CN216337451U - High-sulfur high-solid heavy oil (oil coal slurry) deep hydrodesulfurization system - Google Patents
High-sulfur high-solid heavy oil (oil coal slurry) deep hydrodesulfurization system Download PDFInfo
- Publication number
- CN216337451U CN216337451U CN202122978768.4U CN202122978768U CN216337451U CN 216337451 U CN216337451 U CN 216337451U CN 202122978768 U CN202122978768 U CN 202122978768U CN 216337451 U CN216337451 U CN 216337451U
- Authority
- CN
- China
- Prior art keywords
- liquid separator
- pressure gas
- tubular reactor
- stage
- gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 23
- 239000011593 sulfur Substances 0.000 title claims abstract description 23
- 239000007787 solid Substances 0.000 title claims abstract description 19
- 239000000295 fuel oil Substances 0.000 title claims abstract description 17
- 239000003250 coal slurry Substances 0.000 title abstract description 15
- 239000003921 oil Substances 0.000 title 1
- 239000007788 liquid Substances 0.000 claims abstract description 81
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 31
- 239000001257 hydrogen Substances 0.000 claims abstract description 31
- 239000012071 phase Substances 0.000 claims abstract description 24
- 239000007791 liquid phase Substances 0.000 claims abstract description 22
- 239000002994 raw material Substances 0.000 claims abstract description 22
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 21
- 239000007789 gas Substances 0.000 claims abstract description 15
- 150000002431 hydrogen Chemical class 0.000 claims abstract description 13
- 239000000047 product Substances 0.000 claims description 48
- 239000000758 substrate Substances 0.000 claims description 6
- 239000007795 chemical reaction product Substances 0.000 claims description 4
- 239000010742 number 1 fuel oil Substances 0.000 claims 6
- 239000002002 slurry Substances 0.000 claims 6
- 239000002912 waste gas Substances 0.000 claims 1
- 238000005984 hydrogenation reaction Methods 0.000 abstract description 5
- 238000000926 separation method Methods 0.000 abstract description 5
- 238000006243 chemical reaction Methods 0.000 description 15
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 11
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 11
- 239000000571 coke Substances 0.000 description 8
- 239000012535 impurity Substances 0.000 description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 238000004517 catalytic hydrocracking Methods 0.000 description 3
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 230000007774 longterm Effects 0.000 description 2
- 239000013049 sediment Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000002010 green coke Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 238000005987 sulfurization reaction Methods 0.000 description 1
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
本实用新型公开了一种高硫高含固重油(油煤浆)深度加氢脱硫系统,高硫高含固重油、四级高压气液分离器底部的重质产物、新氢与循环氢混合,四者共同从顶部进入一级管式反应器,产物经一级高压气液分离器分为气相和液相,气相产物进入低压气液分离器,液相产物作为二级管式反应器的原料;二级管式反应器产物进入二级高压气液分离器,气相产物进入低压气液分离器,液相产物作为三级管式反应器的原料;三级管式反应器产物进入三级高压气液分离器,气相产物进入低压气液分离器,液相产物进入四级高压气液分离器进一步分离;低压分离器顶部产物部分外排,部分作为循环氢,底部产物作为后续进一步加工的原料。本实用新型提高加氢反应和加氢脱硫的效率。
The utility model discloses a high-sulfur and high-solids heavy oil (oil-coal slurry) deep hydrodesulfurization system. The high-sulfur and high-solids heavy oil, the heavy product at the bottom of a four-stage high-pressure gas-liquid separator, new hydrogen and circulating hydrogen are mixed , the four together enter the first-stage tubular reactor from the top, the product is divided into gas phase and liquid phase through the first-stage high-pressure gas-liquid separator, the gas-phase product enters the low-pressure gas-liquid separator, and the liquid-phase product is used as the secondary tubular reactor. Raw material; the product of the secondary tubular reactor enters the secondary high-pressure gas-liquid separator, the gas-phase product enters the low-pressure gas-liquid separator, and the liquid-phase product is used as the raw material of the tertiary tubular reactor; the product of the tertiary tubular reactor enters the third-stage tubular reactor In the high-pressure gas-liquid separator, the gas-phase product enters the low-pressure gas-liquid separator, and the liquid-phase product enters the four-stage high-pressure gas-liquid separator for further separation; part of the top product of the low-pressure separator is discharged, part is used as circulating hydrogen, and the bottom product is used for subsequent further processing. raw material. The utility model improves the efficiency of hydrogenation reaction and hydrodesulfurization.
Description
技术领域technical field
本实用新型涉及石油化工技术领域,特别涉及一种高硫高含固重油(油煤浆)深度加氢脱硫系统。The utility model relates to the technical field of petrochemical industry, in particular to a deep hydrodesulfurization system for high-sulfur and high-solids heavy oil (oil-coal slurry).
背景技术Background technique
高硫高含固重油油煤浆因其硫等非烃杂质高、固含量高等原因,对装置的长期稳定运行造成巨大影响,不易于高硫高含固重油油煤浆的深度脱硫。Due to the high non-hydrocarbon impurities such as sulfur and high solid content, the high-sulfur and high-solids heavy oil-coal slurry has a huge impact on the long-term stable operation of the device, and it is not easy to deeply desulfurize the high-sulfur and high-solids heavy oil-coal slurry.
首先,高硫高含固重油油煤浆因其硫含量较高,在加氢裂化过程中硫元素脱除后以硫化氢的形式进入反应体系中。在现有的技术体系中,硫化氢等杂质气体在整个反应过程中始终存在于反应系统中,直至全部反应结束后才从分离系统排出。大量的硫化氢等杂质气体的存在会对反应造成一定的影响,一方面会显著降低氢气分压,制约加氢反应的进行;另一方面,从化学平衡角度考虑,过量的硫化氢存在会抑制加氢脱硫生成硫化氢的反应正向进行,影响脱硫效率。First of all, due to the high sulfur content of high-sulfur and high-solids heavy oil-coal slurry, the sulfur element is removed in the hydrocracking process and then enters the reaction system in the form of hydrogen sulfide. In the existing technical system, impurity gases such as hydrogen sulfide always exist in the reaction system during the entire reaction process, and are not discharged from the separation system until the end of the entire reaction. The presence of a large amount of impurity gases such as hydrogen sulfide will have a certain impact on the reaction. On the one hand, it will significantly reduce the hydrogen partial pressure and restrict the hydrogenation reaction; on the other hand, from the perspective of chemical balance, the presence of excess hydrogen sulfide will inhibit the hydrogenation reaction. The reaction of hydrodesulfurization to hydrogen sulfide proceeds forward, which affects the desulfurization efficiency.
其次,高硫高含固重油油煤浆因固含量较高,较高的固含量就意味着大量的生焦中心。高硫高含固重油油煤浆含有大量的胶质沥青质等生焦组分,同时叠加高固含量,进一步促进焦炭的生成,影响装置的长周期稳定运行。Secondly, the high-sulfur and high-solids heavy oil-coal slurry has a high solid content, which means a large number of green coke centers. The high-sulfur and high-solids heavy oil-coal slurry contains a large amount of coke components such as colloidal asphaltenes, and at the same time superimposed with high solids content, it further promotes the formation of coke and affects the long-term stable operation of the device.
有鉴于此,有必要对管式反应器加氢脱硫工艺技术提出改进措施,提高加氢反应和加氢脱硫的效率。In view of this, it is necessary to propose improvement measures for the hydrodesulfurization process technology of the tubular reactor to improve the efficiency of hydrogenation reaction and hydrodesulfurization.
发明内容SUMMARY OF THE INVENTION
为了克服上述现有技术的不足,本实用新型的目的在于提供一种高硫高含固重油(油煤浆)深度加氢脱硫系统,将一段式反应器优化为三级串联的管式反应器,并且在各级反应器的出口设置高压气液分离器,使各级管式反应器产生的过量硫化氢气体及杂质排出反应体系,同时在各级管式反应器的入口补充新氢,进一步降低硫化氢等杂质气体含量,提高氢分压,促进加氢脱硫反应持续正向进行,达到深度加氢脱硫的目的;另外,管式反应器采用“上进下出”的形式,缩短原料在反应器中的停留、减少返混,降低生焦几率;最后在每个反应器底部设置排料口,使易于生焦的沉积物及部分焦炭排出系统,进一步降低生焦几率,延长装置的运行周期。In order to overcome the above-mentioned deficiencies of the prior art, the purpose of this utility model is to provide a deep hydrodesulfurization system for high-sulfur and high-solids heavy oil (oil-coal slurry), which optimizes the one-stage reactor into a three-stage series-connected tubular reactor. , and set up high-pressure gas-liquid separators at the outlets of the reactors at all levels, so that the excess hydrogen sulfide gas and impurities generated by the tubular reactors at all levels are discharged from the reaction system, and at the same time, new hydrogen is supplemented at the inlets of the tubular reactors at all levels, further Reduce the content of impurity gases such as hydrogen sulfide, increase the hydrogen partial pressure, and promote the continuous forward progress of the hydrodesulfurization reaction to achieve the purpose of deep hydrodesulfurization; In the reactor, reducing back mixing and reducing the probability of coke formation; finally, a discharge port is set at the bottom of each reactor, so that coke-prone sediment and part of the coke can be discharged from the system, further reducing the probability of coke formation and prolonging the operation period of the device .
为了实现上述目的,本实用新型采用的技术方案是:In order to achieve the above purpose, the technical scheme adopted by the present utility model is:
一种高硫高含固重油(油煤浆)深度加氢脱硫系统,包括一级管式反应器1,所述一级管式反应器1顶部的入口端连接新氢管网的新氢12、经循环氢压缩机9压缩的循环氢、来自原料罐区的重油油煤浆原料11与经高压泵泵送的四级高压气液分离器7底部产物组成的混合原料;A high-sulfur and high-solids heavy oil (oil-coal slurry) deep hydrodesulfurization system, comprising a first-stage tubular reactor 1, the inlet end of the top of the first-stage tubular reactor 1 is connected to the
所述一级管式反应器1底部输出端连接一级高压气液分离器4,一级高压气液分离器4顶部气相产物进入低压气液分离器8;The bottom output end of the first-stage tubular reactor 1 is connected to the first-stage high-pressure gas-
一级高压气液分离器4底部液相产物与新氢12混合输入二级管式反应器2顶部的输入端,二级管式反应器2的底部反应产物输出端连接二级高压气液分离器5输入端,二级高压气液分离器5顶部气相产物输出端连接低压气液分离器8,二级高压气液分离器5底物液相产物输出端与新氢12混合后连接三级管式反应器3顶部输入端,三级管式反应器3底部输出端连接三级高压气液分离器6;The liquid phase product at the bottom of the first-stage high-pressure gas-
三级高压气液分离器6顶部气相产物输出端连接低压气液分离器8,三级高压气液分离器6底部液相产物进入四级高压气液分离器7;四级高压气液分离器7顶部气相产物输出端连接低压气液分离器8,底部液相产物经高压泵10泵送至一级管式反应器1顶部;The output end of the gas-phase product at the top of the third-stage high-pressure gas-
所述低压气液分离器8底部为液相产物14,顶部为气相产物,部分作为外排废气13,部分作为循环氢返回。The bottom of the low-pressure gas-
所述一级管式反应器1、二级管式反应器2、三级管式反应器3出口均设置一个高压气液分离器。A high-pressure gas-liquid separator is set at the outlet of the first-stage tubular reactor 1, the second-stage
所述一级管式反应器1、二级管式反应器2、三级管式反应器3均为原料从反应器顶部进入,产物从反应器底部排出。The first-stage tubular reactor 1, the second-stage
所述一级高压气液分离器4、二级高压气液分离器5、三级高压气液分离器6顶部产物混合后进入低压气液分离器8;四级高压气液分离器7顶部气相产物进入低压气液分离器8。The top products of the first-stage high-pressure gas-
所述一级管式反应器1、二级管式反应器2、三级管式反应器3顶部均有补充新氢。The tops of the first-stage tubular reactor 1, the second-stage
所述一级管式反应器1、二级管式反应器2、三级管式反应器3底部均设置有排料口。The bottoms of the first-stage tubular reactor 1, the second-stage
本实用新型的有益效果:The beneficial effects of the present utility model:
本实用新型在各级管式反应器的出口均设置高压气液分离器,将富含硫化氢的气体排出反应系统,有效降低气相产物中的硫化氢对加氢脱硫反应的抑制作用,提高加氢脱硫反应进行的程度,从而达到深度加氢脱硫的目的;另外,本实用新型考虑到高硫高含固重油(油煤浆)易于生焦的性质,将进料方式调整为从各级管式反应器的顶部进料,减少物料的停留时间,减少生焦的几率;最后,根据四级高压气液分离器底部循环物料的性质及低压分离器底部产物的性质要求,调整四级高压气液分离器底部循环物料的循环量及各个反应器的循环比例。In the utility model, high-pressure gas-liquid separators are arranged at the outlets of the tubular reactors at all levels, and the gas rich in hydrogen sulfide is discharged from the reaction system, thereby effectively reducing the inhibitory effect of hydrogen sulfide in the gas-phase product on the hydrodesulfurization reaction, and improving the addition of hydrogen sulfide. The degree of hydrodesulfurization reaction is carried out, so as to achieve the purpose of deep hydrodesulfurization; in addition, the utility model takes into account the properties of high-sulfur and high-solids heavy oil (oil-coal slurry) that is easy to coke, and adjusts the feeding method to The top feeding of the reactor can reduce the residence time of the material and the probability of coke formation; finally, according to the properties of the circulating material at the bottom of the four-stage high-pressure gas-liquid separator and the properties of the product at the bottom of the low-pressure separator, adjust the four-stage high-pressure gas The circulating amount of the circulating material at the bottom of the liquid separator and the circulating ratio of each reactor.
附图说明Description of drawings
图1为本实用新型系统示意图。FIG. 1 is a schematic diagram of the system of the present invention.
具体实施方式Detailed ways
下面结合附图对本实用新型作进一步详细说明。The present utility model will be described in further detail below in conjunction with the accompanying drawings.
如图1所示,一种高硫高含固重油(油煤浆)深度加氢脱硫系统,包括如下步骤:As shown in Figure 1, a high-sulfur and high-solids heavy oil (oil-coal slurry) deep hydrodesulfurization system includes the following steps:
a.来自新氢管网的新氢12、经循环氢压缩机9压缩的循环氢、来自原料罐区的重油油煤浆原料11与经高压泵泵送的四级高压气液分离器7底部产物组成混合原料,混合原料在一级管式反应器1顶部进入发生加氢裂化反应;a. The
b.步骤a经加氢裂化反应后的产物由一级管式反应器1的底部流出,进入一级高压气液分离器4,一级高压气液分离器4顶部气相产物进入低压气液分离器8,底物液相产物作为二级管式反应器2的原料;b. The product after the hydrocracking reaction in step a flows out from the bottom of the first-stage tubular reactor 1 and enters the first-stage high-pressure gas-
c.步骤b一级高压气液分离器4底部液相产物与新氢12混合作为二级管式反应器2原料,反应产物从反应器底部排出进入二级高压气液分离器5。c. Step b The liquid phase product at the bottom of the first-stage high pressure gas-
d.步骤c二级高压气液分离器5顶部气相产物进入低压气液分离器8,底物液相产物作为三级管式反应器3的原料;D. step c secondary high-pressure gas-
e.步骤d二级高压气液分离器5底物液相产物与新氢12混合后作为三级管式反应器3的原料,反应产物从反应器底部排出进入三级高压气液分离器6。e. step d secondary high pressure gas-
f.步骤e三级高压气液分离器6顶部气相产物进入低压气液分离器8,底物液相产物进入四级高压气液分离器7;四级高压气液分离器7顶部气相产物进入低压气液分离器8,底部液相产物经高压泵10泵送至一级管式反应器1顶部。f. step e three-stage high-pressure gas-
g.步骤b、d、f中进入低压气液分离器8中物质发生分离,底部液相产物14作为后续进一步加工的原料;顶部气相产物部分作为外排废气13,部分作为循环氢返回。g. In steps b, d, and f, the substances entering the low-pressure gas-
所述原料包括高硫高含固重油和油煤浆,二者的硫含量均要求大于2.0w%,固含量要求大于3%。The raw materials include high-sulfur and high-solids heavy oil and oil-coal slurry, both of which are required to have a sulfur content greater than 2.0w% and a solid content greater than 3%.
一级管式反应器1、二级管式反应器2、三级管式反应器3出口均设置一个高压气液分离器,实现富含硫化氢气体的分离,降低加氢反应系统气氛中硫化氢含量,促进脱硫反应正向进行,达到深度加氢脱硫的目标。A high-pressure gas-liquid separator is installed at the outlet of the first-stage tubular reactor 1, the second-stage
所述一级管式反应器1、二级管式反应器2、三级管式反应器3均为原料从反应器顶部进入,产物从反应器底部排出。The first-stage tubular reactor 1, the second-stage
所述一级高压气液分离器4、二级高压气液分离器5、三级高压气液分离器6顶部产物混合后进入低压气液分离器8;四级高压气液分离器7顶部气相产物进入低压气液分离器8。需要注意的是二者进入低压气液分离器8的位置不同。The top products of the first-stage high-pressure gas-
所述一级管式反应器1、二级管式反应器2、三级管式反应器3顶部均有补充新氢。The tops of the first-stage tubular reactor 1, the second-stage
根据四级高压气液分离器7底部循环物料的性质及低压分离器底部产物14的性质要求,四级高压分离器7底部液相重质组分可以按照一定的比例分别返回至一级管式反应器1、二级管式反应器2、三级管式反应器3进一步深加工。According to the properties of the circulating material at the bottom of the fourth-stage high-pressure gas-
一级管式反应器1、二级管式反应器2、三级管式反应器3底部均设有排料口,保证反应过程中累积的结焦物和沉积物随时排出装置,保证装置的长周期稳定运行。The bottom of the first-stage tubular reactor 1, the second-stage
Claims (5)
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN202122978768.4U CN216337451U (en) | 2021-11-30 | 2021-11-30 | High-sulfur high-solid heavy oil (oil coal slurry) deep hydrodesulfurization system |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN202122978768.4U CN216337451U (en) | 2021-11-30 | 2021-11-30 | High-sulfur high-solid heavy oil (oil coal slurry) deep hydrodesulfurization system |
Publications (1)
Publication Number | Publication Date |
---|---|
CN216337451U true CN216337451U (en) | 2022-04-19 |
Family
ID=81156356
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
CN202122978768.4U Active CN216337451U (en) | 2021-11-30 | 2021-11-30 | High-sulfur high-solid heavy oil (oil coal slurry) deep hydrodesulfurization system |
Country Status (1)
Country | Link |
---|---|
CN (1) | CN216337451U (en) |
-
2021
- 2021-11-30 CN CN202122978768.4U patent/CN216337451U/en active Active
Similar Documents
Publication | Publication Date | Title |
---|---|---|
CN102168905B (en) | Feed gas processing device for natural gas | |
CN101559311B (en) | Step recovery method for centralizing refinery gas | |
CN204447667U (en) | Oil field associated gas separator | |
CN216337451U (en) | High-sulfur high-solid heavy oil (oil coal slurry) deep hydrodesulfurization system | |
RU56207U1 (en) | INSTALLING OIL CLEANING (OPTIONS) | |
WO2018177401A1 (en) | Method for increasing hydrogen partial pressure in hydrogenation reaction system, design method therefor and use thereof | |
CN104689769B (en) | Spent acid handles the integrated equipment and its operating method of Sulphuric acid ammonium | |
CN202024572U (en) | Natural gas feed gas processing device | |
CN103801545A (en) | Method for recycling silicon cutting sand by utilizing countercurrent washing of silicon cutting waste sand cake | |
CN217578783U (en) | Deep hydrodesulfurization and denitrification system for heavy oil | |
CN107541235B (en) | Two-stage condensation and separation method and separation system for oil gas at tower top of crude oil atmospheric distillation tower | |
CN103242923B (en) | Natural gas desulfurization device and desulfurization process applicable to production platform | |
CN216764813U (en) | Fuel gas heavy component recovery system | |
CN212669616U (en) | Fuel oil hydrogenation ammonia injection cracking device | |
CN214437714U (en) | Silane tail gas processing apparatus | |
CN204385135U (en) | Full cut catalytic gasoline selective hydrodesulfurization device | |
CN205152165U (en) | Carbon dioxide separator is deviate from to supersonic speed natural gas | |
CN1259404A (en) | Acrylonitrile reactor two stage cyclone separator | |
CN210595940U (en) | Heat conduction oil processing device | |
CN109681780B (en) | Complete gas well supercharging system based on reciprocating compressor and operation method | |
CN209155456U (en) | Fluid pressure type gas compression purification system | |
CN222700242U (en) | Hydrogenation process equipment | |
CN206279159U (en) | A kind of floating bed hydrogenation reaction system | |
CN221397549U (en) | Recovery device for biochemical anaerobic sludge | |
CN214991350U (en) | Hydrocracking tail gas recycling system |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
GR01 | Patent grant | ||
GR01 | Patent grant | ||
TR01 | Transfer of patent right |
Effective date of registration: 20250102 Address after: 710600 No. 1 Railway Station Street, Lintong District, Shaanxi, Xi'an Patentee after: THE NORTHWEST RESEARCH INSTITUTE OF CHEMICAL INDUSTRY CO.,LTD. Country or region after: China Address before: 710075 Yanchang Petroleum Research Center, 61 Tangyan Road, Xi'an City, Shaanxi Province Patentee before: SHAANXI YANCHANG PETROLEUM (Group) Co.,Ltd. Country or region before: China |
|
TR01 | Transfer of patent right |