CN108342214A

CN108342214A - The hydrogen usage of the hydrogenation process and online second hydrogenation process of richness production foreign gas

Info

Publication number: CN108342214A
Application number: CN201710062569.4A
Authority: CN
Inventors: 何巨堂
Original assignee: Individual
Current assignee: Luoyang Rui Hua New Energy Technology Development Co Ltd
Priority date: 2017-01-22
Filing date: 2017-01-22
Publication date: 2018-07-31

Abstract

The hydrogen usage of the hydrogenation process and online second hydrogenation process of richness production foreign gas, it is related to the hydrogen usage of direct hydrogenation liquefaction of coal reaction process R1 and the online solvent oil hydrogenation stabilization process R2 using same high-pressure system, since R1 richnesses produce foreign gas, the hot gas separated by high pressure separator of charging of the online R2 of postposition of prior art is contained a large amount of impurities such as H₂O、H₂S、NH₃、HCL、CO、CO₂Catalyst performance and catalyst choice range are influenced, in order to improve cycle hydrogen purity, cooling, water-washing process WS can remove H₂O、H₂S、NH₃, HCL it can be difficult to abjection CO, CO₂Etc. the component for being insoluble in water, membrane separating process FR can remove part CO, and PSA can be with deep removal CO, CO₂, recycle hydrogen and/or new hydrogen after purification introduce R2 and form the low condition of harmful gas concentration conducive to R2 performance catalyst efficiencies, overall high-pressure system hydrogen purity can be improved and be conducive to reduce investment and energy consumption.

Description

The hydrogen usage of the hydrogenation process and online second hydrogenation process of richness production foreign gas

Technical field

The present invention relates to the hydrogen usages of the hydrogenation process and online second hydrogenation process of rich production foreign gas, are related to coal and add The hydrogen usage of hydrogen direct liquefaction reaction process R1 and the online solvent oil hydrogenation stabilization process R2 using same high-pressure system, by Foreign gas is produced in R1 richnesses, the hot gas separated by high pressure separator of charging of the online R2 of postposition of prior art is contained a large amount of impurities such as H₂O、H₂S、NH₃、 HCL、CO、CO₂Catalyst performance and catalyst choice range are influenced, in order to improve cycle hydrogen purity, cooling, water-washing process WS can To remove H₂O、H₂S、NH₃, HCL it can be difficult to abjection CO, CO₂Etc. the component for being insoluble in water, membrane separating process FR can remove portion Divide CO, PSA can be with deep removal CO, CO₂, recycle hydrogen and/or new hydrogen after purification introduce R2 and form the low item of harmful gas concentration Part is conducive to R2 and plays catalyst efficiency, and overall high-pressure system hydrogen purity can be improved and be conducive to reduce investment and energy consumption.

Background technology

Hydrogen supply hydrocarbon is described below.

Hydrogen supply hydrocarbon described herein refers to the hydrocarbon component with hydrogen supply function in the direct liquefaction reaction process of coal hydrogenation, Hydrogen supply hydrocarbon include the double ring arene of fractional saturation, fractional saturation polycyclic aromatic hydrocarbon, be the confession that direct hydrogenation liquefaction of coal process uses The ideal composition of hydrogen solvent naphtha.In hydrogen supply hydrocarbon, the hydrogen supply speed of dihydro body is all higher than tetrahydrochysene body, the dihydro body of thrcylic aromatic hydrocarbon and double The dihydro body of cycloaromatics is compared, and it is low that hydrogen supply speed has height to have；Although experiment it has been proved that polycyclic aromatic hydrocarbon without hydrogen supply capacity, There is the ability for transmitting hydrogen.At 400 DEG C, the opposite hydrogen supply speed of following component is as follows：

Direct hydrogenation liquefaction of coal process is described below.

Direct hydrogenation liquefaction of coal process of the present invention, refers under solvent naphtha existence condition by adding hydrogen to make coal liquefaction Method, according to the different there are many different process of solvent naphtha, the difference of catalyst and hydrogenation process conditions, such as following several Technique：

1. solvent adds hydrogen to extract liquefaction process：If any solvent refined coal process l and II (SRC-1 and SRC-II), Exxon donor solvent process EDS, Japanese New Energy Development Organization liquefaction process (NEDOL) etc., using hydrogen, but pressure is less high, and solvent naphtha has apparent work With；

2. Hydrogenation method：Such as the H coal process (H- of the old and new's liquefaction process (IG and the NewlG) and the U.S. of Germany ) etc. Coal this one kind is belonged to；

3. coal and residual oil joint processing method (C0processing)：Using residual oil as solvent naphtha together with coal once by anti- Device is answered, recycle oil is not had to；Hydrocracking occurs is converted into light oil to residual oil simultaneously.The U.S., Canada, Germany and former Soviet Union etc. are each There is different technique；

4. Chinese Shenhua Group coal direct liquefaction method；

5. a kind of thermally dissolving and catalytic method with lignite preparing liquid fuel that patent CN100547055C states clearly, belongs in lignite Pressure plus hydrogen direct liquefaction process, including Coal liquefaction process and liquefied coal coil hydrogenation modification process totally two processes.In order to carry The conversion ratio and realization coal feedstock of high coal direct liquefaction enter reactor, and coal leads to before entering reactor Coal dust often is made, is made into coal with the solvent naphtha for having good hydrogen supply capacity, coal is pressurized, enters coal liquefaction after heating Reactor.

During direct hydrogenation liquefaction of coal, no matter which kind of coal faces hydrogen direct liquefaction process, and target is to obtain oil product, is chased after The function of asking is " coal turns oil ", it is necessary to which existing chemical change is " coal hydrogenation ", and the common trait of current such technology is to make With solvent naphtha and catalyst, the conventional boiling range of solvent naphtha be generally 200~530 DEG C, it is most be 200~450 DEG C, solvent naphtha is most For distilled oil or its hydrogenation modification oil, contained aromatic hydrocarbons majority is the aromatic hydrocarbons of 2~4 ring structures.Therefore, either which kind of coal faces hydrogen Direct liquefaction process, the outer oil extraction of its generation or liquefied coal coil (being usually coal liquefaction light oil) or liquefied coal coil modified oil, as long as Its composition has raw material compositing characteristic of the present invention, can be processed using the method for the present invention.

Direct hydrogenation liquefaction of coal process of the present invention refers to using coal and molecule hydrogen that may be present as raw material, It is hydrogen supply dissolvent oil with specific oil product (being usually the hydrogenation modification oil of liquefied coal coil), in certain operating condition (as operated Temperature, operating pressure, solvent naphtha/coal weight ratio, hydrogen/solvent naphtha volume ratio and suitable hydrogenation catalyst) under, coal is directly sent out The reaction process of the hydrogenation liquefactions such as raw carbon-carbon bond thermal cracking, free radical stabilized hydrogenation.

Direct hydrogenation liquefaction of coal oil of the present invention, refers to the oil product that the Coal Liquefaction reaction process generates, it It is present in Coal Liquefaction reaction effluent, is the synthesis based on hydrogen supply dissolvent oil, reaction consumption coal and reaction transfer hydrogen Reaction product.

After direct hydrogenation liquefaction of coal reaction process works well, hydrogen supply dissolvent oil generally use Coal Liquefaction reacted The hydrogenation modification oil of the self-produced liquefied coal coil of journey (being usually the distillate that conventional boiling range is higher than 165 DEG C), liquefied coal coil add hydrogen to change Property process main target be production direct hydrogenation liquefaction of coal reaction process solvent naphtha, be exactly specifically to improve in oil product The content of " component with good hydrogen supply function ", for example naphthenic base benzene class, the content of bicyclic alkyl benzene class component are improved, it is based on Liquefied coal coil contains the fact that a large amount of double ring arenes and a large amount of thrcylic aromatic hydrocarbons, and liquefied coal coil hydrogenation modification process is one " suitable The hydrogenation process of degree aromatic hydrocarbons saturation ".

The final goal of Coal liquefaction process is the outer oil product supplied of production, and usual liquefied coal coil hydrogenation modification process generates Hydrogenation modification oil be two parts：A part is used as Coal liquefaction process hydrogen supply dissolvent oil, and a part is used as coal liquefaction The outer oil extraction of liquefaction process.In general, at least part coal liquefaction light oil that Coal liquefaction process generates is used as outside coal liquifaction process Oil extraction A, it is molten that remaining liquefied coal coil is used as liquefied coal coil hydrogenation modification process feedstock oil production Coal liquefaction process hydrogen supply There is the outer oil extraction of A and B two-way in agent oil and outer oil extraction B, the final whereabouts of the outer oil extraction of A and B two-way is typically each by depth at this time Hydrogen grading process is added to produce high-quality oil product such as diesel oil distillate, naphtha cut.

In direct hydrogenation liquefaction of coal reaction process, hydrogen supply dissolvent is substantially a kind of the most important of coal liquefaction positive reaction Foreground catalyst, he quickly provides most of reactive hydrogen of coal liquefaction, it directly decides pyrolysis free radical fragment The speed that flash hydrogcnation is stablized, thus thermal condensation is inhibited to react；In direct hydrogenation liquefaction of coal reaction process, solid catalyst Such as pyrite, molybdenum sulfide are substantially a kind of retarding agents of coal liquefaction negative reaction, and it is big that solid catalyst particle adsorbs viscosity Colloid, asphaltene molecules MK, and MK is made to be contacted with the reactive hydrogen of solid catalyst surface, to inhibit its pyrocondensation；In coal hydrogenation In direct liquefaction reaction process, solid catalyst such as pyrite, molybdenum sulfide etc. substantially simultaneously or a kind of hydrogen supply agent dehydrogen substance The recovery catalyst of SH-Z, solid catalyst particle adsorbs SH-Z, and SH-Z is made to be contacted with the reactive hydrogen of solid catalyst surface, To add hydrogen to be restored to the hydrogen supply hydrocarbon for having hydrogen supply capacity, it directly decides the recovery speed of hydrogen supply agent dehydrogen substance SH-Z； In direct hydrogenation liquefaction of coal reaction process, substantially still a kind of target is hydrocracked anti-solid catalyst such as pyrite etc. simultaneously It should be such as asphaltene, the weak action catalysts of preasphaltene being hydrocracked.Therefore, in direct hydrogenation liquefaction of coal reaction process, In certain sense, solid catalyst such as pyrite, molybdenum sulfide etc. is more like a kind of catalyst of backstage running, to coal liquefaction Target product distillate plays a kind of support property and the effect of promotion property.In coal hydrogenation liquefaction reaction process R10, since hydrogen supply is molten The effect of agent DS is extremely important, and therefore, the operating condition and effect of solvent oil hydrogenation stabilization reaction process are naturally of crucial importance.

The online solvent oil hydrogenation modified-reaction process of existing direct hydrogenation liquefaction of coal technique is reacted with coal hydrogenation liquefaction The flow relationship of process R10, is divided into the off-line type i.e. solvent oil hydrogenation antihunt means of separate high pressure system and postposition is online i.e. Solvent oil hydrogenation steady decrease investment and energy consumption are carried out by the high-pressure system of the hot gas separated by high pressure separator of secondary use R10 products R10P, Off-line type stabilized hydrogenation method good product quality but investment is big, and the online stabilized hydrogenation method investment of postposition is saved, still There is by the H in R10 products₂O、NH₃、H₂S、CO、CO₂, HCL introduce stabilized hydrogenation reaction process to deteriorate hydrogen supply dissolvent The catalyst operation efficiency (cause catalyst life short, hydrogen supply dissolvent unstable quality) of stabilized hydrogenation reaction process and limitation plus The significant deficiency of stabilized hydrogen catalyst choice range.

About existing direct hydrogenation liquefaction of coal reaction process and solvent oil hydrogenation steady production hydrogen supply agent reaction process Path combination method, a document for recording this kind of data are shown in document A01：1. publication title：《Coal direct liquefaction technique with Engineering》, page 130 to page 365；2. retrieval is encoded with books：ISBN is encoded：9-78703-04308-23；3. writing：Wu Xiuzhang, Shu Geping, Li Kejian, Xie Shunmin；4. publishing house：Science Press.

Document A01《Coal direct liquefaction technique and engineering》Page 214 to page 216 to describe hydrogen supply dissolvent stabilized hydrogenation anti- The impurity of process and coal hydrogenation liquefaction reaction process R10, the yield of carburet hydrogen are answered, sees Tables 1 and 2.

1 BSU coal direct liquefaction material balance tables of table

Project	Into/maf.wt%	Into/maf.wt%	Go out/maf.wt%	Go out/maf.wt%	Into-go out/maf.wt%
						H₂S	0.00	0.00	0.72	0.68	0.72
NH₃	0.00	0.00	0.36	0.34	0.36
						CO	0.00	0.00	0.99	0.94	0.99
CO₂	0.00	0.00	1.46	1.39	1.46
						C₁	0.00	0.00	3.46	3.29	3.46
C₂	0.00	0.00	2.79	2.66	2.79
						C₃	0.00	0.00	3.32	3.16	3.32
C₄	0.00	0.00	1.83	1.74	1.83
						Solvent	128.52	122.22	0.00	0.00	-128.52
Oily (220 DEG C of ＜)	0.00	0.00	25.33	24.09	25.33
						Oily (220 DEG C of ＞)	0.00	0.00	30.01	28.54	30.01
Solvent materials	0.00	0.00	128.52	122.22	128.52
						H₂O	0.00	0.00	12.27	11.67	12.27
538 DEG C or more fractions	0.00	0.00	15.21	14.46	15.21
						H₂	5.65	5.37	0.00	0.00	-5.65
Moisture-and-ash-free basis coal	100.00	95.10	8.78	8.35	-91.22
						Ash	5.15	4.90	5.15	4.90	0.00
Catalyst-Fe	1.05	1.00	1.05	1.00	0.00
						Catalyst-other	0.61	0.58	0.23	0.22	-0.38
Sulphur	1.20	1.14	0.69	0.66	-0.51
						DMDS	0.00	0.00	0.00	0.00	0.00
It is total	242.18	230.32	242.18	230.32	0.00

2 BSU solvent hydrogenation unit material balance tables of table

Project	Into/maf.wt%	Into/maf.wt%	Go out/maf.wt%	Go out/maf.wt%	Into-go out/maf.wt%
						H₂S	0.00	0.00	1.41	1.34	1.41
NH₃	0.00	0.00	0.21	0.20	0.21
						CO	0.00	0.00	0.00	0.00	0.00
CO₂	0.00	0.00	0.00	0.00	0.00
						C₁	0.00	0.00	0.71	0.68	0.71
C₂	0.00	0.00	0.03	0.02	0.03
						C₃	0.00	0.00	0.03	0.02	0.03
C₄	0.00	0.00	0.03	0.03	0.03
						Solvent	0.00	0.00	128.73	122.42	128.73
Oily (220 DEG C of ＜)	0.00	0.00	0.00	0.00	0.00
						Oily (220 DEG C of ＞)	0.00	0.00	0.00	0.00	0.00
Solvent feed	128.52	122.22	0.00	0.00	-128.52
						H₂O	0.00	0.00	0.47	0.45	0.47
538 DEG C or more fractions	0.00	0.00	0.00	0.00	0.00
						H₂	1.16	1.11	0.00	0.00	-1.16
Moisture-and-ash-free basis coal	0.00	0.00	0.00	0.00	0.00
						Ash	0.00	0.00	0.00	0.00	0.00
Catalyst-Fe	0.00	0.00	0.00	0.00	0.00
						Catalyst-other	0.00	0.00	0.00	0.00	0.00
Sulphur	0.00	0.00	0.00	0.00	0.00
						DMDS	1.93	1.83	0.00	0.00	-1.93
It is total	131.61	125.16	131.61	125.16	0.00

For hydrogen supply dissolvent stabilized hydrogenation reaction process RXO and coal hydrogenation liquefaction reaction process R10, raw material impurity is contained Amount, impurity hydrogenation conversion, gas Auditory steady-state responses carry out statistical comparison, can obtain to draw a conclusion：

1. liquefaction coal, typically miscellaneous the element such as high coal of oxygen, sulphur, nitrogen content, direct hydrogenation liquefaction of coal process are typically The higher process of impurity conversion ratio, impurity composition such as H₂O、NH₃、H₂S、CO、CO₂Yield it is larger；

2. the high coal of liquefaction coal, the typically content of organic matter, direct hydrogenation liquefaction of coal process is typically organic matter liquefaction The higher process of conversion ratio, conventional gas hydrocarbon such as CH₄、C₂、C₃、C₄Yield it is larger；

3. the raw material hydrocarbon of hydrogen supply dissolvent stabilized hydrogenation reaction process R20, typically miscellaneous element such as oxygen, sulphur, nitrogen content are low Hydro carbons, direct hydrogenation liquefaction of coal process are typically the lower process of impurity conversion ratio, impurity composition such as H₂O、NH₃、H₂S、CO、 CO₂Yield it is smaller；

4. hydrogen supply dissolvent stabilized hydrogenation reaction process RXO, the typically lower process of cracking conversion rate, conventional gas hydrocarbon is such as CH₄、C₂、C₃、C₄Yield it is smaller.

Based on above-mentioned conclusion, it is presently believed that by the introducing of the recycle hydrogen after the extremely low new hydrogen of impurity concentration and/or purification Solvent oil hydrogenation stablizes reaction process, and the foreign gas, carburet hydrogen quantity in reaction process and product are seldom, also, solvent The oily separating obtained hot gas separated by high pressure separator RXOP-V of stabilized hydrogenation reaction process RXO products RXOP, can react into coal hydrogenation liquefaction Journey R10 realizes secondary efficiently use.In this way, both can avoid " by the H in R10 products₂O、NH₃、H₂S、CO、CO₂, HCL introduce plus Stabilized hydrogen reaction process RXO is to deteriorated catalyst operation efficiency and limits stabilized hydrogenation catalyst choice range " technique lack It falls into, while can realize the secondary use of circulating hydrogen again, forward type solvent oil hydrogenation can be formed and stablize reaction process RXO and coal Hydrogenation oil reaction process R10 combined methods form the hydrogenation process of the rich production foreign gas of concise flow a kind of and online the The hydrogen usage of two hydrogenation processes；Certainly, basic thought of the invention is also applied for using low impurity hydrogen process solvent oil such as Distillate, the parallel solvent oil hydrogenation stabilization process of circulating hydrogen of warm high score oil or rear-mounted solvent oil hydrogenation is fractionated to stablize Process.

So far, the basic imagination of the present invention has been formed：The hydrogenation process and online second plus hydrogen mistake of richness production foreign gas The hydrogen usage of journey is related to direct hydrogenation liquefaction of coal reaction process R1 and uses the online solvent oil hydrogenation of same high-pressure system steady The hydrogen usage for determining process R2, since R1 richnesses produce foreign gas, the hot gas separated by high pressure separator of charging of the online R2 of postposition of prior art contains A large amount of impurity such as H₂O、H₂S、NH₃、HCL、CO、CO₂Catalyst performance and catalyst choice range are influenced, in order to improve recycle hydrogen Purity, cooling, water-washing process WS can remove H₂O、H₂S、NH₃, HCL it can be difficult to abjection CO, CO₂Etc. the component for being insoluble in water, Membrane separating process FR can remove part CO, and PSA can be with deep removal CO, CO₂, recycle hydrogen and/or new hydrogen after purification introduce R2 It forms the low condition of harmful gas concentration and is conducive to R2 performance catalyst efficiencies, overall high-pressure system hydrogen purity can be improved and be conducive to Reduce investment and energy consumption.

The present invention can be used for the hydrocarbon material heat from hydrogenation cracking reaction process R1 of rich production foreign gas, be suitable for rich production CO and/or CO₂Hydrocarbon material heat from hydrogenation cracking reaction process R1, hydrocarbon the material such as coal and/or coal tar high particularly suitable for oxygen content plus Hydrogen heat cracking reaction process R1.

The method of the invention has not been reported.

In order to optimize effect of the present invention, group technology can be combined into other multiple technologies.

The hydro carbons of the suitable boiling range of at least part obtained by heat of dissociation high score oil R10P-HS-L can be introduced online solvent Stabilized hydrogenation reaction process RXO can produce short route lightweight hydrogen supply hydrocarbon, and at this moment, RXO reaction products or its high pressure detach hydrocarbon ils Or its high pressure separation gas part enters R1；Short route lightweight hydrogen supply hydrocarbon can be produced and/or match the long flow lightweight hydrogen supply of coal slurry Hydrocarbon, at this moment, the hot high score oil RXOP-HS-L in part enter separation/fractional distillation process and isolate with coal slurry lightweight hydrogen supply hydrocarbon.

A part of raffinate obtained by heat of dissociation high score oil R10P-HS-L can be introduced direct hydrogenation liquefaction of coal reaction process R1。

Joint can be processed oil plant such as coal tar or its fraction, introduce direct hydrogenation liquefaction of coal reaction process R1.

Joint can be processed oil plant such as coal tar or its distillate, introduce online solvent stabilized hydrogenation reaction process RXO.

Online solvent stabilized hydrogenation reaction process RXO, can be two different stabilized hydrogenation reaction process RXO, can be with It is two stabilized hydrogenation reaction process RXO that are not exactly the same but having operative combination relationship, for example,

The solvent oil hydrogenation of high boiling hydrocarbon HBML obtained by heat of dissociation high score oil R10P-HS-L can be stablized reaction process R20 stablizes reaction process R30 with short route solvent oil hydrogenation, carries out the combination of high-pressure system, such as by high boiling hydrocarbon HBML's Solvent oil hydrogenation stablizes a part for hot high score oil obtained by the high pressure hot separator of reaction process R20 products R20P, with short route A part for hot high score oil, mixes obtained by the high pressure hot separator of online solvent hydrogenation process R30 products R30P The initial hydrogenation liquefaction reaction process for entering R10 with coal slurry mixing hydrogen supply hydrocarbon is isolated into separation/fractional distillation process, simultaneously The remainder of hot high score oil obtained by the high pressure hot separator of the online solvent hydrogenation process R30 products R30P of short route is separated Enter the intermediate hydrogenation liquefaction reaction process of R10, while the solvent oil hydrogenation of high boiling hydrocarbon HBML is stablized into reaction process R20 products The remainder of hot high score oil obtained by the high pressure hot separator of R20P introduces the last hydrogenation liquefaction reaction process of R10, in this way, logical Classification injection hydrogen supply dissolvent in batches is crossed, is rationally realized " the sufficient hydrogen supply dissolvent of quantity is dispersed in all reaction compartments ".

Rear-mounted online solvent oil hydrogenation stablizes reaction process R30, can be charging with hot gas separated by high pressure separator R10P-HS-V, can use The cold oil of the warm high score process of hot gas separated by high pressure separator R10P-HS-V is charging, can use the warm high score process of hot gas separated by high pressure separator R10P-HS-V Cold oil hydrogen air lift after oil for charging, other similar materials, short cycle light recycle hydrogen supply agent SR- can be processed simultaneously Enter direct hydrogenation liquefaction of coal process R10 after LBDS pressurizations.

The online solvent hydrogenation process R30 of forward type can process the warm high score process of hot gas separated by high pressure separator R10P-HS-V Liquid after the supercharging of cold oil, can process other similar materials simultaneously, and short cycle light recycle hydrogen supply agent SR-LBDS can be according to Enter direct hydrogenation liquefaction of coal process R10 by pressure itself.

It can be arranged or combine setting high boiling point solvent oil stabilized hydrogenation reaction process R30 production higher boiling hydrogen supply agent HBDS, Processing carrys out the normal boiling point of self-heating high score oil R10P-HS-L between 200~530 DEG C of the hydrocarbon component.

Therefore, an object of the present disclosure is the hydrogen of the hydrogenation process and online second hydrogenation process that propose rich production foreign gas Gas usage.

Second purpose of the invention is to propose a kind of direct liquefaction reaction process light solvent oil of the coal hydrogenation of concise flow Short route round-robin method stablizes reaction process R30 and the sides of combination coal hydrogenation liquefaction reaction process R10 for forward type solvent oil hydrogenation Method.

The purpose of third of the present invention is to propose a kind of direct liquefaction reaction method of coal hydrogenation of the injection hydrogen supply dissolvent of classification in batches.

4th purpose of the invention is the hydrogen of the hydrogenation process and online second hydrogenation process that propose a rich production foreign gas The group technology of usage and the direct liquefaction reaction method of a variety of coal hydrogenations.

Invention content

The hydrogen usage of the hydrogenation process and online second hydrogenation process of rich production foreign gas of the invention, it is characterised in that packet Containing following steps：

The hydrogenation process of the rich production foreign gas, refers to the oxygen-containing member that a part of heat from hydrogenation cracking reaction at least occurs The hydrogenation process R1 of the hydrocarbon material R1F of element；

Online second hydrogenation process refers to adding hydrogen using same high pressure hydrogen system with hydrogenation process R1 Reaction process；

It is described to use same high pressure hydrogen system, refer to the hydrogen object of the second hydrogenation process R2 and hydrogenation process R1 1 kind or several in following of material relationship：

1. the compressor of the circulating hydrogen of hydrogenation process R1, the compressor with the circulating hydrogen of the second hydrogenation process R2 Mutually share；The circulation loop of the circulating hydrogen of at least part hydrogenation process R1 and the second hydrogenation process of at least part The circulation loop of the circulating hydrogen of R2 is parallel relationship；

2. hydrogenation process R1 and the second hydrogenation process R2, there are series relationships on circulating hydrogen circuit, i.e., at least A part of circulating hydrogen series connection is across the second hydrogenation process R2 and hydrogenation process R1；

3. the compressor of the new hydrogen of hydrogenation process R1, the compressor with the new hydrogen of the second hydrogenation process mutually share, The new hydrogen and part to the new hydrogen that whole hydrogenation process R1 are consumed of second hydrogenation process consumption enter second plus hydrogen mistake together Journey；

During normal production, the circulating hydrogen compressor of hydrogenation process R1 does not convey hydrogen to the second hydrogenation process；Newly When the amounts of hydrogen of hydrogen compressor conveying cannot meet the second hydrogenation process and need, the circulating hydrogen compression of hydrogenation process R1 Machine conveys at least part hydrogen to the second hydrogenation process；

The hydrogen that the circulating hydrogen compressor is conveyed to the second hydrogenation process, a kind or several in following：

1. the hydrogen-rich gas R2P-RH of the separation process from the second hydrogenation process product R2P, into the second hydrogenation process；

2. the thermal high separation process R1P-HTS of the product R1P of hydrogenation process R1 obtains hot gas separated by high pressure separator R1P-HTSV, The gas phase of logistics based on hot gas separated by high pressure separator R1P-HTSV is dissolved in water by hydrocarbon gas condensing steps, at least partly foreign gas component Dissolving step after into cold anticyclone separation process obtain cold gas separated by high pressure separator R1P-CTSV, the cold gas separated by high pressure separator R1P-CTSV of at least part Level-one purification circulating air 1ST-PH, at least part one are obtained after membrane separating process FR removes at least part foreign gas Grade purification circulating air 1ST-PH enters the second hydrogenation process；

3. the thermal high separation process R1P-HTS of the product R1P of hydrogenation process R1 obtains hot gas separated by high pressure separator R1P-HTSV, The gas phase of logistics based on hot gas separated by high pressure separator R1P-HTSV is dissolved in water by hydrocarbon gas condensing steps, at least partly foreign gas component The step of after into cold anticyclone separation process obtain cold gas separated by high pressure separator R1P-CTSV, the cold gas separated by high pressure separator R1P-CTSV of at least part passes through Membrane separating process FR obtains level-one purification circulating air 1ST-PH after removing at least part foreign gas, and at least part level-one carries Pure circulating air 1ST-PH obtains two level purification circulating air 2ST- after pressure-swing absorption process removes at least part foreign gas PH, at least part two level purify circulating air 2ST-PH and enter the second hydrogenation process.

The present invention, in general, the hydrogenation process R1 of the rich production foreign gas, refers to that a part of heat from hydrogenation, which at least occurs, to be split Change the hydrocarbon material heat from hydrogenation cracking reaction process R1 containing oxygen element of reaction；

Online second hydrogenation process refers to using the solvent of same high pressure hydrogen system with hydrogenation process R1 Oily stabilized hydrogenation reaction process R2；

Solvent oil hydrogenation stablizes reaction process R2, refers to the hydrogenation process R2 of production hydrogen supply hydrocarbon.

The present invention, generally, at least part circulating hydrogen that circulating hydrogen compressor KC is sent out firstly flows through second plus hydrogen mistake Journey R2 then passes through hydrogenation process R1, and finally returns that circulating hydrogen compressor KC.

The present invention, hydrogenation process R1 are to generate CO and/or CO₂Heat from hydrogenation cracking reaction process R1, can be selected from down One or more of row process：

1. the heat from hydrogenation cracking reaction process R1 of oil product obtained by direct hydrogenation liquefaction of coal liquefaction process, including use hydrogen supply molten The direct hydrogenation liquefaction of coal liquefaction process of agent oil, coal refines process to oil altogether, coal faces hydrogen thermosol liquefaction process；

2. the heat from hydrogenation cracking reaction process R1 of oil product obtained by middle coalite tar or its distillate or its hot procedure； Hot procedure is coking heavy oil process or heavy oil catalytic cracking process or heavy oil catalytic pyrolysis process or heat from hydrogenation cracking process；

3. the heat from hydrogenation cracking reaction process R1 of oil product obtained by high temperature coal-tar or its distillate or its hot procedure；

4. the heat from hydrogenation cracking reaction process R1 of oil product obtained by shale oil or its distillate or its hot procedure；

5. the heat from hydrogenation cracking reaction process R1 of oil product obtained by petroleum based heavy fuel oils or its hot procedure；Hot procedure is Coking heavy oil process or heavy oil catalytic cracking process or heavy oil catalytic pyrolysis process or heat from hydrogenation cracking process；

6. the heat from hydrogenation cracking reaction process R1 of oil product obtained by tar sand base weight oil or its hot procedure；Hot procedure It is oil product obtained by coking heavy oil process or heavy oil catalytic cracking process or heavy oil catalytic pyrolysis process or its hot procedure；

7. the heat from hydrogenation cracking reaction process R1 of hydrocarbon ils of other organic oxygen weight contents higher than 0.5%.

The present invention, in general, CO and/or CO that the hydrogenation process R1 of hydrocarbon material R1F is generated₂Weight yield be 0.5~ 5.0%.

The present invention, in general, CO in cold anticyclone separation gas obtained by the product R1P of separation hydrogenation process R1 and/or CO₂Volumetric concentration be 0.5~5.0%.

The present invention, in general, the volumetric concentration of the foreign gas in the feed hydrogen of the second hydrogenation process R2 is less than 10000PPm。

The present invention, generally, the volumetric concentration of the foreign gas in the feed hydrogen of the second hydrogenation process R2 are less than 5000PPm。

The present invention, preferably, the feed hydrogen of the second hydrogenation process R2, the volumetric concentration of foreign gas therein is less than 5000PPm, CO and/or CO therein₂Volumetric concentration be less than 1000PPm, NH therein₂Volumetric concentration be less than 700PPm.

The present invention, preferably, the feed hydrogen of the second hydrogenation process R2, the volumetric concentration of foreign gas therein are less than 5000PPm, CO and/or CO therein₂Volumetric concentration be less than 100PPm, NH therein₂Volumetric concentration be less than 500PPm.

The present invention, the best, the feed hydrogen of the second hydrogenation process R2, the volumetric concentration of foreign gas therein are less than 5000PPm, CO and/or CO therein₂Volumetric concentration be less than 20PPm, NH therein₂Volumetric concentration be less than 200PPm.

Specific implementation mode

The present invention described in detail below.

Pressure of the present invention, refers to absolute pressure.

Normal boiling point of the present invention refers to vapour of the substance under an atmospheric pressure, liquid equilibrium temperature.

Routine boiling range of the present invention refers to the normal boiling point range of fraction.

Proportion of the present invention, unless stated otherwise, refer to normal pressure, fluid density and normal pressure under the conditions of 15.6 DEG C, The ratio of water density under the conditions of 15.6 DEG C.

The composition or concentration or content or yield value of component of the present invention are unless stated otherwise weight basis Value.

Conventional gas hydrocarbon of the present invention refers to being in gaseous hydro carbons, including methane, ethane, third under normal condition Alkane, butane.

Conventional liq hydrocarbon of the present invention refers to the hydro carbons being in a liquid state under normal condition, including pentane and its boiling point Higher hydro carbons.

Impurity element of the present invention, refer to non-hydrogen in feedstock oil, non-carbon, nonmetallic ingredient for example oxygen, sulphur, nitrogen, Chlorine etc..

Impurity composition of the present invention refers to the hydro-conversion object such as H of non-hydrocarbon component in feedstock oil₂O、H₂S、NH₃、 HCL、CO、CO₂Deng.

Light hydrocarbon of the present invention is naphtha component, refers to that normal boiling point is less than 200 DEG C of conventional liq hydrocarbon.

Middle matter hydrocarbon of the present invention is diesel component, refers to that normal boiling point is 200~330 DEG C of hydro carbons.

Wax oil component of the present invention refers to that normal boiling point is 330~530 DEG C of hydro carbons.

Heavy hydrocarbon of the present invention refers to that normal boiling point is higher than 330 DEG C of hydro carbons.

Hydrogen to oil volume ratio of the present invention refers to the normal of the standard state volume flow of hydrogen and specified oily logistics The ratio of pressure, 20 DEG C of volume flow.

Polycyclic aromatic hydrocarbon mentioned herein, aromatic ring number >=3.

Up flow type hydrogenation reactor of the present invention, reaction compartment or the processing medium in hydrogenation catalyst bed Macroscopic view flowing dominant direction is from top to bottom.

The present invention described in detail below.

DCL/Direct coal liquefaction process is described below.

Hydrocarbon material of the present invention refers to carbon containing, protium liquid and/or solid, such as oil and/or coal.

Expanded bed reactor of the present invention is vertical up-flow reactor, and expanded bed reaction is belonged to when using catalyst Device；The vertical central axis upright for referring to working condition reactor after installing is in ground；Up flow type refers to reaction process object Material main body flow direction travels through reaction compartment or catalyst bed or the catalyst co-flow with uplink from bottom to top；Expanded bed Refer to that working condition catalyst bed is in swelling state, catalyst bed expansion ratio, which is defined as catalyst bed, has reaction former The ratio of the maximum height CWH of working condition when material passes through and the height CUH of the empty bed static condition of the catalyst bed KBED, in general, referred to as slight expanded-bed when KBED is less than 1.10, KBED between 1.25~1.55 when referred to as ebullated bed, and suspension bed It is considered as the expanded bed of most extreme form.

Back-mixing stream expanded bed reaction zone of the present invention refers to the mode of operation of the reaction zone using expanded bed reactor There are liquid stream back-mixings there is circulation fluid in other words；Back-mixing stream or circulation fluid refer to the intermediate product XK or final at flow points K At least part liquid phase XK-L in product X K is as the upstream reaction zones circulating fluid XK-LR return logistics XK, circulating fluid XK- The reaction product of LR flows through K points and is present among XK.The mode for forming back-mixing stream can be any appropriate mode, such as be arranged Built-in inner ring flow cartridge, built-in outer shroud flow cartridge, built-in liquid collecting cup+diversion pipe+circulating pump, external circulation pipe etc..

The liquid collecting cup or liquid trap being arranged in reactor of the present invention, refer to being arranged in reactor for collecting The container of liquid, usual top or upper side opening, bottom or lower side installation diversion pipe are for being discharged collection liquid；Expansion The top liquid trap of bed reactor, is typically mounted on the de- liquid zone of gas-liquid material, obtains liquid and gas-liquid mixed phase logistics or obtain Liquids and gases.

Hot high score device of the present invention, refers to the gas-liquid separation for detaching hydrogenation reaction intermediate product or final product Equipment.

DCL/Direct coal liquefaction process of the present invention refers to the side by adding hydrogen to make coal liquefaction under solvent naphtha existence condition Method according to the difference of solvent naphtha and catalyst, pyrolysis way and adds the difference of hydrogen mode and the difference of process conditions, Ke Yifen For following several techniques：

1. dissolving pyrolysis liquefaction process：Low-ash extract can be made to pyrolysis of coal extracting using heavy solvent, and (Japan claims Swelling charcoal)；Extract the available oils based on mink cell focus at supercritical conditions using light solvent.This method does not have to hydrogen, Though former process yield is high but product is still solid, latter technique such as supercritical extraction (extraction) method (SCE) extract content is not It is too high；

2. solvent adds hydrogen to extract liquefaction process：If any solvent refined coal process l and II (SRC-1 and SRC-II), Exxon donor solvent process EDS, Japanese New Energy Development Organization liquefaction process (NEDOL) etc., using hydrogen, but pressure is less high, and solvent naphtha has apparent work With；

3. Hydrogenation method：Such as the H coal process (H- of the old and new's liquefaction process (IG and the NewlG) and the U.S. of Germany ) etc. Coal this one kind is belonged to；

4. coal and residual oil joint processing method (C0processing)：Using residual oil as solvent naphtha together with coal once by anti- Device is answered, recycle oil is not had to.Hydrocracking occurs is converted into light oil to residual oil simultaneously.The U.S., Canada, Germany and former Soviet Union etc. are each There is different technique；

5. destructive distillation liquefaction process：Coal is first pyrolyzed and obtains tar, then carries out hydrocracking and upgrading to tar；

6. underground liquefaction process：Solvent is injected into subterranean coal, makes coal depolymerization and dissolving, in addition the impact force of fluid makes coal collapse It dissipates, the coal not being completely dissolved is then suspended in solvent, is extracted solution out with pump and is detached processing.

In coal direct liquefaction method, majority belongs to direct hydrogenation liquefaction of coal liquefaction process, and no matter which kind of coal faces the direct liquid of hydrogen Change process, target are to obtain oil product, and the function of pursuit is " coal turns oil ", it is necessary to which existing chemical change is that " coal adds Hydrogen ", the common trait of current such technology are that solvent naphtha and catalyst, the conventional boiling range of solvent naphtha is used to be generally 200~450 DEG C, it is most be 200~400 DEG C, solvent naphtha majority is distilled oil, and contained aromatic hydrocarbons majority is the aromatic hydrocarbons of 2~4 ring structures.Therefore, Either which kind of coal faces hydrogen direct liquefaction process, outer oil extraction that it is generated or liquefied coal coil (be usually coal liquefaction light oil) or coal liquid Carburetion modified oil can be processed as long as its composition has raw material compositing characteristic of the present invention using the method for the present invention.

What patent CN100547055C stated clearly a kind of is pressed with the thermally dissolving and catalytic of lignite preparing liquid fuel is owned by France in lignite Add hydrogen direct liquefaction process, including Coal liquefaction process and liquefied coal coil hydrogenation modification process totally two processes.In order to improve The conversion ratio and realization coal feedstock of coal direct liquefaction enter reactor, and coal enters before reactor usually Coal dust is made, is made into coal with the solvent naphtha for having good hydrogen supply capacity, coal is pressurized, it is anti-to enter coal liquefaction after heating Answer device.

Coal liquefaction process of the present invention is referred to using coal and molecule hydrogen that may be present as raw material, with spy Fixed oil product (being usually the hydrogenation modification oil of liquefied coal coil) is hydrogen supply dissolvent oil, certain operating condition (such as operation temperature, Operating pressure, solvent naphtha/coal weight ratio, hydrogen/solvent naphtha volume ratio and suitable hydrogenation catalyst) under, carbon directly occurs for coal The thermal cracking of carbon key, hydrogenation liquefaction reaction process.

Liquefied coal coil of the present invention refers to the oil product that the Coal liquefaction process generates, it is present in coal hydrogenation It is the combined reaction product based on hydrogen supply dissolvent oil, reaction consumption coal and reaction transfer hydrogen in liquefaction reaction effluent.

After Coal liquefaction process works well, the self-produced coal liquid of hydrogen supply dissolvent oil generally use Coal liquefaction process The hydrogenation modification oil of carburetion (being usually the distillate that conventional boiling range is higher than 165 DEG C), liquefied coal coil hydrogenation modification process it is main Target is production Coal liquefaction process solvent naphtha, is exactly specifically to improve in oil product " the group with good hydrogen supply function Point " content, for example improve naphthenic base benzene class, the content of bicyclic alkyl benzene class component, contained based on liquefied coal coil a large amount of bicyclic The fact that aromatic hydrocarbons and a large amount of thrcylic aromatic hydrocarbons, liquefied coal coil hydrogenation modification process be one " appropriate aromatic hydrocarbons saturation " plus hydrogen mistake Journey.

Up flow type expanded bed hydrogenation reactor of the present invention, the basic element of character usually have：

1. reactor shell；

2. the opening (or to take over) in reactor shell；

3. the up flow type being arranged in reactor enclosure body adds hydrogen main reaction space, usually using catalyst when working condition, Usually using charging distributed component for being uniformly distributed charging；

4. being arranged in the feed distributor of bottom in reactor enclosure body；

5. being arranged in the liquid collection cups LD and liquid conduits LK of epimere or middle epimere in reactor enclosure body；

6. reactor intermediate feed distributor (or distributor), the mixer of catalyst bed interlayer, such as cold hydrogen box；

7. rectification part is exported, such as collector, liquid phase discharge vortex-proof device, mixed phase product fairlead.

8. the measuring instrumentss that may be installed：The temperature-measuring part such as thermocouple of reaction bed temperature is tested, reactor is measured The pressure gauge of system specific location pressure measures liquid level instrument such as glass plate, floating drum, double flange difference gauges, the guided wave of liquid level Radar, ray level-sensing device etc.：

Up-flow reactor of the present invention, accessory are external insulation material, support element (skirt or journal stirrup), base Plinth, ladder, operating platform and fire-fighting accessory that may be present such as steam smothering ring.According to the conditions such as ground geology, meteorology are built, tie The conditions such as weight of equipment, height are closed, up-flow reactor of the present invention needs piling to control under its basis as needed The sinking speed on its basis.

Coal hydrogenation liquefaction reaction process R10 of the present invention, usually using up-flow reactor, working method can select：

1. floating bed hydrogenation reactor；

2. boiling bed hydrogenation reactor usually draws off the decreased catalysis of activity from bed bottom in an intermittent fashion Agent fills into fresh catalyst from bed top in an intermittent fashion and maintains bed catalyst reserve；

3. slight expanded-bed.

Solvent oil hydrogenation of the present invention stablizes reaction process R20, the reactor used, and working method can select：

1. floating bed hydrogenation reactor；

3. up flow type slight expanded-bed；

4. upflow fixed bed；

5. down-flow fixed bed；

6. the low liquid phase systemic circulation hydrogenation reactor of hydrogen to oil volume ratio.

Suspended-bed reactor of the present invention, structure type can be any one suitable forms, can be empty cylinder Suspended-bed reactor is to form piston flow or can be using internal cycle guide shell thus shape there are the back-mixing stream of interior cycle Can make top reaction compartment liquid flow into lower part using its outer circulating tube to react empty at circulation in inside or internal outside circulation Between shaper outer circulation stream back-mixing flow pattern, can be using top product liquid collect and flow guide system to by cycle plus Pressure system forms the back-mixing flow pattern for forcing inner recirculation flow.

The characteristic of the present invention is described below.

The general control principle of the gas-phase presulfiding hydrogen concentration of the hydrogenation process of the present invention described in detail below.

As needed, any hydrogenation process can be added in any supplement sulphur, but be typically incorporated into most upstream Hydrogenation process entrance, to ensure reaction process necessary minimum concentration of hydrogen sulfide such as 500PPm (v) or 1000PPm (v) or it is expected specified value, to ensure that the necessary hydrogen sulfide sectional pressure of catalyst is not less than minimum specified value.The supplement sulphur can Be sulfide hydrogen or can be converted into hydrogen sulfide to material of the hydroconversion process without ill-effect, such as it is hydrogen sulfide containing Gas or oil product, or the molten sulfur or carbon disulfide or dimethyl disulfide etc. of hydrogen sulfide are generated after being contacted with high-temperature hydrogen.

The rule of the high pressure separation process of the hydrogenation reaction effluent of the present invention described in detail below.

The high pressure separation process of hydrogenation reaction effluent generally comprises cold high pressure separator, when hydrocarbon in hydrogenation reaction effluent Oil density big (such as close with water density) or viscosity are big or when being difficult to detach with water emulsification, it is also necessary to it is usual that operation temperature be arranged For 150~450 DEG C of high pressure hot separator, hydrogenation reaction effluent enters high pressure hot separator and is separated into one in volume at this time On the hot gas separated by high pressure separator gas that is mainly made of hydrogen and one be mainly made of conventional liq hydrocarbon and solid that may be present Hot high score fluid body, hot gas separated by high pressure separator enter the cold high pressure separator that operation temperature is usually 20~80 DEG C be separated into cold high score oil and Cold gas separated by high pressure separator realizes following target since a large amount of high boiling components enter in hot high score fluid body：Cold high score oil density becomes smaller Or viscosity becomes smaller or is easily isolated with water.High pressure hot separator is arranged in the high pressure separation process of hydrogenation reaction effluent, is also equipped with The advantages of reducing thermal loss because hot high score fluid body can be undergone to avoid hot gas separated by high pressure separator using air cooler or water cooler Cool process.Meanwhile the hydrogenation process that the hot high score fluid body in part can be returned to upstream recycles, to improve The overall raw material property of the hydrogenation process of the recycle oil is received, or cycle plus hydrogen are carried out to the recycle oil.

Hydrogenation reaction effluent or hot gas separated by high pressure separator enter before cold anticyclone separate section, usually first reduce temperature and (are usually Feed and exchange heat with reactive moieties) (temperature should be higher than that in the hydrogenation reaction effluent gas phase that sulphur hydrogenates ammonia to about 220~100 DEG C Crystallization temperature), then usually injection washings form water filling back end hydrogenation reaction effluent thereto, washings for absorbing ammonia and Issuable other impurity such as hydrogen chloride etc., and the aqueous solution after absorbing ammonia necessarily absorbs hydrogen sulfide.In cold anticyclone separation unit Point, the water filling back end hydrogenation reaction effluent is separated into：One be mainly made of hydrogen in volume cold gas separated by high pressure separator, a master Will by cold high score that conventional liq hydrocarbon and dissolved hydrogen form oil, one it is being mainly made of water and dissolved with ammonia, hydrogen sulfide it is cold High score water.The cold high score water, the content of wherein ammonia are generally 0.5~15% (w), preferably 1~8% (w).Note washings One purpose is the ammonia and hydrogen sulfide absorbed in hydrogenation reaction effluent, prevents from forming sulphur hydrogenation ammonia or more sulphur ammonia Crystallization Pluggings change Hot device channel increases system pressure drop.The injection rate of the washings should be determined according to following principles：On the one hand, washings are noted It is divided into vapour phase water and liquid phase water after entering hydrogenation reaction effluent, liquid phase water has to be larger than zero, preferably washs water inventory 30% or more；In another aspect, washings are used to absorb the ammonia in hydrogenation reaction effluent, the ammonia density of gas separated by high pressure separator is prevented too Height reduces catalyst activity, and the lower the ammonia volumetric concentration of usual gas separated by high pressure separator the better, generally no greater than 200PPm (v), preferably less In 50PPm (v).The cold high pressure separator operating pressure is that hydrogenation reaction partial pressure subtracts actual pressure drop, cold anticyclone The difference of separate section operating pressure and hydrogenation reaction pressure, it is unsuitable too low or excessively high, generally 0.35~3.2MPa, be usually 0.5~1.5MPa.The hydrogen volume concentration value of the cold gas separated by high pressure separator, should not too low (cause device operating pressure rise), one As should be not less than 70% (v), preferably be not less than 80% (v), be preferably not below 85% (v).As previously described at least partially, usually 85~100% cold gas separated by high pressure separator is returned to be recycled in hydrogenation reaction part, to provide hydrogenation reaction part necessary amounts of hydrogen And hydrogen concentration；In order to improve plant investment efficiency, it is necessary to assure cycle hydrogen concentration is not less than lower limit value above-mentioned, for this purpose, according to Specific feedstock property, reaction condition, product distribution can exclude a part of cold gas separated by high pressure separator to exclude the first that reaction generates Alkane, ethane.For the cold gas separated by high pressure separator of discharge, conventional membrane separation process or pressure swing adsorption technique may be used or oil wash technique is real Existing hydrogen and the separation of non-hydrogen gas component, and the hydrogen of recycling is used as new hydrogen.

New hydrogen enters plus hydrogen partial is to supplement the hydrogen of hydrogenation process consumption, and the higher the better for new hydrogen hydrogen concentration, generally Not preferably less than 95% (v), preferably not below 99% (v).All new hydrogen can be introduced any hydrogenation reaction part, be preferably introduced the One hydrogenation reactor.

The present invention stablizes reaction process R2 in solvent oil hydrogenation, and the hydrogen gas stream used can be entirely new hydrogen, can be with Entirely impurity CO and/or CO₂The low recycle hydrogen of gas concentration can be the gaseous mixture of the two.

The present invention stablizes reaction process R2 in solvent oil hydrogenation, can use partial impurities CO and/or CO₂Gas concentration is high Recycle hydrogen, still, quantity should be a small amount of and had better not cause the volumetric concentration of impurity composition in hydrogen stream to be more than Operating provision value.

Claims

1. the hydrogen usage of the hydrogenation process and online second hydrogenation process of richness production foreign gas, it is characterised in that include following step Suddenly：

The hydrogenation process of the rich production foreign gas, refer at least occurring a part of heat from hydrogenation cracking reaction containing oxygen element The hydrogenation process R1 of hydrocarbon material R1F；

Online second hydrogenation process refers to using the hydrogenation reaction of same high pressure hydrogen system with hydrogenation process R1 Process；

It is described to use same high pressure hydrogen system, refer to that the hydrogen material of the second hydrogenation process R2 and hydrogenation process R1 closes It is a kind or several in following：

1. the compressor of the circulating hydrogen of hydrogenation process R1, mutual with the compressor of the circulating hydrogen of the second hydrogenation process R2 It shares；The circulation loop of the circulating hydrogen of at least part hydrogenation process R1 is with the second hydrogenation process R2's of at least part The circulation loop of circulating hydrogen is parallel relationship；

2. hydrogenation process R1 and the second hydrogenation process R2, there are series relationships on circulating hydrogen circuit, i.e., at least one Divide circulating hydrogen series connection across the second hydrogenation process R2 and hydrogenation process R1；

3. the compressor of the new hydrogen of hydrogenation process R1, the compressor with the new hydrogen of the second hydrogenation process mutually share, second The new hydrogen and part to the new hydrogen that whole hydrogenation process R1 are consumed of hydrogenation process consumption enter the second hydrogenation process together；

During normal production, the circulating hydrogen compressor of hydrogenation process R1 does not convey hydrogen to the second hydrogenation process；New hydrogen pressure When the amounts of hydrogen of contracting machine conveying cannot meet the second hydrogenation process and need, the circulating hydrogen compressor of hydrogenation process R1, to Second hydrogenation process conveys at least part hydrogen；

2. the thermal high separation process R1P-HTS of the product R1P of hydrogenation process R1 obtains hot gas separated by high pressure separator R1P-HTSV, it is based on The gas phase of the logistics of hot gas separated by high pressure separator R1P-HTSV is dissolved in the molten of water by hydrocarbon gas condensing steps, at least partly foreign gas component Cold gas separated by high pressure separator R1P-CTSV is obtained into cold anticyclone separation process after solution step, the cold gas separated by high pressure separator R1P-CTSV of at least part passes through Membrane separating process FR obtains level-one purification circulating air 1ST-PH after removing at least part foreign gas, and at least part level-one carries Pure circulating air 1ST-PH enters the second hydrogenation process；

3. the thermal high separation process R1P-HTS of the product R1P of hydrogenation process R1 obtains hot gas separated by high pressure separator R1P-HTSV, it is based on The gas phase of the logistics of hot gas separated by high pressure separator R1P-HTSV is dissolved in the step of water by hydrocarbon gas condensing steps, at least partly foreign gas component Cold gas separated by high pressure separator R1P-CTSV is obtained into cold anticyclone separation process after rapid, the cold gas separated by high pressure separator R1P-CTSV of at least part is by film point Level-one purification circulating air 1ST-PH is obtained after removing at least part foreign gas from process FR, the purification of at least part level-one follows Ring gas 1ST-PH obtains two level purification circulating air 2ST-PH after pressure-swing absorption process removes at least part foreign gas, until Few a part of two level purification circulating air 2ST-PH enters the second hydrogenation process.

2. method according to claim 1, it is characterised in that：

The hydrogenation process R1 of the rich production foreign gas, refer at least occurring a part of heat from hydrogenation cracking reaction contains oxygen element Hydrocarbon material heat from hydrogenation cracking reaction process R1；

Online second hydrogenation process refers to adding using the solvent naphtha of same high pressure hydrogen system with hydrogenation process R1 Stabilized hydrogen reaction process R2；

3. method according to claim 1, it is characterised in that：

At least part circulating hydrogen that circulating hydrogen compressor KC is sent out firstly flows through the second hydrogenation process R2 and then passes through plus hydrogen Reaction process R1, and finally return that circulating hydrogen compressor KC.

4. according to claims 1 or 2 or 3 the methods, it is characterised in that：

Hydrogenation process R1 is to generate CO and/or CO₂Heat from hydrogenation cracking reaction process R1, one kind during following or It is several：

1. the heat from hydrogenation cracking reaction process R1 of oil product obtained by direct hydrogenation liquefaction of coal liquefaction process, including use hydrogen supply dissolvent oily Direct hydrogenation liquefaction of coal liquefaction process, oil coal refines process altogether, coal faces hydrogen thermosol liquefaction process；

2. the heat from hydrogenation cracking reaction process R1 of oil product obtained by middle coalite tar or its distillate or its hot procedure；Heat adds Work process is coking heavy oil process or heavy oil catalytic cracking process or heavy oil catalytic pyrolysis process or heat from hydrogenation cracking process；

5. the heat from hydrogenation cracking reaction process R1 of oil product obtained by petroleum based heavy fuel oils or its hot procedure；Hot procedure is heavy oil Coking or heavy oil catalytic cracking process or heavy oil catalytic pyrolysis process or heat from hydrogenation cracking process；

6. the heat from hydrogenation cracking reaction process R1 of oil product obtained by tar sand base weight oil or its hot procedure；Hot procedure is weight Oil product obtained by oily coking or heavy oil catalytic cracking process or heavy oil catalytic pyrolysis process or its hot procedure；

5. method according to claim 4, it is characterised in that：

The CO and/or CO that the hydrogenation process R1 of hydrocarbon material R1F is generated₂Weight yield be 0.5~5.0%.

6. method according to claim 4, it is characterised in that：

Detach the CO and/or CO in cold anticyclone separation gas obtained by the product R1P of hydrogenation process R1₂Volumetric concentration be 0.5 ~5.0%.

7. method according to claim 4, it is characterised in that：

The volumetric concentration of foreign gas in the feed hydrogen of second hydrogenation process R2 is less than 10000PPm.

8. method according to claim 4, it is characterised in that：

The volumetric concentration of foreign gas in the feed hydrogen of second hydrogenation process R2 is less than 5000PPm.

9. method according to claim 4, it is characterised in that：

The feed hydrogen of second hydrogenation process R2, the volumetric concentration of foreign gas therein are less than 5000PPm, CO therein and/or CO₂Volumetric concentration be less than 1000PPm, NH therein₂Volumetric concentration be less than 700PPm.

10. method according to claim 4, it is characterised in that：

The feed hydrogen of second hydrogenation process R2, the volumetric concentration of foreign gas therein are less than 5000PPm, CO therein and/or CO₂Volumetric concentration be less than 100PPm, NH therein₂Volumetric concentration be less than 500PPm.

11. method according to claim 4, it is characterised in that：

The feed hydrogen of second hydrogenation process R2, the volumetric concentration of foreign gas therein are less than 5000PPm, CO therein and/or CO₂Volumetric concentration be less than 20PPm, NH therein₂Volumetric concentration be less than 200PPm.