Abstract:
Disclosed is a process for producing light olefins, the process comprising: continuously contacting an oxygen-containing compound raw material with catalyst to have a dehydration reaction so as to prepare low-carbon alkene, the reaction pressure P of the dehydration reaction being 1-2 MPa, and the weight hourly space velocity H of the dehydration reaction being 15-50 h −1 . The process of preparing light olefins has a simple and continuous operation process, reduces investment, greatly increases production of light olefins and has a high safety.

Description:
TECHNICAL FIELD 
       [0001]    The present invention relates to a process for producing light olefins from oxygen-containing compound feedstock. Specifically, the present invention relates to a process for increasing the output of light olefins in a process for producing light olefins from oxygen-containing compound feedstock. 
       BACKGROUND OF THE INVENTION 
       [0002]    Lower olefins (C2-C4 olefins) are the fundamental starting materials for the organic chemical industry, and have an important role in the modern petroleum and chemical industry. On the whole, the process for producing light olefins may be divided into two general classes, i.e. the traditional petroleum way and the novel non-petroleum way. Since the 1910s, the world began to investigate the process for producing light olefins from non-petroleum resources (especially the oxygen-containing compound feedstock) and made some progresses. 
         [0003]    The process of producing light olefins through the dehydration reaction of the oxygen-containing compound produces a certain amount of water as by-product except the hydrocarbon products, for example, about 44% of the hydrocarbon products from methanol and about 46% of the hydrocarbon products from ethanol. It is known that the reaction producing light olefins with the oxygen-containing compound feedstock is a reaction in which the amount of molecules increases, and therefore the lower reaction pressure is favorable for the chemical equilibrium to proceed toward the production of light olefins. Therefore, upon producing light olefins, in order to obtain a desired yield of light olefins, the prior art generally uses a lower reaction pressure. This lower reaction pressure (typically 0.1-0.3 MPa) directly results in that if desired to increase the throughput of the oxygen-containing compound feedstock in order to increase the output of light olefins, the prior art will therefore have to increase the size or amount of the reactor so as to maintain the yield of light olefins at an acceptable level. Obviously, this will accordingly increase the investment and maintenance cost of the plant. 
         [0004]    In the process for producing light olefins according to the prior art, in order to guarantee a continuous production process, the catalyst is circulated between the reactor and the regenerator. In order to facilitate the circulation, the reactor and the regenerator are generally operated at the substantially same pressure. Under this situation, the reactor is in a hydrocarbon atmosphere, and the regenerator is in an oxygen-containing atmosphere. If the reactor and the regenerator are not well segregated, there will be a large potential safety hazard. 
         [0005]    In addition, a cyclone similar to that used in the catalytic cracking unit is widely used in the plant for producing light olefins according to the prior art. Therefore, it is inevitable for the catalyst natural loss during the production, in particular in case that the catalyst fine powder having a particle size of less than 20 microns becomes more and more in the catalyst. This will have a detrimental effect on the subsequent product separation, and will be adverse for the catalyst to be reused. 
       SUMMARY OF THE INVENTION 
       [0006]    The purpose of the present invention is to provide a process for producing light olefins, which process overcomes the foresaid disadvantages in the prior art and is capable of directly utilizing the existing reactor and easily achieving the purpose of increasing the output of light olefins. 
         [0007]    The present inventors have surprisingly found through an industrious investigation that if increasing the reaction pressure and correspondingly and simultaneously and correspondingly increasing the WHSV of the oxygen-containing compound feedstock, the yield of light olefin can be maintained at a level which is comparable to or even higher than that of the prior art, instead decreases as previously expected in the prior art, resulting in that for an existing reactor, the technical solution of increasing the reaction pressure and the WHSV of the reactor according to the present invention will remarkably increase the throughput of the oxygen-containing compound feedstock in the reactor and accordingly increase the output of light olefins (i.e. increase the production of light olefins). This finding made by the present inventions breaks through the routine knowledge of those skilled in the art, and therefore accomplish the present invention based on this finding. 
         [0008]    Specifically speaking, the present invention relates to the following contents. 
         [0000]    1. A process for producing light olefins (or increasing the output of light olefins), wherein in the process for producing light olefins by continuously contacting an oxygen-containing compound feedstock and a catalyst to conduct a dehydration reaction, the reaction pressure P of the dehydration reaction is 0.5-10 MPa, preferably 0.75-3.5 MPa, more preferably 0.8-3 MPa, most preferably 1-2 MPa, the weight hourly space velocity H of the dehydration reaction is 7-250 h −1 , preferably 8-150 h −1 , more preferably 10-100 h −1 , more preferably 15-80 h −1 , most preferably 15-50 h −1 .
 
2. The process according to any of previous aspects, wherein during the dehydration reaction, H and P satisfy a mathematical function of H=f(P), which is a strictly increasing function, wherein P (unit: MPa) is in the interval [0.55, 10.0], preferably in the interval [0.75, 3.5], more preferably in the interval [0.8, 3.0], most preferably in the interval [1.0, 2.0], H (unit: h −1 ) is in the interval [7, 250], preferably in the interval [8, 150], more preferably in the interval [10, 100], more preferably in the interval [15, 80], most preferably in the interval [15, 50].
 
3. The process according to any of previous aspects, comprising the following steps:
 
continuously contacting the oxygen-containing compound feedstock and the catalyst to conduct the dehydration reaction to obtain a light olefins-rich hydrocarbon and a spent catalyst,
 
transporting at least a part of the spent catalyst to the regeneration reaction to obtain a regenerated catalyst, and
 
circulating at least a part of the regenerated catalyst to the dehydration reaction,
 
wherein the reaction pressure P of the dehydration reaction is at least 0.35 MPa, preferably 0.4 MPa, 0.5 MPa, 0.6 MPa, 0.7 MPa, 0.8 MPa, 0.9 MPa, 1.0 MPa, 1.1 MPa, 1.2 MPa, 1.3 MPa, 1.4 MPa, 1.5 MPa, 1.6 MPa, 1.7 MPa, 1.8 MPa, 1.9 MPa or 2.0 MPa higher than the regeneration pressure of the regeneration reaction.
 
4. The process according to any of previous aspects, further comprising a step of separating the light olefins-rich hydrocarbon to obtain a C 4   +  hydrocarbon, and optionally further comprising the following steps:
 
continuously contacting the C 4   +  hydrocarbon and a further catalyst to conduct a further reaction to produce a further light olefins-rich hydrocarbon and a further spent catalyst,
 
transporting at least a part of the further spent catalyst to the regeneration reaction to obtain a further regenerated catalyst, and
 
circulating at least a part of the regenerated catalyst and/or at least a part of the further regenerated catalyst to the dehydration reaction and/or the further reaction.
 
5. The process according to any of previous aspects, wherein one or more reactors are used for the dehydration reaction and/or the further reaction, and each independently selected from a fluidized bed reactor, a dense bed reactor, a riser reactor, an ebullated bed reactor, a slurry bed reactor and a combination thereof, preferably selected from a riser reactor, more preferably each independently selected from an isodiametric riser reactor, a riser reactor with an equal linear velocity, a variable diameter riser reactor and a riser-dense bed hybrid reactor.
 
6. The process according to any of previous aspects, wherein the oxygen-containing compound feedstock is selected from at least one of alcohol, ether and ester, preferably selected from at least one of R1-O—R2, R1-OC(═O)O—R2, R1-C(═O)O—R2 and R1-C(═O)—R2 (wherein, R1 and R2 are identical or different each other, each independently selected from H and C1-6 branched or linear alkyl, preferably each independently selected from H and C1-4 branched or linear alkyl, with the proviso that at most one of R1 and R2 is hydrogen), more preferably selected from at least one of methanol, ethanol, dimethylether, diethylether, methyl-ethyl-ether, methylene carbonate and methyl formate.
 
7. The process according to any of previous aspects, wherein the catalyst and the further catalyst are identical or different each other, each independently selected from at least one of zeolite catalysts, preferably each independently selected from at least one of aluminosilicophosphate zeolite catalysts and aluminosilicate molecular sieve catalysts.
 
8. The process according to any of previous aspects, wherein the reaction conditions of the regeneration reaction comprise: reaction temperature 450-850° C., preferably 550-700° C.; reaction pressure 0.1-0.5 MPa, preferably 0.15-0.3 MPa; oxygen-containing atmosphere, preferably air atmosphere or oxygen atmosphere.
 
9. The process according to any of previous aspects, wherein the spent catalyst and/or the further spent catalyst and/or the regenerated catalyst and/or the further regenerated catalyst are obtained by separation through a filter.
 
10. The process according to any of previous aspects, wherein the transporting and the circulating are performed via one or more (preferably one or two) catalyst hoppers ( 9 ).
 
11. The process according to any of previous aspects, further comprising a step of circulating at least a part of the spent catalyst and/or at least a part of the further spent catalyst to the dehydration reaction and/or the further reaction.
 
12. The process according to any of previous aspects, wherein the catalyst and/or the further catalyst have a total carbon content of 3-25 wt %, most preferably 6-15 wt %.
 
13. The process according to any of previous aspects, wherein with the proviso that the size and amount of the reactors for the dehydration reaction are kept the same, the process enables to increase the output of light olefins by 50%, preferably 100%, more preferably 150%, 200%, 500% or 790%, most preferably 1000% or higher.
 
14. The process according to any of previous aspects, further comprising a step of circulating an incompletely-reacted oxygen-containing compound feedstock to the dehydration reaction.
 
15. The process according to any of previous aspects, comprising the following steps:
 
continuously contacting the oxygen-containing compound feedstock and the catalyst in a riser-type reactor to conduct the dehydration reaction to produce a light olefins-rich hydrocarbon and a spent catalyst;
 
separating the olefins-rich hydrocarbon and the spent catalyst in a hydrocarbon-catalyst separation zone, introducing the separated olefins-rich hydrocarbon into a product separation-recovery system, stripping the spent catalyst through a stripping region of the riser-type reactor, withdrawing the spent catalyst from the riser-type reactor and transporting it to a spent catalyst receiver;
 
transporting the spent catalyst in the spent catalyst receiver directly to a regenerator via a catalyst hopper, or transporting it firstly to a spent catalyst feeding tank via a catalyst hopper and then to a regenerator, and regenerating the spent catalyst in an oxygen-containing atmosphere in the regenerator to obtain a regenerated catalyst;
 
transporting the regenerated catalyst directly to a catalyst hopper, or withdrawing the regenerated catalyst firstly from the regenerator and transporting it to the regenerated catalyst receiver, and then to a catalyst hopper;
 
transporting the regenerated catalyst in the catalyst hopper to the regenerated catalyst feeding tank, and then back to the riser-type reactor.
 
       Technical Effects 
       [0009]    Compared with the prior art, the process for producing light olefins according to the present invention have the following advantages. 
         [0010]    The process for producing light olefins of the present invention, by means of increasing the reaction pressure and simultaneously and correspondingly increasing the WHSV of the oxygen-containing compound feedstock, with the proviso that the size and amount of the existing reactor or reaction plant is kept the same, enables to maintain the yield of light olefins at a level comparable to or even higher than that of the prior art, and remarkably increase the output of light olefins (e.g. by up to 790% or higher). Therefore, the process for producing light olefins according to the present invention is a process of increasing the output of light olefins, and can be applied to the reconstruction or upgrading of the existing light olefins production plant. 
         [0011]    The process for producing light olefins according to the present invention, with the proviso of ensuring to achieve a predetermined output of light olefins, compared with the prior art, can remarkably reduce the size and amount of the reactor or reaction plant, and accordingly reduce the scale and investment cost of the whole light olefins production plant. Therefore, the process for producing light olefins according to the present invention is a new-generation process for producing light olefins with a high production capability, and can be applied to build a new-generation light olefins production plant with a smaller scale, a lower investment cost and a higher light olefin output than those of the existing light olefins production plant. 
         [0012]    The process for producing light olefins according to the present invention maintains the operation of the regenerator under a lower pressure and the operation of the reactor under a higher pressure, and therefore reduces the overall complexity of the process for producing light olefins and the production plant. 
         [0013]    The process for producing light olefins according to the present invention has a reaction pressure of the reactor remarkably higher than a regeneration pressure of the regenerator, and therefore the use of a pressure switch device (e.g. a lock hopper or a catalyst hopper) enables to implement the complete segregation of the hydrocarbon atmosphere of the reactor and the oxygen-containing atmosphere of the regenerator and the catalyst circulation, and accordingly ensure the overall safety of the production process and the production plant. 
         [0014]    Other features and advantages of the present invention will be further discussed in the following part of Detailed Description of Invention. 
     
    
     
       BRIEF DESCRIPTION OF DRAWINGS 
         [0015]    The drawings, which constitute a part of the specification, are used to provide a further understanding of the present invention, and serve to explain the present invention together with the following Detailed Description of Invention, but are not intended to limit the present invention. In the drawings: 
           [0016]      FIG. 1  is a flowchart of the process for producing light olefins from the oxygen-containing compound according to the first specific embodiment of the present invention 
           [0017]      FIG. 2  is a flowchart of the process for producing light olefins from the oxygen-containing compound according to the second specific embodiment of the present invention 
           [0018]      FIG. 3  is a flowchart of the process for producing light olefins from the oxygen-containing compound according to the third specific embodiment of the present invention 
           [0019]      FIG. 4  is a flowchart of the process for producing light olefins from the oxygen-containing compound according to the fourth specific embodiment of the present invention 
           [0020]      FIG. 5  is a flowchart of the process for producing light olefins from the oxygen-containing compound according to the fifth specific embodiment of the present invention 
           [0021]      FIG. 6  is a flowchart of the process for producing light olefins from the oxygen-containing compound according to the sixth specific embodiment of the present invention 
           [0022]      FIG. 7  is a flowchart of the process for producing light olefins from the oxygen-containing compound according to the seventh specific embodiment of the present invention 
       
    
    
       [0023]    The present invention can comprise other specific embodiments, and is not limited to the above seven embodiments. 
       REFERENCE IN THE DRAWINGS 
       [0000]    
       
           1  riser reactor;  2  internal heat remover;  3  dense bed reactor;  4  stripping region;  5  sedimentation zone;  6  filter;  7  regenerator;  8  spent catalyst receiver;  9  catalyst hopper;  10  spent catalyst feeding tank;  11  regenerated catalyst receiver;  12  regenerated catalyst feeding tank;  13  external heat remover;  14  internal heat remover;  15  internal heat remover;  16  pipeline;  17  pipeline;  18  pipeline;  19  pipeline;  20  pipeline;  21  pipeline;  22  pipeline;  23  pipeline;  24  feeding line;  25  reaction product line;  26  flue gas line;  27  pipeline;  28  pre-lifting line. 
           201  riser reactor;  202  internal riser and distributor;  203  dense bed reactor;  204  stripping region;  205  sedimentation zone;  206  filter;  207  regenerator;  208  spent catalyst receiver;  209  catalyst hopper;  210  regenerated catalyst receiver;  211  catalyst mixer;  212  regenerated catalyst feeding tank;  213  pipeline;  214  internal heat remover;  215  internal heat remover;  216  pipeline;  217  pipeline;  218  pipeline;  219  pre-lifting line;  220  quenching medium line;  221  pipeline;  222  pipeline;  223  pipeline;  224  feeding line;  225  reaction product line;  226  flue gas line;  227  pipeline;  301  riser reactor;  302  diameter-expanded riser;  303  dense bed reactor;  304  stripping region;  305  sedimentation zone;  306  filter;  307  regenerator;  308  spent catalyst receiver;  309  catalyst hopper;  310  spent catalyst feeding tank;  311  regenerated catalyst receiver;  312  regenerated catalyst feeding tank;  313  external heat remover;  314  internal heat remover;  315  internal heat remover;  316  pipeline;  317  pipeline;  318  pipeline;  319  pipeline;  320  pipeline;  321  pipeline;  322  pipeline;  323  pipeline;  324  feeding line;  325  reaction product line;  326  flue gas line;  327  pipeline;  328  pre-lifting line;  329  feeding line;  330  further riser-type reactor;  331  pipeline;  332  pipeline;  401  riser reactor;  402  internal riser and distribution plate;  403  dense bed reactor;  404  stripping region;  405  sedimentation zone;  406  filter;  407  regenerator;  408  spent catalyst receiver;  409  catalyst hopper;  410  regenerated catalyst receiver;  411  catalyst mixer;  412  regenerated catalyst feeding tank;  413  external heat remover;  414  internal heat remover;  415  internal heat remover;  416  pipeline;  417  pipeline;  418  pipeline;  419  pre-lifting line;  420  quenching medium line;  421  pipeline;  422  pipeline;  423  pipeline;  424  feeding line;  425  reaction product line;  426  flue gas line;  427  pipeline;  428  pre-lifting line;  429  feeding line;  430  pipeline;  431  first reaction zone;  432  second reaction zone;  433  necking and quick separator;  434  stripping region;  435  sedimentation zone;  436  filter;  437  pipeline;  438  pipeline;  501  riser reactor;  502  internal riser and quick separator;  503  dense bed reactor;  504  stripping region;  505  sedimentation zone;  506  filter;  507  regenerator;  508  spent catalyst receiver;  509  catalyst hopper;  510  spent catalyst feeding tank;  511  regenerated catalyst receiver;  512  catalyst feeding tank;  513  external heat remover;  514  internal heat remover;  515  internal heat remover;  516  pipeline;  517  pipeline;  518  pipeline;  519  pipeline;  520  pipeline;  521  pipeline;  522  pipeline;  523  pipeline;  524  feeding line;  525  reaction product line;  526  flue gas line;  527  pipeline;  528  quenching medium line;  529  external heat remover;  530  first reaction zone;  531  second reaction zone and necking;  532  pre-lifting line;  533  feeding line;  534  pipeline;  535  pipeline;  601  first reaction zone;  602  second reaction zone;  603  necking and quick separator;  604  stripping region;  605  sedimentation zone;  606  filter;  607  regenerator;  608  spent catalyst receiver;  609  catalyst hopper;  610  regenerated catalyst receiver;  611  catalyst mixer;  612  external heat remover;  613  external heat remover;  614  internal heat remover;  615  internal heat remover;  616  pipeline;  617  pipeline;  618  pipeline;  619  pre-lifting line;  620  flue gas line;  621  pipeline;  622  pipeline;  623  pipeline;  624  feeding line;  625  reaction product line;  626  pre-lifting line;  627  further riser-type reactor;  628  quick separator;  629  sedimentation zone;  630  stripping region;  631  filter;  632  reaction product line;  633  pipeline;  634  pipeline;  635  feeding line;  636  catalyst feeding tank;  637  pipeline;  701  fluidized bed reactor;  702  feeding line;  703  reaction product line;  704  flue gas line;  705  sedimentation zone;  706  filter;  707  regenerator;  708  spent catalyst receiver;  709  catalyst hopper;  710  spent catalyst feeding tank;  711  regenerated catalyst receiver;  712  regenerated catalyst feeding tank;  713  internal heat remover;  714  internal heat remover;  715  external heat remover;  716  pipeline;  717  pipeline;  718  pipeline;  719  pipeline;  720  pipeline;  721  pipeline;  722  pipeline;  723  pipeline;  724  main air. 
       
     
       DETAILED DESCRIPTION OF INVENTION 
       [0026]    Hereinafter, the specific embodiments of the present invention will be discussed in details with reference to the drawings. It should be understood that the specific embodiments described herein are only intended to explain the present invention and the present invention is not limited thereto in any way. 
         [0027]    In the context of the specification, the term “reactor” and “further reactor” refer to two reactors being independent each other. In the present invention, the term “C 4   +  hydrocarbon” refers to the hydrocarbon containing 4 or more carbon atoms. 
         [0028]    In the context of the specification, the term “light olefins” refers to ethylene and propylene. In the context of the present specification, the term “yield of light olefins” refers to the once through yield of light olefins, the term “output of light olefins” refers to the once through output of light olefins per reactor in unit time, and the term “weight hourly space velocity” refers to the mass of the reactant passing through the unit mass of the catalyst in unit time. 
         [0000]      Yield=the output of the product/the sum of the output of the hydrocarbon products except the oxygen-containing compound*100. 
         [0029]    The hydrocarbon products except the oxygen-containing compound specifically include hydrogen and the hydrocarbons containing no oxygen and one or more carbon atoms. 
         [0030]    According to the present invention, a process for producing light olefins is provided, wherein an oxygen-containing compound feedstock and a catalyst are continuously contacted to conduct a dehydration reaction to produce light olefins. 
         [0031]    The process according to the present invention can comprise the following steps: continuously contacting an oxygen-containing compound feedstock and a catalyst to conduct the dehydration reaction to obtain a light olefins-rich hydrocarbon and a spent catalyst, transporting at least a part of the spent catalyst to the regeneration reaction to obtain a regenerated catalyst, and circulating at least a part of the regenerated catalyst to the dehydration reaction. Specifically speaking, the process can comprise the following steps: continuously contacting an oxygen-containing compound feedstock and a catalyst in a reactor (e.g. a riser-type reactor) to conduct the dehydration reaction to produce a light olefins-rich hydrocarbon and a spent catalyst; separating the olefins-rich hydrocarbon and the spent catalyst in a hydrocarbon-catalyst separation zone, introducing the separated olefins-rich hydrocarbon into a product separation-recovery system, stripping the spent catalyst through a stripping region of reactor, withdrawing the spent catalyst from the reactor and transporting it to a spent catalyst receiver; transporting the spent catalyst in the spent catalyst receiver directly to a regenerator via a catalyst hopper, or transporting it firstly to a spent catalyst feeding tank via a catalyst hopper and then to a regenerator, and regenerating the spent catalyst in an oxygen-containing atmosphere in the regenerator to obtain a regenerated catalyst; withdrawing the regenerated catalyst from the regenerator and transporting it to the regenerated catalyst receiver, and then to the regenerated catalyst feeding tank via a catalyst hopper, or transporting the regenerated catalyst directly to a catalyst hopper; and then transporting back to the reactor. 
         [0032]    The regenerator according to the present invention can be any type of the regenerators known to those skilled in the art and conventionally used in the art, for example, a fluidized bed regenerator or an ebullated bed regenerator, but not limited thereto. 
         [0033]    The process according to the present invention can also comprise the following steps: withdrawing a part of the spent catalyst from the reactor or the spent catalyst receiver; transporting the withdrawn spent catalyst directly to the reactor, or removing the heat from the withdrawn spent catalyst to cool it and then transporting the cooled catalyst to the reactor, or transporting the withdrawn spent catalyst to a catalyst mixer located at the lower part of the reactor to mix with the regenerated catalyst therein and then transporting the mixed catalyst to the reactor; wherein the withdrawn spent catalyst is in an amount sufficient to maintain the continuous operation of the catalyst in the reactor together with the regenerated catalyst that is transported to the regenerated catalyst feeding tank via a catalyst hopper. The process according to the present invention can also comprise the following steps: withdrawing a part of the spent catalyst from the reactor or the spent catalyst receiver; transporting the withdrawn spent catalyst directly to the regenerated catalyst feeding tank, or removing the heat from the withdrawn spent catalyst to cool it and then transporting the cooled catalyst to the regenerated catalyst feeding tank; after mixing with the regenerated catalyst, transporting the mixed catalyst to the reactor; wherein the withdrawn spent catalyst is in an amount sufficient to maintain the continuous operation of the catalyst in the reactor together with the regenerated catalyst that is transported to the regenerated catalyst feeding tank via a catalyst hopper. 
         [0034]    According to the present invention, the oxygen-containing compound feedstock is well known to those skilled in the art, can be selected from at least one of alcohol, ether and ester, or can be other industrially or naturally sourced oxygen-containing compounds. The present invention has no specific limitation thereto. It is preferable for the oxygen-containing compound feedstock to be selected from at least one of R1-O—R2, R1-OC(═O)O—R2, R1-C(═O)O—R2 and R1-C(═O)—R2, wherein, R1 and R2 are identical or different each other, each independently selected from H and C1-6 branched or linear alkyl, preferably each independently selected from H and C1-4 branched or linear alkyl, with the proviso that at most one of R1 and R2 is hydrogen. It is more preferable for the oxygen-containing compound feedstock to be selected from at least one of methanol, ethanol, dimethylether, diethylether, methyl-ethyl-ether, methylene carbonate and methyl formate, in particular, methanol. 
         [0035]    According to the present invention, a diluent is sometimes needed in the dehydration reaction. Water vapor is generally used as diluent, or hydrogen, methane, ethane, nitrogen, carbon monoxide or the like can be used as diluent. If used, the mole ratio of the oxygen-containing compound feedstock to the diluent is generally 40:1-0.4:1, preferably 11:1-0.7:1, more preferably 7:1-1.3:1. 
         [0036]    According to the present invention, the used catalyst can be those well known to those skilled in the art. For example, the catalyst can be a zeolite catalyst. The zeolite can be an aluminosilicophosphate zeolite and/or an aluminosilicate zeolite. The aluminosilicophosphate zeolite can be selected from one or more of SAPO and SRM zeolites, and the aluminosilicate zeolite can be selected from one or more of ZSM and ZRP zeolites. In addition, the zeolite can be supported with one or more elements selected from alkaline earth metal, K, Mg, Ca, Ba, Zr, Ti, Co, Mo, Ni, Pt, Pd, La, Ce, Cu, Fe, B, Si, P, Sn, Pb, Ga, Cr, V, Sc, Ge, Mn, La, Al, Ni, and Fe. 
         [0037]    The process according to the present invention can also comprise a step of separating the light olefins-rich hydrocarbon to obtain a C 4   +  hydrocarbon 
         [0038]    The process according to the present invention can optionally comprise the following steps: continuously contacting the C 4   +  hydrocarbon and a further catalyst to conduct a further reaction to produce a further light olefins-rich hydrocarbon and a further spent catalyst, 
         [0000]    transporting at least a part of the further spent catalyst to the regeneration reaction to obtain a further regenerated catalyst, and circulating at least a part of the regenerated catalyst and/or at least a part of the further regenerated catalyst to the dehydration reaction and/or the further reaction. For example, the process can comprise transporting the C 4   +  hydrocarbon obtained from the separation with the product separation-recovery system to the further reactor (e.g. a riser-type reactor) to conduct the further reaction. 
         [0039]    According to the present invention, the further catalyst and the catalyst can be identical or different, and the further catalyst can be well known to those skilled in the art. For example, the further catalyst can be a zeolite catalyst. The zeolite can be an aluminosilicophosphate zeolite and/or an aluminosilicate zeolite. The aluminosilicophosphate zeolite can be selected from one or more of SAPO and SRM zeolites, and the aluminosilicate zeolite can be selected from one or more of ZSM and ZRP zeolites. In addition, the zeolite can be supported with one or more elements selected from alkaline earth metal, K, Mg, Ca, Ba, Zr, Ti, Co, Mo, Ni, Pt, Pd, La, Ce, Cu, Fe, B, Si, P, Sn, Pb, Ga, Cr, V, Sc, Ge, Mn, La, Al, Ni and Fe. 
         [0040]    The process according to the present invention can also comprise the following steps: transporting the regenerated catalyst in the regenerated catalyst feeding tank to the further reactor to contact with the C 4   +  hydrocarbon and conduct the further reaction, and transporting the resulting further light olefins-rich hydrocarbon and the resulting further spent catalyst together to the hydrocarbon-catalyst separation zone of the reactor. 
         [0041]    The process according to the present invention can also comprise the following steps: transporting the spent catalyst in the reactor to the further reactor to contact with the C 4   +  hydrocarbon and conduct the further reaction; separating the resulting further light olefins-rich hydrocarbon and the resulting further spent catalyst in the further reactor; and transporting the separated further light olefins-rich hydrocarbon to the product separation-recovery system, and transporting the separated further spent catalyst to the spent catalyst receiver. 
         [0042]    The process according to the present invention can also comprise the following steps: transporting the spent catalyst in the reactor to the further reactor to contact with the C 4   +  hydrocarbon and conduct the further reaction, and transporting the resulting further light olefins-rich hydrocarbon and the resulting further spent catalyst together to the hydrocarbon-catalyst separation zone of the reactor. 
         [0043]    The process according to the present invention can also comprise the following steps: transporting the regenerated catalyst in the regenerator directly to the further reactor to contact with the C 4   +  hydrocarbon and conduct the further reaction to obtain a further light olefins-rich hydrocarbon and a further spent catalyst; separating the further light olefins-rich hydrocarbon and the further spent catalyst in the further reactor; transporting the separated further light olefins-rich hydrocarbon to the product separation-recovery system; and transporting the further spent catalyst directly to the regenerator to conduct the regeneration. 
         [0044]    According to the present invention, the number of the reactor and/or the further reactor can be one or more, and the present invention has no specific limitation thereto. In addition, the reactor and/or the further reactor are identical or different each other, and each independently selected from a fluidized bed reactor, a dense bed reactor, a riser reactor, an ebullated bed reactor, a slurry bed reactor and a combination thereof. It is preferable that the reactor and/or the further reactor are identical or different each other, and each independently selected from a riser reactor, more preferably each independently selected from an isodiametric riser reactor, a riser reactor with an equal linear velocity, a variable diameter riser reactor and a riser-dense bed hybrid reactor. In addition, in the vertical direction from the bottom to the top, the riser-type reactor can be also provided with a pre-lifting region, a riser, a quenching medium line, a diameter-expanded riser, a necking, a quick separator, a stripping region, a dense-phase region, a sedimentation zone, a catalyst mixer, and a filter, which are industrially common devices, so that the reactor can be continuously operated; wherein the sedimentation zone, the filter and the like can constitute the hydrocarbon-catalyst separation zone, and the hydrocarbon-catalyst separation zone can also comprise other devices useful for the separation of the spent catalyst and the hydrocarbon. The present invention has no limitation thereto. According to the present invention, the dense bed part of the riser-type reactor can form no dense bed, i.e. “zero-bed” operating mode. 
         [0045]    Since the process for producing olefins from the oxygen-containing compound feedstock is an exothermic reaction, the reactor according to the present invention can be provided with one or more quenching medium lines to control the reaction temperature. According to a specific embodiment of the present invention, one or more quenching medium lines can be provided at the mid-downstream of the reactor (relative to the reactant direction) so as to inject a quenching medium to the reactor. The shock chilling medium can be a quenching agent or a cooled catalyst. The quenching agent can be an un-preheated oxygen-containing compound feedstock and/or water. 
         [0046]    According to the present invention, in general, the reaction temperature of the dehydration reaction is 200-700° C., preferably 250-600° C. In particular, in order to achieve the present inventive object of increasing the production of light olefins, the reaction pressure P of the dehydration reaction is 0.5-10 MPa, preferably 0.75-3.5 MPa, more preferably 0.8-3 MPa, most preferably 1-2 MPa. In addition, the weight hourly space velocity H of the dehydration reaction is generally 7-250 h −1 , preferably 8-150 h −1 , more preferably 10-100 h −1 , more preferably 15-80 h −1 , most preferably 15-50 h −1 . 
         [0047]    According to a particularly preferable embodiment of the present invention, in the dehydration reaction (in other words, if intending to remarkably increase the output of light olefins upon doing a modification based on an existing reactor or reaction plant), H and P satisfy a mathematical function of H=f(P), which is a strictly increasing function. Among others, P (unit: MPa) is in the interval [0.55, 10.0], preferably in the interval [0.75, 3.5], more preferably in the interval [0.8, 3.0], more preferably in the interval [1.0, 2.0], and H (unit: h −1 ) is in the interval [7, 250], preferably in the interval [8, 150], more preferably in the interval [10, 100], more preferably in the interval [15, 80], most preferably in the interval [15, 50]. According to this strictly increasing function, when the reaction pressure P of the dehydration reaction is increased in the specific numeric interval as defined in the present invention, the weight hourly space velocity H of the dehydration reaction should be correspondingly increased in the specific numeric interval as defined in the present invention. The present invention has no limitation to the increasing manner and the increasing amplitude of the reaction pressure P and the weight hourly space velocity H, as long as based on the normal judgement of those skilled in the art, the numerical values are indeed increased respectively; and it is not allowed to remain the numerical values unchanged or decrease the numerical values. According to one specific embodiment of the present invention, it is preferable that the reaction pressure P and the weight hourly space velocity H are increased in proportion or in the same or different amplitude, sometimes in the same scale or synchronously, until the expected amplitude of increasing the production of light olefins is accomplished. In some cases, when the reaction pressure P arrives at the upper limit (e.g. 3 MPa) of a certain numeric interval as defined previously in the present invention, it is generally preferable that the weight hourly space velocity H arrives at the upper limit (e.g. 50 h −1 ) of a certain numeric interval as defined previously in the present invention too, but not limited thereto. 
         [0048]    It should be particularly noted that, when any one or both of the reaction pressure P and the weight hourly space velocity H are not in the numeric range or the numeric interval as previously defined herein, even increasing the reaction pressure P and simultaneously and correspondingly increasing the weight hourly space velocity H cannot obtain the effect of remarkably increasing the production of light olefins of the present invention, as shown in the Example. This is totally unexpected by those skilled in the art. 
         [0049]    According to the present invention, the reaction conditions of the further reaction comprise: reaction temperature 200-700° C., preferably 300-600° C.; reaction pressure 0.1-6 MPa, preferably 0.8-2 MPa. The process according to the present invention can also comprise: controlling the ratio of the reaction pressure P of the reactor to the regeneration pressure of the regenerator to be 3-100:1. More specifically speaking, according to the present invention, the reaction pressure P of the dehydration reaction is at least 0.35 MPa, preferably 0.4 MPa, 0.5 MPa, 0.6 MPa, 0.7 MPa, 0.8 MPa, 0.9 MPa, 1.0 MPa, 1.1 MPa, 1.2 MPa, 1.3 MPa, 1.4 MPa, 1.5 MPa, 1.6 MPa, 1.7 MPa, 1.8 MPa, 1.9 MPa or 2.0 MPa higher than the regeneration pressure of the regeneration reaction. Alternatively according to the present invention, the reaction pressure P of the dehydration reaction is at most 5 MPa, preferably 4 MPa, 3.5 MPa, 3.3 MPa, 3 MPa, 2.5 MPa, 2.3 MPa, 2 MPa, 1.5 MPa, 1.3 MPa or 1 MPa higher than the regeneration pressure of the regeneration reaction. 
         [0050]    According to the present invention, since the production of light olefins from the oxygen-containing compound feedstock and the regenerate of the spent catalyst are the exothermic reactions, one or more internal heat removers can be installed in the reactor, the regenerator, the regenerated catalyst feeding tank or the regenerated catalyst receiver. The internal heat remover can be in form of coil pipe, elbow pipe and the like. The heat in the reactor can be removed by the liquid such as water or carbon tetrachloride flowing in the internal heat remover. Other internal heat remover commonly used in the industry can be also applied in the present invention. 
         [0051]    The present inventors have found that contacting the oxygen-containing compound feedstock with a certainly-coked catalyst can be favorable for the reaction to proceed quickly. This is because, on one hand, the coke deposited in the catalyst continuously reacts as active center with the oxygen-containing compound feedstock to introduce the alkyl groups; on the other hand, the coke deposited in the catalyst is continuously dealkylated to form the light olefins such as propylene and ethylene. This is the so-called “hydrocarbon pool” reaction. Accordingly, the process according to the present invention can also comprise circulating at least a part of the spent catalyst and/or at least a part of the further spent catalyst to the dehydration reaction or the reactor. 
         [0052]    According to a specific embodiment of the present invention, a part of the spent catalyst can be withdrawn from the reactor or the spent catalyst receiver, the withdrawn spent catalyst is transported, directly or via heat removal to reduce the temperature, back to the reactor, or transported to the catalyst mixer located at the lower part of the reactor, in which the spent catalyst and the regenerated catalyst are mixed, and then the resulting mixed catalyst is transported back to the reactor for reaction. 
         [0053]    According to another specific embodiment of the present invention, a part of the spent catalyst can be withdrawn from the reactor or the spent catalyst receiver, the withdrawn spent catalyst is transported, directly or via heat removal to reduce the temperature, to regenerated catalyst feeding tank, in which the spent catalyst and the regenerated catalyst are mixed, and then the resulting mixed catalyst is transported back to the reactor; wherein the withdrawn spent catalyst is in an amount sufficient to maintain the continuous operation of the catalyst in the reactor together with the regenerated catalyst that is present in the regenerated catalyst feeding tank and transported via a catalyst hopper. 
         [0054]    According to the present invention, a part of the spent catalyst withdrawn from the reactor or the spent catalyst receiver can be transported via the external heat remover, in which the heat is removed so as to reduce the temperature. Said external heat remover can be well known to those skilled in the art, and the heat removal device such as coil pipe and elbow pipe can be installed in the external heat remover to reduce the temperature of the spent catalyst flowing therethrough. 
         [0055]    According to the present invention, the catalyst mixer can be connected to the reactor, preferably in a vertical manner, for mixing one or more the hot regenerated catalyst, the heat-removed regenerated catalyst, and the spent catalyst that are transported to the reactor. The catalyst mixer has a temperature of 200-600° C., preferably 300-500° C., and a pressure of 0.5-10 MPa. 
         [0056]    According to the present invention, the total carbon content of the catalyst(s) transported to the reactor (the feeding zone) and/or the further reactor (the feeding zone) can be 3-25 wt %, preferably 6-15 wt %. Here, the catalyst transported to the reactor or the further reactor can be from the regenerated catalyst feeding tank, or can be from the spent catalyst receiver and/or the reactor, wherein the catalyst from the regenerated catalyst feeding tank can be a regenerated catalyst, or a mixed catalyst of the regenerated catalyst and the spent catalyst. 
         [0057]    According to the present invention, it can be understood by those skilled in the art that the light olefins-rich hydrocarbon can be separated by the product separation-recovery system to produce a fraction of C 4   +  hydrocarbon. In order to increase the output of the light olefins, the C 4   +  hydrocarbon can be transported to the further reactor to conduct the further reaction for cracking the C 4   +  hydrocarbon into light olefins. 
         [0058]    According to a specific embodiment of the present invention, the regenerated catalyst in the regenerated catalyst feeding tank can be transported to the further reactor to contact with the C 4   +  hydrocarbon and conduct the further reaction, and the resulting further light olefins-rich hydrocarbon and the resulting further spent catalyst are transported together to the hydrocarbon-catalyst separation zone of the reactor; wherein the further light olefins-rich hydrocarbon and the further spent catalyst that are transported to the hydrocarbon-catalyst separation zone of the reactor can be mixed with the light olefins-rich hydrocarbon and the spent catalyst that are produced in the reactor, and the resulting mixture is then subjected to the separation. 
         [0059]    According to a further specific embodiment of the present invention, the spent catalyst in the reactor can be transported to the further reactor to contact with the C 4   +  hydrocarbon and conduct the further reaction, the resulting further light olefins-rich hydrocarbon and the resulting further spent catalyst can be separated in the further reactor, the separated further light olefins-rich hydrocarbon is transported to the product separation-recovery system, and the separated further spent catalyst is transported to the spent catalyst receiver. 
         [0060]    According to a further specific embodiment of the present invention, the spent catalyst that has been stripped in the stripping region of the reactor can be transported to the further reactor to contact with the C 4   +  hydrocarbon and conduct the further reaction, the resulting further light olefins-rich hydrocarbon and the resulting further spent catalyst are transported together to the hydrocarbon-catalyst separation zone of the reactor; wherein the further light olefins-rich hydrocarbon and the further spent catalyst that are transported back to the reactor can be mixed with the light olefins-rich hydrocarbon and the spent catalyst that are produced in the reactor, and the resulting mixture is then subjected to the separation. 
         [0061]    According to a more further specific embodiment of the present invention, the regenerated catalyst in the regenerator can be directly transported to the further reactor to contact with the C 4   +  hydrocarbon and conduct the further reaction to produce a further light olefins-rich hydrocarbon and a further spent catalyst is separated in the further reactor; the further light olefins-rich hydrocarbon and the further spent catalyst are separated in the further reactor, the separated further light olefins-rich hydrocarbon can be transported to the product separation-recovery system, and the separated further spent catalyst can be directly transported to the regenerator for regeneration. 
         [0062]    According to the present invention, the reaction conditions that are well known to those skilled in the art and can produce light olefins can be applied to the dehydration reaction for producing olefin in the reactor and the further reaction in the further reactor, and the substantially same or different reaction conditions can be applied to the above two reactions. Since the reaction feedstock in the further reactor and the reaction feedstock in the reactor are not completely identical, therefore it is preferable that depending on the feedstock in the further reactor, the reaction conditions, which are different from those of the reactor, are applied to the further reaction, which can be understood by those skilled in the art, wherein the further reaction can mainly comprise the cracking reaction of C 4   +  hydrocarbon. It is preferable that the reaction conditions in two reactors can be selected, for example, in the following ranges: the reaction temperature can be 200-700° C., preferably 250-600° C.; the reaction pressure can be 0.5-10 MPa, preferably 1-3.5 MPa. 
         [0063]    In order to separate the (further) light olefins-rich hydrocarbon and the (further) spent catalyst produced after the reaction in the reactor or the further reactor, or to separate the regenerated catalyst and the flue gas produced after the regeneration in the regenerator, the conventional cyclone separator can be used, which is well known to those skilled in the art, and will not be discussed in detail. 
         [0064]    According to a preferred specific embodiment of the present invention, the light olefins-rich hydrocarbon and the spent catalyst can be separated with a filter. In addition, the further light olefins-rich hydrocarbon and the further spent catalyst can be also separated with a filter. Moreover, the (further) regenerated catalyst and the flue gas can be also separated with a filter. The use of the filter to separate the catalyst can effectively remove the catalyst powder and dust entrained in the hydrocarbon or the flue gas. Compared with the cyclone separator conventionally used in the prior art, the use of the filter can maximally reduce the natural loss of the catalyst in the production. This is one of remarkable dominances of the present invention. 
         [0065]    According to the present invention, the filter can be prepared with a porous material, for example, selected from metal sintered porous material and/or ceramic porous material. The filter has a filter fineness for 2 μm particle of as high as 99.9%, preferably a filter fineness for 1.2 μm particle of as high as 99.9%. In addition, the filter can be purged with a purge gas to clean off the filter cake. Herein, the purge gas can be selected from one or more of a hydrocarbon-containing gas, dry gas, nitrogen, and water vapor. 
         [0066]    The process according to the present invention can also comprise circulating an incompletely-reacted oxygen-containing compound feedstock (including various oxygen-containing compounds newly formed in the dehydration reaction, especially dimethyl ether) to the step of the dehydration reaction to accomplish the full utilization of the reaction feedstock. 
         [0067]    According to the present invention, transporting at least a part of the spent catalyst and/or at least a part of the further spent catalyst to the regeneration reaction and/or transporting at least a part of the regenerated catalyst and/or at least a part of the further regenerated catalyst to the dehydration reaction and/or the further reaction can be conveniently accomplished by means of one or more (preferably one or two) catalyst hopper. Herein, the catalyst hopper is sometimes also known as the lock hopper. In the context of the present specification, in particular in the drawings and the Example, the catalyst hopper is taken as an example to explain the technology idea of the present invention and various specific embodiments, but the present invention is not limited thereto. 
         [0068]    According to the present invention, the catalyst hopper can safely and effectively transport the catalyst from a higher pressure hydrocarbon environment of the reactor to a lower pressure oxygen environment of the regenerator, and from a lower pressure oxygen environment of the regenerator to a higher pressure hydrocarbon environment of the reactor. 
         [0069]    That is to say, on one hand, the use of the catalyst hopper can segregate the hydrocarbon atmosphere of the reactor from the regenerative oxygen-containing atmosphere of the regenerator, ensuring the safety of the process of the present invention; on the other hand, can flexibly adjust and control the operation pressure of the reactor and the regenerator, in particular in case of not increasing the operation pressure of the regenerator, can increase the operation pressure of the reactor and thereby increase the plant&#39;s throughput. 
         [0070]    For example, the step of transporting a catalyst from a reactor (higher pressure hydrocarbon environment) to a regenerator (lower pressure oxygen environment) through a catalyst hopper can comprise: 1. purging the evacuated catalyst hopper with a hot nitrogen to drive the residual oxygen to the regenerator; 2. purging the catalyst hopper with dry gas to drive out the nitrogen; 3. pressurizing the evacuated catalyst hopper with dry gas; 4. filling the evacuated catalyst hopper with the spent catalyst transported from the spent catalyst receiver; 5. depressurizing the filled catalyst hopper by venting the dry gas in the pressurized catalyst hopper; 6. purging the filled catalyst hopper with hot nitrogen to drive out the dry gas; 7. discharging the spent catalyst from the filled catalyst hopper to the spent catalyst feeding tank. For example, the step of circulating a catalyst from a regenerator (lower pressure oxygen environment) to a reactor (higher pressure hydrocarbon environment) through a catalyst hopper can comprise: 1. purging the regenerated catalyst-filled catalyst hopper with hot nitrogen to drive the oxygen to the regenerator; 2. purging the catalyst hopper with dry gas to drive out the nitrogen; 3. pressurizing the filled catalyst hopper with dry gas; 4. discharging the regenerated catalyst from the filled catalyst hopper to the regenerated catalyst feeding tank; 5. depressurizing the evacuated catalyst hopper by venting the dry gas in the pressurized catalyst hopper; 6. purging the evacuated catalyst hopper with hot nitrogen to drive out the dry gas; 7. filling the evacuated catalyst hopper with the regenerated catalyst transported from the regenerated catalyst receiver. 
         [0071]    Since the catalyst is transported with the catalyst hopper in batch, according to the present invention, the function of the regenerated catalyst feeding tank and the spent catalyst circulating line is to transport the catalyst to the reactor in a more continuous manner. However, the present inventors have found that transporting the spent catalyst to the regenerator and transporting the regenerated catalyst from the regenerator can be done in batch. Upon transporting the spent catalyst from the catalyst hopper to the regenerator or upon transporting the regenerated catalyst from the regenerator to the catalyst hopper, the transport can be accomplished by means of the gravity between the regenerator and the catalyst hopper or the pressure difference between the pipelines without installing the spent catalyst feeding tank or the regenerated catalyst receiver. 
         [0072]    According to the present invention, in case that the further reactor and the reactor are communicated with each other, those skilled in the art can understand that the pressures in two reactors can be identical, that is to say, if necessary, the catalyst hopper can also accomplish the transport and circulating of the catalyst in the further reactor. 
         [0073]    According to the present invention, the regeneration reaction conditions are well known to those skilled in the art, for example, the reaction conditions of the regeneration reaction comprise: reaction temperature 450-850° C., preferably 550-700° C.; reaction pressure 0.1-0.5 MPa, preferably 0.15-0.3 MPa, for example normal pressure; oxygen-containing atmosphere. The oxygen-containing atmosphere can be air, a nitrogen-diluted air, an oxygen-rich gas as fluidizing medium. 
         [0074]    According to the present invention, with the proviso that the size and amount of the reactor for the dehydrogenation reaction are kept the same; in other words, upon doing a modification based on an existing reactor or reaction plant, increasing the reaction pressure and WHSV of the reactor in the specific ranges as defined according to the present invention can remarkably increase the throughput of the oxygen-containing compound feedstock of the reactor and accordingly increase the output of the light olefins. In this case, the output of light olefins can be increased by up to 50%, preferably 100%, more preferably 150%, 200%, 500% or 790%, most preferably even up to 1000% or higher. 
         [0075]    It should be emphasized that, according to the present invention, on the basis that the yield of light olefins is kept at a level substantially identical to or slightly higher than that of the prior art, the object of increasing the output of light olefins is accomplished by increasing the throughput of the oxygen-containing compound feedstock of the reactor or reaction plant. Therefore, the amplitude of increasing of the output of the light olefins according to the present invention is remarkably higher, compared with the achievement of increasing the output of light olefins by simply increasing the throughput of the oxygen-containing compound feedstock of the reactor or reaction plant at the expense of compromising the yield of light olefins (for example, the reduction amplitude &gt;20%). According to the present invention, the yield of light olefins can be maintained at a level comparable to or even higher than that of the prior art, for example, generally 60%-95% or 78%-95%. 
         [0076]    From another viewpoint, with the proviso that a predetermined output of light olefins is achieved, compared to the prior art, the production of light olefins according to the process of the present invention as previously defined can remarkably reduce the size and amount of the reactor or reaction plant, and therefore reduce the scale and investment cost of the whole light olefins production plant. The specific embodiments of the present invention will be further described with reference to the drawings, but the present invention is not limited thereto. For convenience of describing the present invention, a riser-type reactor is taken as an example of the reactor, but the present invention is not limited thereto. 
       First Specific Embodiment 
       [0077]      FIG. 1  is a flowchart of the process for producing light olefins from the oxygen-containing compound feedstock according to the first specific embodiment of the present invention. 
         [0078]    As shown in  FIG. 1 , the oxygen-containing compound feedstock from the feeding line  24  is transported to the riser reactor  1  of the riser-type reactor, and is contacted with the catalyst from the pipeline  23  and lifted by means of the pre-lifting line  28  to conduct the dehydration reaction to produce olefins. After the reaction, the resulting hydrocarbon product enters the dense bed reactor  3 . An excessive heat is removed from the dense bed reactor  3  with the internal heat remover  2 . The hydrocarbon product is further reacted in the dense bed reactor  3 . The resulting light olefins-rich hydrocarbon and the spent catalyst are transported to the sedimentation zone  5 . After sedimentation, the spent catalyst returns to the dense bed reactor  3 . The light olefins-rich hydrocarbon and the entrapped spent catalyst fine powder are filtered with the filter  6 . The light olefins-rich hydrocarbon is transported to a product separation-recovery system (not shown) via the pipeline  2 . After filtering, the spent catalyst fine powder settles and returns to the dense bed reactor  3 . The spent catalyst is stripped in the stripping region  4 . After stripping, a part of the spent catalyst is transported to the spent catalyst receiver  8  via the pipeline  16 , and the other part of the spent catalyst is subjected to a heat-removal with the external heat remover  13  and transported to the regenerated catalyst feeding tank  12 . 
         [0079]    The spent catalyst from the spent catalyst receiver  8  is transported to the catalyst hopper  9  via the pipeline  17 , transported to the spent catalyst feeding tank  10  via the pipeline  18  after the pressure release, and then transported to the regenerator  7  via the pipeline  19 . The spent catalyst is counter-current contacted with the main air from the pipeline  27  and subjected to regeneration by coke-burning. The excessive heat is removed with the internal heat remover  15  (the removed heat can be controlled with the amount of the heat-removing stream and the depth by which the internal heat remover  15  is embedded into the dense bed layer). The flue gas is transported via the pipeline  26  to the subsequent energy recovery and purification system (not shown). The regenerated catalyst is transported to the regenerated catalyst receiver  11  via the pipeline  20 . The excessive heat of the regenerated catalyst is removed with the internal heat remover  14 . After the heat removal, the regenerated catalyst is transported to the catalyst hopper  9  via the pipeline  21 . After increasing the pressure, the regenerated catalyst is transported to the regenerated catalyst feeding tank  12  via the pipeline  22  and mixed with the spent catalyst from the heat remover  13 . The mixed catalyst is transported to the pre-lifting region of the riser reactor  1  via the pipeline  23 . 
       Second Specific Embodiment 
       [0080]      FIG. 2  is a flowchart of the process for producing light olefins from the oxygen-containing compound feedstock according to the second specific embodiment of the present invention. 
         [0081]    As shown in  FIG. 2 , the catalyst from the pipeline  223  and the spent catalyst from the pipeline  213  are mixed in the catalyst mixer  211 . The mixed catalyst is lifted with the pre-lifting gas from the pre-lifting line  219  and transported to the riser reactor  201  of the riser-type reactor. The oxygen-containing compound feedstock is transported to the riser reactor  201  via the feeding line  224 , and contacted with the catalyst from the mixer  211  to conduct the dehydration reaction to produce olefins. After the reaction, the resulting hydrocarbon product is further reacted in the internal riser and distributor  202 , and then transported to the dense bed reactor  203 . The quenching medium from the quenching medium line  220  is transported to the riser reactor  201  to control the reaction temperature. The unconverted feedstock is further contacted with the catalyst and reacted in the dense bed reactor  203 . The excessive reaction heat is withdrawn with the internal heat remover  215 . The resulting light olefins-rich hydrocarbon and the spent catalyst are transported to the sedimentation zone  205 . After sedimentation, the spent catalyst returns to the dense bed reactor  203 . The light olefins-rich hydrocarbon and the entrapped spent catalyst fine powder are filtered with the filter  206 . The light olefins-rich hydrocarbon is transported to a product separation-recovery system (not shown) via the pipeline  225 . After filtering, the spent catalyst fine powder settles and returns to the dense bed reactor  203 . The spent catalyst is stripped in the stripping region  204 . After stripping, a part of the spent catalyst is transported back to the catalyst mixer  211  via the pipeline  213 , and another part of the spent catalyst is transported to the spent catalyst receiver  208  via the pipeline  216 . 
         [0082]    The spent catalyst from the spent catalyst receiver  208  is transported to the catalyst hopper  209  via the pipeline  217 , and transported to the regenerator  207  via the pipeline  221  after the pressure release. The spent catalyst is counter-current contacted with the main air from the pipeline  227  and subjected to regeneration by coke-burning. The flue gas is transported via the pipeline  226  to the subsequent energy recovery and purification system (not shown). The regenerated catalyst is transported to the regenerated catalyst receiver  210  via the pipeline  215 . The excessive heat of the regenerated catalyst is removed with the internal heat remover  214 . After the heat removal, the regenerated catalyst is transported to the catalyst hopper  209  via the pipeline  218 . After increasing the pressure, the regenerated catalyst is transported to the regenerated catalyst feeding tank  212  via the pipeline  222  and transported to the catalyst mixer  211  via the pipeline  223 . 
       Third Specific Embodiment 
       [0083]      FIG. 3  is a flowchart of the process for producing light olefins from the oxygen-containing compound feedstock according to the third specific embodiment of the present invention. 
         [0084]    As shown in  FIG. 3 , the oxygen-containing compound feedstock is transported to the riser reactor  301  of the riser-type reactor via the feeding line  324 , and contacted with the catalyst from the pipeline  323  to conduct the dehydration reaction to produce olefins. After the reaction, the resulting hydrocarbon product is further reacted in the diameter-expanded riser  302 , and then further reacted in the dense bed reactor  303 . The resulting light olefins-rich hydrocarbon and the spent catalyst are transported to the sedimentation zone  305 . After sedimentation, the spent catalyst returns to the dense bed reactor. The light olefins-rich hydrocarbon and the entrapped spent catalyst fine powder are filtered with the filter  306 . The light olefins-rich hydrocarbon is transported to a product separation-recovery system (not shown) via the pipeline  325 . After filtering, the spent catalyst fine powder settles and returns to the stripping region  304  of the dense bed reactor  203 . After stripping, a part of the spent catalyst is transported back to the spent catalyst receiver  308  via the pipeline  316 , and another part of the spent catalyst is transported to the external heat remover  313 , and transported to the regenerated catalyst feeding tank  312  after heat removal. 
         [0085]    The spent catalyst from the spent catalyst receiver  308  is transported to the catalyst hopper  309  via the pipeline  317 , transported to the spent catalyst feeding tank  310  via the pipeline  318  after the pressure release, and then transported to the regenerator  307  via the pipeline  319 . The spent catalyst is counter-current contacted with the main air from the pipeline  327  and subjected to regeneration by coke-burning. The excessive heat is removed with the internal heat remover  315  (the removed heat can be controlled with the amount of the heat-removing stream and the depth by which the internal heat remover  315  is embedded into the dense bed layer). The flue gas is transported via the pipeline  326  to the subsequent energy recovery and purification system (not shown). The regenerated catalyst is transported to the regenerated catalyst receiver  311  via the pipeline  320 . The excessive heat of the regenerated catalyst is removed with the internal heat remover  314 . After the heat removal, the regenerated catalyst is transported to the catalyst hopper  309  via the pipeline  321 . After increasing the pressure, the regenerated catalyst is transported to the regenerated catalyst feeding tank  312  via the pipeline  322  and mixed with the spent catalyst from the external heat remover  313 . The mixed catalyst is transported to the riser reactor  301  and to the further riser-type reactor  330  via the pipelines  323  and  332 . 
         [0086]    The catalyst from the pipeline  332  is transported to the pre-lifting region of the further riser-type reactor  330 , and further transported to the further riser-type reactor  330  by lifting with the pre-lifting media from the pre-lifting line  328 . The C 4   +  hydrocarbon obtained from the separation of the product separation-recovery system is transported to the further riser-type reactor  330  via the feedstock feeding line  329  and contacted with the catalyst to conduct the further reaction. The resulting light olefins-rich hydrocarbon is transported to the dense bed-fluidized bed  303  via the pipeline  331 . 
       Fourth Specific Embodiment 
       [0087]      FIG. 4  is a flowchart of the process for producing light olefins from the oxygen-containing compound feedstock according to the fourth specific embodiment of the present invention. 
         [0088]    As shown in  FIG. 4 , the catalyst from the pipeline  423  and the spent catalyst from the external heat remover  413  are mixed in the catalyst mixer  411 . The mixed catalyst is lifted with the pre-lifting gas from the pre-lifting line  419  and transported to the riser reactor  401  of the riser-type reactor. The oxygen-containing compound feedstock is transported to the riser reactor  401  via the feeding line  424 , and contacted with the catalyst from the catalyst mixer  411  to conduct the dehydration reaction to produce olefins. After the reaction, the resulting hydrocarbon product and the catalyst are transported to the dense bed reactor  403  via the internal riser and distribution plate  402 . The quenching medium from the quenching medium line  420  is transported to the riser reactor  401  to control the reaction temperature. The unconverted feedstock is further contacted with the catalyst and reacted in the dense bed reactor  403 . The excessive reaction heat is withdrawn with the internal heat remover  415 . The resulting light olefins-rich hydrocarbon and the spent catalyst are transported to the sedimentation zone  205 . After sedimentation, the spent catalyst is transported to the stripping region  404 . The light olefins-rich hydrocarbon and the entrapped spent catalyst fine powder are filtered with the filter  406 . After filtering, the light olefins-rich hydrocarbon is transported to a product separation-recovery system (not shown) via the pipeline  425 , and the spent catalyst fine powder settles and returns to the dense bed reactor  403 . The spent catalyst is stripped in the stripping region  404 . After stripping, a part of the spent catalyst is transported back to the catalyst mixer  411  via the internal heat remover  413 , and another part of the spent catalyst is transported to the first reaction zone  431  of the further riser-type reactor via the pipeline  430 . The C 4   +  hydrocarbon obtained from the separation of the product separation-recovery system is transported to the first reaction zone  431  of the further riser-type reactor via the pipeline  429  and contacted with the catalyst from the pipeline  430  to conduct the further reaction. The resulting light olefins-rich hydrocarbon and the resulting catalyst are transported to the second reaction zone  432  to continue the reaction, and then to the sedimentation zone  435  via the quick separator  433  at the necking. The light olefins-rich hydrocarbon and the entrapped spent catalyst fine powder are filtered with the filter  436 . After filtering, the light olefins-rich hydrocarbon is transported to a product separation-recovery system (not shown) via the pipeline  437 . The catalyst is stripped in the stripping region  434  and then transported to the catalyst circulation system via the pipelines  438  and  416 . 
         [0089]    The spent catalyst from the spent catalyst receiver  408  is transported to the catalyst hopper  409  via the pipeline  417 , and transported to the regenerator  407  via the pipeline  421  after the pressure release. The spent catalyst is counter-current contacted with the main air from the pipeline  227  and subjected to regeneration by coke-burning. The flue gas is transported via the pipeline  426  to the subsequent energy recovery and purification system (not shown). The regenerated catalyst is transported to the regenerated catalyst receiver  410  via the pipeline  415 . The excessive heat of the regenerated catalyst is removed with the internal heat remover  414 . After the heat removal, the regenerated catalyst is transported to the catalyst hopper  409  via the pipeline  418 . After increasing the pressure, the regenerated catalyst is transported to the regenerated catalyst feeding tank  412  via the pipeline  422  and transported to the catalyst mixer  411  via the pipeline  423 . 
       Fifth Specific Embodiment 
       [0090]      FIG. 5  is a flowchart of the process for producing light olefins from the oxygen-containing compound feedstock according to the fifth specific embodiment of the present invention. 
         [0091]    As shown in  FIG. 5 , the oxygen-containing compound feedstock is transported to the riser reactor  501  of the riser-type reactor via the feeding line  524 , and contacted with the catalyst from the pipeline  523  to conduct the dehydration reaction to produce olefins. After the reaction, the resulting hydrocarbon product and the catalyst are transported to the dense bed reactor  503  via the internal riser and quick separator  502 . The quenching medium from the quenching medium line  528  is transported to the riser reactor  501  to control the reaction temperature. The unconverted feedstock is further contacted with the catalyst and reacted in the dense bed reactor  503 . The resulting light olefins-rich hydrocarbon and the spent catalyst are transported to the sedimentation zone  505 . The light olefins-rich hydrocarbon and the entrapped spent catalyst fine powder are filtered with the filter  406 . After filtering, the light olefins-rich hydrocarbon is transported to a product separation-recovery system (not shown) via the pipeline  525 , and the spent catalyst fine powder settles and returns to the dense bed reactor  503 . The spent catalyst is stripped in the stripping region  404 . After stripping, a part of the spent catalyst is transported to the spent catalyst receiver  508  via the pipeline  516 , another part of the spent catalyst is transported to the first reaction zone  530  of the further riser-type reactor via the pipeline  535 , and the remaining part of spent catalyst is transported to the external heat remover  513  and to the internal riser and quick separator  502  after the heat removal. The C 4   +  hydrocarbon obtained from the separation of the product separation-recovery system is further transported the first reaction zone  530  and the second reaction zone and necking  531  of the further riser-type reactor via the pipeline  533 , and contacted with the catalyst, which is from the pipeline  535  and lifted with a pre-lifting gas via the pre-lifting line  532 , to conduct the further reaction. The resulting light olefins-rich hydrocarbon and the resulting catalyst are transported to the dense bed  503  via the pipeline  534 . 
         [0092]    A part of the spent catalyst from the spent catalyst receiver  508  is transported to the external heat remover  529 , and then to the regenerated catalyst feeding tank  512  after heat removal. Another part of the spent catalyst from the spent catalyst receiver  508  is transported to the catalyst hopper  509  via the pipeline  517 , and then to the spent catalyst feeding tank  510  via the pipeline  518  after the pressure release, and then to the regenerator  507  via the pipeline  519 . The spent catalyst is counter-current contacted with the main air from the pipeline  527  and subjected to regeneration by coke-burning. The excessive heat is removed with the internal heat remover  515 . The flue gas is transported via the pipeline  526  to the subsequent energy recovery and purification system (not shown). The regenerated catalyst is transported to the regenerated catalyst receiver  511  via the pipeline  520 . The excessive heat of the regenerated catalyst is removed with the internal heat remover  514 . After the heat removal, the regenerated catalyst is transported to the catalyst hopper  509  via the pipeline  521 . After increasing the pressure, the regenerated catalyst is transported to the regenerated catalyst feeding tank  512  via the pipeline  522 . The spent catalyst from the spent catalyst receiver  508  is transported to the regenerated catalyst feeding tank  512  after the heat removal with the heat remover  529 , and mixed with the regenerated catalyst. The mixed catalyst is transported to the riser reactor  501  via the pipeline  523 . 
       Sixth Specific Embodiment 
       [0093]    As shown in  FIG. 6 , the catalyst from the pipeline  637  and the spent catalyst from the external heat remover  613  are mixed in the catalyst mixer  611 . The mixed catalyst is lifted with the pre-lifting gas from the pre-lifting line  619  and transported to the first reaction zone  601  of the riser-type reactor. The feedstock is transported to the first reaction zone  601  via the feeding line  624 , and contacted with the catalyst from the catalyst mixer  611  to conduct the dehydration reaction to produce olefins. After the reaction, the product and the catalyst are transported to the second reaction zone  602 . The unconverted feedstock is further contacted with the catalyst and reacted in the second reaction zone  602 . The resulting light olefins-rich hydrocarbon and the spent catalyst are transported to the sedimentation zone  605  via the necking and quick separator  603 . The light olefins-rich hydrocarbon and the entrapped spent catalyst fine powder are filtered with the filter  606 . After filtering, the light olefins-rich hydrocarbon is transported to a product separation-recovery system (not shown) via the pipeline  625 , and the spent catalyst fine powder settles and returns to the stripping region  604 . The spent catalyst is stripped in the stripping region, a part of the spent catalyst is transported to the spent catalyst receiver  608  via the pipeline  616 , another part of the spent catalyst is transported to the external heat remover  613  and then to the catalyst mixer  611  via the pipeline  624  after heat removal, and the remaining part of the spent catalyst is transported to the regenerated catalyst feeding tank  636  via the external heat remover  612  after the heat removal. 
         [0094]    The spent catalyst from the spent catalyst receiver  608  is transported to the catalyst hopper  609  via the pipeline  617 , and transported to the regenerator  607  via the pipeline  621  after the pressure release. The spent catalyst is counter-current contacted with the main air from the pipeline  622  and subjected to regeneration by coke-burning. The flue gas is transported via the pipeline  620  to the subsequent energy recovery and purification system (not shown). The excessive heat is removed with the internal heat remover  615 . The regenerated catalyst is transported to the regenerated catalyst receiver  610 . The excessive heat of the regenerated catalyst is removed with the internal heat remover  614 . After the heat removal, the regenerated catalyst is transported to the catalyst hopper  609  via the pipeline  618 . After increasing the pressure, the regenerated catalyst is transported to the regenerated catalyst feeding tank  636  via the pipeline  623  and mixed with the spent catalyst from the external heat remover  612 . The mixed catalyst is transported to the catalyst mixer  611  via the pipeline  637 . 
         [0095]    The regenerated catalyst from the pipeline  633  is pre-lifted with the pre-lifting gas  626 , and contacted with the C 4   +  olefins from the feeding line  635  to conduct the further reaction in the further riser-type reactor  627 . The hydrocarbon product and the catalyst are separated with the quick separator  628  to produce the light olefins-rich hydrocarbon and the spent catalyst. The separated hydrocarbon product is subjected to the sedimentation in the sedimentation zone  629  and the filtering with filter  631 . After the filtering, the hydrocarbon product is transported via the pipeline  632  to a subsequent separation system (not shown). The spent catalyst is stripped in the stripping region  630 . After stripping, the spent catalyst is transported to the regenerator  607  via the pipeline  634  for regeneration. 
       Seventh Specific Embodiment 
       [0096]      FIG. 7  is a flowchart of the process for producing light olefins from the oxygen-containing compound according to the seventh specific embodiment of the present invention. 
         [0097]    As shown in  FIG. 7 , the oxygen-containing compound feedstock and the diluent from the feeding line  702  are transported to the fluidized bed reactor  701 , and contacted with the catalyst from the pipeline  723  to conduct the dehydration reaction to produce olefins. The excessive heat is removed with an internal heat remover  713  from the fluidized bed reactor  701 . The resulting light olefins-rich hydrocarbon and a part of the resulting spent catalyst are transported to the sedimentation zone  5 . After the sedimentation, the spent catalyst returns back to the fluidized bed reactor  701 . The light olefins-rich hydrocarbon and the entrapped spent catalyst fine powder are filtered with the filter  706 . After filtering, the light olefins-rich hydrocarbon is transported to a product separation-recovery system (not shown) via the pipeline  703  and the spent catalyst fine powder settles and returns to the fluidized bed reactor. The other part of the resulting spent catalyst is transported to the spent catalyst receiver  708  via the pipeline  716  and stripped. 
         [0098]    The spent catalyst from the spent catalyst receiver  708  is transported to the catalyst hopper  709  via the pipeline  717 , and transported to the spent catalyst feeding tank  710  via the pipeline  718 , and then to the regenerator  707  via the pipeline  719 . The spent catalyst is counter-current contacted with the main air from the pipeline  724  and subjected to regeneration by coke-burning. The excessive heat is removed with the internal heat remover  715 . The flue gas is transported via the pipeline  704  to the subsequent energy recovery and purification system (not shown). The regenerated catalyst is transported to the regenerated catalyst receiver  711  via the pipeline  720 . The excessive heat of the regenerated catalyst is removed with the internal heat remover  714 . After the heat removal, the regenerated catalyst is transported to the catalyst hopper  709  via the pipeline  721 . After increasing the pressure, the regenerated catalyst is transported to the regenerated catalyst feeding tank  712  via the pipeline  722 , and then transported to the fluidized bed reactor  701  via the pipeline  723  after being stripped. 
       EXAMPLE 
       [0099]    The following examples are used to illustrate the present invention, but the present invention is not limited to these examples. 
       Examples 1-6 
       [0100]    Examples 1-6 were conducted according to the process as shown in  FIG. 1  (when Examples and Comparative Examples were conducted according to the process as shown in  FIG. 1 , the same reactors were used) with the substantially same reaction conditions but different reaction pressures and weight hourly space velocities. The reaction feedstock, the catalyst, the reaction conditions and the product yield were listed in Table 1. 
         [0101]    It could be seen from Examples 1-6 that the technical solution of the present invention, i.e. increasing the reaction pressure and simultaneously and correspondingly increasing the WHSV, and maintaining the substantially equivalent other reaction conditions, could accomplish the yield of light olefins as high as 84.9%. 
       Example 7-8 
       [0102]    Examples 7-8 were conducted according to the process as shown in  FIG. 1 . Compared with Example 4, in Examples 7-8, when the reaction pressure was increased, the WHSV was not correspondingly increased, and other operation conditions were substantially kept as the same. The reaction feedstock, the catalyst, the reaction conditions and the product yield were listed in Table 2. 
         [0103]    It could be seen from Example 4, Example 7 and Example 8 that compared with Example 4, if only increasing the reaction pressure without correspondingly increasing the WHSV under the substantially same other reaction conditions, the output and yield of light olefins would decrease, wherein the yield of light olefins decreased from 84.3% of Example 4 to 82.9% of Example 8; the output of light olefins decreased from 3.73 kg/h of Example 4 to 2.64 kg/h of Example 8. 
       Example 9 
       [0104]    Example 9 was conducted according to the process as shown in  FIG. 1 , Compared with Example 3, the operation conditions were substantially kept as the same with only changing the carbon content of the catalyst at the inlet of the reactor (Carbon content of the catalyst at the inlet of the reactor refers to the carbon content of the catalyst at the inlet of the reactor, which catalyst has not been contacted with the feedstock). The reaction feedstock, the catalyst, the reaction conditions and the product yield were listed in Table 2. 
         [0105]    It could be seen from Example 3 and Example 9 that compared with Example 3, if the reaction pressure and the weight hourly space velocity were substantially kept as the same, when the carbon content of the catalyst at the inlet of the reactor decreased from 7.3% to 4.5%, the output of light olefins decreased from 3.84 kg/h to 3.58 kg/h; the yield of light olefins decreased from 84.9% to 84.3%; the mass ratio of ethylene to propylene increased. 
       Example 10 
       [0106]    Example 10 was conducted according to the process as shown in  FIG. 3 . The reaction feedstock, the catalyst, the reaction conditions and the product yield were listed in Table 2. 
         [0107]    It could be seen from Example 10 that the yield of light olefins was 93.3%, the output of light olefin was 4.03 kg/h. 
       Example 11 
       [0108]    Example 11 was conducted according to the process as shown in  FIG. 7 . The reaction feedstock (feedstock=ethanol), the catalyst, the reaction conditions and the product yield were listed in Table 2. It could be seen from Example 11 that the yield of light olefins was 82.8%, the output of light olefin was 3.26 kg/h. 
       Example 12 
       [0109]    Example 12 was conducted according to the process as shown in  FIG. 2 . The reaction feedstock, the catalyst, the reaction conditions and the product yield were listed in Table 4. 
         [0110]    Example 12 was a technical solution in which both the production of light olefins and the production of gasoline were increased. It could be seen from Example 12 that the propylene yield was 65.9%, the gasoline yield was 25.3%, the propylene output was 1.98 kg/h, the gasoline output was 0.76 kg/h. 
       Comparative Examples 1-6 
       [0111]    Comparative Examples 1-6 were conducted with the same reactors, feedstocks and catalysts as those of Examples 1-10, and were conducted according to the process as shown in  FIG. 1 . Compared with Examples 1-10, Comparative Example 1 was conducted in a conventional condition for producing light olefins from methanol, wherein the carbon content of the catalyst at the inlet of the reactor is remarkably lower, and the reaction pressure and the weight hourly space velocity were remarkably lower than those of the present invention; for Comparative Examples 2-6, only the reaction pressure and the WHSV were changed, and other operation conditions were substantially kept as the same with those of Examples 1-10. The reaction feedstock, the catalyst, the reaction conditions and the product yield of Comparative Examples 1-6 were listed in Table 3. 
         [0112]    Comparative Example 1 was conducted in a conventional condition for producing light olefins from methanol. Comparative Example 2 was only different from Comparative Example 1 in the carbon content of the catalyst at the inlet of the reactor. Compared with Comparative Example 1, the carbon content of the catalyst at the inlet of the reactor was increased from 1.5% of Comparative Example 1 to 7.2% of Comparative Example 2, the output of light olefins was decreased from 0.47 kg/h of Comparative Example 1 to 0.43 kg/h of Comparative Example 2; the conversion rate was decreased from 100% of Comparative Example 1 to 80.2% of Comparative Example 2. 
         [0113]    Except for the reaction pressure and the weight hourly space velocity, Comparative Example 2 had the substantially same carbon content of the catalyst at the inlet of the reactor as Examples 1-8. Compared with Comparative Example 2, Examples 1-8 had the substantially same or slightly higher light olefins yields and the remarkably higher light olefins outputs. For example, the yield of light olefins was increased from 79.2% of Comparative Example 2 to 84.9% of Example 3; the output of light olefins was increased from 0.43 kg/h of Comparative Example 2 to 3.84 kg/h of Example 3, and the increasing amplitude was as high as 793.02%. 
         [0114]    For Comparative Example 3 and Example 3, except the weight hourly space velocity, the other reaction conditions were kept as the same. Comparative Example 3 had a remarkably higher weight hourly space velocity than Example 3. Compared with Comparative Example 3, after using the present invention, the output of light olefins was increased from 0.46 kg/h of Comparative Example 3 to 3.84 kg/h of Example 3, and the increasing amplitude was as high as 734.78%; the yield of light olefins was increased from 82.9% of Comparative Example 3 to 84.9% of Example 3. 
         [0115]    For Comparative Example 4 and Example 2, except for the reaction pressure, the other reaction conditions were kept as the same. Comparative Example 4 had a remarkably lower reaction pressure than Example 2. Compared with Comparative Example 4, after using the present invention, the output of light olefins was increased from 0.44 kg/h of Comparative Example 4 to 2.54 kg/h of Example 2, and the increasing amplitude was as high as 477.27%; the yield of light olefins was increased from 79.4% of Comparative Example 4 to 84.4% of Example 2. 
         [0116]    For Comparative Example 5 and Example 2, except for the weight hourly space velocity, the other reaction conditions were kept as the same. Comparative Example 5 had a remarkably lower weight hourly space velocity than Example 2. Compared with Comparative Example 5, after using the present invention, the output of light olefins was increased from 0.43 kg/h of Comparative Example 5 to 2.54 kg/h of Example 2, and the increasing amplitude was as high as 490.70%; the yield of light olefins was increased from 75.3% of Comparative Example 5 to 84.4% of Example 2. 
         [0117]    For Comparative Example 6 and Example 1, except for the reaction pressure, the other reaction conditions were kept as the same. Comparative Example 6 had a remarkably higher reaction pressure than Example 1. Compared with Comparative Example 6, after using the present invention, the output of light olefins was increased from 0.33 kg/h of Comparative Example 6 to 1.11 kg/h of Example 1, and the increasing amplitude was as high as 236.36%; the yield of light olefins was increased from 33.4% of Comparative Example 6 to 83.7% of Example 1. 
         [0000]    
       
         
               
               
               
               
               
               
               
             
               
               
               
               
               
               
               
             
           
               
                   
                 TABLE 1 
               
               
                   
                   
               
               
                   
                 Example 1 
                 Example 2 
                 Example 3 
                 Example 4 
                 Example 5 
                 Example 6 
               
               
                   
                   
               
             
             
               
                   
               
             
          
           
               
                 The reaction feedstock 
                 methanol 
                 methanol 
                 methanol 
                 methanol 
                 methanol 
                 methanol 
               
               
                 (the mass fraction of the 
               
               
                 oxygen-containing 
               
               
                 compound &gt;98 wt %) 
               
               
                 Catalyst (Sinopec 
                 SAPO-34 
                 SAPO-34 
                 SAPO-34 
                 SAPO-34 
                 SAPO-34 
                 SAPO-34 
               
               
                 Catalyst Co., Ltd. Qilu 
                 zeolite 
                 zeolite 
                 zeolite 
                 zeolite 
                 zeolite 
                 zeolite 
               
               
                 Division) 
                 catalyst 
                 catalyst 
                 catalyst 
                 catalyst 
                 catalyst 
                 catalyst 
               
               
                 Reaction conditions 
               
               
                 Reaction 
                 450 
                 450 
                 450 
                 450 
                 450 
                 450 
               
               
                 temperature, ° C. 
               
               
                 Reaction pressure, MPa 
                 0.7 
                 0.8 
                 1.2 
                 2.5 
                 5.0 
                 7 
               
               
                 WHSV, h −1   
                 10 
                 22 
                 30 
                 41 
                 93 
                 163 
               
               
                 Carbon content of the 
                 7.2 
                 7.2 
                 7.3 
                 7.3 
                 7.2 
                 7.3 
               
               
                 catalyst at the inlet of 
               
               
                 the reactor, wt % 
               
               
                 Regeneration 
               
               
                 conditions 
               
               
                 Regeneration 
                 580 
                 580 
                 570 
                 570 
                 580 
                 580 
               
               
                 temperature, ° C. 
               
               
                 Regeneration pressure, 
                 0.4 
                 0.4 
                 0.4 
                 0.4 
                 0.6 
                 0.4 
               
               
                 MPa 
               
               
                 The feedstock amount 
                 3.02 
                 6.90 
                 10.35 
                 17.97 
                 43.14 
                 65.43 
               
               
                 (as pure), kg/h 
               
               
                 Mol (feedstock)/mol 
                 5.1 
                 5.1 
                 5.1 
                 5.1 
                 5.1 
                 5.1 
               
               
                 (diluent) 
               
               
                 The conversion rate of 
                 100 
                 100 
                 100 
                 56.3 
                 23.2 
                 14.7 
               
               
                 the feedstock, wt % 
               
               
                 The output of light 
               
               
                 olefins, kg/h 
               
               
                 Ethylene 
                 0.56 
                 1.27 
                 1.89 
                 1.75 
                 1.57 
                 1.48 
               
               
                 Propylene 
                 0.55 
                 1.27 
                 1.95 
                 1.98 
                 2.09 
                 1.95 
               
               
                 Butylene 
                 0.11 
                 0.25 
                 0.39 
                 0.38 
                 0.38 
                 0.39 
               
               
                 Ethylene + propylene 
                 1.11 
                 2.54 
                 3.84 
                 3.73 
                 3.66 
                 3.43 
               
               
                 The yield of light 
               
               
                 olefins*, wt % 
               
               
                 Ethylene 
                 42.3 
                 42.1 
                 41.8 
                 39.6 
                 35.8 
                 35.2 
               
               
                 Propylene 
                 41.4 
                 42.3 
                 43.1 
                 44.7 
                 47.8 
                 46.3 
               
               
                 Butylene 
                 8.1 
                 8.4 
                 8.6 
                 8.7 
                 8.6 
                 9.3 
               
               
                 Ethylene + propylene 
                 83.7 
                 84.4 
                 84.9 
                 84.3 
                 83.6 
                 81.5 
               
               
                   
               
               
                 Yield = the output of the product/the sum of the output of the hydrocarbon products except the oxygen-containing compound * 100. 
               
             
          
         
       
     
         [0000]    
       
         
               
               
               
               
               
               
             
           
               
                 TABLE 2 
               
               
                   
               
               
                   
                 Example 7 
                 Example 8 
                 Example 9 
                 Example 10 
                 Example 11 
               
               
                   
               
             
             
               
                 The reaction feedstock (the 
                 methanol 
                 methanol 
                 methanol 
                 methanol 
                 ethanol 
               
               
                 mass fraction of the oxygen- 
                   
                   
                   
                   
                   
               
               
                 containing compound &gt;98 wt %) 
                   
                   
                   
                   
                   
               
               
                 Catalyst (Sinopec Catalyst 
                 SAPO-34 
                 SAPO-34 
                 SAPO-34 
                 SAPO-34 
                 SAPO-34 
               
               
                 Co., Ltd. Qilu Division) 
                 zeolite 
                 zeolite 
                 zeolite 
                 zeolite 
                 zeolite 
               
               
                   
                 catalyst 
                 catalyst 
                 catalyst 
                 catalyst 
                 catalyst 
               
               
                 Reaction conditions 
                   
                   
                   
                   
                   
               
               
                 Reaction temperature, ° C. 
                 450 
                 450 
                 430 
                 450 
                 470 
               
               
                 Reaction pressure, MPa 
                 2.8 
                 3.2 
                 1.5 
                 2.3 
                 1 
               
               
                 WHSV, h −1   
                 36 
                 26 
                 26 
                 40 
                 25 
               
               
                 Carbon content of the catalyst 
                 7.3 
                 7.2 
                 4.5 
                 10.2 
                 8.2 
               
               
                 at the inlet of the reactor, wt % 
                   
                   
                   
                   
                   
               
               
                 Regeneration conditions 
                   
                   
                   
                   
                   
               
               
                 Regeneration temperature, ° C. 
                 590 
                 590 
                 550 
                 650 
                 600 
               
               
                 Regeneration pressure, MPa 
                 0.4 
                 0.4 
                 0.3 
                 0.6 
                 0.3 
               
               
                 The feedstock amount  
                 16.10 
                 11.50 
                 9.71 
                 16.54 
                 8.63 
               
               
                 (as pure), kg/h 
                   
                   
                   
                   
                   
               
               
                 Mol (feedstock)/mol (diluent) 
                 5.1 
                 5.1 
                 5.1 
                 5.1 
                 3.5 
               
               
                 The conversion rate of the 
                 58.7 
                 63.4 
                 100 
                 59.9 
                 100 
               
               
                 feedstock, wt % 
                   
                   
                   
                   
                   
               
               
                 The output of light olefins, kg/h 
                   
                   
                   
                   
                   
               
               
                 Ethylene 
                 1.60 
                 1.20 
                 2.10 
                 2.26 
                 1.36 
               
               
                 Propylene 
                 1.86 
                 1.44 
                 1.48 
                 1.77 
                 1.90 
               
               
                 Butylene 
                 0.37 
                 0.29 
                 0.36 
                 0.00 
                 0.35 
               
               
                 Ethylene + propylene 
                 3.46 
                 2.64 
                 3.58 
                 4.03 
                 3.26 
               
               
                 The yield of light olefins*, wt % 
                   
                   
                   
                   
                   
               
               
                 Ethylene 
                 38.7 
                 37.7 
                 49.5 
                 52.3 
                 34.6 
               
               
                 Propylene 
                 45.0 
                 45.2 
                 34.8 
                 41.0 
                 48.2 
               
               
                 Butylene 
                 8.9 
                 9.2 
                 8.6 
                 0 
                 9 
               
               
                 Ethylene + propylene 
                 83.7 
                 82.9 
                 84.3 
                 93.3 
                 82.8 
               
               
                   
               
               
                 *Yield = the output of the product/the sum of the output of the hydrocarbon products except the oxygen-containing compound * 100. 
               
             
          
         
       
     
         [0000]    
       
         
               
               
               
               
               
               
               
             
               
               
               
               
               
               
               
             
           
               
                   
                 TABLE 3 
               
               
                   
                   
               
               
                   
                 Comparative 
                 Comparative 
                 Comparative 
                 Comparative 
                 Comparative 
                 Comparative 
               
               
                   
                 Example 1 
                 Example 2 
                 Example 3 
                 Example 4 
                 Example 5 
                 Example 6 
               
               
                   
                   
               
             
             
               
                   
               
             
          
           
               
                 The reaction 
                 methanol 
                 methanol 
                 methanol 
                 methanol 
                 methanol 
                 methanol 
               
               
                 feedstock (the 
               
               
                 mass fraction of 
               
               
                 the oxygen- 
               
               
                 containing 
               
               
                 compound &gt;98 wt 
               
               
                 %) 
               
               
                 Catalyst 
                 SAPO-34 
                 SAPO-34 
                 SAPO-34 
                 SAPO-34 
                 SAPO-34 
                 SAPO-34 
               
               
                 (Sinopec 
                 zeolite 
                 zeolite 
                 zeolite 
                 zeolite 
                 zeolite 
                 zeolite 
               
               
                 Catalyst Co., Ltd. 
                 catalyst 
                 catalyst 
                 catalyst 
                 catalyst 
                 catalyst 
                 catalyst 
               
               
                 Qilu Division) 
               
               
                 Reaction 
               
               
                 conditions 
               
               
                 Reaction 
                 450 
                 450 
                 450 
                 450 
                 450 
                 450 
               
               
                 temperature, ° C. 
               
               
                 Reaction 
                 0.12 
                 0.12 
                 1.5 
                 0.12 
                 0.9 
                 12 
               
               
                 pressure, MPa 
               
               
                 WHSV, h −1   
                 5 
                 5 
                 352 
                 22 
                 1 
                 8 
               
               
                 Carbon content 
                 1.2 
                 7.2 
                 7.2 
                 7.2 
                 7.3 
                 7.2 
               
               
                 of the catalyst at 
               
               
                 the inlet of the 
               
               
                 reactor, wt % 
               
               
                 Regeneration 
               
               
                 conditions 
               
               
                 Regeneration 
                 580 
                 580 
                 570 
                 570 
                 580 
                 570 
               
               
                 temperature, ° C. 
               
               
                 Regeneration 
                 0.4 
                 0.4 
                 0.4 
                 0.4 
                 0.4 
                 0.4 
               
               
                 pressure, MPa 
               
               
                 The feedstock 
                 1.38 
                 1.55 
                 34.51 
                 4.31 
                 1.29 
                 12.94 
               
               
                 amount (as pure), 
               
               
                 kg/h 
               
               
                 Mol (feedstock)/ 
                 5.1 
                 5.1 
                 5.1 
                 5.1 
                 5.1 
                 5.1 
               
               
                 mol (diluent) 
               
               
                 The conversion 
                 100 
                 80.2 
                 3.7 
                 29.5 
                 100 
                 17.3 
               
               
                 rate of the 
               
               
                 feedstock, wt % 
               
               
                 The output of 
               
               
                 light olefins, kg/h 
               
               
                 Ethylene 
                 0.24 
                 0.20 
                 0.20 
                 0.20 
                 0.19 
                 0.12 
               
               
                 Propylene 
                 0.23 
                 0.23 
                 0.26 
                 0.24 
                 0.24 
                 0.21 
               
               
                 Butylene 
                 0.05 
                 0.05 
                 0.05 
                 0.05 
                 0.05 
                 0.16 
               
               
                 Ethylene + propylene 
                 0.47 
                 0.43 
                 0.46 
                 0.44 
                 0.43 
                 0.33 
               
               
                 The yield of light 
               
               
                 olefins*, wt % 
               
               
                 Ethylene 
                 40.5 
                 36.6 
                 36.7 
                 36.6 
                 33.7 
                 12.3 
               
               
                 Propylene 
                 38.1 
                 42.6 
                 46.2 
                 42.8 
                 41.6 
                 21.1 
               
               
                 Butylene 
                 8.6 
                 8.6 
                 8.2 
                 8.4 
                 9.2 
                 16.0 
               
               
                 Ethylene + propylene 
                 78.6 
                 79.2 
                 82.9 
                 79.4 
                 75.3 
                 33.4 
               
               
                   
               
               
                 *Yield = the output of the product/the sum of the output of the hydrocarbon products except the oxygen-containing compound * 100. 
               
             
          
         
       
     
         [0000]    
       
         
               
               
             
           
               
                 TABLE 4 
               
               
                   
               
               
                   
                 Example 12 
               
               
                   
               
             
             
               
                 The reaction feedstock (the mass fraction of the  
                 dimethylether 
               
               
                 oxygen-containing compound &gt;98 wt %) 
                   
               
               
                 Catalyst (Sinopec Catalyst Co., Ltd. Qilu Division) 
                 ZSM-5 zeolite 
               
               
                   
                 catalyst 
               
               
                 Reaction conditions 
                   
               
               
                 Reaction temperature, ° C. 
                 500 
               
               
                 Reaction pressure, MPa 
                 1.5 
               
               
                 WHSV, h −1   
                 19 
               
               
                 Carbon content of the catalyst at the inlet  
                 10.2 
               
               
                 of the reactor, wt % 
                   
               
               
                 Regeneration conditions 
                   
               
               
                 Regeneration temperature, ° C. 
                 650 
               
               
                 Regeneration pressure, MPa 
                 0.2 
               
               
                 The feedstock amount (as pure), kg/h 
                 6.56 
               
               
                 Mol (feedstock)/mol (diluent) 
                 1.6 
               
               
                 The conversion rate of the feedstock, wt % 
                 100 
               
               
                 The output of the major products, kg/h 
                   
               
               
                 Ethylene 
                 0.12 
               
               
                 Propylene 
                 1.98 
               
               
                 Gasoline 
                 0.76 
               
               
                 Ethylene + propylene 
                 2.10 
               
               
                 The yield of the major products*, wt % 
                   
               
               
                 Ethylene 
                 4.1 
               
               
                 Propylene 
                 65.9 
               
               
                 Gasoline 
                 25.3 
               
               
                   
               
               
                 Yield = the output of the product/the sum of the output of the hydrocarbon products except the oxygen-containing compound * 100. 
               
             
          
         
       
     
       Example I 
       [0118]    Example I was performed according to the process as shown in  FIG. 1 , wherein the reaction feedstock, the catalyst, the reaction conditions and the product yield were listed in Table I. 
       Example II 
       [0119]    Example II was performed according to the process as shown in  FIG. 3 , wherein the reaction feedstock, the catalyst, the reaction conditions and the product yield were listed in Table I. 
       Example III 
       [0120]    Example III was performed according to the process as shown in  FIG. 2 , wherein the reaction feedstock, the catalyst, the reaction conditions and the product yield were listed in Table II. 
         [0121]    It could be seen from Table I that the present process had the yields of ethylene and propylene higher than those of the prior art. It could be seen from Table II that the present process had the yields of propylene and gasoline of 65.9% and 25.3%, which were higher than those of the prior art. Since the reaction system of the present invention had a higher pressure than the existing industrial plants, therefore under the same other reaction conditions, the reaction system of the present invention would have a higher feedstock throughput than the existing industrial plant. 
         [0000]    
       
         
               
               
               
             
           
               
                 TABLE I 
               
               
                   
               
               
                   
                 Example I 
                 Example II 
               
               
                   
               
             
             
               
                 The reaction feedstock (the mass fraction  
                 Industrial 
                 Industrial 
               
               
                 of the oxygen-containing compound 
                 methanol 
                 methanol 
               
               
                 feedstock &gt;98 wt %) 
                   
                   
               
               
                 Catalyst (Sinopec Catalyst Co.,  
                 SAPO-34  
                 SAPO-34  
               
               
                 Ltd. Qilu Division) 
                 zeolite 
                 zeolite 
               
               
                   
                 catalyst 
                 catalyst 
               
               
                 The reaction conditions of the riser-type reactor 
                   
                   
               
               
                 Temperature, ° C. 
                 430 
                 450 
               
               
                 Pressure, MPa 
                 1.5 
                 2.3 
               
               
                 The regeneration conditions of the regenerator 
                   
                   
               
               
                 Regeneration pressure, MPa 
                 0.3 
                 0.6 
               
               
                 Regeneration temperature, ° C. 
                 550 
                 650 
               
               
                 Regenerated catalyst content (preset), wt % 
                 0.2 
                 0.4 
               
               
                 The reaction conditions of the further  
                   
                   
               
               
                 riser-type reactor 
                   
                   
               
               
                 Temperature, ° C. 
                 — 
                 450 
               
               
                 Pressure, MPa 
                 — 
                 2.3 
               
               
                 Product yield 
                   
                   
               
               
                 Ethylene, % 
                 49.5 
                 52.3 
               
               
                 Propylene, % 
                 34.8 
                 41.0 
               
               
                 Butylene, % 
                 8.6 
                 0.0 
               
               
                   
               
             
          
         
       
     
         [0000]    
       
         
               
               
             
           
               
                 TABLE II 
               
               
                   
               
               
                   
                 Example III 
               
               
                   
               
             
             
               
                 The reaction feedstock (the mass fraction of the oxygen- 
                 Industrial 
               
               
                 containing compound feedstock &gt;98 wt %) 
                 dimethylether 
               
               
                 Catalyst (Sinopec Catalyst Co., Ltd. Qilu Division) 
                 ZSM-5 zeolite 
               
               
                   
                 catalyst 
               
               
                 The reaction conditions of the riser-type reactor 
                   
               
               
                 Temperature, ° C. 
                 500 
               
               
                 Pressure, MPa 
                 1.5 
               
               
                 The regeneration conditions of the regenerator 
                   
               
               
                 Regeneration pressure, MPa 
                 0.2 
               
               
                 Regeneration temperature, ° C. 
                 650 
               
               
                 Regenerated catalyst content (preset), wt % 
                 0.4 
               
               
                 Product yield 
                   
               
               
                 Ethylene, % 
                 4.1 
               
               
                 Propylene, % 
                 65.9 
               
               
                 Gasoline, % 
                 25.3