A CN 201510578474A CN 105236645 A CN105236645 A CN 105236645A
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- hydrogen sulfide
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
The present invention relates to a hydrogenation acid water hydrogen sulfide recycling process and a system thereof. According to the process, the tower kettle liquid of a desulfurization tower and hydrogenation acid water are subjected to heat exchange to make the acid water be heated so as to conveniently perform the subsequent treatment, the tower kettle liquid is cooled, the cooled tower kettle liquid can enter a deamination tower so as to be subjected to further treatment, the acid water and hot steam countercurrent steam stripping is used to obtain the high purity hydrogen sulfide gas so as to ensure the high removal rate of the hydrogen sulfide, pressurization is performed through a hydrogen sulfide compressor, and the pressurized material is injected into the hydrogen mixing pipeline of a hydrogenation reaction system so as to reduce the injection amount of carbon disulfide, such that the cost is saved, the sulfur emission is reduced, the economy of the hydrogenation system is improved, and the effects of energy saving and environmental protection are achieved.
Description
Technical field
The invention belongs to hydrogenation sour water processing technology field, be specifically related to recycling technique and the system of sour water hydrogen sulfide after a kind of hydrogenation.
Background technology
Oil hydrogenation reaction used catalyst mostly is oxidation state, does not have activity, needs sulfuration to be sulphided state at the hydrogenation initial stage, simultaneously for keeping active, preventing by hydrogen reducing is elemental metals, supplement enough sulphur to maintain, particularly in coal tar hydrogenating process, because feed sulphur content is less, supplement the sulfocompound such as Methyl disulfide and dithiocarbonic anhydride to maintain the activity of catalyzer, the hydrogen sulfide desulfurization again that reaction generates, meet the requirement of environmental protection, artificial interpolation sulphur, and then take off.Facility investment is large, and working cost is high.
Summary of the invention
The object of the present invention is to provide a kind of can hydrogen sulfide in efficient removal sour water the hydrogenation sour water hydrogen sulfide of recycle and reuse, economy, energy-saving and environmental protection recycles technique.
The object of the present invention is to provide and a kind ofly can realize above-mentioned technique and the hydrogenation sour water hydrogen sulfide recycling system that removal efficiency is high, stable, safety performance is high.
To achieve these goals, the technical solution adopted in the present invention is:
A kind of hydrogenation sour water hydrogen sulfide is recycled technique and is realized by following steps:
(1) to enter after the hydrogenation sour water being pressurized to 0.8 ~ 1.0MPa is heated to 110 ~ 140 DEG C in thionizer with 1.0MPa steam as stripped vapor by the desulfurization of adverse current stripping mode;
(2) the hydrogenation sour water heat exchange of the tower reactor hydrothermal solution after desulfurization and step (1) is lowered the temperature and is discharged afterwards, carry out deamination process, simultaneously, the hydrogen sulfide deviate from from thionizer tower top is divided into two portions, wherein a part of desulfuration retrieving arrangement hydrogen sulfide pipeline, another part enters after compression is pressurized to 8 ~ 25MPa in hydrogen sulfide compressor and discharges after the voltage stabilizing of surge tank buffering, recycles.
Above-mentioned steps (1) middle control thionizer bottom temperature is 150 ~ 170 DEG C, pressure is 0.6 ~ 0.8MPa, tower top temperature is 30 ~ 50 DEG C, and tower top pressure is 0.58 ~ 0.78MPa.
Realize the system that above-mentioned hydrogenation sour water hydrogen sulfide recycles technique, comprise force (forcing) pump, desulfurization interchanger, thionizer, surge tank and hydrogen sulfide compressor, wherein: force (forcing) pump is communicated with sour water inlet channel, the sour water entrance of desulfurization interchanger is communicated with force (forcing) pump by pipeline, sour water outlet is communicated with the fluid inlet of thionizer by pipeline, tower bottoms entrance to be communicated with liquid outlet at the bottom of the still of thionizer by pipeline and tower bottoms is exported and is communicated with deammoniation tower by pipeline; The steam-in of thionizer is communicated with steam-pipe, the outlet of tower top hydrogen sulfide is communicated with surge tank entrance with sulfur recovery unit hydrogen sulfide pipeline respectively by pipeline, and the outlet of surge tank is communicated with hydrogen sulfide compressor by pipeline.
It is utilize thionizer tower bottoms and the heat exchange of hydrogenation sour water that sour water is heated up to be convenient to subsequent disposal that hydrogenation sour water hydrogen sulfide of the present invention recycles technique, tower bottoms cooling simultaneously can go deammoniation tower to process further, utilize sour water and hot steam adverse current stripping, obtain the hydrogen sulfide that purity is higher, ensure the high decreasing ratio of hydrogen sulfide, again by injecting the mixed hydrogen pipeline of hydrogenation reaction system after hydrogen sulfide compressor pressurization, to reduce the injection rate of dithiocarbonic anhydride, both the requirement maintaining catalyst activity can have been met, reduce desulfurization equipment scale simultaneously, play two effects obtained at one stroke, thus it is cost-saving, reduce sulphur emissions, both improve the economy of hydrogenation system, reach again the effect of energy-conserving and environment-protective, in addition, system run all right provided by the invention, security is high, be suitable for industrial application.
Accompanying drawing explanation
Fig. 1 is that the sour water hydrogen sulfide of embodiment 1 recycles process flow sheet.
Embodiment
Now by reference to the accompanying drawings technical scheme of the present invention is further described, but the present invention is not limited only to following enforcement situation.
Embodiment 1
As shown in Figure 1, the hydrogenation sour water hydrogen sulfide recycling system of the present embodiment is formed by pipeline serial connection by force (forcing) pump 1, desulfurization interchanger 2, thionizer 3, surge tank 4 and hydrogen sulfide compressor 5.
Wherein: hydrogenation sour water water inlet pipe is communicated with by the water-in of pipeline with force (forcing) pump 1, the water outlet of force (forcing) pump 1 is communicated with the sour water entrance of desulfurization interchanger 2 by pipeline, this desulfurization interchanger 2 also comprises tower bottoms entrance, tower bottoms outlet and sour water outlet, its tower bottoms entrance is communicated with the liquid outlet of thionizer 3 by pipeline, sour water is exported and is communicated with the tower top fluid inlet of thionizer 3 by pipeline, namely utilizes hydrothermal solution and sour water at the bottom of the still of discharging at the bottom of thionizer 3 still in this desulfurization interchanger 2, carry out heat exchange and makes the temperature of sour water rise to 110 ~ 140 DEG C.The tower bottoms outlet of desulfurization interchanger 2 is communicated with deammoniation tower by pipeline, and the tower bottoms after heat exchange being lowered the temperature is delivered to the further deamination process of deammoniation tower.The thionizer 3 of the present embodiment is common stripping type thionizer 3, it offers sour water entrance on the top sidewall of tower body, top end socket offers hydrogen sulfide outlet, tower reactor sidewall offers steam-in, liquid outlet at the bottom of still is offered at the bottom of tower, the sour water entrance of thionizer 3 and the sour water outlet of desulfurization interchanger 2, sour water after heat exchange being heated up is introduced in thionizer 3, steam-in is communicated with steam-pipe, hot steam is passed in thionizer 3 body, the sour water of steam rise and fall forms adverse current, by adverse current stripping mode, the hydrogen sulfide in sour water is separated, at the bottom of the still of thionizer 3, liquid outlet is communicated with desulfurization interchanger 2, at the bottom of the still heat up stripping, hydrothermal solution introduces desulfurization interchanger 2 and sour water generation heat exchange.The hydrogen sulfide outlet of the thionizer 3 of the present embodiment is exported with tower top hydrogen sulfide respectively by pipeline and is communicated with surge tank 4 entrance with sulfur recovery unit hydrogen sulfide pipeline respectively by pipeline, desulfurizer is gone to carry out sulfur recovery a hydrogen sulfide part for disengaging, another part is voltage stabilizing buffer memory in surge tank 4, the top exit of surge tank 4 is communicated with hydrogen sulfide compressor 5 by pipeline, be delivered to hydrogenation reaction system after hydrogen sulfide being compressed supercharging by hydrogen sulfide compressor 5 and mix hydrogen pipeline, participate in reaction.
Realize hydrogenation sour water hydrogen sulfide recycling technique by above-mentioned system to be made up of following steps:
(1) enter in desulfurization interchanger 2 after the hydrogenation sour water that hydrogenation system produces is forced into 0.8 ~ 1.0MPa by force (forcing) pump 1, heat exchange is carried out with the tower reactor hydrothermal solution of thionizer 3, enter in thionizer 3 after being heated to 130 DEG C, the middle pressure steam of 1.0Mpa is passed into as stripped vapor in the tower reactor of thionizer 3, the hot steam risen and descending sour water form adverse current, by hot steam stripping mode, the hydrogen sulfide in sour water is separated, regulate the amount of stripped vapor, control bottom temperature 160 DEG C, pressure is 0.7MPa, adjusting tower jacking doses, control tower top temperature 40 DEG C, control tower pressure on top surface 0.65MPa, overhead extraction 40 DEG C of hydrogen sulfide.
(2) the hydrogenation sour water heat exchange of the tower reactor hydrothermal solution after desulfurization and step (1) is lowered the temperature and is discharged afterwards, carry out deamination process, simultaneously, the highly purified hydrogen sulfide deviate from from thionizer 3 tower top is divided into two portions, wherein a part of desulfuration retrieving arrangement hydrogen sulfide pipeline, another part cushions to enter after voltage stabilizing after compression is pressurized to 18MPa in hydrogen sulfide compressor 5 through surge tank 4 and discharges, and recycles.
Embodiment 2
The hydrogenation sour water hydrogen sulfide of the present embodiment is recycled technique and is made up of following steps:
(1) enter in desulfurization interchanger 2 after the hydrogenation sour water that hydrogenation system produces is forced into 0.8 ~ 1.0MPa by force (forcing) pump 1, heat exchange is carried out with the tower reactor hydrothermal solution of thionizer 3, enter in thionizer 3 after being heated to 110 DEG C, the middle pressure steam of 1.0Mpa is passed into as stripped vapor in the tower reactor of thionizer 3, the hot steam risen and descending sour water form adverse current, by hot steam stripping mode, the hydrogen sulfide in sour water is separated, regulate the amount of stripped vapor, control bottom temperature 150 DEG C, pressure is 0.6MPa, adjusting tower jacking doses, control tower top temperature 30 DEG C, control tower pressure on top surface 0.58MPa, overhead extraction 30 DEG C of hydrogen sulfide.
(2) the hydrogenation sour water heat exchange of the tower reactor hydrothermal solution after desulfurization and step (1) is lowered the temperature and is discharged afterwards, carry out deamination process, simultaneously, the highly purified hydrogen sulfide deviate from from thionizer 3 tower top is divided into two portions, wherein a part of desulfuration retrieving arrangement hydrogen sulfide pipeline, another part cushions to enter after voltage stabilizing after compression is pressurized to 8MPa in hydrogen sulfide compressor 5 through surge tank 4 and discharges, and recycles.
Embodiment 3
The hydrogenation sour water hydrogen sulfide of the present embodiment is recycled technique and is made up of following steps:
(1) enter in desulfurization interchanger 2 after the hydrogenation sour water that hydrogenation system produces is forced into 0.8 ~ 1.0MPa by force (forcing) pump 1, heat exchange is carried out with the tower reactor hydrothermal solution of thionizer 3, enter in thionizer 3 after being heated to 140 DEG C, the middle pressure steam of 1.0Mpa is passed into as stripped vapor in the tower reactor of thionizer 3, the hot steam risen and descending sour water form adverse current, by hot steam stripping mode, the hydrogen sulfide in sour water is separated, regulate the amount of stripped vapor, control bottom temperature 170 DEG C, pressure is 0.8MPa, adjusting tower jacking doses, control tower top temperature 50 C, control tower pressure on top surface 0.78MPa, overhead extraction 50 DEG C of hydrogen sulfide.
(2) the hydrogenation sour water heat exchange of the tower reactor hydrothermal solution after desulfurization and step (1) is lowered the temperature and is discharged afterwards, carry out deamination process, simultaneously, the highly purified hydrogen sulfide deviate from from thionizer 3 tower top is divided into two portions, wherein a part of desulfuration retrieving arrangement hydrogen sulfide pipeline, another part cushions to enter after voltage stabilizing after compression is pressurized to 25MPa in hydrogen sulfide compressor 5 through surge tank 4 and discharges, and recycles.
In above-described embodiment, unspecified annexation and technological operation belong to routine techniques, and those skilled in the art all can be known.
Claims (3)
1. hydrogenation sour water hydrogen sulfide recycles a technique, it is characterized in that being realized by following steps:
(1) to enter after the hydrogenation sour water being pressurized to 0.8 ~ 1.0MPa is heated to 110 ~ 140 DEG C in thionizer (3) with 1.0MPa steam as stripped vapor by the desulfurization of adverse current stripping mode;
(2) the hydrogenation sour water heat exchange of the tower reactor hydrothermal solution after desulfurization and step (1) is lowered the temperature and is discharged afterwards, carry out deamination process, simultaneously, the hydrogen sulfide deviate from from thionizer (3) tower top is divided into two portions, wherein a part of desulfuration retrieving arrangement hydrogen sulfide pipeline, another part enters after compression is pressurized to 8 ~ 25MPa in hydrogen sulfide compressor (5) and discharges after the voltage stabilizing of surge tank (4) buffering, recycles.
2. hydrogenation sour water hydrogen sulfide according to claim 1 recycles technique, it is characterized in that: described step (1) middle control thionizer (3) bottom temperature is 150 ~ 170 DEG C, pressure is 0.6 ~ 0.8MPa, tower top temperature is 30 ~ 50 DEG C, and tower top pressure is 0.58 ~ 0.78MPa.
3. one kind realizes the system of the hydrogenation sour water hydrogen sulfide recycling technique described in the claims 1 or 2, it is characterized in that: this system comprises force (forcing) pump (1), desulfurization interchanger (2), thionizer (3), surge tank (4) and hydrogen sulfide compressor (5), wherein: force (forcing) pump (1) is communicated with sour water inlet channel, the sour water entrance of desulfurization interchanger (2) is communicated with force (forcing) pump (1) by pipeline, sour water outlet is communicated with by the fluid inlet of pipeline with thionizer (3), tower bottoms entrance to be communicated with liquid outlet at the bottom of the still of thionizer (3) by pipeline and tower bottoms is exported and is communicated with deammoniation tower by pipeline, the steam-in of thionizer (3) is communicated with steam-pipe, the outlet of tower top hydrogen sulfide is communicated with surge tank (4) entrance with the hydrogen sulfide pipeline of sulfur recovery unit respectively by pipeline, and the outlet of surge tank (4) is communicated with hydrogen sulfide compressor (5) by pipeline.
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| CN201510578474.9A CN105236645A (en) | 2015-09-14 | 2015-09-14 | Hydrogenation acid water hydrogen sulfide recycling process and system thereof |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105642371A (en) * | 2016-01-19 | 2016-06-08 | 康乃尔化学工业股份有限公司 | Sulfur-tolerant shift catalyst circulating vulcanization process |
| CN108557934A (en) * | 2018-04-28 | 2018-09-21 | 海南金海浆纸业有限公司 | A kind of reduction alkali collection condensed water COD methods |
| CN111252839A (en) * | 2020-01-18 | 2020-06-09 | 河北荣特化工股份有限公司 | Novel process for treating hydrogenation type waste water and waste gas |
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| CN101898805A (en) * | 2010-02-09 | 2010-12-01 | 神华集团有限责任公司 | Two-tower stripping treatment method for sewage in coal chemical engineering equipment |
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| JP2006169079A (en) * | 2004-12-20 | 2006-06-29 | Oita Univ | Method of separating and recovering ammonia and hydrogen sulfide from desulfurization waste water |
| US20140056777A1 (en) * | 2009-10-22 | 2014-02-27 | Mitsubishi Heavy Industries, Ltd. | Ammonia recovery device and recovery method |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105642371A (en) * | 2016-01-19 | 2016-06-08 | 康乃尔化学工业股份有限公司 | Sulfur-tolerant shift catalyst circulating vulcanization process |
| CN105642371B (en) * | 2016-01-19 | 2019-01-22 | 康乃尔化学工业股份有限公司 | A kind of sulfur-resistant transformation catalyst circulating sulfuration technique |
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| CN111252839A (en) * | 2020-01-18 | 2020-06-09 | 河北荣特化工股份有限公司 | Novel process for treating hydrogenation type waste water and waste gas |
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