CN106831288B - The MTP method of mixed alcohol side entry feed - Google Patents
The MTP method of mixed alcohol side entry feed Download PDFInfo
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- CN106831288B CN106831288B CN201710127573.4A CN201710127573A CN106831288B CN 106831288 B CN106831288 B CN 106831288B CN 201710127573 A CN201710127573 A CN 201710127573A CN 106831288 B CN106831288 B CN 106831288B
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
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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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
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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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Abstract
The invention belongs to coal chemical industries and technical field of petrochemical industry, are related to a kind of MTP method of mixed alcohol side entry feed.The following steps are included: a. in DME reactor, using refined methanol as raw material, generates DME under the action of alumina base catalyst；B.DME reactor product DME points are three parts, and first part enters MTP reactor, and reaction generates the product of by-product ethylene, gasoline and LPG based on propylene；Second part DME gas in c.DME reactor product enters MTP reactor from side line and participates in reaction；Part III DME in d.DME reactor product isolates gas-liquid two-phase, and gas phase enters MTP reactor and participates in reacting, and after undercooling, enters MTP reactor from side line；E. mixed alcohol is led into MTP reactor from side line and participates in reaction.The present invention is easy to control reaction process；Improve ethylene, propene yield；Reduce cost of goods manufactured.
Description
Technical field
The invention belongs to coal chemical industry and technical field of petrochemical industry, it is related to a kind of preparing propylene from methanol (MTP) process
Optimisation technique, the MTP method of specifically a kind of mixed alcohol side entry feed.
Background technique
The low-carbon alkenes such as ethylene, propylene are important organic chemical industry's basic material, are mainly derived from the cracking of naphtha.
In recent years, domestic ethylene and propylene demand sharp increase, but China's oil yield has been far from satisfying the market demand, in this way
Situation under, the diversification of ethylene and production of propylene raw material becomes the key subjects of relationship national energy structural adjustment.
Under traditional handicraft, ethylene and propylene are mainly derived from steam cracking device and oil plant catalytic cracking (FCC) device,
About 43% FCC apparatus is come from from steam cracking device, about 57% at present, low-carbon alkene is the main by-product of technical process
Object, imbalance between supply and demand is very prominent, and increasingly depleted with petroleum resources, is the new of raw materials for production there is an urgent need to substitute petroleum
Type production technology.Currently, methanol-to-olefins (MTO) and preparing propylene from methanol (MTP) are main two in the efficient utilization of coal resource
Route.Uop Inc.'s fluidized bed MTO technique, Dalian materialization DMTO technology, Lucci corporation fixed bed MTP technique is (with methanol
For raw material produce propylene) exploitation success, imply ethylene and propylene can be used as principal product by reaction preparation.In China,
The technology for preparing methanol using coal as raw material is mature, methanol market excess capacity, can will be superfluous by MTO and MTP technique
Methanol conversion be base stock ethylene, after propylene, obtain the product of more high values by various reactions.
The technology path of mainstream includes two kinds, i.e. fluidized-bed reaction technique and fixed bed reaction technique at present.Wherein fluidize
For bed process using the MTO of the DMTO technique of the Dalian Chemistry and Physics Institute, the Chinese Academy of Sciences and Uop Inc. as representative, technique uses SAPO-34 molecular sieve
Catalyst, and catalyst comparatively fast needs cyclic regeneration because inactivating, raw material is the methanol of water content 5%, anti-using recirculating fluidized bed
It answers device to can be very good to solve the problems, such as the very exothermic during methanol-to-olefins, the substantially comparable ethylene of yield and third can be produced
Alkene.Fixed-bed process is using the MTP technology of odd (Lurgi) the company exploitation in German Shandong as representative, and the ZSM-5 type catalyst used is because of knot
Burnt rate is low and inactivation is slower, and MTP technique is based on insulation fix bed system, and raw material is refined methanol, and charging methanol is reacted in DME first
Reaction generates DME in device, and reaction product DME is selective in the MTP reactor of six beds to be converted into propylene, while generating second
The by-products such as alkene, gasoline and LPG.
Have multinomial patent at present both at home and abroad to be related to producing the technology of low-carbon alkene especially propylene using methanol as raw material, it is main
Have EP0448000, WO2007/140844A1, DE10027159A1, CN101309886A, CN1431982A,
CN101811920B etc. belongs to the scope of above-mentioned MTP technology.The common feature of these patents is: used technique road
Line is designed according to German Shandong surprise MTP process route, is all made of two sections of fixed beds and is reacted, and is original with refined methanol
Material converts methanol into DME under aluminium oxide catalyst effect first in one section of DME reactor, reaction product DME and water,
Recycle hydrocarbons are mixed, are preheated, and from top, MTP reactor head, which enters in heat-insulating fixed bed reactors, reacts, in ZSM-5 base MTP
It under the action of catalyst, ultimately generates based on propylene, the by-products such as a small amount of ethylene of by-product, a certain amount of gasoline and LPG.
Methanol-to-olefins (MTP) reaction is strong exothermal reaction, the extremely difficult control of reaction temperature, in order to maintain temperature curve in institute
Within the temperature range of needing, reaction is divided into DME and MTP two reactor to disperse reaction heat by technique, MTP reactor head into
It is added vapor and recycle hydrocarbons in material, vapor can be used as the heat absorption material of exothermic reaction to control the temperature rise of catalyst bed,
The addition of vapor can be reduced the formation of carbon deposit simultaneously；In order to improve propene yield and yield, C2 that refined unit is recycled back to,
C4, C5/C6 also enter the first bed of reactor together and are converted into alkene, while can also be used as the heat absorption material control of exothermic reaction
The temperature of catalyst bed processed.In order to preferably control reaction temperature, between each bed of main reactor be added intermediate feed into
Row cools down, and next catalyst bed is entered after the gas phase and liquid phase DME hybrid cooling of side entry feed.Most cooling capacity be by from
What the liquid gasification rich in water of the supercooling of the second to the 6th bed injection provided.
Traditional MTP operational process of craft is complicated, and rate-determining steps are relatively complicated, while the technique is in industrialization operational process
In, Propylene Selectivity and yield are all relatively low, and unit consumption of product is high, and production run is at high cost, to reduce the profitability of device；
DME lime set is used to have the defects that as the control means of each bed temperature of MTP reactor in another process flow certain, due to
MTP reaction belongs to strong exothermal reaction, and the lime set amount needed is often very big, causes bed temperature runaway since lime set is insufficient frequent occurrence
Phenomenon, lime set pumps also because of long-term heavy-duty service, easy to damage, therefore, how to optimize process flow, and it is difficult to reduce operation
Degree, while the yield for improving the products such as ethylene, propylene is great meaning.
Summary of the invention
The purpose of the present invention is: for the deficiency of prior art technology, a kind of MTP method of mixed alcohol side entry feed is provided,
It enables the method to reduce reaction heat from thermodynamics source, to make rate；It can reduce the process components such as nozzle, expansion joint
Operation reaction process be easier to control；It can reduce cost of material, improve the receipts load of the products such as ethylene, propylene, reduce consumption
Material reduces cost of goods manufactured, solve MTP commercial plant presently, there are raw material single alcohol purified treatment is mixed with coal chemical technology
The problems such as method missing.
To achieve the goals above, the method for the present invention the following steps are included:
A. using refined methanol as raw material, 250~280 DEG C is preheated to and is entered in DME reactor, in the work of alumina base catalyst
With lower generation dimethyl ether (DME) and water；
B.DME reaction product DME points are three parts, and first part DME is isolated with from subsequent MTP reactor outlet
Recycle hydrocarbons mixing, then mix with process steam, the heated stove heating of mixed material enters to 430-460 DEG C and divides equipped with ZSM-5
The MTP reactor of son sieve base catalyst, reaction generate the product of by-product ethylene, gasoline and LPG based on propylene；
Second part DME gas enters MTP reactor from side line and participates in reacting in c.DME reaction product；
Part III DME material isolates gas-liquid two-phase in DME knockout drum in d.DME reaction product, and wherein gas phase is rich
Containing DME, liquid phase is rich in process water；MTP reactor is directly entered after DME gas mixing in gas phase portion and step c to participate in instead
It answers；After liquid phase part supercooling, enters MTP reactor from side line after the pump pressurization of DME lime set, play reduction reactor batch temperature
Effect；
E. by pump by C1~C10 mix alcohol from side line lead to MTP reactor participate in reaction, using mixed alcohol catalyst work
With the lower strong endothermic reaction that producing olefin hydrocarbon with alcohols dehydration occurs, the fuel factor of MTP reaction is neutralized, by MTP reactor batch temperature control
System is within the scope of required temperature.
Preferably, the mixed alcohol source of MTP reactor pump-around charging is from by-product in Fischer-Tropsch synthesis higher hydrocarbon technique
Mixed alcohol perhaps passes through to be originated from the mixed alcohol of the hydrocarbonaceous mixed alcohol of rectifying side take-off in methanol synthesizing process or above two source
After crossing pretreatment, the mixed raw polyol compounded with water, water content can be adjusted in 5-99%.(wherein mix the typical group prejudice of alcohol
Table 1)
Preferably, it by methanol, the dimethyl ether of side entry feeds all in MTP reactor mixed in pure and mild original material, rolls over
It is counted as methanol and calculates weight (hourly) space velocity (WHSV), specific algorithm is that the DME of 1M is converted to the CH3OH of 2M；Mixed alcohol quality is rubbed divided by corresponding
That quality, obtains corresponding CH3OH molal quantity；The weight (hourly) space velocity (WHSV) of raw material is 0.5-1.5kg methanol/(kg in MTP reactor
cat.h)。
Preferably, the mixed alcohol of MTP reactor pump-around charging, carries out pretreatment purification, preprocessing means include before charging
But it is not limited to ion exchange, alkali process, absorption and other physical chemistry processing methods etc., pre-treatment step are as follows: successively desulfurization
Deodorization, sand filtration, highly basic are heated to 55~60 DEG C of hydrolysis and use NaBH except ester, deacidification, at 50~80 DEG C4Reduction treatment.
Preferably, MTP reactor used catalyst is the type ZSM 5 molecular sieve base catalyst of ZSM-5 type or modification, at
Part includes molecular screen primary powder, binder, auxiliary agent, extruded moulding after each composition mixing.
The invention has the advantages that
In conventional process for preparing propylene from methanol route, C will be enriched in1~C10Mixed alcohol make jointly with methanol after pretreatment
It for raw material, is introduced through MTP technique side line liquid phase cold burden entrance, under the action of ZSM-5 molecular sieve catalyst, dehydration occurs
Generate corresponding alkene, the product distribution of modulation methanol conversion process.The method of the present invention can pass through technological design and theoretical meter
It calculates, under the premise of not changing primary product distribution, it is former as reaction to substitute part methanol to introduce a certain amount of mixed alcohol from side line
Material, the mode into reactor are rich in the DME lime set liquid phase feeding system of process water by replacing original side line, entrance second to
6th bed, it is therefore intended that the dehydration of alcohols endothermic reaction is occurred in catalyst bed by mixed alcohol, low-carbon alkene is generated and (removes methanol system
Alkene is outside exothermic reaction, and the reaction of other advanced dehydration of alcohols alkene is the endothermic reaction), the heat release of MTP reaction is neutralized, together
The yield of light olefins such as Shi Tigao ethylene, propylene.The substitution of mixed raw polyol, reduces the reaction of methanol conversion mistake to a certain extent
Fuel factor in journey, while reducing the dosage of methanol feedstock, operation difficulty and cost of material are reduced, the steady of operation is improved
Qualitative and low-carbon alkene actual recovery.In addition, the by-product of F- T synthesis, methanol synthesizing process can be derived from due to mixing alcohol,
Both the load of environmentally friendly aftertreatment technology had been reduced, cheap raw material is also provided for MTP technique, has been utilized as coal for mixed alcohol
Chemical industry cause provides good resource utilization approach, the profitability of lifting device.
Detailed description of the invention
Fig. 1 is a kind of process principle figure of existing MTP method.
Fig. 2 is the process principle figure of embodiment of the present invention method 1,2.
Specific embodiment
The method of comparative example and the embodiment of the present invention is described further with reference to the accompanying drawing.
Comparative example:
As shown in Figure 1, its technique is tried on fixed-bed reactor in middle pattern, DME pre-reaction using refined methanol as raw material
260 DEG C of device R-111 inlet temperature, 370 DEG C of outlet temperature, methanol weight (hourly) space velocity (WHSV) is 2.0h in R-111 reactor-1, MTP reactor
Methanol (and dimethyl ether) weight (hourly) space velocity (WHSV) is 1.5h in R-151-1, the reaction temperature of R-151 reactor is 475 DEG C, reactor outlet
Pressure 10kPa.Partial pressure of the methanol (dimethyl ether is converted to methanol) in main reactor is 23kPa, and diluent gas is vapor.It urges
Agent is ZSM-5 based molecular sieve catalyst, and Si/Al=100, reactor outlet product is analyzed through on-line chromatograph the results are shown in Table 1.
Embodiment one:
As shown in Figure 2, comprising the following steps:
A. in DME reactor (single stage adiabatic fixed bed reactors R-111), using refined methanol as raw material, from anti-after preheating
Device R-111 top feed is answered, generates DME (dimethyl ether) under the action of alumina base catalyst；
B. DME reactor product DME points are three parts, and first part DME divides with from subsequent MTP reactor outlet
The recycle hydrocarbons mixing separated out, then mix with process steam, the heated stove heating of mixed material to after 450 DEG C from top into being equipped with
The first bed of MTP reactor (R-151) of ZSM-5 molecular sieve base catalyst, reaction product once pass through the second to the 6th catalysis
Agent bed, reaction generate the product of by-product ethylene, gasoline and LPG based on propylene；
C. in DME reactor product second part DME gas from side line enter the second to the 6th bed of MTP reactor ginseng
With react；
D. Part III DME material isolates gas-liquid two-phase in DME knockout drum D-112 in DME reactor product,
Middle gas phase is rich in DME, and liquid phase is rich in process water；MTP reactor is directly entered after gas phase portion and DME gas mixing in step c
Second to the 6th bed participate in reaction, liquid phase part therein is crossed be cooled to 60 DEG C after, through DME lime set pump pressurization after from side line enter
The second to the 6th bed of MTP reactor plays the role of reducing reactor batch temperature；
E. it is originated from by-product in Fischer-Tropsch synthesis higher hydrocarbon technique in the future by pumpC1~C10 Alcohol is mixed from head tank C-
111, which lead to the second to the 6th catalyst bed inlet MTP reactor R-151 through side line, participates in reaction, is being catalyzed using mixed alcohol
The strong endothermic reaction that producing olefin hydrocarbon with alcohols dehydration occurs under the action of agent, neutralizes the fuel factor of MTP reaction, by MTP reactor bed
Temperature controls within the scope of required temperature.
In above-mentioned steps, 260 DEG C of inlet temperature of DME pre-reactor R-111,370 DEG C of outlet temperature, in R-111 reactor
Methanol weight (hourly) space velocity (WHSV) is 2.0h-1, methanol (and dimethyl ether) weight (hourly) space velocity (WHSV) is 1.0h in MTP reactor R-151-1, mix alcohol side line into
Material weight (hourly) space velocity (WHSV) is 0.5h-1, it is 1.5h that the processing of total carbon caused by the two air speed, which is equal to methanol weight (hourly) space velocity (WHSV),-1.R-151 reaction
The reaction temperature of device is 475 DEG C, reactor outlet pressure 10kPa.Methanol (dimethyl ether is converted to methanol) is in main reactor
Partial pressure is 23kPa, and diluent gas is vapor.Catalyst is ZSM-5 based molecular sieve catalyst, and Si/Al=100, reactor goes out
Mouth product the results are shown in Table 1 through on-line chromatograph analysis.
Embodiment two:
The processing step and parameter and embodiment of embodiment two are essentially identical, and difference is only that in the step e of embodiment two,
Mixed alcohol is led to before MTP reactor, pretreatment purification is carried out to it, sloughs the substance that can make catalyst poisoning, in order to avoid cause to be catalyzed
The agent lost of life, low-carbon alkene actual recovery are low；Pre-treatment step are as follows: successively desulfurization deodorization (gas liquid ratio 0.1), sand filtration, highly basic
60 DEG C of hydrolysis are heated to except ester, deacidification, use NaBH at 70 DEG C4Reduction treatment.Reactor outlet product is analyzed through on-line chromatograph
It the results are shown in Table 2.
Above-mentioned implementation comparative example is used for illustrative purposes only, rather than is limitation of the present invention, related technical field
Technical staff can also make a variety of changes and deform, therefore is used under the premise of not departing from the spirit and scope of the invention
Equivalent technical solution also should belong to scope of the invention, and protection scope of the present invention should have various claims to limit.
Table 1 mixes alcohol typical case's constituent
(water content is adjustable in 5-99%)
The reaction product of 2 embodiment of table and comparative example composition
Claims (1)
1. a kind of MTP method of mixed alcohol side entry feed, it is characterized in that: include the following steps,
A. using refined methanol as raw material, 250~280 DEG C is preheated to and is entered in DME reactor, under the action of alumina base catalyst
Generate DME；
B.DME reactor product DME point is three parts, first part DME with isolated from subsequent MTP reactor outlet
Recycle hydrocarbons mixing, then mixed with process steam, the heated stove heating of mixed material enters to 430-460 DEG C is equipped with ZSM-5 molecule
The MTP reactor of base catalyst is sieved, reaction generates the product of by-product ethylene, gasoline and LPG based on propylene；
Second part DME gas enters MTP reactor from side line and participates in reacting in c.DME reactor product；
Part III DME material isolates gas-liquid two-phase in DME knockout drum in d.DME reactor product, and wherein gas phase is rich in
DME, liquid phase are rich in process water；It is directly entered the participation of MTP reactor after gas phase portion and DME gas mixing in step c to react, liquid
It mutually partially crosses after being cooled to 60 DEG C, enters MTP reactor from side line after the pump pressurization of DME lime set, playing reduces reactor bed temperature
The effect of degree；
E. C1~C10 is mixed by alcohol by pump and leads to the participation reaction of MTP reactor from side line, under the effect of the catalyst using mixed alcohol
The strong endothermic reaction of producing olefin hydrocarbon with alcohols dehydration occurs, neutralizes the fuel factor of MTP reaction, the control of MTP reactor batch temperature is existed
Within the scope of required temperature；
The mixed alcohol source of MTP reactor pump-around charging is from the mixed alcohol of by-product in Fischer-Tropsch synthesis higher hydrocarbon technique, or comes
Mixed alcohol from the hydrocarbonaceous mixed alcohol of rectifying side take-off in methanol synthesizing process or above two source by pretreatment after,
The mixed raw polyol compounded with water, water content are adjusted in 5-99%；
By methanol, the dimethyl ether of side entry feeds all in MTP reactor mixed in pure and mild original material, it is converted to methanol calculating
Weight (hourly) space velocity (WHSV), specific algorithm are that the DME of 1M is converted to the CH3OH of 2M；By mixed alcohol quality divided by corresponding molal weight, phase is obtained
Corresponding CH3OH molal quantity；The weight (hourly) space velocity (WHSV) of raw material is 0.5-1.5kg methanol/(kg cat.h) in MTP reactor；
The mixed alcohol of MTP reactor pump-around charging, carries out pretreatment purification before charging, and preprocess method selects alkali process；
Pre-treatment step are as follows: successively desulfurization deodorization, sand filtration, highly basic are heated to 55~60 DEG C of hydrolysis and remove ester, deacidification, at 50~80 DEG C
It is lower to use NaBH4 reduction treatment；
MTP reactor used catalyst is the type ZSM 5 molecular sieve base catalyst of ZSM-5 type or modification, and composition includes molecule
Sieve original powder, binder, auxiliary agent, extruded moulding after each composition mixing.
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| CN110054539B (en) * | 2019-05-10 | 2022-05-20 | 国家能源投资集团有限责任公司 | Device and method for preparing propylene from methanol |
| CN110183301B (en) * | 2019-05-31 | 2022-06-28 | 国家能源投资集团有限责任公司 | Methanol-to-propylene system and method for starting and feeding by using same |
| CN114409497B (en) * | 2022-01-24 | 2023-07-18 | 山西大学 | Method for simulating/predicting catalytic reaction mechanism and intermediate activity |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101417914A (en) * | 2007-10-26 | 2009-04-29 | 中国石油化工股份有限公司 | Method for preparing propylene from methanol using hydrocarbons as part material |
| CN101723779A (en) * | 2008-10-10 | 2010-06-09 | 中国石油化工股份有限公司 | Method for producing dimethyl ether and olefin by dehydration on mixed alcohol |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101417914A (en) * | 2007-10-26 | 2009-04-29 | 中国石油化工股份有限公司 | Method for preparing propylene from methanol using hydrocarbons as part material |
| CN101723779A (en) * | 2008-10-10 | 2010-06-09 | 中国石油化工股份有限公司 | Method for producing dimethyl ether and olefin by dehydration on mixed alcohol |
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